JPH10118687A - Treatment method of organic wastewater - Google Patents
Treatment method of organic wastewaterInfo
- Publication number
- JPH10118687A JPH10118687A JP27922396A JP27922396A JPH10118687A JP H10118687 A JPH10118687 A JP H10118687A JP 27922396 A JP27922396 A JP 27922396A JP 27922396 A JP27922396 A JP 27922396A JP H10118687 A JPH10118687 A JP H10118687A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- nitrogen
- phosphorus
- wastewater
- organic wastewater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims description 46
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 94
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 77
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000011574 phosphorus Substances 0.000 claims abstract description 34
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 34
- 238000000855 fermentation Methods 0.000 claims abstract description 33
- 230000004151 fermentation Effects 0.000 claims abstract description 32
- 239000002253 acid Substances 0.000 claims abstract description 23
- 239000002245 particle Substances 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims abstract description 11
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 claims abstract description 10
- 239000007787 solid Substances 0.000 claims abstract description 9
- 150000002681 magnesium compounds Chemical class 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 65
- 239000010802 sludge Substances 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 10
- 229910052567 struvite Inorganic materials 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 230000001546 nitrifying effect Effects 0.000 claims description 2
- 239000002699 waste material Substances 0.000 abstract description 6
- 229940125758 compound 15 Drugs 0.000 abstract description 4
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 150000001875 compounds Chemical class 0.000 abstract 1
- 238000005469 granulation Methods 0.000 description 30
- 230000003179 granulation Effects 0.000 description 30
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- 244000005700 microbiome Species 0.000 description 10
- 239000003795 chemical substances by application Substances 0.000 description 8
- 241000894006 Bacteria Species 0.000 description 7
- 235000011121 sodium hydroxide Nutrition 0.000 description 7
- 239000008187 granular material Substances 0.000 description 6
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 6
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 5
- 239000000347 magnesium hydroxide Substances 0.000 description 5
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 5
- 230000014759 maintenance of location Effects 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- -1 ammonium ions Chemical class 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000004060 metabolic process Effects 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- 239000003929 acidic solution Substances 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- VTEIFHQUZWABDE-UHFFFAOYSA-N 2-(2,5-dimethoxy-4-methylphenyl)-2-methoxyethanamine Chemical compound COC(CN)C1=CC(OC)=C(C)C=C1OC VTEIFHQUZWABDE-UHFFFAOYSA-N 0.000 description 1
- 241000219310 Beta vulgaris subsp. vulgaris Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 235000021536 Sugar beet Nutrition 0.000 description 1
- FPWJLQXCGHQXLL-UHFFFAOYSA-N [P].OP(O)(O)=O Chemical compound [P].OP(O)(O)=O FPWJLQXCGHQXLL-UHFFFAOYSA-N 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 229940126142 compound 16 Drugs 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000000386 donor Substances 0.000 description 1
- 235000019441 ethanol Nutrition 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052588 hydroxylapatite Inorganic materials 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000003002 pH adjusting agent Substances 0.000 description 1
- XYJRXVWERLGGKC-UHFFFAOYSA-D pentacalcium;hydroxide;triphosphate Chemical compound [OH-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O XYJRXVWERLGGKC-UHFFFAOYSA-D 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229940085991 phosphate ion Drugs 0.000 description 1
- 239000002367 phosphate rock Substances 0.000 description 1
- 150000003018 phosphorus compounds Chemical class 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 235000000346 sugar Nutrition 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
Classifications
-
- Y02W10/12—
Landscapes
- Removal Of Specific Substances (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、食品工場廃水等の
りん及び窒素を高濃度に含有する有機性廃水中の有機
物、りん及び窒素を高効率に除去する有機性廃水の処理
方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating organic wastewater, such as food factory wastewater, which efficiently removes organic substances, phosphorus and nitrogen from organic wastewater containing high concentrations of phosphorus and nitrogen. is there.
【０００２】[0002]
【従来の技術】近年のりん・窒素規制の強化に伴い、廃
水処理施設において、ＢＯＤ、ＣＯＤに代表される有機
物はもとより、りん、窒素の除去まで考慮した高度処理
の必要性に迫られている。特に、有機物、りん、窒素共
に高濃度に含有した食品工場廃水等では、高効率の廃水
処理方法の構築が急務である。有機性廃水の処理方法と
しては、処理効率、経済性の面から生物学的処理方法が
とられることが多く、生物学的処理方法は、好気性微生
物の代謝作用を応用した活性汚泥法に代表される好気性
微生物法と、嫌気性微生物の代謝作用を応用した嫌気性
微生物法に大きく分けられるが、近年、高負荷、省エネ
ルギー型嫌気性処理装置として、嫌気性微生物の自己固
定能を利用した上向流式嫌気性汚泥床法（ＵＡＳＢ法）
が開発された。2. Description of the Related Art With the recent tightening of phosphorus and nitrogen regulations, wastewater treatment facilities have been required to perform advanced treatment that takes into account not only removal of organic substances such as BOD and COD, but also phosphorus and nitrogen. . In particular, for food factory wastewater containing high concentrations of organic substances, phosphorus, and nitrogen, it is urgently necessary to establish a highly efficient wastewater treatment method. Organic wastewater is often treated in a biological manner in terms of treatment efficiency and economy, and the biological treatment is typically represented by an activated sludge method utilizing the metabolism of aerobic microorganisms. Aerobic microorganism method and anaerobic microorganism method using metabolism of anaerobic microorganisms. Upflow anaerobic sludge bed method (UASB method)
Was developed.
