JP6239327B2 - Organic wastewater treatment method and apparatus, and chemical fertilizer manufacturing method and apparatus - Google Patents
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- 238000004065 wastewater treatment Methods 0.000 title claims description 40
- 239000000126 substance Substances 0.000 title claims description 39
- 239000003337 fertilizer Substances 0.000 title claims description 33
- 238000004519 manufacturing process Methods 0.000 title claims description 14
- 239000010802 sludge Substances 0.000 claims description 212
- 239000007788 liquid Substances 0.000 claims description 159
- 229920000642 polymer Polymers 0.000 claims description 125
- 238000000926 separation method Methods 0.000 claims description 122
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 claims description 101
- 229910052567 struvite Inorganic materials 0.000 claims description 101
- 238000011282 treatment Methods 0.000 claims description 94
- 238000006243 chemical reaction Methods 0.000 claims description 66
- 238000011084 recovery Methods 0.000 claims description 59
- 238000002156 mixing Methods 0.000 claims description 58
- 230000002776 aggregation Effects 0.000 claims description 53
- 208000005156 Dehydration Diseases 0.000 claims description 50
- 230000018044 dehydration Effects 0.000 claims description 50
- 238000006297 dehydration reaction Methods 0.000 claims description 50
- 238000003860 storage Methods 0.000 claims description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 238000005054 agglomeration Methods 0.000 claims description 40
- 210000003608 fece Anatomy 0.000 claims description 26
- 239000010871 livestock manure Substances 0.000 claims description 26
- 239000002351 wastewater Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 20
- 239000000852 hydrogen donor Substances 0.000 claims description 15
- 238000004220 aggregation Methods 0.000 claims description 13
- 238000005345 coagulation Methods 0.000 claims description 11
- 230000015271 coagulation Effects 0.000 claims description 11
- 230000008569 process Effects 0.000 claims description 11
- 239000010815 organic waste Substances 0.000 claims description 9
- 238000003795 desorption Methods 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims description 5
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000010865 sewage Substances 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 21
- 238000012545 processing Methods 0.000 description 12
- 239000000701 coagulant Substances 0.000 description 8
- 239000008394 flocculating agent Substances 0.000 description 8
- 230000007246 mechanism Effects 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 7
- 239000012535 impurity Substances 0.000 description 7
- 238000003825 pressing Methods 0.000 description 7
- 235000015097 nutrients Nutrition 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 238000002425 crystallisation Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 239000010800 human waste Substances 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 229910052749 magnesium Inorganic materials 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 229910052698 phosphorus Inorganic materials 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 3
- -1 ammonium ions Chemical class 0.000 description 3
- 229920006317 cationic polymer Polymers 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 3
- 238000005189 flocculation Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- 239000003002 pH adjusting agent Substances 0.000 description 3
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 2
- JKNCOURZONDCGV-UHFFFAOYSA-N 2-(dimethylamino)ethyl 2-methylprop-2-enoate Chemical compound CN(C)CCOC(=O)C(C)=C JKNCOURZONDCGV-UHFFFAOYSA-N 0.000 description 2
- DPBJAVGHACCNRL-UHFFFAOYSA-N 2-(dimethylamino)ethyl prop-2-enoate Chemical compound CN(C)CCOC(=O)C=C DPBJAVGHACCNRL-UHFFFAOYSA-N 0.000 description 2
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 229920006322 acrylamide copolymer Polymers 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000002361 compost Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 210000002700 urine Anatomy 0.000 description 2
- UUGXDEDGRPYWHG-UHFFFAOYSA-N (dimethylamino)methyl 2-methylprop-2-enoate Chemical compound CN(C)COC(=O)C(C)=C UUGXDEDGRPYWHG-UHFFFAOYSA-N 0.000 description 1
- VMEZXMFPKOMWHR-UHFFFAOYSA-N (dimethylamino)methyl prop-2-enoate Chemical compound CN(C)COC(=O)C=C VMEZXMFPKOMWHR-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-M Acrylate Chemical compound [O-]C(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-M 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- ZHNUHDYFZUAESO-UHFFFAOYSA-N Formamide Chemical group NC=O ZHNUHDYFZUAESO-UHFFFAOYSA-N 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-M Methacrylate Chemical compound CC(=C)C([O-])=O CERQOIWHTDAKMF-UHFFFAOYSA-M 0.000 description 1
- 238000011276 addition treatment Methods 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 125000003368 amide group Chemical group 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 125000002560 nitrile group Chemical group 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 239000002699 waste material 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Treatment Of Sludge (AREA)
- Fertilizers (AREA)
- Biological Treatment Of Waste Water (AREA)
- Removal Of Specific Substances (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
本発明は、有機性廃水処理方法及び装置に関する。特に、屎尿と浄化槽汚泥などの有機性汚泥を含有する有機性廃水の処理方法及び装置並びに当該有機性廃水処理から化成肥料を製造する方法及び装置に関する。 The present invention relates to an organic wastewater treatment method and apparatus. In particular, the present invention relates to a method and apparatus for treating organic wastewater containing organic sludge such as manure and septic tank sludge, and a method and apparatus for producing chemical fertilizer from the organic wastewater treatment.
屎尿及び家庭用浄化槽で発生する有機性汚泥を含む有機性廃水の生物処理が行われている。屎尿及び家庭用浄化槽由来の有機性廃水には、夾雑物が多量に含まれるため、夾雑物を除去して脱水処理を行い、分離液を生物処理に供する。脱水処理により多量の有機性汚泥の脱水ケーキが発生するため、脱水ケーキの減容化が種々検討されている。また、脱水ケーキを助燃剤や堆肥として再利用するために、含水率の低減化が必要とされている。このため、有機性廃水に凝集剤を添加して、凝集フロックとして凝集させた後に脱水処理が行われている。 Biological treatment of organic wastewater containing organic sludge generated in sewage and household septic tanks is performed. Since organic wastewater derived from manure and domestic septic tanks contains a large amount of impurities, the impurities are removed and dehydrated, and the separated liquid is subjected to biological treatment. Since a large amount of dehydrated cake of organic sludge is generated by dehydration, various attempts have been made to reduce the volume of dehydrated cake. Further, in order to reuse the dehydrated cake as a combustion aid or compost, it is necessary to reduce the water content. For this reason, a dehydration process is performed after adding a flocculant to organic wastewater and making it coagulate | flocculate as a coagulation floc.
また、生物処理に先立つ脱水処理において、屎尿及び有機性汚泥を含む有機性廃水は全量が凝集剤添加後に脱水されるため、有機性排水中に含まれている有機物も除去されてしまう。有機性排水中に含まれている有機物は、後続の生物処理において微生物の栄養素となる水素供与体である。有機性廃水の全量脱水処理により、有機物が不足すると、生物処理が不十分となるため、通常はメタノールなどの水素供与体を多量に添加することが必要となる。 In addition, in the dehydration process prior to the biological treatment, the entire amount of organic wastewater containing manure and organic sludge is dehydrated after the addition of the flocculant, so that organic substances contained in the organic wastewater are also removed. The organic matter contained in the organic wastewater is a hydrogen donor that becomes a nutrient for microorganisms in the subsequent biological treatment. When organic matter is insufficient due to the total amount of organic wastewater dehydration treatment, biological treatment becomes insufficient. Therefore, it is usually necessary to add a large amount of a hydrogen donor such as methanol.
したがって、現状の屎尿及び有機性汚泥を含む有機性廃水の処理では、脱水処理に必要な凝集剤及び生物処理に必要な栄養源を多量に添加しなければならず、維持管理費が高額になっている。 Therefore, in the current treatment of organic wastewater containing manure and organic sludge, a large amount of flocculant necessary for dehydration and nutrients necessary for biological treatment must be added, resulting in high maintenance costs. ing.
また、有機性汚泥に含まれているリン及びアンモニウムは化成肥料として再利用できることが周知であり、屎尿及び浄化槽汚泥からのリンを回収する方法及び装置が種々提案されている（特許文献４）。 Moreover, it is well known that phosphorus and ammonium contained in organic sludge can be reused as a chemical fertilizer, and various methods and apparatuses for recovering phosphorus from manure and septic tank sludge have been proposed (Patent Document 4).
本発明は、脱水処理と生物処理とを組み合わせた有機性廃水の処理において、発生する脱水ケーキの低含水率化及び減容化を達成しながら、維持管理費を低額に抑えることができ、化成肥料として有用なリン酸マグネシウムアンモニウム（以下「ＭＡＰ」という。）を効率的に回収する処理方法及び装置を提供することを目的とする。 In the treatment of organic wastewater combining dehydration treatment and biological treatment, the present invention can reduce maintenance and maintenance costs while achieving low water content and volume reduction of the dehydrated cake that is generated. It aims at providing the processing method and apparatus which collect | recover efficiently magnesium ammonium phosphate (henceforth "MAP") useful as a fertilizer.
また、本発明は、脱水処理と生物処理とを組み合わせた有機性廃水の処理において、ＭＡＰを回収して化成肥料を製造する方法及び装置を提供することを目的とする。 Moreover, this invention aims at providing the method and apparatus which collect | recovers MAP and manufactures a chemical fertilizer in the process of the organic waste water which combined dehydration process and biological treatment.
本発明は、屎尿及び／又は有機性汚泥と、生物処理からの余剰汚泥との混合汚泥を脱水処理した後に生物処理する有機性廃水処理方法において、脱水処理に供する混合汚泥の一部に高分子凝集剤を添加しないことにより、脱水ケーキの低含水率化及び減容化を達成しながら、高分子凝集剤の添加量を削減すると同時に、後続の生物処理に必要な水素供与体の添加量を削減することができ、ＭＡＰを効率的に回収できる処理方法を提供する。 The present invention relates to an organic wastewater treatment method in which mixed sludge of manure and / or organic sludge and surplus sludge from biological treatment is dehydrated and then biologically treated. By not adding a flocculant, while reducing the water content and volume of the dehydrated cake, the amount of the polymer flocculant is reduced, and at the same time, the amount of hydrogen donor required for the subsequent biological treatment is reduced. Provided is a processing method that can reduce MAP and efficiently recover MAP.