【０００３】ＵＡＳＢ法については、「用水と廃水」
（１９８９年 Ｖｏｌ．３１、Ｎｏ．１、第５〜１１
頁）に詳細が記載されており、第５頁左欄第２２行〜右
欄第６行には、「これら新方式のメタン発酵リアクター
は、水理学的滞留時間（ＨＲＴ）とは独立に汚泥滞留時
間（ＳＲＴ）をコントロールでき、高濃度の生物量を反
応器内に保持し高容積負荷を許容し、結果として適用排
水種の低濃度化拡大が図られた。これら３方式のメタン
発酵リアクターは、包括固定化菌体法のように人為的な
操作によるのとは対照的に、微生物自身のもつ凝集・集
塊機能（Aggregation ）を積極的に利用した、いわば自
己固定化(Self-Immobilization) 法ということができ
る。」と記載されている。また、第７頁右欄第１〜５行
には、「その結果、糖系、有機酸、アルコールなどの易
分解性の排水種では２５〜３５ｋｇＣＯＤCr／ｍ3 ・日
の容積負荷で８５〜９５％の除去が可能であり、従来の
嫌気性処理の常識からでは考えられないような高速・高
率処理性能を発揮することができる。」と記載されてお
り、実績としては、第７頁右欄１９〜２１行には、「甜
菜糖排水（９〜１７ｋｇＣＯＤCr／ｍ3 ・日）、アルコ
ール蒸留（同９〜１５）など食品・飲料産業排水の分野
で卓越した性能を発揮している。」と記載されている通
り、食品産業等の高濃度有機性廃水に適している。[0003] Regarding the UASB method, "water and wastewater"
(1989 Vol. 31, No. 1, Nos. 5-11
Page 5, the left column, line 22 to the right column, line 6 states, "These new methane fermentation reactors have sludge independent of hydraulic residence time (HRT). The residence time (SRT) can be controlled, a high concentration of biomass can be maintained in the reactor, and a high volume load can be tolerated. In contrast to self-immobilization, the self-immobilization (Aggregation) function of the microorganism itself is used in contrast to the artificial operation such as the comprehensive immobilization cell method. ) Law. " Also, on page 7, right column, lines 1-5, "As a result, for easily decomposable drainage species such as sugars, organic acids, and alcohols, 25-35 kg COD Cr / m 3 · It can remove 95%, and can exhibit high-speed and high-rate processing performance that cannot be considered from the common sense of conventional anaerobic processing. " In the right column, lines 19-21, "Excellent performance is demonstrated in the fields of wastewater in the food and beverage industry, such as sugar beet wastewater (9-17 kg COD Cr / m 3 · day) and alcohol distillation (9-15 days). It is suitable for high-concentration organic wastewater in the food industry and the like.
【０００４】[0004]
【発明が解決しようとする課題】高濃度有機性廃水の高
負荷処理としては、上記記載のＵＡＳＢ法が適している
が、除去原理は嫌気性微生物の代謝によるので、有機物
はメタンガスとして除去が可能であるものの、りん、窒
素については菌体量増加相当しか除去できないという問
題があった。従来のりん除去方法としては、アルミニウ
ム塩や鉄塩等の金属塩とりんとを反応させる凝集沈殿
法、りん鉱石や骨炭等の種晶にヒドロキシアパタイトの
形でりんを析出させる晶析法（接触脱りん法）、微生物
のりん過剰摂取作用を利用した生物学的脱りん法、例え
ば、嫌気・好気法等がある。しかし、これらの処理プロ
セスから発生するりん化合物を含有した２次生成物の処
分が問題となり、しかも、上記方法では窒素除去は期待
できないものである。本発明は、りん及び窒素を含有し
た高濃度有機性廃水から有機物、りん及び窒素を効率よ
く処理することが可能であり、廃棄物の発生も極めて少
ない有機性廃水の処理方法を提供することを目的とする
ものである。The UASB method described above is suitable for high-load treatment of high-concentration organic wastewater. However, since the principle of removal is based on metabolism of anaerobic microorganisms, organic substances can be removed as methane gas. However, there was a problem that phosphorus and nitrogen could only be removed in an amount corresponding to the increase in the amount of bacterial cells. Conventional phosphorus removal methods include a coagulation precipitation method in which a metal salt such as an aluminum salt or an iron salt is reacted with phosphorus, and a crystallization method in which phosphorus is precipitated in the form of hydroxyapatite on a seed crystal such as phosphate rock or bone charcoal (contact desorption). Phosphorus method) and biological dephosphorization methods utilizing the excessive phosphorus uptake action of microorganisms, such as anaerobic and aerobic methods. However, disposal of secondary products containing phosphorus compounds generated from these treatment processes becomes a problem, and nitrogen removal cannot be expected by the above method. The present invention provides an organic wastewater treatment method capable of efficiently treating organic matter, phosphorus and nitrogen from high-concentration organic wastewater containing phosphorus and nitrogen, and generating very little waste. It is the purpose.
【０００５】[0005]
【課題を解決するための手段】本発明者らは、このよう
な課題を解決するために鋭意検討の結果、ＵＡＳＢ法に
より有機物を高負荷でメタンガスに変換した後、マグネ
シウム化合物を添加して、有機性廃水中のりん酸イオン
及びアンモニウムイオンをりん酸マグネシウムアンモニ
ウムの固体粒子として回収することにより、廃水中のり
ん及び窒素を除去し、さらに、有機性廃水中に窒素が高
濃度に含有される場合、残留した窒素を生物学的硝化脱
窒法により除去することで、河川放流水程度にまで処理
できるという事実を見出し、本発明に到達した。Means for Solving the Problems The present inventors have conducted intensive studies to solve such problems, and as a result, after converting organic substances to methane gas under high load by the UASB method, adding a magnesium compound, By recovering phosphate ions and ammonium ions in organic wastewater as solid particles of magnesium ammonium phosphate, phosphorus and nitrogen in wastewater are removed, and nitrogen is contained in organic wastewater at a high concentration. In this case, the present inventors have found that by removing the remaining nitrogen by a biological nitrification and denitrification method, it can be treated to a level equivalent to river discharge water, and arrived at the present invention.
【０００６】すなわち、第１の発明は、次の３つの工程
の順で、有機性廃水中の有機物、りん及び窒素を除去す
ることを特徴とする有機性廃水の処理方法を要旨とする
ものであり、その３つの工程とは、（１）りん及び窒素
を含有する有機性廃水を酸生成槽で酸発酵を行う工程、
（２）上向流式嫌気性汚泥床型メタン発酵槽でメタン発
酵を行う工程、（３）マグネシウム化合物を添加し、ｐ
Ｈを８〜１０に調整するとともに、曝気によって攪拌混
合を行うことにより、生成したりん酸マグネシウムアン
モニウムの固体粒子を回収する工程である。また、第２
の発明は、前記の処理方法で得られた処理水をさらに生
物学的硝化脱窒することにより、有機性廃水中の有機
物、りん及び窒素を除去することを特徴とする有機性廃
水の処理方法を要旨とするものである。That is, the first invention has a gist of a method for treating organic wastewater, which comprises removing organic substances, phosphorus and nitrogen from the organic wastewater in the order of the following three steps. There are three steps: (1) a step in which organic wastewater containing phosphorus and nitrogen is subjected to acid fermentation in an acid generation tank;
(2) a step of performing methane fermentation in an upward flow anaerobic sludge bed type methane fermentation tank, (3) adding a magnesium compound,
This step is a step of adjusting the H to 8 to 10 and stirring and mixing by aeration to collect the generated solid particles of magnesium ammonium phosphate. Also, the second
The present invention further provides a method for treating organic wastewater, wherein the treated water obtained by the above-mentioned treatment method is further subjected to biological nitrification and denitrification to remove organic substances, phosphorus and nitrogen in the organic wastewater. It is the gist.
【０００７】[0007]
【発明の実施の形態】以下、図面を参照しつつ、本発明
を具体的に説明する。図１は、本発明の有機性廃水の処
理方法の一例を示す概略図である。図１において、第１
工程として、まず、りん及び窒素を含有する有機性廃水
を原水４として酸生成槽１に供給し、ここで酸発酵を行
う。酸生成槽１では、嫌気性微生物の作用により有機物
の加水分解及び有機酸生成を行う。酸生成槽１での水理
学的滞留時間は廃水中の有機成分により異なり、炭水化
物のような分解容易な成分の場合は、２〜６時間程度で
よいが、タンパク質、脂肪等の分解が困難な成分には、
８〜２０時間を要する。酸生成槽１内は撹拌装置５によ
り常時撹拌混合を行い、槽内の温度は５〜７０℃で嫌気
性微生物の活性を保持することができるが、好ましくは
２０〜４０℃に調整する。酸生成槽１内のｐＨは、有機
性廃水の性状にもよるが、３〜９が好ましく、最適のｐ
Ｈは６〜７である。ｐＨが３未満又は９を超える場合、
嫌気性微生物の活性が低下しやすくなる。ｐＨ調整剤と
して酸性溶液又はアルカリ剤６を用いて調整することが
好ましく、酸性溶液としては塩酸を、アルカリ剤として
は苛性ソーダを用いることが好ましい。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be specifically described below with reference to the drawings. FIG. 1 is a schematic diagram showing an example of the method for treating organic wastewater of the present invention. In FIG. 1, the first
As a process, first, organic wastewater containing phosphorus and nitrogen is supplied as raw water 4 to the acid generation tank 1, where acid fermentation is performed. In the acid generation tank 1, hydrolysis of organic substances and generation of organic acids are performed by the action of anaerobic microorganisms. The hydraulic retention time in the acid generation tank 1 differs depending on the organic components in the wastewater. In the case of easily decomposable components such as carbohydrates, it may be about 2 to 6 hours, but it is difficult to decompose proteins and fats. Ingredients include
It takes 8 to 20 hours. The acid generating tank 1 is constantly stirred and mixed by the stirrer 5 and the temperature in the tank is 5 to 70 ° C. to maintain the activity of the anaerobic microorganism, but preferably adjusted to 20 to 40 ° C. The pH in the acid generation tank 1 is preferably 3 to 9, although it depends on the properties of the organic wastewater.
H is 6-7. If the pH is less than 3 or more than 9,
The activity of anaerobic microorganisms tends to decrease. It is preferable to use an acidic solution or an alkaline agent 6 as a pH adjuster, and it is preferable to use hydrochloric acid as an acidic solution and caustic soda as an alkaline agent.
【０００８】次に、第２工程として、酸生成槽１で処理
された酸生成槽１の処理水８を上向流式嫌気性汚泥床型
（ＵＡＳＢ型）メタン発酵槽２（以下、メタン発酵槽と
いう。）の底部に供給する。メタン発酵槽２の内部に
は、メタン生成菌からなるグラニュールを充填し、メタ
ン発酵槽２の原水１０は、メタン発酵槽２の底でグラニ
ュールからなるスラッジベッドと均一に接触し、メタン
発酵が起こる。なお、ここでは、メタン発酵槽２で処理
されたメタン発酵槽２の処理水１３の一部を循環水１１
として、酸生成槽１の処理水８と混合し、これをメタン
発酵槽２の原水１０としてメタン発酵槽２底部より供給
する。生成したメタン９とグラニュールとメタン発酵槽
２の処理水１３は、メタン発酵槽２の上部に設けられた
三相分離装置１２により分離される。メタン９はメタン
発酵槽２の上部より回収され、グラニュールはメタン発
酵槽２の底部に沈降し、メタン発酵槽２の処理水１３は
メタン発酵槽２の上部より溢流する。メタン発酵槽２の
容積は、供給される有機性廃水の成分及び濃度により異
なるが、５〜１５ｋｇＣＯＤ／ｍ3 ・日の容積負荷とな
ることが好ましく、さらには５〜１０ｋｇＣＯＤ／ｍ3
・日の容積負荷となることが好ましい。また、メタン発
酵槽２の原水１０の水理学的滞留時間としては、６〜２
４時間、さらには１０〜２０時間とすることが好まし
い。さらに、最初に充填するグラニュールの量も供給さ
れる有機性廃水の成分及び濃度により異なるが、０．１
〜０．５ｋｇＣＯＤ／ｋｇＶＳＳ・日となるように充填
することが好ましい。[0008] Next, as a second step, the treated water 8 in the acid generating tank 1 treated in the acid generating tank 1 is supplied to the anaerobic sludge bed type (UASB type) methane fermentation tank 2 (hereinafter referred to as methane fermentation). To the bottom of the tank.) The inside of the methane fermenter 2 is filled with granules made of methane-producing bacteria, and the raw water 10 of the methane fermenter 2 uniformly contacts the sludge bed made of granules at the bottom of the methane fermenter 2, Happens. Here, a part of the treated water 13 of the methane fermentation tank 2 treated in the methane fermentation tank 2
, Mixed with the treated water 8 of the acid production tank 1 and supplied as raw water 10 of the methane fermentation tank 2 from the bottom of the methane fermentation tank 2. The generated methane 9, granules, and treated water 13 in the methane fermentation tank 2 are separated by a three-phase separation device 12 provided in an upper part of the methane fermentation tank 2. The methane 9 is collected from the upper part of the methane fermenter 2, the granules settle at the bottom of the methane fermenter 2, and the treated water 13 in the methane fermenter 2 overflows from the upper part of the methane fermenter 2. The volume of the methane fermenter 2 depends on the components and concentration of the organic wastewater to be supplied, but preferably has a volume load of 5 to 15 kg COD / m 3 · day, and more preferably 5 to 10 kg COD / m 3.