本発明によれば、高分子凝集剤の添加とＭＡＰ回収とを連動させた有機性排水処理方法及び装置並びに化成肥料の製造方法及び装置が提供される。
［１］屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理する有機性廃水処理方法であって、
当該混合汚泥に高分子凝集剤を添加せずに脱水処理して第１分離液を得る工程と、
当該混合汚泥に高分子凝集剤を添加してから脱水処理して第２分離液を得る工程と、
を交互に行い、
前記高分子凝集剤を添加する場合には、脱水処理の際に発生する第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収することを特徴とする有機性廃水処理方法。
［２］前記混合汚泥に高分子凝集剤を添加せずに脱水処理する工程は、高分子凝集剤を添加する工程と添加しない工程との合計時間の６０％以下とする、［１］に記載の有機性廃水処理方法。
［３］前記混合汚泥に高分子凝集剤を添加せずに脱水処理することによって得られる第１分離液を生物処理における水素供与体として利用する、［１］又は［２］に記載の有機性廃水処理方法。
［４］前記脱水処理は、高分子凝集剤を添加した混合汚泥を濃縮する濃縮工程と、濃縮した混合汚泥を脱水する脱水工程と、を含み、
前記第２分離液は、当該濃縮工程で得られる、［１］〜［３］のいずれか１項に記載の有機性廃水処理方法。
［５］前記濃縮工程で得られる濃縮物に無機凝集剤をさらに添加した後、脱水処理を行う［４］に記載の有機性排水処理方法。
［６］前記脱水処理後の分離液を生物処理における水素供与体として利用する、［５］に記載の有機性廃水処理方法。
［７］屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理するための有機性廃水処理装置であって、
屎尿及び／又は有機性汚泥と、生物処理からの余剰汚泥とを混合する混合槽と、
当該混合槽の下流に位置づけられ、混合汚泥を脱水する脱水装置と、
当該混合槽と当該脱水装置の間に位置づけられ、当該混合槽からの当該混合汚泥に高分子凝集剤を添加して凝集させる凝集反応槽と、
当該混合槽から、当該凝集反応槽を経由せずに、当該脱水装置に当該混合汚泥を直接送るバイパス経路と、
高分子凝集剤を添加した混合汚泥を脱水して得られる第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収するＭＡＰ回収装置と、
当該脱水装置からの分離液及び当該ＭＡＰ回収装置からの脱離液を貯留する分離液貯留槽と、
当該分離液貯留槽からの分離液を処理する生物処理槽と、
当該生物処理槽の下流に位置づけられている固液分離槽と、
を具備する、有機性廃水処理装置。
［８］前記混合槽からの混合汚泥を前記凝集反応槽に送る経路と、前記凝集反応槽を経由せずに前記混合槽からの混合汚泥を前記脱水装置に直接送るバイパス経路と、の切り替えを行う第１切替弁と、
前記脱水装置からの第１分離液を前記分離液貯留槽に送る経路と、前記脱水装置からの第２分離液を前記ＭＡＰ回収装置に送る経路と、の切り替えを行う第２切替弁と、
をさらに具備し、当該第１切替弁と第２切替弁とは連動する、［７］に記載の有機性廃水処理装置。
［９］前記脱水装置は、
高分子凝集剤を添加した混合汚泥に対しては濃縮機として作用し、高分子凝集剤を添加していない混合汚泥に対してはしさ分離機として作用するスクリーンと、
当該スクリーンの下流に位置づけられている脱水機と、
を含み、当該スクリーンからの分離水及び当該脱水機からの分離水をそれぞれ別個にＭＡＰ回収装置に送る経路と分離液貯留槽に送る経路に切り替える切替弁をさらに具備する、［７］又は［８］に記載の有機性廃水処理装置。
［１０］前記脱水装置は、スクリーンとして機能する濃縮部と、当該濃縮部の後段に圧搾部と、を具備し、当該濃縮部からの分離水及び当該圧搾部からの分離水をそれぞれ別個にＭＡＰ回収装置に送る経路と分離液貯留槽に送る経路に切り替える切替弁をさらに具備する、［７］又は［８］に記載の有機性廃水処理装置。
［１１］前記凝集反応槽には、
凝集反応槽への高分子凝集剤の添加を制御する凝集剤添加制御機構と、
高分子凝集剤を添加しない工程の後に開放する自動弁が設けられているドレン配管と、
が接続されている、［７］〜［１０］のいずれか１項に記載の有機性排水処理装置。
［１２］さらに前記混合槽と前記凝集反応槽との間にラインミキサを設け、当該ラインミキサに高分子凝集剤を添加する凝集剤添加配管が接続されている、［７］〜［１１］のいずれか１項に記載の有機性廃水処理装置。
［１３］屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理する有機性廃水処理において、
当該混合汚泥に高分子凝集剤を添加せずに脱水処理して第１分離液を得る工程と、
当該混合汚泥に高分子凝集剤を添加してから脱水処理して第２分離液を得る工程と、
を交互に行い、
前記高分子凝集剤を添加する場合には、脱水処理の際に発生する第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収するＭＡＰ回収工程を含むことを特徴とする、化成肥料の製造方法。
［１４］前記混合汚泥に高分子凝集剤を添加せずに脱水処理する工程は、高分子凝集剤を添加する工程と添加しない工程との合計時間の６０％以下とする、［１３］に記載の化成肥料の製造方法。
［１５］前記混合汚泥に高分子凝集剤を添加せずに脱水処理することによって得られる第１分離液を生物処理における水素供与体として利用する、［１３］又は［１４］に記載の化成肥料の製造方法。
［１６］前記脱水処理は、高分子凝集剤を添加した混合汚泥を濃縮する濃縮工程と、濃縮した混合汚泥を脱水する脱水工程と、を含み、
前記第２分離液は、当該濃縮工程で得られる、［１３］〜［１５］のいずれか１項に記載の化成肥料の製造方法。
［１７］前記濃縮工程で得られる濃縮物に無機凝集剤をさらに添加した後、脱水処理を行う、［１６］に記載の化成肥料の製造方法。
［１８］前記脱水処理後の分離液を生物処理における水素供与体として利用する、［１７］に記載の化成肥料の製造方法。
［１９］屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理するための有機性廃水処理において、
屎尿及び／又は有機性汚泥と、生物処理からの余剰汚泥とを混合する混合槽と、
当該混合槽の下流に位置づけられ、混合汚泥を脱水する脱水装置と、
当該混合槽と当該脱水装置の間に位置づけられ、当該混合槽からの当該混合汚泥に高分子凝集剤を添加して凝集させる凝集反応槽と、
当該混合槽から、当該凝集反応槽を経由せずに、当該脱水装置に当該混合汚泥を直接送るバイパス経路と、
高分子凝集剤を添加した混合汚泥を脱水して得られる第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収するＭＡＰ回収装置と、
を具備する、化成肥料の製造装置。
当該脱水装置からの分離液及び当該ＭＡＰ回収装置からの脱離液を貯留する分離液貯留槽と、
当該分離液貯留槽からの分離液を処理する生物処理槽と、
当該生物処理槽の下流に位置づけられている固液分離槽と、
［２０］前記混合槽からの混合汚泥を前記凝集反応槽に送る経路と、前記混合槽からの混合汚泥を前記凝集反応槽を経由せずに前記脱水装置に直接送るバイパス経路と、の切り替えを行う第１切替弁と、
前記脱水装置からの第１分離液を前記分離液貯留槽に送る経路と、前記脱水装置からの第２分離液を前記ＭＡＰ回収装置に送る経路と、の切り替えを行う第２切替弁と、
をさらに具備し、当該第１切替弁と第２切替弁とは連動する、［１９］に記載の化成肥料の製造装置。
［２１］前記脱水装置は、
高分子凝集剤を添加した混合汚泥に対しては濃縮機として作用し、高分子凝集剤を添加していない混合汚泥に対してはしさ分離機として作用するスクリーンと、
当該スクリーンの下流に位置づけられている脱水機と、
を含み、当該スクリーンからの分離水及び当該脱水機からの分離水をそれぞれ別個にＭＡＰ回収装置に送る経路と分離液貯留槽に送る経路に切り替える切替弁をさらに具備する、［１９］又は［２０］に記載の化成肥料の製造装置。
［２２］前記脱水装置は、スクリーンとして機能する濃縮部と、当該濃縮部の後段に圧搾部と、を具備し、当該濃縮部からの分離水及び当該圧搾部からの分離水をそれぞれ別個にＭＡＰ回収装置に送る経路と分離液貯留槽に送る経路に切り替える切替弁をさらに具備する、［１９］又は［２０］に記載の化成肥料の製造装置。
［２３］前記凝集反応槽には、
凝集反応槽への高分子凝集剤の添加を制御する凝集剤添加制御機構と、
高分子凝集剤を添加しない工程の後に開放する自動弁が設けられているドレン配管と、
が接続されている、［１９］〜［２２］のいずれか１項に記載の化成肥料の製造装置。
［２４］さらに前記混合槽と前記凝集反応槽との間にラインミキサを設け、当該ラインミキサに高分子凝集剤を添加する凝集剤添加配管が接続されている、［１９］〜［２３］のいずれか１項に記載の化成肥料の製造装置。
According to the present invention, there are provided an organic wastewater treatment method and apparatus and a chemical fertilizer manufacturing method and apparatus in which addition of a polymer flocculant and MAP recovery are linked.
[1] An organic wastewater treatment method for biological treatment after dewatering mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment,
A step of dehydrating the mixed sludge without adding a polymer flocculant to obtain a first separation liquid;
Adding a polymer flocculant to the mixed sludge and then dehydrating to obtain a second separation liquid;
Alternately
An organic wastewater treatment method, wherein when adding the polymer flocculant, magnesium ammonium phosphate (MAP) is recovered from the second separation liquid generated during the dehydration treatment.
[2] The step of dehydrating the mixed sludge without adding a polymer flocculant is 60% or less of the total time of the step of adding the polymer flocculant and the step of not adding the polymer flocculant. Organic wastewater treatment method.
[3] The organic material according to [1] or [2], wherein the first separation liquid obtained by dehydrating the mixed sludge without adding a polymer flocculant is used as a hydrogen donor in biological treatment. Wastewater treatment method.
[4] The dehydration treatment includes a concentration step of concentrating the mixed sludge added with the polymer flocculant, and a dehydration step of dehydrating the concentrated mixed sludge.
The organic wastewater treatment method according to any one of [1] to [3], wherein the second separation liquid is obtained in the concentration step.
[5] The organic wastewater treatment method according to [4], wherein an inorganic flocculant is further added to the concentrate obtained in the concentration step, and then dehydration is performed.
[6] The organic wastewater treatment method according to [5], wherein the separation liquid after the dehydration treatment is used as a hydrogen donor in biological treatment.
[7] An organic wastewater treatment apparatus for biological treatment after dewatering mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment,
A mixing tank for mixing manure and / or organic sludge with surplus sludge from biological treatment;
A dehydrator positioned downstream of the mixing tank and dewatering the mixed sludge;
An agglomeration reaction tank that is positioned between the mixing tank and the dehydrator, and adds and aggregates the polymer flocculant to the mixed sludge from the mixing tank;
A bypass path for directly sending the mixed sludge from the mixing tank to the dehydrator without going through the agglomeration reaction tank;
A MAP recovery device for recovering magnesium ammonium phosphate (MAP) from the second separated liquid obtained by dehydrating the mixed sludge added with the polymer flocculant;
A separation liquid storage tank for storing a separation liquid from the dehydration apparatus and a desorption liquid from the MAP recovery apparatus;
A biological treatment tank for treating the separated liquid from the separated liquid storage tank;
A solid-liquid separation tank positioned downstream of the biological treatment tank;
An organic wastewater treatment apparatus comprising:
[8] Switching between a route for sending the mixed sludge from the mixing tank to the coagulation reaction tank and a bypass route for sending the mixed sludge from the mixing tank directly to the dehydrator without passing through the coagulation reaction tank A first switching valve to perform;
A second switching valve for switching between a route for sending the first separation liquid from the dehydration device to the separation liquid storage tank and a route for sending the second separation liquid from the dehydration device to the MAP recovery device;
The organic wastewater treatment apparatus according to [7], wherein the first switching valve and the second switching valve are interlocked.
[9] The dehydrator
A screen that acts as a concentrator for mixed sludge to which a polymer flocculant has been added, and that acts as a separator for mixed sludge to which no polymer flocculant has been added,
A dehydrator located downstream of the screen;
[7] or [8] further comprising a switching valve for switching between a path for separately sending the separated water from the screen and the separated water from the dehydrator to the path for sending to the MAP recovery device and the path for sending to the separation liquid storage tank. ] The organic waste water treatment apparatus as described in.
[10] The dehydrating apparatus includes a concentrating unit functioning as a screen, and a pressing unit at a subsequent stage of the concentrating unit, and separately separates the separated water from the concentrating unit and the separated water from the pressing unit. The organic wastewater treatment apparatus according to [7] or [8], further comprising a switching valve that switches between a route to be sent to the recovery device and a route to be sent to the separation liquid storage tank.
[11] In the agglomeration reaction tank,
A coagulant addition control mechanism for controlling the addition of the polymer coagulant to the coagulation reaction tank;
A drain pipe provided with an automatic valve that opens after the step of not adding the polymer flocculant;
Is an organic wastewater treatment apparatus according to any one of [7] to [10].
[12] Furthermore, a line mixer is provided between the mixing tank and the aggregation reaction tank, and a flocculant addition pipe for adding a polymer flocculant to the line mixer is connected. [7] to [11] The organic wastewater treatment apparatus according to any one of the above.
[13] In organic wastewater treatment for biological treatment after dewatering mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment,
A step of dehydrating the mixed sludge without adding a polymer flocculant to obtain a first separation liquid;
Adding a polymer flocculant to the mixed sludge and then dehydrating to obtain a second separation liquid;
Alternately
In the case of adding the polymer flocculant, a chemical fertilizer manufacturing method comprising a MAP recovery step of recovering magnesium ammonium phosphate (MAP) from the second separation liquid generated during the dehydration process .
[14] The step of dehydrating the mixed sludge without adding the polymer flocculant is 60% or less of the total time of the step of adding the polymer flocculant and the step of not adding the polymer flocculant. Of chemical fertilizer.
[15] The chemical fertilizer according to [13] or [14], wherein the first separated liquid obtained by dehydrating the mixed sludge without adding a polymer flocculant is used as a hydrogen donor in biological treatment. Manufacturing method.
[16] The dehydration treatment includes a concentration step of concentrating the mixed sludge added with the polymer flocculant, and a dehydration step of dehydrating the concentrated mixed sludge,
The method for producing a chemical fertilizer according to any one of [13] to [15], wherein the second separation liquid is obtained in the concentration step.
[17] The method for producing a chemical fertilizer according to [16], wherein an inorganic flocculant is further added to the concentrate obtained in the concentration step, and then dehydration is performed.
[18] The method for producing a chemical fertilizer according to [17], wherein the separation liquid after the dehydration treatment is used as a hydrogen donor in biological treatment.