-It is preferable to have a daily volume load. The hydraulic retention time of the raw water 10 in the methane fermentation tank 2 is 6 to 2
It is preferably 4 hours, more preferably 10 to 20 hours. Furthermore, the amount of granules to be initially charged also depends on the composition and concentration of the organic wastewater supplied,
It is preferable that the filling be performed so as to be 0.5 kgCOD / kgVSs.day.
【０００９】メタン発酵槽２内のｐＨは６〜８になるよ
うにアルカリ剤７により調整することが好ましく、使用
するアルカリ剤７としては苛性ソーダを用いることが望
ましい。ｐＨが６未満又は８を超える場合には、メタン
生成菌の活性が低下しやすくなる。メタン発酵槽２内の
温度は、使用するグラニュールを形成するメタン生成菌
種によって異なり、低温菌では０〜２０℃、中温菌では
２０〜４０℃、高温菌では４０〜６５℃とするが、通常
は中温菌を用い、槽内の温度を３０〜３８℃に調整する
ことが好ましい。また、メタン発酵槽２内の上昇流速は
０．１〜２ｍ／時、さらには０．５〜１．５ｍ／時とす
ることが好ましい。このような処理を行うことにより、
有機性廃水中のＣＯＤの８０％以上が除去され、生成し
たメタンガスは燃料として有効利用される。The pH in the methane fermenter 2 is preferably adjusted with an alkaline agent 7 so as to be 6 to 8, and it is desirable to use caustic soda as the alkaline agent 7 to be used. When the pH is less than 6 or more than 8, the activity of the methanogen tends to decrease. The temperature in the methane fermenter 2 depends on the type of methane-producing bacteria that form the granules to be used, and is 0 to 20 ° C for low-temperature bacteria, 20 to 40 ° C for medium-temperature bacteria, and 40 to 65 ° C for high-temperature bacteria. Usually, it is preferable to use a mesophilic bacterium and adjust the temperature in the tank to 30 to 38 ° C. Further, the rising flow rate in the methane fermentation tank 2 is preferably 0.1 to 2 m / hour, more preferably 0.5 to 1.5 m / hour. By performing such processing,
80% or more of the COD in the organic wastewater is removed, and the generated methane gas is effectively used as fuel.
【００１０】さらに、本発明においては、第３工程とし
て、メタン発酵槽２の処理水１３を造粒脱りん槽３の原
水１４として造粒脱りん槽３に供給する。ここで、造粒
脱りん槽３の容積は、０．５〜７０ｋｇＰ／ｍ3 ・日の
容積負荷となることが好ましく、さらには、１〜１０ｋ
ｇＰ／ｍ3 ・日の容積負荷となることが好ましい。ま
た、造粒脱りん槽３の原水１４の水理学的滞留時間は１
０分以上とすることが好ましく、特に、３０〜６０分と
することが好ましい。造粒脱りん槽３の内部は、混合性
を良くするために、二重円筒管から構成されており、造
粒脱りん槽３の原水１４は内部の円筒管中に供給され、
造粒脱りん槽３の内部にマグネシウム化合物１５が添加
される。ここで、マグネシウム化合物１５は、〔Ｍ
ｇ2+〕／〔ＰＯ4 3- 〕が１以上となるように添加され、
特に、〔Ｍｇ2+〕／〔ＰＯ4 3- 〕が１以上２以下となる
ように添加されることが好ましい。用いられるマグネシ
ウム化合物１５としては、特に限定されるものではない
が、水酸化マグネシウム溶液や塩化マグネシウム溶液を
用いることが好ましい。また、造粒脱りん槽３の内部で
のｐＨを８〜１０に調整することが必要であり、好まし
くは、ｐＨが８〜９．５となるようにアルカリ剤７を添
加して調整する。アルカリ剤７としては、特に限定され
るものではないが、苛性ソーダを用いることが好まし
い。また、造粒脱りん槽３の内部は常時撹拌混合する。
撹拌方法としては、撹拌翼により機械的に撹拌してもよ
いが、所要動力、維持管理性の面から、空気１６を造粒
脱りん槽３の底部より供給し、撹拌することが好まし
い。このような処理を行うことにより、造粒脱りん槽３
の原水１４に含まれるりん酸イオンとアンモニウムイオ
ンがマグネシウムイオンと反応して、りん酸マグネシウ
ムアンモニウムの固体粒子１７が生成される。Further, in the present invention, as a third step, the treated water 13 of the methane fermentation tank 2 is supplied to the granulation dephosphorization tank 3 as raw water 14 of the granulation dephosphorization tank 3. Here, the volume of the granulation dephosphorization tank 3 is preferably a volume load of 0.5 to 70 kgP / m 3 · day, and more preferably 1 to 10 kP / m 3.