[19] In organic wastewater treatment for biological treatment after dewatering mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment,
A mixing tank for mixing manure and / or organic sludge with surplus sludge from biological treatment;
A dehydrator positioned downstream of the mixing tank and dewatering the mixed sludge;
An agglomeration reaction tank that is positioned between the mixing tank and the dehydrator, and adds and aggregates the polymer flocculant to the mixed sludge from the mixing tank;
A bypass path for directly sending the mixed sludge from the mixing tank to the dehydrator without going through the agglomeration reaction tank;
A MAP recovery device for recovering magnesium ammonium phosphate (MAP) from the second separated liquid obtained by dehydrating the mixed sludge added with the polymer flocculant;
An apparatus for producing chemical fertilizer, comprising:
A separation liquid storage tank for storing a separation liquid from the dehydration apparatus and a desorption liquid from the MAP recovery apparatus;
A biological treatment tank for treating the separated liquid from the separated liquid storage tank;
A solid-liquid separation tank positioned downstream of the biological treatment tank;
[20] Switching between a route for sending the mixed sludge from the mixing tank to the coagulation reaction tank and a bypass route for sending the mixed sludge from the mixing tank directly to the dehydrator without passing through the coagulation reaction tank A first switching valve to perform;
A second switching valve for switching between a route for sending the first separation liquid from the dehydration device to the separation liquid storage tank and a route for sending the second separation liquid from the dehydration device to the MAP recovery device;
The chemical fertilizer manufacturing apparatus according to [19], wherein the first switching valve and the second switching valve are interlocked with each other.
[21] The dehydrator includes:
A screen that acts as a concentrator for mixed sludge to which a polymer flocculant has been added, and that acts as a separator for mixed sludge to which no polymer flocculant has been added,
A dehydrator located downstream of the screen;
[19] or [20], further comprising a switching valve for switching between a path for separately sending the separated water from the screen and the separated water from the dehydrator to the MAP recovery device and a path for sending the separated water to the separation liquid storage tank. ]. The chemical fertilizer manufacturing apparatus of description.
[22] The dehydrator includes a concentrating unit functioning as a screen, and a squeezing unit downstream of the concentrating unit, and separately separates the separated water from the concentrating unit and the separated water from the squeezing unit, respectively. The chemical fertilizer manufacturing apparatus according to [19] or [20], further comprising a switching valve that switches between a route to be sent to the recovery device and a route to be sent to the separation liquid storage tank.
[23] In the agglomeration reaction tank,
A coagulant addition control mechanism for controlling the addition of the polymer coagulant to the coagulation reaction tank;
A drain pipe provided with an automatic valve that opens after the step of not adding the polymer flocculant;
The apparatus for producing chemical fertilizer according to any one of [19] to [22], wherein:
[24] Further, a line mixer is provided between the mixing tank and the aggregation reaction tank, and a flocculant addition pipe for adding a polymer flocculant to the line mixer is connected. [19] to [23] The chemical fertilizer manufacturing apparatus of any one of Claims.
本発明の有機性廃水処理方法によれば、発生する脱水ケーキの低含水率化及び減容化を達成しながら、脱水処理に必要な凝集剤添加量及び生物処理に必要な水素供与体としての薬品添加量を削減することができるので、維持管理費を削減できると共に、化成肥料として有用なＭＡＰを効率的に回収することができる。 According to the organic wastewater treatment method of the present invention, while achieving a low water content and volume reduction of the dehydrated cake generated, the amount of flocculant added necessary for dehydration and the hydrogen donor necessary for biological treatment Since the amount of chemicals added can be reduced, maintenance costs can be reduced and MAP useful as a chemical fertilizer can be efficiently recovered.
図１に、本発明の有機性廃水の処理装置の概略と当該処理装置を用いた処理フローの概略を示す。
屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理するための有機性廃水処理装置は、屎尿及び／又は有機性汚泥と、生物処理からの余剰汚泥とを混合する混合槽１０と、混合槽１０の下流に位置づけられている混合汚泥を脱水する脱水装置４０と、混合槽１０と脱水装置４０の間に位置づけられている混合槽１０からの混合汚泥に凝集剤を添加して凝集させる凝集反応槽２０と、混合槽１０から凝集反応槽２０へ混合汚泥を送る経路３０と、混合槽１０から凝集反応槽２０を経由せずに脱水装置４０に混合汚泥を直接送るバイパス経路３０Ａと、脱水装置４０からの分離液を貯留する分離液貯留槽５０と、分離液貯留槽５０からの分離液を処理する生物処理槽６０と、生物処理槽６０の下流に位置づけられている固液分離槽６１と、脱水装置４０からの凝集剤を添加した混合汚泥を脱水して得られる第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収するＭＡＰ回収装置８０と、を具備する。
In FIG. 1, the outline of the processing apparatus of the organic wastewater of this invention and the outline of the processing flow using the said processing apparatus are shown.
Organic wastewater treatment equipment for biological treatment after dehydration of mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment includes human waste and / or organic sludge and biological treatment A mixing tank 10 that mixes excess sludge from the mixing tank 10, a dehydrator 40 that dehydrates the mixed sludge located downstream of the mixing tank 10, and a mixing tank 10 that is positioned between the mixing tank 10 and the dehydrator 40. Dehydration without adding the agglomeration agent 20 to the agglomeration reaction tank 20 from the mixing tank 10 to the agglomeration reaction tank 20, a route 30 for sending the mixed sludge from the agitation tank 10 to the agglomeration reaction tank 20. 30 A of bypass paths which send mixed sludge directly to the apparatus 40, the separation liquid storage tank 50 which stores the separation liquid from the dehydration apparatus 40, the biological treatment tank 60 which processes the separation liquid from the separation liquid storage tank 50, and biological treatment MAP recovery for recovering magnesium ammonium phosphate (MAP) from the solid-liquid separation tank 61 positioned downstream of 60 and the second separation liquid obtained by dehydrating the mixed sludge added with the flocculant from the dehydrator 40 Device 80.
混合槽１０は、屎尿及び浄化槽汚泥（有機性汚泥）を受け入れて貯留する中継槽であってもよいし、中継槽とは別に設けてもよい。
図１に示す装置では、バイパス経路３０Ａに混合汚泥を送るため、混合槽１０からの混合汚泥を凝集反応槽２０に送る経路３０との切り替えを行う第１切替弁Ｖ１、Ｖ２が経路３０及びバイパス経路３０Ａに設けられている。また、脱水装置４０からの第１分離液を分離液貯留槽５０に送る経路４０ａと、脱水装置４０からの第２分離液をＭＡＰ回収装置８０に送る経路４０ｂと、の切り替えを行う第２切替弁Ｖｐが脱水装置４０と分離貯留槽５０との間の経路４３に設けられている。なお、図１において第２切替弁Ｖｐは経路４０ａと４０ｂの両者に設けられているが、これらをまとめてＶｐとして説明する。
The mixing tank 10 may be a relay tank that receives and stores human waste and septic tank sludge (organic sludge), or may be provided separately from the relay tank.
In the apparatus shown in FIG. 1, in order to send the mixed sludge to the bypass path 30 </ b> A, the first switching valves V <b> 1 and V <b> 2 that perform switching with the path 30 that sends the mixed sludge from the mixing tank 10 to the aggregation reaction tank 20 include the path 30 and the bypass. It is provided in the path 30A. In addition, a second switching is performed to switch between a path 40a for sending the first separation liquid from the dehydration apparatus 40 to the separation liquid storage tank 50 and a path 40b for sending the second separation liquid from the dehydration apparatus 40 to the MAP recovery apparatus 80. A valve Vp is provided in a path 43 between the dehydrator 40 and the separation storage tank 50. In FIG. 1, the second switching valve Vp is provided in both the paths 40a and 40b, and these are collectively described as Vp.
図１の部分拡大図に示すように、脱水装置４０が濃縮用スクリーン４１と脱水機４２とを含む場合には、スクリーン４１からの分離液用配管４１ａに、ＭＡＰ回収装置８０に送る経路４０ｂと分離液貯留槽５０に送る経路４０ａとに切り替える切替弁Ｖｐ１及びＶｐ２が設けられている。 As shown in the partially enlarged view of FIG. 1, when the dehydrating device 40 includes a concentrating screen 41 and a dehydrating device 42, a path 40 b that is sent to the separation liquid pipe 41 a from the screen 41 to the MAP recovery device 80; Switching valves Vp <b> 1 and Vp <b> 2 that switch to the path 40 a that is sent to the separation liquid storage tank 50 are provided.
切替弁Ｖ１、Ｖ２、Ｖｐ、Ｖｐ１、Ｖｐ２としては、公知の自動切替弁を用いることができ、例えば、空気作動弁、電磁弁、電動弁などを用いることができる。切替弁Ｖ１、Ｖ２、Ｖｐ、Ｖｐ１、Ｖｐ２は連動しており、Ｖ１が「開」、Ｖ２が「閉」の場合にＶｐ又はＶｐ１及びＶｐ２は経路４０ｂに切り替え、Ｖ１が「閉」、Ｖ２が「開」の場合にＶｐ又はＶｐ１及びＶｐ２は経路４０ａに切り替える。 As the switching valves V1, V2, Vp, Vp1, and Vp2, known automatic switching valves can be used. For example, an air operated valve, an electromagnetic valve, an electric valve, or the like can be used. The switching valves V1, V2, Vp, Vp1, and Vp2 are interlocked. When V1 is “open” and V2 is “closed”, Vp or Vp1 and Vp2 are switched to the path 40b, and V1 is “closed” and V2 is In the case of “open”, Vp or Vp1 and Vp2 are switched to the path 40a.
脱水装置４０としては、通常の脱水機、たとえば遠心脱水機、ベルトプレス型脱水機、フィルタープレス型脱水機、スクリュープレス型脱水機、ロータリープレス型脱水機、電気浸透式脱水機などを用いることができる。特に、スクリュープレス脱水機は、低動力で低含水率を達成することができるので好ましい。スクリュープレス脱水機は、円筒形外筒の内部に、円筒形外筒と同心のスクリュー軸及びスクリュー羽根を備え、混合汚泥供給側の濃縮部と、円筒形外筒とスクリュー軸との間の空間が混合汚泥の進行方向に向かって次第に狭くなる脱水ケーキ排出側の圧搾部と、が形成されており、円筒形外筒に分離液排出用の複数の開孔を備える。軸摺動型スクリュープレス脱水機は、脱水汚泥出口方向と並行にスクリュー軸が移動し、脱水汚泥を強制排出する機構を有する。これらのスクリュープレス脱水機を用いることで、脱水ケーキの含水率を大幅に低下させることができる。また、スクリーン機能を奏する濃縮部を前段に含みスクリーンと脱水機とが一体化されている脱水装置ばかりでなく、独立したスクリーンと脱水機とを組み合わせてなる脱水装置を用いることもできる。 As the dehydrator 40, a normal dehydrator such as a centrifugal dehydrator, a belt press dehydrator, a filter press dehydrator, a screw press dehydrator, a rotary press dehydrator, an electroosmotic dehydrator, or the like may be used. it can. In particular, a screw press dehydrator is preferable because it can achieve a low water content with low power. The screw press dehydrator includes a screw shaft and screw blades concentric with the cylindrical outer cylinder inside the cylindrical outer cylinder, and a space between the concentrated portion on the mixed sludge supply side and the cylindrical outer cylinder and the screw shaft. Is formed with a pressing portion on the dewatered cake discharge side that gradually narrows in the traveling direction of the mixed sludge, and the cylindrical outer cylinder includes a plurality of openings for discharging the separated liquid. The shaft sliding screw press dehydrator has a mechanism for forcibly discharging dewatered sludge by moving the screw shaft in parallel with the direction of the dewatered sludge outlet. By using these screw press dehydrators, the moisture content of the dehydrated cake can be significantly reduced. Further, not only a dehydrator in which a concentrating unit having a screen function is included in the previous stage and the screen and the dehydrator are integrated, but also a dehydrator in which an independent screen and a dehydrator are combined can be used.
図１に示す装置では、脱水装置４０は、凝集剤添加混合汚泥Ａに対しては濃縮機として作用し、凝集剤無添加混合汚泥Ｂに対してはしさ分離機として作用するスクリーン４１と、スクリーン４１の下流に位置づけられている脱水機４２と、を含む。スクリーン４１からの分離液を送る経路４１ａには、ＭＡＰ回収装置８０に送る経路４０ｂ又は脱水機４２からの分離液を分離液貯留槽５０に送る経路４３のいずれかに切り替える切替弁Ｖｐ１及びＶｐ２が設けられている。 In the apparatus shown in FIG. 1, the dehydrator 40 acts as a concentrator for the flocculant-added mixed sludge A, and acts as a shear separator for the flocculant-free mixed sludge B, 41, and a dehydrator 42 positioned downstream of 41. In the path 41a for sending the separation liquid from the screen 41, switching valves Vp1 and Vp2 for switching to either the path 40b for sending to the MAP recovery device 80 or the path 43 for sending the separation liquid from the dehydrator 42 to the separation liquid storage tank 50 are provided. Is provided.
スクリーン４１は、目幅０．７〜６ｍｍを有することが好ましい。目幅が広すぎると、小さな夾雑物を除去できないため、しさ分離機として機能しない。目幅が狭すぎると、目詰まりにより流量負荷が過剰になる。スクリーンとしては、回転式、重力式、加圧式などの通常のスクリーンを用いることができる。 The screen 41 preferably has a mesh width of 0.7 to 6 mm. If the width of the mesh is too wide, small impurities cannot be removed, so it will not function as a thickness separator. If the mesh width is too narrow, the flow load becomes excessive due to clogging. As the screen, a normal screen such as a rotary type, a gravity type, or a pressure type can be used.
凝集反応槽２０は、混合汚泥及び添加した高分子凝集剤を撹拌混合して、凝集フロックを形成できればよく、公知の撹拌装置を具備する槽を用いることもできる。混合汚泥と高分子凝集剤との混合は、混合汚泥の細部にまで高分子凝集剤を均一に分散させるために、撹拌することが好ましい。これにより、高分子凝集剤の添加量を削減でき、凝集汚泥が緻密になるため脱水処理後の脱水ケーキの含水率を低減できる。撹拌する手段としては、撹拌翼、シャフト、モーターから構成される通常の撹拌機を好適に挙げることができる。また、凝集反応槽２０の直前の配管にラインミキサ１１を組み込むこともできる。外部のモーターで回転させる撹拌翼を配管内に設けたラインミキサが好ましい。 The agglomeration reaction tank 20 only needs to form agglomeration floc by stirring and mixing the mixed sludge and the added polymer flocculant, and a tank equipped with a known agitation device can also be used. The mixed sludge and the polymer flocculant are preferably mixed in order to uniformly disperse the polymer flocculant in the details of the mixed sludge. Thereby, the addition amount of the polymer flocculant can be reduced, and the water content of the dehydrated cake after the dehydration treatment can be reduced because the aggregated sludge becomes dense. As a means for stirring, a normal stirrer composed of a stirring blade, a shaft, and a motor can be preferably exemplified. In addition, the line mixer 11 can be incorporated in the piping immediately before the agglomeration reaction tank 20. A line mixer in which a stirring blade rotated by an external motor is provided in the pipe is preferable.
凝集反応槽２０には、凝集反応槽２０へ高分子凝集剤を添加する凝集剤添加装置が設けられている。凝集剤添加装置は、通常用いられる薬注装置でよいが、凝集剤添加及び無添加の切り替えを行う制御機構を具備することが好ましい。 The agglomeration reaction tank 20 is provided with a flocculant addition device for adding a polymer flocculant to the agglomeration reaction tank 20. The flocculant addition device may be a commonly used chemical injection device, but preferably includes a control mechanism for switching between addition and no addition of the flocculant.
脱水装置４０にて分離された第１分離液を貯留する分離液貯留槽５０、生物処理槽６０及び固液分離槽６１は、通常の有機性廃水処理で用いられる装置でよい。分離液貯留槽５０には、ＭＡＰ回収装置８０からの脱離液及びプラント内の雑排水も送液され、後段の生物処理に送られるまで一定時間貯留される。分離液貯留槽５０は、分離液の組成変動を緩和するために、分離液を少なくとも０．５日間貯留できる容量を有することが好ましい。生物処理槽６０は、脱窒素処理、嫌気性処理又は好気性処理を行う装置であることが好ましい。生物処理槽６０及び後続の固液分離槽６１から生じる余剰汚泥を混合槽１０に戻す余剰汚泥送配管６２を具備する。また、固液分離槽６１からの汚泥を生物処理槽６０に戻す汚泥戻し配管６２Ａを設けてもよい。 The separation liquid storage tank 50, the biological treatment tank 60, and the solid-liquid separation tank 61 that store the first separation liquid separated by the dehydration apparatus 40 may be apparatuses used in ordinary organic wastewater treatment. The separation liquid storage tank 50 is also supplied with the desorbed liquid from the MAP recovery device 80 and miscellaneous wastewater in the plant, and is stored for a certain period of time until it is sent to the biological treatment at the subsequent stage. The separation liquid storage tank 50 preferably has a capacity capable of storing the separation liquid for at least 0.5 days in order to alleviate the composition fluctuation of the separation liquid. The biological treatment tank 60 is preferably a device that performs denitrification treatment, anaerobic treatment, or aerobic treatment. The surplus sludge feed pipe 62 for returning surplus sludge generated from the biological treatment tank 60 and the subsequent solid-liquid separation tank 61 to the mixing tank 10 is provided. Further, a sludge return pipe 62 </ b> A for returning sludge from the solid-liquid separation tank 61 to the biological treatment tank 60 may be provided.
脱水装置４０にて得られる含水率７０％以下の脱水ケーキは、堆肥及び助燃剤として再利用できるため、用途に応じて適宜振り分ける脱水汚泥振分コンベア７０を設けてもよい。 Since the dehydrated cake having a moisture content of 70% or less obtained by the dehydrator 40 can be reused as compost and a combustion aid, a dewatered sludge distribution conveyor 70 that appropriately sorts according to the use may be provided.
ＭＡＰ回収装置８０は、リン酸イオン、アンモニウムイオン及びマグネシウムイオンの反応によって生成するＭＡＰの晶析現象を利用して、リンとアンモニウムイオンを含む汚泥にマグネシウム源（塩化マグネシウム、水酸化マグネシウム等）を添加して、過飽和状態で種晶と接触させ、種晶表面にＭＡＰ回収を晶析させて回収する装置であり、マグネシウム源添加手段、ｐＨ調整剤添加手段を具備する従来公知の晶析反応槽を用いることができるが、高速処理を可能とする流動式が好ましい。ｐＨ調整剤添加手段は、ＭＡＰ回収装置８０に送られる第２分離液のｐＨをＭＡＰ晶析反応に適するｐＨ範囲７．５〜１０．０に調節するためにｐＨ調整剤を添加する手段であり、従来公知のものでよい。 The MAP recovery device 80 uses a MAP crystallization phenomenon generated by the reaction of phosphate ions, ammonium ions, and magnesium ions, and supplies a magnesium source (magnesium chloride, magnesium hydroxide, etc.) to sludge containing phosphorus and ammonium ions. Addition, contact with seed crystal in supersaturated state, MAP recovery is crystallized and recovered on the surface of the seed crystal, and a conventionally known crystallization reaction tank equipped with a magnesium source addition means and a pH adjuster addition means However, a fluid type capable of high-speed processing is preferable. The pH adjusting agent adding means is a means for adding a pH adjusting agent to adjust the pH of the second separated liquid sent to the MAP recovery device 80 to a pH range of 7.5 to 10.0 suitable for the MAP crystallization reaction. A conventionally known one may be used.
ＭＡＰ回収装置８０には、ＭＡＰ又は化成肥料を取り出す製品取出用配管８２、及びＭＡＰ又は化成肥料を取り出した後の脱離液を分離液貯留槽５０に送る脱離液用配管８１が設けられている。 The MAP recovery device 80 is provided with a product extraction pipe 82 for taking out MAP or chemical fertilizer, and a desorption liquid pipe 81 for sending the desorption liquid after taking out MAP or chemical fertilizer to the separation liquid storage tank 50. Yes.
図２は、本発明の有機性廃水装置の別の実施形態を示す。図１と同じ構成要素には同じ符号を付して、説明を省略する。
屎尿及び／又は有機性汚泥と、生物処理において発生する余剰汚泥と、の混合汚泥を脱水処理した後に、生物処理するための有機性廃水処理装置は、屎尿及び／又は有機性汚泥と、生物処理からの余剰汚泥とを混合する混合槽１０と、当該混合槽１０の下流に位置づけられ、混合汚泥を脱水する脱水装置４０と、当該混合槽１０と当該脱水装置４０の間に位置づけられ、当該混合槽１０からの当該混合汚泥に凝集剤を添加して凝集させる凝集反応槽２０Ａと、当該凝集反応槽２０Ａへの凝集剤の添加を制御する凝集剤添加制御機構と、当該脱水装置４０からの分離液を貯留する分離液貯留槽５０と、当該分離液貯留槽５０からの分離液を処理する生物処理槽６０と、生物処理槽６０の下流に位置づけられている固液分離槽６１と、脱水装置４０からの凝集剤を添加した混合汚泥を脱水して得られる第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収するＭＡＰ回収装置８０と、を具備する。図２に示す有機性廃水処理装置は、図１に示すバイパス経路３０Ａを含まず、凝集剤添加制御機構によって凝集剤の添加の有無が制御される。
FIG. 2 shows another embodiment of the organic wastewater device of the present invention. The same components as those in FIG. 1 are denoted by the same reference numerals, and description thereof is omitted.
Organic wastewater treatment equipment for biological treatment after dehydration of mixed sludge of manure and / or organic sludge and surplus sludge generated in biological treatment includes human waste and / or organic sludge and biological treatment The mixing tank 10 that mixes the excess sludge from the above, the dehydrator 40 that is located downstream of the mixing tank 10 and dehydrates the mixed sludge, and is positioned between the mixing tank 10 and the dehydrator 40, and the mixing Aggregation reaction tank 20A for adding and coagulating the flocculant to the mixed sludge from the tank 10, a flocculant addition control mechanism for controlling the addition of the flocculant to the aggregation reaction tank 20A, and separation from the dehydrator 40 A separation liquid storage tank 50 for storing liquid, a biological treatment tank 60 for processing a separation liquid from the separation liquid storage tank 50, a solid-liquid separation tank 61 positioned downstream of the biological treatment tank 60, and a dehydrator 4 The MAP recovery device 80 for recovering the magnesium ammonium phosphate (MAP) mixing the sludge with added flocculant from the second separated liquid obtained by dehydration of, comprising a. The organic wastewater treatment apparatus shown in FIG. 2 does not include the bypass path 30A shown in FIG. 1, and the presence / absence of addition of the flocculant is controlled by the flocculant addition control mechanism.
凝集反応槽２０Ａには、凝集剤を添加しない工程の後に開放する自動弁Ｖ３が設けられているドレン配管２１が接続されている。ドレン配管２１は、混合槽１０に接続されている。なお、ドレン配管２１を設けなくてもよい。 The agglomeration reaction tank 20A is connected to a drain pipe 21 provided with an automatic valve V3 that is opened after the step of not adding the aggregating agent. The drain pipe 21 is connected to the mixing tank 10. The drain pipe 21 may not be provided.
次に、図１に示すフローを用いて、本発明の有機性廃水処理方法を説明する。
処理対象となる有機性廃水は、屎尿及び／又は浄化槽汚泥（有機性汚泥）を含む。通常、屎尿及び浄化槽汚泥は、トイレットペーパーなどの夾雑物を含有しており、まず破砕処理が行われる。従来は、破砕後の夾雑物を除去する前処理が行われていたが、最近では前処理を行わず夾雑物を含有したままの屎尿及び浄化槽汚泥を処理することも行われている。本発明では、夾雑物の含有の有無、屎尿と浄化槽汚泥との混合比率、及び破砕の程度及び有無にかかわらず、屎尿及び／又は浄化槽汚泥を含む有機性廃水を処理対象とすることができる。
Next, the organic wastewater treatment method of the present invention will be described using the flow shown in FIG.
The organic wastewater to be treated includes manure and / or septic tank sludge (organic sludge). Usually, urine and septic tank sludge contain impurities such as toilet paper, and are first crushed. Conventionally, pretreatment for removing the crushed contaminants has been performed, but recently, pretreatment is not performed and the sewage and septic tank sludge containing impurities are also treated. In the present invention, it is possible to treat organic wastewater containing manure and / or septic tank sludge regardless of the presence or absence of impurities, the mixing ratio of manure and septic tank sludge, and the degree and presence of crushing.
有機性廃水は、混合槽１０において、生物処理により発生する余剰汚泥と混合されて、混合汚泥となる。次いで、混合汚泥は、経路３０を経由して凝集反応槽２０に送られ、高分子凝集剤と撹拌混合され、凝集フロックが形成されて凝集剤添加汚泥Ａとなる。凝集剤添加汚泥Ａは、脱水装置４０に送られ、スクリーン４１で濃縮され、さらに脱水機４２で脱水されて、第２分離液と脱水ケーキとに分けられる。第２分離液は、ＭＡＰ回収装置８０に送られる。ＭＡＰ回収装置８０では、通常のＭＡＰ回収と同様に、マグネシウム源が添加された後、晶析法によりＭＡＰを析出させて沈殿物を回収する。回収されたＭＡＰは化成肥料として再利用することができる。 The organic wastewater is mixed with surplus sludge generated by biological treatment in the mixing tank 10 to become mixed sludge. Next, the mixed sludge is sent to the agglomeration reaction tank 20 via the path 30 and is stirred and mixed with the polymer flocculant to form an agglomerate floc and become the flocculant-added sludge A. The flocculant-added sludge A is sent to the dewatering device 40, concentrated by the screen 41, further dehydrated by the dehydrator 42, and divided into the second separated liquid and the dewatered cake. The second separation liquid is sent to the MAP recovery device 80. In the MAP recovery device 80, in the same manner as in the normal MAP recovery, after the magnesium source is added, MAP is precipitated by a crystallization method and the precipitate is recovered. The collected MAP can be reused as a chemical fertilizer.