Preferably, the volume load is gP / m 3 · day. The hydraulic retention time of the raw water 14 in the granulation dephosphorization tank 3 is 1
The time is preferably 0 minutes or more, particularly preferably 30 to 60 minutes. The inside of the granulation and dephosphorization tank 3 is composed of a double cylindrical tube in order to improve the mixing property, and the raw water 14 of the granulation and dephosphorization tank 3 is supplied into the internal cylindrical tube,
The magnesium compound 15 is added to the inside of the granulation dephosphorization tank 3. Here, the magnesium compound 15 is represented by [M
g 2+ ] / [PO 4 3- ] is 1 or more,
In particular, it is preferable that [Mg 2+ ] / [PO 4 3- ] be added so that it is 1 or more and 2 or less. The magnesium compound 15 to be used is not particularly limited, but a magnesium hydroxide solution or a magnesium chloride solution is preferably used. Further, it is necessary to adjust the pH inside the granulation dephosphorization tank 3 to 8 to 10, and preferably, the alkali agent 7 is added so that the pH becomes 8 to 9.5. The alkali agent 7 is not particularly limited, but it is preferable to use caustic soda. Further, the inside of the granulation dephosphorization tank 3 is constantly stirred and mixed.
As the stirring method, mechanical stirring may be performed by a stirring blade, but it is preferable to supply the air 16 from the bottom of the granulation and dephosphorization tank 3 and perform stirring from the viewpoint of required power and maintainability. By performing such processing, the granulation dephosphorization tank 3
The phosphate ions and ammonium ions contained in the raw water 14 react with magnesium ions to generate solid particles 17 of magnesium ammonium phosphate.
【００１１】生成したりん酸マグネシウムアンモニウム
の固体粒子１７は、造粒脱りん槽３下部の沈殿部におい
て沈降分離され、槽底部より１〜２週間の間隔で引き抜
かれ、化成肥料として有効利用される。ここで、造粒脱
りん槽３の原水１４はメタン発酵槽２の処理水１３であ
り、総アルカリ度は一般的に１０００ｍｇ／リットル以
上を示し、りん酸マグネシウムアンモニウム粒子の造粒
に有効に働いて、取扱い容易な粒径０．５〜１ｍｍのり
ん酸マグネシウムアンモニウムの固体粒子を得ることが
可能となる。造粒脱りん槽３の原水１４中のりん酸イオ
ンとアンモニウムイオンが除去された造粒脱りん槽３の
処理水１８は造粒脱りん槽３の上部より溢流する。この
ようにして、原水４中のりん酸イオン濃度を、りん酸態
りん濃度として８ｍｇ／リットル以下にまで減少させる
ことができる。The produced solid particles 17 of magnesium ammonium phosphate are settled and separated in the sedimentation section at the bottom of the granulation and dephosphorization tank 3 and are withdrawn from the bottom of the tank at intervals of one to two weeks, and are effectively used as chemical fertilizer. . Here, the raw water 14 of the granulation and dephosphorization tank 3 is the treated water 13 of the methane fermentation tank 2 and the total alkalinity generally shows 1000 mg / liter or more, and effectively works for granulation of magnesium ammonium phosphate particles. Thus, solid particles of magnesium ammonium phosphate having a particle size of 0.5 to 1 mm which can be easily handled can be obtained. The treated water 18 of the granulation dephosphorization tank 3 from which the phosphate ions and ammonium ions in the raw water 14 of the granulation dephosphorization tank 3 have been removed overflows from the upper part of the granulation dephosphorization tank 3. In this way, the phosphate ion concentration in the raw water 4 can be reduced to a phosphoric acid phosphorus concentration of 8 mg / liter or less.
【００１２】図２は、本発明の有機性廃水の処理方法の
他の例を示す概略図である。すなわち、原水４中の窒素
濃度が高いか、あるいはアンモニア性窒素以外の窒素成
分で構成されており、図１に示した処理工程のみでは河
川放流水程度にまで窒素除去が達成されないような場
合、前記した工程の後に、造粒脱りん槽３の処理水１８
を生物学的硝化脱窒する工程を付加するものである。生
物学的硝化脱窒法としては、造粒脱りん槽３の処理水１
８中の残留有機物や原水４の一部を添加して、これを水
素供与体として利用する脱窒素工程と、硝化工程とを直
列的に結合させ、硝化工程からの流出水（硝化液）を脱
窒素工程にリサイクルさせるという循環式硝化脱窒法
や、曝気−非曝気の間欠曝気方式による活性汚泥法を採
用することができる。循環式硝化脱窒法は、図２に示し
たように撹拌装置５により常時撹拌混合される脱窒槽１
９と、後続する硝化槽２０より構成され、硝化槽２０は
空気１６により好気状態に保たれており、硝酸態窒素Ｎ
Ｏｘ−Ｎが生成する。そして、硝化液の一部を循環用ポ
ンプ２１により循環水２２として前段の脱窒槽１９に循
環させ、硝化槽２０にて生成した硝酸態窒素ＮＯｘ−Ｎ
を脱窒槽１９で窒素ガスに還元する。また、脱窒槽１９
に、造粒脱りん槽３の処理水１８中に残留したＢＯＤ成
分、あるいはそれだけでは不足する場合には原水４中の
一部を添加することによってＢＯＤ成分を供給し、これ
を脱窒菌の水素供与体として利用してＮＯｘ−Ｎのガス
化（Ｎ2 ガス）を行う。このようにして有機性廃水中の
窒素が除去された処理水２３が得られる。なお、硝化槽
２０に繊維状担体等の硝化菌固定化担体を投入すること
で、反応槽容積の縮小が可能である。FIG. 2 is a schematic view showing another example of the method for treating organic wastewater of the present invention. That is, when the nitrogen concentration in the raw water 4 is high, or the raw water 4 is composed of nitrogen components other than ammoniacal nitrogen, and only the treatment process shown in FIG. 1 cannot achieve nitrogen removal to about the river discharge water, After the above steps, the treated water 18 in the granulation dephosphorization tank 3
And a step of biological nitrification and denitrification. As the biological nitrification and denitrification method, the treated water 1 in the granulation dephosphorization tank 3 is used.
8 and a denitrification step in which a part of the raw water 4 is used as a hydrogen donor and a nitrification step are connected in series, and effluent water (nitrification liquid) from the nitrification step is converted. A recirculation type nitrification denitrification method of recycling to a denitrification step or an activated sludge method by an intermittent aeration method with aeration and non-aeration can be adopted. In the recirculation type nitrification denitrification method, as shown in FIG.