凝集剤としてさらに無機凝集剤を混合汚泥に添加してもよい。この場合には、スクリーン４１の下流側末端で無機凝集剤を添加する。無機凝集剤を添加した場合は、スクリーン４１からの分離液だけを第２分離液としてＭＡＰ回収装置８０に送り、脱水機４２からの分離液は第１分離液として分離液貯留槽５０に送る。 An inorganic flocculant may be further added to the mixed sludge as a flocculant. In this case, an inorganic flocculant is added at the downstream end of the screen 41. When the inorganic flocculant is added, only the separation liquid from the screen 41 is sent to the MAP recovery device 80 as the second separation liquid, and the separation liquid from the dehydrator 42 is sent to the separation liquid storage tank 50 as the first separation liquid.
一方、バイパス経路３０Ａを経由して、高分子凝集剤の添加なしに脱水装置４０に送られる混合汚泥は、スクリーン４１でしさ分離され、脱水機４２で脱水されて、第１分離液と脱水ケーキとに分けられる。第１分離液は、分離液貯留槽５０に所定時間貯留された後、生物処理槽６０に送られ、生物処理された後、固液分離槽６１で固液分離される。固液分離された水は浄化水として放流されるか又はさらに高度処理に供された後に放流される。固液分離された汚泥は、返送汚泥として生物処理槽６０に戻され、余剰汚泥は有機性廃水との混合に使用するため混合槽１０に送られる。 On the other hand, the mixed sludge sent to the dehydrator 40 without addition of the polymer flocculant via the bypass path 30A is separated by the screen 41 and dehydrated by the dehydrator 42, and the first separated liquid and the dehydrated cake. And divided. The first separation liquid is stored in the separation liquid storage tank 50 for a predetermined period of time, then sent to the biological treatment tank 60, subjected to biological treatment, and then solid-liquid separated in the solid-liquid separation tank 61. The solid-liquid separated water is discharged as purified water or discharged after being subjected to advanced treatment. The solid-liquid separated sludge is returned to the biological treatment tank 60 as return sludge, and the excess sludge is sent to the mixing tank 10 for use in mixing with organic waste water.
図２に示すフローでは、屎尿及び／又は有機性汚泥は、生物処理槽６０及び固液分離槽６１から余剰汚泥送配管６２を経由して供給される余剰汚泥と、混合槽１０にて混合される。混合汚泥は、経路３０を介して凝集反応槽２０Ａに送られる。 In the flow shown in FIG. 2, manure and / or organic sludge is mixed in the mixing tank 10 with surplus sludge supplied from the biological treatment tank 60 and the solid-liquid separation tank 61 via the surplus sludge feed pipe 62. The The mixed sludge is sent to the agglomeration reaction tank 20A via the path 30.
凝集反応槽２０Ａにて高分子凝集剤が添加されなかった混合汚泥は、脱水装置４０に送られる。混合汚泥は、スクリーン４１でしさ分が除去され、脱水機４２で脱水されて、第１分離液と脱水ケーキとに分けられる。第１分離液は、分離液貯留槽５０に所定時間貯留された後、生物処理槽６０に送られ、生物処理された後、固液分離槽６１で固液分離される。固液分離された水は浄化水として放流されるか又はさらに高度処理に供された後に放流される。固液分離された汚泥は、返送汚泥として生物処理槽６０に戻され、余剰汚泥は有機性廃水との混合に使用するため混合槽１０に送られる。 The mixed sludge to which the polymer flocculant has not been added in the aggregation reaction tank 20 </ b> A is sent to the dehydrator 40. The mixed sludge is removed by the screen 41, dehydrated by the dehydrator 42, and divided into the first separated liquid and the dehydrated cake. The first separation liquid is stored in the separation liquid storage tank 50 for a predetermined period of time, then sent to the biological treatment tank 60, subjected to biological treatment, and then solid-liquid separated in the solid-liquid separation tank 61. The solid-liquid separated water is discharged as purified water or discharged after being subjected to advanced treatment. The solid-liquid separated sludge is returned to the biological treatment tank 60 as return sludge, and the excess sludge is sent to the mixing tank 10 for use in mixing with organic waste water.
次いで、凝集反応槽２０Ａで高分子凝集剤が添加されなかった混合汚泥の残りは、ドレン弁Ｖ３を開放してドレン２１から抜き出され、混合槽１０に戻され、新たに供給される屎尿及び／又は有機性汚泥と新たな余剰汚泥がさらに添加されて、再び凝集反応槽２０Ａに送られる。凝集反応槽２０Ａにて凝集剤が添加され、凝集剤添加汚泥Ａが形成される。このとき、ドレン弁Ｖ３は閉じられており、凝集剤添加汚泥Ａは脱水装置４０に送られる。凝集剤添加汚泥Ａは、スクリーン４１で濃縮され、脱水機４２で脱水されて、第２分離液と脱水ケーキとに分けられる。第２分離液は、ＭＡＰ回収装置８０に送られる。ＭＡＰ回収装置８０では、通常のＭＡＰ回収と同様に、マグネシウム源が添加された後、晶析法によりＭＡＰを析出させて沈殿物を回収する。回収されたＭＡＰは化成肥料として再利用することができる。なお、凝集剤として無機凝集剤を添加する場合は、図１に示す装置における場合と同様に、スクリーン４１の下流側末端で無機凝集剤を添加し、無機凝集剤が添加されていないスクリーン４１からの分離液だけをＭＡＰ回収装置８０に送る。 Next, the remainder of the mixed sludge to which the polymer flocculant has not been added in the flocculation reaction tank 20A is extracted from the drain 21 by opening the drain valve V3, returned to the mixing tank 10, and newly supplied urine and / Organic sludge and new surplus sludge are further added and sent again to the agglomeration reaction tank 20A. In the flocculation reaction tank 20A, the flocculating agent is added, and the flocculating agent added sludge A is formed. At this time, the drain valve V3 is closed, and the flocculant-added sludge A is sent to the dehydrator 40. The flocculant-added sludge A is concentrated by the screen 41, dehydrated by the dehydrator 42, and divided into the second separated liquid and the dehydrated cake. The second separation liquid is sent to the MAP recovery device 80. In the MAP recovery device 80, in the same manner as in the normal MAP recovery, after the magnesium source is added, MAP is precipitated by a crystallization method and the precipitate is recovered. The collected MAP can be reused as a chemical fertilizer. When adding an inorganic flocculant as the flocculant, as in the case of the apparatus shown in FIG. 1, the inorganic flocculant is added at the downstream end of the screen 41, and the screen 41 to which no inorganic flocculant is added is added. Only the separated liquid is sent to the MAP recovery device 80.
図１及び図２に示す装置においては、脱水装置４０として、スクリーン４１と脱水機４２との組み合わせを用いているが、前段の濃縮部と後段の圧搾部とを一体化してなるスクリュープレス型脱水機を用いることもできる。この場合は、濃縮部がスクリーン４１に相当し、圧搾部が脱水機４２に相当する。高分子凝集剤が添加された場合には、濃縮部及び圧搾部からの分離液を第２分離液としてＭＡＰ回収装置８０に送る。高分子凝集剤に加えて無機凝集剤が添加される場合には、無機凝集剤は濃縮部の後、圧搾部の前で添加される。濃縮部からの分離液が第２分離液としてＭＡＰ回収装置８０に送られる。高分子凝集剤が添加されなかった場合には、濃縮部からの分離液及び圧搾部からの分離液を第１分離液として分離液貯留槽５０及び後段の生物処理槽６０に送る。 In the apparatus shown in FIGS. 1 and 2, a combination of a screen 41 and a dehydrator 42 is used as the dehydrating apparatus 40, but a screw press type dehydration formed by integrating a pre-concentration part and a post-squeezing part. A machine can also be used. In this case, the concentration unit corresponds to the screen 41 and the pressing unit corresponds to the dehydrator 42. When the polymer flocculant is added, the separation liquid from the concentration part and the pressing part is sent to the MAP recovery device 80 as the second separation liquid. When an inorganic flocculant is added in addition to the polymer flocculant, the inorganic flocculant is added after the concentration part and before the pressing part. The separation liquid from the concentration unit is sent to the MAP recovery device 80 as the second separation liquid. When the polymer flocculant is not added, the separation liquid from the concentrating part and the separation liquid from the pressing part are sent as the first separation liquid to the separation liquid storage tank 50 and the biological treatment tank 60 in the subsequent stage.
図１及び図２に示す装置において、混合槽１０にて形成される混合汚泥を凝集反応槽２０又は２０Ａに送る経路３０に、ラインミキサ１１を設けてもよい。混合汚泥には、ラインミキサ１１にて高分子凝集剤が添加され、さらに凝集反応槽２０又は２０Ａにて高分子凝集剤が添加される。ラインミキサにおける高分子凝集剤の添加量は、処理すべき有機性廃水の性状によっても異なるが、ラインミキサ１１にて添加される高分子凝集剤は、凝集反応槽にて添加される高分子凝集剤と同等量以上であることが好ましい。ラインミキサにおける高分子凝集剤の添加がない場合（すなわち、凝集反応槽２０又は２０Ａでの高分子凝集剤の添加のみ）と、ラインミキサにおける高分子凝集剤の添加がある場合（すなわち、ラインミキサ１１と凝集反応槽２０又は２０Ａでの高分子凝集剤の添加）との高分子凝集剤の総添加量は、ほぼ同等量とすることができる。ラインミキサ１１と凝集反応槽２０又は２０Ａで高分子凝集剤を添加する場合には、無機凝集剤を使用せずに、高分子凝集剤と無機凝集剤との併用の場合と同等の脱水効果を得ることができる。ラインミキサ１１での高分子凝集剤の添加及び混合によって、混合汚泥と高分子凝集剤とは、より一層均一に混合される。 In the apparatus shown in FIGS. 1 and 2, the line mixer 11 may be provided in a path 30 for sending the mixed sludge formed in the mixing tank 10 to the aggregation reaction tank 20 or 20A. A polymer flocculant is added to the mixed sludge by the line mixer 11, and further the polymer flocculant is added by the agglomeration reaction tank 20 or 20A. The addition amount of the polymer flocculant in the line mixer varies depending on the properties of the organic waste water to be treated, but the polymer flocculant added in the line mixer 11 is polymer agglomeration added in the agglomeration reaction tank. The amount is preferably equal to or greater than the agent. When there is no addition of the polymer flocculant in the line mixer (that is, only addition of the polymer flocculant in the agglomeration reaction tank 20 or 20A) and when there is addition of the polymer flocculant in the line mixer (that is, the line mixer) 11 and the addition of the polymer flocculant in the agglomeration reaction tank 20 or 20A) can be made substantially equal. When a polymer flocculant is added in the line mixer 11 and the flocculence reaction tank 20 or 20A, an inorganic flocculant is not used, and a dehydration effect equivalent to that in the case of the combined use of the polymer flocculant and the inorganic flocculant is achieved. Can be obtained. By adding and mixing the polymer flocculant in the line mixer 11, the mixed sludge and the polymer flocculant are mixed more uniformly.
上述のように、本発明においては、有機性廃水と余剰汚泥との混合汚泥に高分子凝集剤を添加せずに直接脱水処理する工程を含む。高分子凝集剤の添加と無添加とは任意の長さの時間で交互に行われる。高分子凝集剤無添加の総時間は、高分子凝集剤添加時間との合計の６０％以下、好ましくは４０％以下、特に好ましくは２０％以下とする。６０％を越えると、余剰汚泥発生量が多くなり、混合汚泥中の余剰汚泥の比率が多くなるため、脱水ケーキの低含水率化及び脱水ケーキの減容化が達成されない。高分子凝集剤使用量の削減効果を得るためには、高分子凝集剤無添加の総時間は１％以上とすることが好ましく、５％以上がより好ましい。 As described above, the present invention includes a step of directly dehydrating the mixed sludge of organic waste water and excess sludge without adding a polymer flocculant. Addition and non-addition of the polymer flocculant are alternately performed for an arbitrary length of time. The total time without addition of the polymer flocculant is 60% or less, preferably 40% or less, particularly preferably 20% or less of the total time with the polymer flocculant addition time. If it exceeds 60%, the amount of surplus sludge generated increases, and the ratio of surplus sludge in the mixed sludge increases, so that the moisture content of the dehydrated cake and the volume reduction of the dehydrated cake cannot be achieved. In order to obtain the effect of reducing the amount of the polymer flocculant used, the total time without addition of the polymer flocculant is preferably 1% or more, and more preferably 5% or more.
また、本発明においては、高分子凝集剤を添加した場合には、凝集剤添加汚泥Ａを脱水して得られる第２分離液をＭＡＰ回収に送液し、ＭＡＰを回収して化成肥料を製造する。高分子凝集剤を添加しない場合には、混合汚泥中のＳＳ分が多すぎて、ＭＡＰ回収装置が閉塞してしまうため、凝集剤無添加汚泥Ｂを脱水して得られる第１分離液はＭＡＰ回収に送ることを回避する。また、凝集剤無添加汚泥Ｂは、有機物を豊富に含むため、後続の生物処理に送り、微生物の栄養素となる水素供与体として利用する。 In the present invention, when a polymer flocculant is added, the second separation liquid obtained by dewatering the flocculant-added sludge A is sent to MAP recovery, and MAP is recovered to produce a chemical fertilizer. To do. When the polymer flocculant is not added, the mixed sludge contains too much SS and the MAP recovery device is blocked. Therefore, the first separation liquid obtained by dewatering the flocculant-free sludge B is MAP. Avoid sending to collection. Moreover, since the flocculant-free sludge B contains abundant organic substances, it is sent to the subsequent biological treatment and used as a hydrogen donor that becomes a nutrient of microorganisms.