9 and a subsequent nitrification tank 20. The nitrification tank 20 is maintained in an aerobic state by air 16, and nitrate nitrogen N
Ox-N is produced. Then, a part of the nitrification solution is circulated as circulating water 22 by the circulation pump 21 to the denitrification tank 19 in the preceding stage, and the nitrate nitrogen NOx-N generated in the nitrification tank 20 is circulated.
Is reduced to nitrogen gas in the denitrification tank 19. In addition, the denitrification tank 19
In addition, the BOD component remaining in the treated water 18 of the granulation and dephosphorization tank 3 or, if insufficient, a portion of the raw water 4 is added to supply the BOD component, and this is added to the hydrogen of the denitrifying bacteria. utilized as donor perform gasification of NOx-N a (N 2 gas). Thus, the treated water 23 from which nitrogen in the organic wastewater has been removed is obtained. It is possible to reduce the volume of the reaction tank by charging a nitrifying bacteria-immobilized carrier such as a fibrous carrier into the nitrification tank 20.
【００１３】また、本発明における生物学的硝化脱窒法
として、曝気−非曝気の間欠曝気方式による活性汚泥法
も適用することができる。この方式では、曝気槽での曝
気装置のＯＮ−ＯＦＦ運転により好気−嫌気状態が交互
に起こり、造粒脱りん槽３の処理水１８中のＢＯＤ成分
が除去される。また、窒素成分の硝化作用、ＮＯｘ−Ｎ
の窒素ガス化が起こり、有機性廃水中の窒素除去が可能
である。以上に示すように、本発明の一連のシステムに
より、有機性廃水中のＣＯＤ、ＢＯＤ、りん、窒素共に
８０％以上の除去が可能であり、河川放流水程度まで処
理でき、さらに廃棄物の発生を極めて少なくすることが
できる。Further, as the biological nitrification denitrification method in the present invention, an activated sludge method using an intermittent aeration method with aeration and non-aeration can be applied. In this method, an aerobic-anaerobic state occurs alternately by the ON-OFF operation of the aeration device in the aeration tank, and the BOD component in the treated water 18 of the granulation dephosphorization tank 3 is removed. In addition, nitrification of nitrogen components, NOx-N
Of the organic wastewater can be removed. As described above, the series of systems of the present invention can remove 80% or more of COD, BOD, phosphorus, and nitrogen in organic wastewater, can process up to about river discharge water, and generate waste. Can be extremely reduced.
【００１４】[0014]
【実施例】次に、本発明を実施例によって具体的に説明
する。 実施例１ ＣＯＤCr１５００ｍｇ／リットル、溶解性りん濃度３０
０ｍｇ／リットル、溶解性窒素２００ｍｇ／リットルを
含有する製油工場廃水を水理学的滞留時間１５時間で酸
生成槽（容量：５００リットル）に供給した。なお、２
４重量％の苛性ソーダを用いて酸生成槽内のｐＨを６に
調整し、温度を３０℃に調整した。その後、酸生成槽の
処理水を容積負荷５ｋｇＣＯＤ／ｍ3 ・日、汚泥負荷
０．３ｋｇＣＯＤ／ｋｇＶＳＳ・日でＵＡＳＢ型メタン
発酵槽（容量：２４０リットル）に供給し、水理学的滞
留時間を７時間とした。なお、２４重量％の苛性ソーダ
を用いてメタン発酵槽内のｐＨを７に調整し、温度を３
５℃に調整した。Next, the present invention will be described specifically with reference to examples. Example 1 COD Cr 1500 mg / L, soluble phosphorus concentration 30
Refinery wastewater containing 0 mg / L and 200 mg / L of soluble nitrogen was fed to an acid generator (volume: 500 L) with a hydraulic residence time of 15 hours. In addition, 2
The pH in the acid generating tank was adjusted to 6 using 4% by weight of caustic soda, and the temperature was adjusted to 30 ° C. Thereafter, the treated water in the acid production tank was supplied to a UASB-type methane fermentation tank (capacity: 240 liters) at a volume load of 5 kg COD / m 3 · day and a sludge load of 0.3 kg COD / kg VSS · day, and the hydraulic retention time was 7 days. Time. The pH in the methane fermentation tank was adjusted to 7 using 24% by weight of caustic soda, and the temperature was adjusted to 3%.
The temperature was adjusted to 5 ° C.
【００１５】次に、メタン発酵槽の処理水を水理学的滞
留時間６０分で造粒脱りん槽（容量：３０リットル）に
供給し、３５重量％の水酸化マグネシウムを〔Ｍｇ2+〕
／〔ＰＯ4 3- 〕＝１となるように添加した。水酸化マグ
ネシウムの添加により、造粒脱りん槽内のｐＨは８．５
にまで上昇したので、ｐＨの調整は行わなかった。１週
間の連続通水の結果、粒径０．３〜０．５ｍｍのりん酸
マグネシウムアンモニウムの固体粒子が造粒脱りん槽底
部より回収された。１週間の連続通水の平均処理水質を
表１に示す。Next, the treated water of the methane fermentation tank is supplied to a granulation dephosphorization tank (capacity: 30 liters) with a hydraulic retention time of 60 minutes, and 35% by weight of magnesium hydroxide is added to [Mg 2+ ].
/ [PO 4 3- ] = 1. The pH in the granulation dephosphorization tank was 8.5 by adding magnesium hydroxide.
The pH was not adjusted. As a result of continuous water passing for one week, solid particles of magnesium ammonium phosphate having a particle diameter of 0.3 to 0.5 mm were collected from the bottom of the granulation dephosphorization tank. Table 1 shows the average treated water quality for one week of continuous water flow.
【００１６】[0016]
【表１】 [Table 1]
【００１７】表１より明らかなように、本発明の処理方
法によれば、造粒脱りん槽の処理水は原水に対して、Ｃ
ＯＤCr９０％、溶解性りん９７％、溶解性窒素８０％の
除去率が得られた。一方、メタン発酵槽の処理水を、ア
ルミニウムや鉄の金属塩による従来の凝集沈殿法で処理
すると、溶解性りんについては、原水に対して９５％以
上の除去率が得られたものの、溶解性窒素については、
３０％程度の除去率しか得られなかった。また、生成し
たスラッジはスラリー状で取扱いが困難であり、脱水
後、廃棄物として処分せざるを得なかった。As is apparent from Table 1, according to the treatment method of the present invention, the treated water in the granulation and dephosphorization tank is C
A removal rate of 90% OD Cr , 97% soluble phosphorus and 80% soluble nitrogen was obtained. On the other hand, when the treated water of the methane fermentation tank is treated by the conventional coagulation and sedimentation method using a metal salt of aluminum or iron, a soluble phosphorus removal rate of 95% or more relative to the raw water was obtained. For nitrogen,
Only a removal rate of about 30% was obtained. Further, the generated sludge was in a slurry state and difficult to handle, and had to be disposed of as waste after dehydration.
【００１８】実施例２ ＣＯＤCr５０００ｍｇ／リットル、溶解性りん濃度２０
０ｍｇ／リットル、溶解性窒素７００ｍｇ／リットルを
含有するアルコール蒸留残液を水理学的滞留時間６時間
で酸生成槽（実施例１で用いたものと同じ）に供給し
た。なお、２４重量％の苛性ソーダを用いて酸生成槽内
のｐＨを６に調整し、温度を３０℃に調整した。その
後、酸生成槽の処理水を容積負荷１０ｋｇＣＯＤ／ｍ3
・日、汚泥負荷０．４ｋｇＣＯＤ／ｋｇＶＳＳ・日でＵ
ＡＳＢ型メタン発酵槽（実施例１で用いたものとと同
じ）に供給し、水理学的滞留時間を１２時間とした。な
お、２４重量％の苛性ソーダを用いてメタン発酵槽内の
ｐＨを７に調整し、温度を３５℃に調整した。Example 2 COD Cr 5000 mg / liter, soluble phosphorus concentration 20
An alcohol distillation residue containing 0 mg / liter and 700 mg / liter of soluble nitrogen was fed to an acid generator (same as used in Example 1) with a hydraulic residence time of 6 hours. The pH in the acid generating tank was adjusted to 6 using 24% by weight of caustic soda, and the temperature was adjusted to 30 ° C. Thereafter, the treated water in the acid generation tank was loaded with a volume load of 10 kg COD / m 3.
・ Day, sludge load 0.4kgCOD / kgVSS ・ day
The mixture was fed to an ASB type methane fermenter (same as that used in Example 1), and the hydraulic residence time was set to 12 hours. The pH in the methane fermentation tank was adjusted to 7 using 24% by weight of caustic soda, and the temperature was adjusted to 35 ° C.
【００１９】次に、メタン発酵槽の処理水を水理学的滞
留時間６０分で造粒脱りん槽（実施例１で用いたものと
同じ）に供給し、３５重量％水酸化マグネシウムを〔Ｍ
ｇ2+〕／〔ＰＯ4 3- 〕＝１となるように添加した。水酸
化マグネシウムの添加により、造粒脱りん槽内のｐＨは
８．５にまで上昇したので、ｐＨの調整は行わなかっ
た。１週間の連続通水の結果、粒径０．３〜０．５ｍｍ
のりん酸マグネシウムアンモニウム粒子が造粒脱りん槽
底部より回収された。さらに、造粒脱りん槽の処理水を
循環式硝化脱窒槽（硝化槽の容量：１８０リットル、脱
窒槽の容量：１２０リットル）に供給した。脱窒槽、硝
化槽共にＭＬＳＳは３０００ｍｇ／リットルとし、硝化
槽には生物担体として、直径５〜１０ｍｍの繊維状担体
を硝化槽容積の２０％投入した。脱窒槽の滞留時間を６
時間、硝化槽の滞留時間を９時間とし、循環比Ｒは原水
に対して１．５とした。１週間の連続通水の平均処理水
質を表２に示す。Next, the treated water of the methane fermentation tank was supplied to a granulation dephosphorization tank (same as that used in Example 1) with a hydraulic residence time of 60 minutes, and 35% by weight of magnesium hydroxide was added to [M
g 2+] / [added PO 4 3-] = 1 and becomes like. Since the pH in the granulation dephosphorization tank was increased to 8.5 by the addition of magnesium hydroxide, the pH was not adjusted. One week continuous water flow results in a particle size of 0.3-0.5 mm
Was recovered from the bottom of the granulation dephosphorization tank. Further, the treated water in the granulation dephosphorization tank was supplied to a circulating nitrification denitrification tank (nitrification tank capacity: 180 liters, denitrification tank capacity: 120 liters). Both the denitrification tank and the nitrification tank had an MLSS of 3000 mg / liter, and a fibrous carrier having a diameter of 5 to 10 mm was charged into the nitrification tank as a biological carrier at 20% of the volume of the nitrification tank. Denitrification tank stay time 6
Time, the residence time in the nitrification tank was 9 hours, and the circulation ratio R was 1.5 with respect to the raw water. Table 2 shows the average treated water quality for one week of continuous water flow.
【００２０】[0020]
【表２】 [Table 2]
【００２１】表２から明らかなように、本発明の処理方
法によれば、循環式硝化脱窒槽の処理水は原水に対し
て、ＣＯＤCr９８％、溶解性りん９７％、溶解性窒素９
１％の除去率が得られた。一方、メタン発酵槽の処理水
をアルミニウムや鉄の金属塩による従来の凝集沈殿法で
処理すると、溶解性りんについては、原水に対して９５
％以上の除去率が得られたものの、溶解性窒素について
は、３０％程度の除去率しか得られなかった。また、生
成したスラッジはスラリー状で取扱いが困難であり、脱
水後、廃棄物として処分せざるを得なかった。As is clear from Table 2, according to the treatment method of the present invention, the treated water in the circulating nitrification denitrification tank is 98% COD Cr , 97% soluble phosphorus and 9% soluble nitrogen, based on the raw water.