高分子凝集剤の添加及び無添加の時間の長さ及び切り替えのタイミングは、生物処理の状態や混合汚泥の性状によって設定することができる。たとえば、屎尿及び／又は有機性汚泥中の水素供与体が多い場合は、凝集剤無添加汚泥Ｂが少量であっても生物処理に必要な栄養素を提供することができるため、高分子凝集剤の添加時間を長くしてもよい。この場合、ＭＡＰ回収処理に送る第２分離液の量が増えるため、ＭＡＰ回収すなわち化成肥料の製造量を増やすことができる。 The length of time of addition and non-addition of the polymer flocculant and the switching timing can be set according to the state of biological treatment and the properties of the mixed sludge. For example, when there is a large amount of hydrogen donor in human waste and / or organic sludge, nutrients necessary for biological treatment can be provided even with a small amount of flocculant-free sludge B. The addition time may be lengthened. In this case, since the amount of the second separation liquid to be sent to the MAP recovery process increases, the amount of MAP recovery, that is, the production of chemical fertilizer can be increased.
高分子凝集剤の添加及びＭＡＰ回収経路への切り替えの例を図３に示す。なお、図３に示す凝集剤は高分子凝集剤である。無機凝集剤を添加する場合は、高分子凝集剤の添加のタイミングに合わせて、脱水装置４０にて行う。 An example of addition of the polymer flocculant and switching to the MAP recovery route is shown in FIG. The flocculant shown in FIG. 3 is a polymer flocculant. When adding an inorganic flocculant, it is performed by the dehydrator 40 in accordance with the timing of addition of the polymer flocculant.
図３は凝集剤添加時間と無添加時間を任意の異なる長さに設定して交互に行う場合のタイムチャートである。図３（１）〜（３）は、凝集剤添加の切り替えは、図１に示す切替弁Ｖ１、Ｖ２の開閉をタイマー設定により自動的に切り替え、バイパス経路３０Ａを利用して行われる。ＭＡＰ回収経路への切り替えは、切替弁Ｖｐ又はＶｐ１及びＶｐ２を切替弁Ｖ１に連動させ、凝集剤添加汚泥Ａが脱水処理されるタイミングに合わせて切替弁Ｖｐ又はＶｐ１及びＶｐ２を作動させて行う。 FIG. 3 is a time chart in the case where the flocculant addition time and the non-addition time are set alternately at different lengths. 3 (1) to 3 (3), the switching of the flocculant addition is automatically performed by switching the switching valves V1 and V2 shown in FIG. 1 according to the timer setting and using the bypass path 30A. Switching to the MAP recovery path is performed by operating the switching valves Vp or Vp1 and Vp2 in synchronization with the timing at which the flocculant-added sludge A is dehydrated by interlocking the switching valves Vp or Vp1 and Vp2 with the switching valve V1.
図３（４）〜（６）は、切替弁Ｖ１、Ｖ２及びバイパス経路３０Ａを使用せずに、凝集剤添加制御機構を有する凝集反応槽２０Ａへの高分子凝集剤の添加及び無添加を交互に行う場合のタイムチャートである。高分子凝集剤の添加は、凝集剤添加装置のＯＮ／ＯＦＦをタイマー設定により自動的に切り替えることで行うことができる。ＭＡＰ回収経路への切り替えは、凝集剤添加装置のＯＮ／ＯＦＦタイマーに連動させ、凝集剤添加汚泥Ａが脱水処理されるタイミングに合わせて切替弁Ｖｐ又はＶｐ１及びＶｐ２を作動させて行う。 3 (4) to (6) show that the addition of the polymer flocculant and the non-addition of the polymer flocculant to the agglomeration reaction tank 20A having the flocculant addition control mechanism are alternately performed without using the switching valves V1, V2 and the bypass path 30A. It is a time chart in the case of performing to. The addition of the polymer flocculant can be performed by automatically switching ON / OFF of the flocculant addition apparatus by a timer setting. Switching to the MAP recovery path is performed by operating the switching valve Vp or Vp1 and Vp2 in synchronization with the timing at which the flocculant added sludge A is dehydrated in conjunction with the ON / OFF timer of the flocculant adding device.
図３（７）〜（９）は、図２に示す処理装置において、切替弁Ｖ１、Ｖ２及びバイパス経路３０Ａを使用せずに、ドレン弁Ｖ３の開閉調節及び凝集剤添加制御機構を有する凝集反応槽２０Ａへの高分子凝集剤の添加の有無を切り替える場合のタイムチャートである。ドレン弁Ｖ３の開放は、凝集反応槽２０Ａへの高分子凝集剤無添加の後に行うことが好ましい。 FIGS. 3 (7) to (9) show the agglomeration reaction in the processing apparatus shown in FIG. 2 that has an open / close adjustment of the drain valve V3 and a coagulant addition control mechanism without using the switching valves V1, V2 and the bypass path 30A. It is a time chart in the case of switching the presence or absence of addition of the polymer flocculant to the tank 20A. The drain valve V3 is preferably opened after the addition of the polymer flocculant to the aggregation reaction tank 20A.
図３（１）〜（９）のいずれにおいても、切替弁Ｖｐ又はＶｐ１及びＶｐ２のＭＡＰ回収装置８０への切り替えは、凝集剤添加汚泥Ａを脱水処理するタイミングに合わせて行う。 In any of FIGS. 3 (1) to 3 (9), the switching valve Vp or Vp1 and Vp2 is switched to the MAP recovery device 80 in accordance with the timing of dewatering the flocculant-added sludge A.
なお、ラインミキサ１１を具備する装置の場合、高分子凝集剤添加のタイミングは、凝集反応槽２０Ａへの添加のタイミングと同時である。
後続の脱水処理により含水率７０％以下の脱水ケーキを得るためには、高分子凝集剤を添加しない時間は、高分子凝集剤を添加する時間と無添加の時間との合計の６０％以下とする。高分子凝集剤を添加しないことにより、有機性廃水中に含まれる有機成分（水素供与体）が脱水処理後の分離液に含まれるため、生物処理に必要な水素供与体（微生物の栄養源）の追加供給を削減することができる。凝集剤の添加と無添加とを交互に行うことにより生じる分離液中有機成分量の変動は、分離液貯留槽５０での貯留時間を例えば０．５日以上と長期化することで、相殺することができる。
In the case of an apparatus equipped with the line mixer 11, the timing of addition of the polymer flocculant is the same as the timing of addition to the aggregation reaction tank 20A.
In order to obtain a dehydrated cake having a water content of 70% or less by the subsequent dehydration treatment, the time during which the polymer flocculant is not added is 60% or less of the total of the time during which the polymer flocculant is added and the time when no polymer flocculant is added. To do. By not adding a polymer flocculant, the organic component (hydrogen donor) contained in the organic wastewater is contained in the separated liquid after dehydration treatment, so the hydrogen donor required for biological treatment (microbe nutrient source) The additional supply of can be reduced. The fluctuation in the amount of organic components in the separation liquid caused by alternately adding and not adding the flocculant is offset by extending the storage time in the separation liquid storage tank 50 to, for example, 0.5 days or longer. be able to.
凝集反応槽に添加される凝集剤は、高分子凝集剤である。特にラインミキサを具備する装置を用いる場合には、ラインミキサ及び凝集反応槽に高分子凝集剤のみを添加することができる。脱水効率を向上させるために、高分子凝集剤と無機凝集剤とを併用する場合は、凝集反応槽２０又は２０Ａにて高分子凝集剤を添加した後に、脱水装置４０にて脱水される直前、好ましくは濃縮機スクリーン４１の下流側末端にて、汚泥に無機凝集剤を添加することが好ましい。高分子凝集剤を先に添加して無機凝集剤を後で添加することにより、脱水性能が向上し、高分子凝集剤の添加量を削減することができる。 The flocculant added to the flocculation reaction tank is a polymer flocculant. In particular, when using an apparatus equipped with a line mixer, only the polymer flocculant can be added to the line mixer and the agglomeration reaction tank. When using a polymer flocculant and an inorganic flocculant in combination to improve the dehydration efficiency, after adding the polymer flocculant in the aggregation reaction tank 20 or 20A, immediately before being dehydrated in the dehydrator 40, Preferably, an inorganic flocculant is added to the sludge at the downstream end of the concentrator screen 41. By adding the polymer flocculant first and adding the inorganic flocculant later, the dewatering performance is improved, and the amount of the polymer flocculant added can be reduced.
高分子凝集剤としては、カチオン系高分子凝集剤、両性高分子凝集剤等が挙げられる。カチオン性高分子凝集剤としては、ジメチルアミノエチルアクリレートの四級化物の重合物、ジメチルアミノエチルアクリレートの四級化物とアクリルアミドとの共重合物などのアクリレート系高分子凝集剤；ジメチルアミノエチルメタクリレートの四級化物の重合物、ジメチルアミノエチルメタクリレートの四級化物とアクリルアミドとの共重合物などのメタクリレート系高分子凝集剤；アミド基、ニトリル基、アミン塩酸塩、ホルムアミド基等を含むポリビニルアミジン；ポリアクリルアミドのマンニッヒ変性物などが挙げられ、例えば市販のエバグロース（水ｉｎｇ株式会社 登録商標）シリーズを用いることができる。両性高分子凝集剤としては、ジメチルアミノメチルアクリレートの四級化物とアクリルアミドとアクリル酸との共重合物、ジメチルアミノメチルメタクリレートの四級化物とアクリルアミドとアクリル酸との共重合物などをあげることができる。高分子凝集剤の添加量は、混合汚泥の性状などによっても異なるが、汚泥中の固形物乾燥重量（ＤＳ）に対して０．５〜３．０ｗｔ％であることが好ましく、１．０〜２．５ｗｔ％であることがより好ましい。 Examples of the polymer flocculant include cationic polymer flocculants and amphoteric polymer flocculants. Cationic polymer flocculants include acrylate-based polymer flocculants such as dimethylaminoethyl acrylate quaternized polymer, dimethylaminoethyl acrylate quaternized acrylamide copolymer, and dimethylaminoethyl methacrylate. Methacrylate-based polymer flocculants such as quaternized polymers, dimethylaminoethyl methacrylate quaternized products and acrylamide copolymers; polyvinylamidines containing amide groups, nitrile groups, amine hydrochlorides, formamide groups, etc .; poly Examples include Mannich modified products of acrylamide. For example, commercially available Ebagulose (registered trademark of Mizuing Inc.) series can be used. Examples of the amphoteric polymer flocculants include dimethylaminomethyl acrylate quaternized products of acrylamide and acrylic acid, dimethylaminomethyl methacrylate quaternized products of acrylamide and acrylic acid, and the like. it can. The addition amount of the polymer flocculant varies depending on the properties of the mixed sludge, but is preferably 0.5 to 3.0 wt% with respect to the solid dry weight (DS) in the sludge, and is 1.0 to More preferably, it is 2.5 wt%.
また、高分子凝集剤の凝集力を低下させることなく、混合汚泥に均一に分散させ、混合汚泥の細部にまで浸透させ、混合汚泥の表面電荷の中和と、高分子の吸着又は架橋作用による凝集とを同時に行わせるため、混合汚泥と凝集剤とを１０００回転／分以上の撹拌翼の回転数で撹拌することが好ましい。 Moreover, without reducing the cohesive force of the polymer flocculant, uniformly disperse it in the mixed sludge, penetrate into the details of the mixed sludge, neutralize the surface charge of the mixed sludge, and adsorb or crosslink the polymer In order to perform coagulation simultaneously, it is preferable to stir the mixed sludge and the coagulant at a rotation speed of a stirring blade of 1000 rotations / minute or more.
無機凝集剤としては、ポリ硫酸第二鉄、ポリ塩化第二鉄、塩化第二鉄、硫酸アルミニウム、塩化アルミニウム、ポリ塩化アルミニウムを好ましく用いることができる。中でもポリ硫酸第二鉄が特に好ましい。無機凝集剤の添加量は、混合汚泥の性状などによっても異なり、用いる無機凝集剤の種類によっても異なるが、汚泥中の固形物乾燥重量（ＤＳ）に対して０．５〜７．０ｗｔ％であることが好ましく、特に１．５〜５ｗｔ％程度であることがより好ましい。 As the inorganic flocculant, polyferric sulfate, polyferric chloride, ferric chloride, aluminum sulfate, aluminum chloride, and polyaluminum chloride can be preferably used. Of these, polyferric sulfate is particularly preferred. The amount of the inorganic flocculant added varies depending on the properties of the mixed sludge, etc., and also varies depending on the type of the inorganic flocculant used, but is 0.5 to 7.0 wt% with respect to the solid dry weight (DS) in the sludge. It is preferable that the ratio is about 1.5 to 5 wt%.
なお、本発明の処理装置の構成は上述の構成に限定されるものではなく、特許請求の範囲の記載を逸脱しない限りにおいて種々変更してもよい。たとえば、図１及び図２において余剰汚泥送配管６２に余剰汚泥貯留槽を設けてもよい。図２において、混合槽１０と凝集反応槽２０との間にラインミキサを複数台設けてもよい。図２において、凝集反応槽２０からのドレン２１の接続先は、混合槽１０として示しているが、混合槽１０の前段にある屎尿及び浄化槽汚泥の受入槽（図示せず）でも、余剰汚泥送配管６２に設けられた余剰汚泥貯留槽（図示せず）でもよい。また、図１において、バイパス経路３０Ａと切替弁Ｖ１及びＶ２を設けているが、バイパス経路３０Ａを混合槽１０に接続させて、切替弁の代わりに専用のポンプ及び破砕装置を設けてもよい。さらに、図１及び図２において、第２切替弁Ｖｐを経路４０ａと４０ｂの両者にそれぞれ設けているが、経路４０ａと４０ｂとの切り替え点に３方弁を１個設けてもよい。同様に、スクリーン４１からの分離液用配管４１ａからの経路にも２個の切替弁Ｖｐ１及びＶｐ２を設けているが、切り替え点に３方弁を１個設けてもよい。 The configuration of the processing apparatus of the present invention is not limited to the above-described configuration, and various changes may be made without departing from the scope of the claims. For example, an excess sludge storage tank may be provided in the excess sludge feed pipe 62 in FIGS. In FIG. 2, a plurality of line mixers may be provided between the mixing tank 10 and the aggregation reaction tank 20. In FIG. 2, the connection destination of the drain 21 from the agglomeration reaction tank 20 is shown as the mixing tank 10, but surplus sludge is fed also in the waste tank and septic tank sludge receiving tank (not shown) in the previous stage of the mixing tank 10. An excess sludge storage tank (not shown) provided in the pipe 62 may be used. In FIG. 1, the bypass path 30A and the switching valves V1 and V2 are provided. However, the bypass path 30A may be connected to the mixing tank 10 and a dedicated pump and crushing device may be provided instead of the switching valve. Further, in FIGS. 1 and 2, the second switching valve Vp is provided in both the paths 40a and 40b, but one three-way valve may be provided at the switching point between the paths 40a and 40b. Similarly, the two switching valves Vp1 and Vp2 are provided in the path from the separation liquid pipe 41a from the screen 41, but one three-way valve may be provided at the switching point.
以下、実施例を用いて本発明を具体的に説明するが、本発明はこれらに限定されるものではない。
［実施例１］
破砕したままで夾雑物を除去していない屎尿及び浄化槽汚泥を含む有機性廃水に、生物処理において生じた余剰汚泥を混合して得た混合汚泥５０ｋＬ／日を本発明の処理方法で処理する場合と、従来方法で処理する場合を比較した。
EXAMPLES Hereinafter, although this invention is demonstrated concretely using an Example, this invention is not limited to these.
[Example 1]
When processing the mixed sludge 50 kL / day obtained by mixing surplus sludge generated in biological treatment with organic wastewater containing sewage and septic tank sludge that has not been removed with crushed impurities removed, by the treatment method of the present invention Compared with the case of processing by the conventional method.
図１に示す装置を用い、凝集剤の添加及び無添加の切り替え及びＭＡＰ回収への切り替えは、図３（１）に示すタイムチャートに従って行い、Ｔ１＝４８分、Ｔ２＝１２分と設定し、混合汚泥の約２０％に対して凝集剤を添加しなかった。 Using the apparatus shown in FIG. 1, switching between addition and non-addition of a flocculant and switching to MAP recovery are performed according to the time chart shown in FIG. 3 (1), and T1 = 48 minutes and T2 = 12 minutes are set. No flocculant was added to about 20% of the mixed sludge.
無機凝集剤としてポリ硫酸第二鉄、高分子凝集剤としてエバグロースＣＳ−３２０（水ｉｎｇ株式会社製カチオン系高分子凝集剤）を用いた。無機凝集剤は、濃縮スクリーン４１で高分子凝集剤添加混合汚泥を濃縮した後の濃縮物に添加した。濃縮スクリーン４１で分離された分離水は第２分離液としてＭＡＰ回収装置８０に送った。 Poly ferric sulfate was used as the inorganic flocculant, and Ebagulose CS-320 (cationic polymer flocculant manufactured by Mizuing Co., Ltd.) was used as the polymer flocculant. The inorganic flocculant was added to the concentrate after the polymer flocculant-added mixed sludge was concentrated by the concentration screen 41. The separated water separated by the concentration screen 41 was sent to the MAP recovery device 80 as a second separated liquid.
本実施例では、後続の生物処理を脱窒素処理としたため、窒素（Ｎ）の分解を促進させるために、水素供与体としてメタノールを生物処理槽に添加した。
各薬剤の添加量と、脱水ケーキの含水率、処理水の水質を表１及び表２に示す。
In this example, since the subsequent biological treatment was denitrification treatment, methanol was added to the biological treatment tank as a hydrogen donor in order to promote the decomposition of nitrogen (N).
Tables 1 and 2 show the amount of each chemical added, the water content of the dehydrated cake, and the quality of the treated water.
回収したＭＡＰの成分を化成肥料の基準値と比較した試験結果を表３に示す。
［実施例２］
図１に示す装置を用い、高分子凝集剤の添加と無添加との切り替え及びＭＡＰ回収への切り替えは図３（１）に示すタイムチャートに従って、Ｔ１＝３９分、Ｔ２＝２１分と設定し、混合汚泥の約３５％に対して高分子凝集剤を添加しなかった以外は実施例１と同様に行い、各薬剤の添加量と、脱水ケーキの含水率及び処理水の水質を測定した。結果を表１及び表２に示す。
Table 3 shows the test results comparing the collected MAP components with the reference value of the chemical fertilizer.
[Example 2]
Using the apparatus shown in FIG. 1, the switching between addition and non-addition of the polymer flocculant and switching to MAP recovery are set as T1 = 39 minutes and T2 = 21 minutes according to the time chart shown in FIG. The same procedure as in Example 1 was conducted except that the polymer flocculant was not added to about 35% of the mixed sludge, and the amount of each agent added, the water content of the dehydrated cake, and the quality of the treated water were measured. The results are shown in Tables 1 and 2.
回収したＭＡＰの成分を化成肥料の基準値と比較した試験結果を表３に示す。
［実施例３］
バイパス経路を含まない図２に示す装置を用いて、高分子凝集剤の添加及び無添加の切り替え及びＭＡＰ回収への切り替えを図３（４）に示すタイムチャートに従って、Ｔ１＝３９分、Ｔ２＝２１分と設定し、混合汚泥の約３５％に対して高分子凝集剤を添加しなかった以外は実施例１と同様に行い、各薬剤の添加量と、脱水ケーキの含水率及び処理水の水質を測定した。結果を表１及び表２に示す。
Table 3 shows the test results comparing the collected MAP components with the reference value of the chemical fertilizer.
[Example 3]
Using the apparatus shown in FIG. 2 that does not include the bypass route, switching of addition and non-addition of the polymer flocculant and switching to MAP recovery are performed according to the time chart shown in FIG. 3 (4), T1 = 39 minutes, T2 = It was set as 21 minutes, and was performed in the same manner as in Example 1 except that the polymer flocculant was not added to about 35% of the mixed sludge. The amount of each agent added, the water content of the dehydrated cake, and the treated water Water quality was measured. The results are shown in Tables 1 and 2.
［実施例４］
図２に示す装置を用いて、高分子凝集剤の添加及び無添加の切り替え及びＭＡＰ回収への切り替えを図３（７）に示すタイムチャートに従って、Ｔ１＝３９分、Ｔ２＝２１分、Ｔ３＝３分と設定し、混合汚泥の約３５％に対して高分子凝集剤を添加しなかった以外は実施例１と同様に行い、各薬剤の添加量と、脱水ケーキの含水率及び処理水の水質を測定した。結果を表１及び表２に示す。
[Example 4]
Using the apparatus shown in FIG. 2, switching between addition and non-addition of a polymer flocculant and switching to MAP recovery is performed according to the time chart shown in FIG. 3 (7), T1 = 39 minutes, T2 = 21 minutes, T3 = Set as 3 minutes, except that the polymer flocculant was not added to about 35% of the mixed sludge, the same as in Example 1, the amount of each agent added, the water content of the dehydrated cake and the treated water Water quality was measured. The results are shown in Tables 1 and 2.
［比較例］
図１に示す装置を用いて、高分子凝集剤の添加の切り替えを行わず、全量を脱水した。
[Comparative example]
Using the apparatus shown in FIG. 1, the entire amount was dehydrated without switching the addition of the polymer flocculant.
処理水の水質を表２に示す。 Table 2 shows the quality of the treated water.
各検査項目の検査方法は以下の通りである。
水素イオン濃度：JIS K 0102-12.1
生物化学的酸素要求量(BOD)：JIS K-0102-21及び-32.1
化学的酸素要求量（CODMn）：JIS K-0102-17
浮遊物質量（SS）：昭和46年環境庁告示第59号付表8
全窒素：JIS K-0102-45.1
全リン：JIS K-0102-46.3.3
色度：平成4年厚生省令第69号 45
大腸菌群数：昭和37年厚生省・建設省令第1号
The inspection method for each inspection item is as follows.
Hydrogen ion concentration: JIS K 0102-12.1
Biochemical oxygen demand (BOD): JIS K-0102-21 and -32.1
Chemical oxygen demand (COD Mn ): JIS K-0102-17
Suspended solids (SS): 1986 Environment Agency Notification No. 59, Appendix 8
Total nitrogen: JIS K-0102-45.1
Total phosphorus: JIS K-0102-46.3.3
Chromaticity: Ministry of Health and Welfare Ordinance No. 69 45
Number of coliforms: Ministry of Health and Welfare Ordinance No. 1 in 1957
混合汚泥の２０％に対して凝集剤を添加しなかった場合（実施例１）の薬剤の添加量は、混合汚泥の全量に凝集剤を添加した場合に比較して、無機凝集剤を約５５％、高分子凝集剤を約２０％、メタノールを約５０％削減できた。混合汚泥の３５％に対して凝集剤を添加しなかった場合（実施例２）の薬剤の添加量の削減率は、無機凝集剤が約６１％、高分子凝集剤が約３５％、メタノールが約８６％、同じく実施例３では、無機凝集剤が約６６％、高分子凝集剤が約３６％、メタノールが約８６％、ラインミキサを用いて高分子凝集剤のみを添加した場合（実施例４）の薬剤の添加量の削減率は、無機凝集剤が１００％、高分子凝集剤が約３０％、メタノールが約８６％であった。各実施例とも脱水ケーキの含水率は７０％以下を達成し、処理水は放流水質基準を達成した。 When the flocculant is not added to 20% of the mixed sludge (Example 1), the amount of the chemical added is about 55 compared with the case where the flocculant is added to the total amount of the mixed sludge. %, The polymer flocculant was reduced by about 20%, and the methanol was reduced by about 50%. When the flocculant is not added to 35% of the mixed sludge (Example 2), the reduction rate of the added amount of the chemical is about 61% for the inorganic flocculant, about 35% for the polymer flocculant, and methanol. About 86%, also in Example 3, the inorganic flocculant is about 66%, the polymer flocculant is about 36%, methanol is about 86%, and only the polymer flocculant is added using a line mixer (Example) The reduction rate of the added amount of the agent in 4) was 100% for the inorganic flocculant, about 30% for the polymer flocculant, and about 86% for methanol. In each example, the moisture content of the dewatered cake was 70% or less, and the treated water achieved the discharged water quality standard.
本発明の処理方法によれば、凝集剤無添加処理の総時間が凝集剤添加時と無添加時との合計時間の６０％以下となるように凝集剤の添加と無添加とを切り替えることにより、脱水ケーキの含水率７０％及び処理水の水質基準を達成しながら、メタノール、無機凝集剤、高分子凝集剤のいずれも添加量を削減できた。 According to the treatment method of the present invention, by switching between addition and non-addition of the flocculant so that the total time of the flocculant-free addition treatment is 60% or less of the total time when the flocculant is added and when no flocculant is added. In addition, while achieving the moisture content of the dehydrated cake of 70% and the water quality standard of the treated water, the amounts of addition of methanol, inorganic flocculant, and polymer flocculant could be reduced.
本方法により回収したＭＡＰは、化成肥料としての基準値を満たすことが確認できた。 It was confirmed that the MAP collected by this method satisfies the standard value as a chemical fertilizer.
脱水処理と生物処理とを併用する屎尿及び浄化槽汚泥を含む有機性廃水の処理における凝集剤及び生物処理における栄養源となる薬剤の使用量を削減できると共に、回収したＭＡＰを化成肥料として再利用できる。 It is possible to reduce the amount of coagulant used in the treatment of organic wastewater including manure and septic tank sludge that use dehydration and biological treatment in combination, and the nutrient source in biological treatment, and the recovered MAP can be reused as a chemical fertilizer. .
Claims (12)
当該生物処理において発生する余剰汚泥を返送して、屎尿及び／又は有機性汚泥との混合汚泥を形成し、
当該混合汚泥に高分子凝集剤を添加せずに脱水処理して第１分離液を得て、当該第１分離液を、リン酸マグネシウムアンモニウム（ＭＡＰ）を回収する工程を経ずに直接、生物処理における水素供与体として利用するために分離液貯留槽に送る工程と、
当該混合汚泥に高分子凝集剤を添加してから脱水処理して第２分離液を得て、当該第２分離液を、リン酸マグネシウムアンモニウム（ＭＡＰ）を回収する工程に送る工程と、
を交互に行ない、
当該混合汚泥を脱水処理した後の第１分離液と、当該第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収した後の脱離液と、を生物処理することを特徴とする有機性廃水処理方法。 An organic wastewater treatment method for biologically treating organic wastewater containing manure and / or organic sludge,
Return the excess sludge generated in the biological treatment, to form a mixed sludge of sewage and / or organic sludge,
The mixed sludge is dehydrated without adding a polymer flocculant to obtain a first separation liquid, and the first separation liquid is directly biological without passing through the step of recovering magnesium ammonium phosphate (MAP). Sending to a separate liquid reservoir for use as a hydrogen donor in the process;
Adding a polymer flocculant to the mixed sludge and then dehydrating to obtain a second separation liquid, and sending the second separation liquid to a process of collecting magnesium ammonium phosphate (MAP) ;
Alternately
Organic wastewater characterized by biologically treating a first separation liquid after dehydrating the mixed sludge and a desorption liquid after recovering magnesium ammonium phosphate (MAP) from the second separation liquid Processing method.
前記第２分離液は、当該濃縮工程で得られる、請求項１又は２に記載の有機性廃水処理方法。 The dehydration treatment includes a concentration step of concentrating the mixed sludge added with the polymer flocculant, and a dehydration step of dehydrating the concentrated mixed sludge,
The organic wastewater treatment method according to claim 1 or 2, wherein the second separation liquid is obtained in the concentration step.
前記第１分離液は、当該濃縮工程及び当該脱水工程で得られる、請求項１又は２に記載の有機性廃水処理方法。The organic wastewater treatment method according to claim 1 or 2, wherein the first separation liquid is obtained in the concentration step and the dehydration step.
当該混合槽には、当該生物処理槽からの余剰汚泥を返送する余剰汚泥配管と、余剰汚泥と屎尿及び／又は有機性汚泥との混合汚泥を当該凝集反応槽に送る経路と、が接続されており、
当該凝集反応槽には、当該凝集反応槽に送られて高分子凝集剤が添加された当該混合汚泥を当該脱水装置に送る経路が接続されており、
当該凝集反応槽を経由せずに、当該混合槽と当該脱水装置との間を直接連通させるバイパス経路が設けられており、
当該脱水装置には、当該バイパス経路からの混合汚泥を当該脱水装置で脱水して得られる第１分離液を当該分離液貯留槽に送る経路、又は当該凝集反応槽からの高分子凝集剤を添加した混合汚泥を当該脱水装置で脱水して得られる第２分離液を当該ＭＡＰ回収装置に送る経路のいずれかに送る切替弁を有する経路が接続されており、
当該分離液貯留槽には、第１分離液を当該生物処理槽に送る経路が接続されており、
当該混合槽からの混合汚泥を当該凝集反応槽に送る経路と、当該バイパス経路と、の切り替えを行う第１切替弁と、
当該脱水装置からの第１分離液を当該分離液貯留槽に送る経路と、当該脱水装置からの第２分離液を当該MAP回収装置に送る経路と、の切り替えを行う第２切替弁と、
を具備し、
当該第１切替弁と第２切替弁とは連動し、当該第１切替弁により混合汚泥を当該凝集反応槽に送る経路に切り換える際には、当該第２切替弁により第２分離液を当該ＭＡＰ回収装置に送る経路に切り換え、当該第１切替弁により混合汚泥を当該バイパス経路に送る際には、当該第２切替弁により第１分離液を当該分離液貯留槽に送る経路に切り換えることを特徴とする、有機性廃水処理装置。 Organically treating organic wastewater containing manure and / or organic sludge comprising a mixing tank, an agglomeration reaction tank, a dehydration device, a separation liquid storage tank, a biological treatment tank, and a MAP recovery device A wastewater treatment device,
The mixing tank is connected to a surplus sludge pipe for returning surplus sludge from the biological treatment tank and a route for sending the mixed sludge of surplus sludge and manure and / or organic sludge to the agglomeration reaction tank. And
The agglomeration reaction tank is connected to a route for sending the mixed sludge, to which the polymer flocculant is added, sent to the agglomeration reaction tank, to the dehydrator,
Without passing through the agglomeration reaction tank, a bypass path is provided for direct communication between the mixing tank and the dehydrator,
To the dehydrator, a polymer flocculant from the path for sending the first separation liquid obtained by dehydrating the mixed sludge from the bypass path to the separation liquid storage tank or the coagulation reaction tank is added. A path having a switching valve for sending the second separated liquid obtained by dehydrating the mixed sludge to the MAP recovery apparatus is connected to the MAP recovery apparatus,
A path for sending the first separation liquid to the biological treatment tank is connected to the separation liquid storage tank,
A first switching valve for switching between a path for sending the mixed sludge from the mixing tank to the aggregation reaction tank and the bypass path;
A second switching valve for switching between a route for sending the first separation liquid from the dehydration device to the separation liquid storage tank and a route for sending the second separation liquid from the dehydration device to the MAP recovery device;
Comprising
The first switching valve and the second switching valve are interlocked, and when the first switching valve is switched to a route for sending mixed sludge to the agglomeration reaction tank, the second switching valve causes the second separation liquid to flow to the MAP. When switching to the path for sending to the recovery device and sending the mixed sludge to the bypass path by the first switching valve, the second switching valve switches to the path for sending the first separation liquid to the separation liquid storage tank. to, organic waste water treatment device.
高分子凝集剤を添加した混合汚泥に対しては濃縮機として作用し、高分子凝集剤を添加していない混合汚泥に対してはしさ分離機として作用するスクリーンと、
当該スクリーンの下流に位置づけられている脱水機と、
を含み、当該スクリーンからの分離水及び当該脱水機からの分離水をそれぞれ別個にＭＡＰ回収装置に送る経路と分離液貯留槽に送る経路とに切り替える切替弁をさらに具備する、請求項６又は７に記載の有機性廃水処理装置。 The dehydrator is
A screen that acts as a concentrator for mixed sludge to which a polymer flocculant has been added, and that acts as a separator for mixed sludge to which no polymer flocculant has been added,
A dehydrator located downstream of the screen;
Hints, further comprising a switching valve for switching to a path for sending the separated liquid reservoir separated water and the separated water from the dehydrator and route sent to separately MAP recovery device each from the screen, according to claim 6 or 7 Organic wastewater treatment equipment described in 1.
当該生物処理において発生する余剰汚泥を返送して、屎尿及び／又は有機性汚泥との混合汚泥を形成し、
当該混合汚泥に高分子凝集剤を添加せずに脱水処理して第１分離液を得て、当該第１分離液を、リン酸マグネシウムアンモニウム（ＭＡＰ）を回収する工程を経ずに直接、生物処理における水素供与体として利用するために分離液貯留槽に送る工程と、
当該混合汚泥に高分子凝集剤を添加してから脱水処理して第２分離液を得て、当該第２分離液を、リン酸マグネシウムアンモニウム（ＭＡＰ）を回収して化成肥料を製造する工程に送る工程と、
を交互に行ない、
当該混合汚泥を脱水処理した後の第１分離液と、当該第２分離液からリン酸マグネシウムアンモニウム（ＭＡＰ）を回収した後の脱離液と、を生物処理することを特徴とする、化成肥料の製造方法。 In organic wastewater treatment for biological treatment of organic wastewater containing manure and / or organic sludge,
Return surplus sludge generated in the biological treatment to form mixed sludge with manure and / or organic sludge ,
The mixed sludge is dehydrated without adding a polymer flocculant to obtain a first separation liquid, and the first separation liquid is directly biological without passing through the step of recovering magnesium ammonium phosphate (MAP). Sending to a separate liquid reservoir for use as a hydrogen donor in the process;
To obtain a second separation liquid is dehydrated after the addition of polymeric flocculant to the mixed sludge, the second separated liquid, we produce recovered and fertilizer magnesium ammonium phosphate (MAP) process The process of sending to
No line alternately,
Chemical fertilizer characterized by biologically treating the first separation liquid after dehydrating the mixed sludge and the desorption liquid after recovering magnesium ammonium phosphate (MAP) from the second separation liquid Manufacturing method.
混合槽と、凝集反応槽と、脱水装置と、分離液貯留槽と、生物処理槽と、ＭＡＰ回収装置と、を具備し、A mixing tank, an agglomeration reaction tank, a dehydration device, a separation liquid storage tank, a biological treatment tank, and a MAP recovery device,
当該混合槽には、当該生物処理槽からの余剰汚泥を返送する余剰汚泥配管と、余剰汚泥と屎尿及び／又は有機性汚泥との混合汚泥を当該凝集反応槽に送る経路と、が接続されており、The mixing tank is connected to a surplus sludge pipe for returning surplus sludge from the biological treatment tank and a route for sending the mixed sludge of surplus sludge and manure and / or organic sludge to the agglomeration reaction tank. And
当該凝集反応槽には、当該凝集反応槽に送られて高分子凝集剤が添加された当該混合汚泥を当該脱水装置に送る経路が接続されており、The agglomeration reaction tank is connected to a route for sending the mixed sludge, to which the polymer flocculant is added, sent to the agglomeration reaction tank, to the dehydrator,
当該凝集反応槽を経由せずに、当該混合槽と当該脱水装置との間を直接連通させるバイパス経路が設けられており、Without passing through the agglomeration reaction tank, a bypass path is provided for direct communication between the mixing tank and the dehydrator,
当該脱水装置には、当該バイパス経路からの混合汚泥を当該脱水装置で脱水して得られる第１分離液を当該分離液貯留槽に送る経路、又は当該凝集反応槽からの高分子凝集剤を添加した混合汚泥を当該脱水装置で脱水して得られる第２分離液を当該ＭＡＰ回収装置に送る経路のいずれかに送る切替弁を有する経路が接続されており、To the dehydrator, a polymer flocculant from the path for sending the first separation liquid obtained by dehydrating the mixed sludge from the bypass path to the separation liquid storage tank or the coagulation reaction tank is added. A path having a switching valve for sending the second separated liquid obtained by dehydrating the mixed sludge to the MAP recovery apparatus is connected to the MAP recovery apparatus,
当該分離液貯留槽には、第１分離液を当該生物処理槽に送る経路が接続されており、A path for sending the first separation liquid to the biological treatment tank is connected to the separation liquid storage tank,
さらに、当該混合槽からの混合汚泥を当該凝集反応槽に送る経路と、当該バイパス経路と、の切り替えを行う第１切替弁と、Furthermore, a first switching valve for switching between a path for sending the mixed sludge from the mixing tank to the aggregation reaction tank, and the bypass path;
当該脱水装置からの第１分離液を当該分離液貯留槽に送る経路と、当該脱水装置からの第２分離液を当該MAP回収装置に送る経路と、の切り替えを行う第２切替弁と、A second switching valve for switching between a route for sending the first separation liquid from the dehydration device to the separation liquid storage tank and a route for sending the second separation liquid from the dehydration device to the MAP recovery device;
を具備し、Comprising
当該第１切替弁と第２切替弁とは連動し、当該第１切替弁により混合汚泥を当該凝集反応槽に送る経路に切り換える際には、当該第２切替弁により第２分離液を当該ＭＡＰ回収装置に送る経路に切り換え、当該第１切替弁により混合汚泥を当該バイパス経路に送る際には、当該第２切替弁により第１分離液を当該分離液貯留槽に送る経路に切り換えることを特徴とする、化成肥料の製造装置。The first switching valve and the second switching valve are interlocked, and when the first switching valve is switched to a route for sending mixed sludge to the agglomeration reaction tank, the second switching valve causes the second separation liquid to flow to the MAP. When switching to the path for sending to the recovery device and sending the mixed sludge to the bypass path by the first switching valve, the second switching valve switches to the path for sending the first separation liquid to the separation liquid storage tank. And manufacturing equipment for chemical fertilizer.
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