A removal rate of 1% was obtained. On the other hand, when the treated water in the methane fermentation tank is treated by the conventional coagulation and sedimentation method using a metal salt of aluminum or iron, the soluble phosphorus is reduced by 95% relative to the raw water.
%, But only about 30% of soluble nitrogen was obtained. Further, the generated sludge was in a slurry state and difficult to handle, and had to be disposed of as waste after dehydration.
【００２２】[0022]
【発明の効果】本発明によれば、りん及び窒素を含有し
た高濃度有機性廃水から、有機物、りん及び窒素を効率
良く除去することが可能であり、さらに、廃棄物の発生
を極めて少なくすることができる。According to the present invention, organic matter, phosphorus and nitrogen can be efficiently removed from high-concentration organic wastewater containing phosphorus and nitrogen, and furthermore, the generation of waste can be extremely reduced. be able to.
【図１】本発明の有機性廃水の処理方法の一例を示す概
略図である。FIG. 1 is a schematic view showing an example of a method for treating organic wastewater of the present invention.
【図２】本発明の有機性廃水の処理方法の別の例を示す
概略図である。FIG. 2 is a schematic view showing another example of the method for treating organic wastewater of the present invention.
１ 酸生成槽 ２ ＵＡＳＢ型メタン発酵槽 ３ 造粒脱りん槽 ４ 原水 ５ 撹拌装置 ６ 酸性溶液又はアルカリ剤 ７ アルカリ剤 ８ 酸生成槽の処理水 ９ メタン 10 メタン発酵槽の原水 11 メタン発酵槽の処理水循環水 12 三相分離装置 13 メタン発酵槽の処理水 14 造粒脱りん槽の原水 15 マグネシウム化合物 16 空気 17 りん酸マグネシウムアンモニウムの固体粒子 18 造粒脱りん槽の処理水 19 脱窒槽 20 硝化槽 21 循環用ポンプ 22 循環水 23 生物学的脱窒槽の処理水 DESCRIPTION OF SYMBOLS 1 Acid production tank 2 UASB type methane fermentation tank 3 Granulation dephosphorization tank 4 Raw water 5 Stirrer 6 Acid solution or alkali agent 7 Alkaline agent 8 Treatment water of acid generation tank 9 Methane 10 Raw water of methane fermentation tank 11 Treated water circulating water 12 Three-phase separator 13 Treated water of methane fermentation tank 14 Raw water of granulated dephosphorization tank 15 Magnesium compound 16 Air 17 Solid particles of magnesium ammonium phosphate 18 Treated water of granulated dephosphorization tank 19 Denitrification tank 20 Nitrification Tank 21 Circulation pump 22 Circulating water 23 Treated water in biological denitrification tank
Claims (2)
有機物、りん及び窒素を除去することを特徴とする有機
性廃水の処理方法。 （１）りん及び窒素を含有する有機性廃水を酸生成槽で
酸発酵を行う工程、 （２）上向流式嫌気性汚泥床型メタン発酵槽でメタン発
酵を行う工程、 （３）マグネシウム化合物を添加し、ｐＨを８〜１０に
調整するとともに、曝気によって攪拌混合を行うことに
より、生成したりん酸マグネシウムアンモニウムの固体
粒子を回収する工程。1. A method for treating organic wastewater, comprising removing organic matter, phosphorus and nitrogen from the organic wastewater in the following three steps. (1) a step of conducting acid fermentation of organic wastewater containing phosphorus and nitrogen in an acid production tank; (2) a step of conducting methane fermentation in an upward flow anaerobic sludge bed type methane fermentation tank; (3) a magnesium compound And adjusting the pH to 8 to 10 and stirring and mixing by aeration to collect the generated solid particles of magnesium ammonium phosphate.
中の有機物、りん及び窒素を除去することを特徴とする
有機性廃水の処理方法。 （４）請求項１記載の処理方法によって得られた処理水
を生物学的硝化脱窒する工程。2. A method for treating organic wastewater, which further comprises adding the following step to remove organic substances, phosphorus and nitrogen in the organic wastewater. (4) A step of biologically nitrifying and denitrifying the treated water obtained by the treatment method according to claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP27922396A JPH10118687A (en) | 1996-10-22 | 1996-10-22 | Treatment method of organic wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP27922396A JPH10118687A (en) | 1996-10-22 | 1996-10-22 | Treatment method of organic wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH10118687A true JPH10118687A (en) | 1998-05-12 |
Family
ID=17608150
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP27922396A Pending JPH10118687A (en) | 1996-10-22 | 1996-10-22 | Treatment method of organic wastewater |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH10118687A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| WO2005005328A1 (en) | 2003-07-14 | 2005-01-20 | Ebara Corporation | Method of utilizing recovered magnesium ammonium phosphate and apparatus therefor |
| JP2006289168A (en) * | 2005-04-06 | 2006-10-26 | Maezawa Ind Inc | Wastewater treatment equipment |
| WO2007023170A1 (en) * | 2005-08-23 | 2007-03-01 | Thomas Dockhorn | Device and method for treating waste waters |
| WO2007076953A1 (en) * | 2005-12-23 | 2007-07-12 | Fraunhofer Gesellschaft zur Förderung der angewandten Forschung e.V. | Anaerobic purification of wastewater |
| EP1698595A4 (en) * | 2003-11-21 | 2010-03-17 | Ebara Corp | METHOD FOR FORMING / RECOVERING MAGNESIUM / AMMONIUM PHOSPHATE, AND APPARATUS THEREFOR |
| WO2013153531A1 (en) | 2012-04-11 | 2013-10-17 | Universidade Do Minho | Nanoporous, aluminium-supported alumina membrane, method for producing same and use thereof |
| CN106976977A (en) * | 2017-05-19 | 2017-07-25 | 上海惠果环境工程有限公司 | Cultivating wastewater purification and recovery system |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| WO2005005328A1 (en) | 2003-07-14 | 2005-01-20 | Ebara Corporation | Method of utilizing recovered magnesium ammonium phosphate and apparatus therefor |
| EP1650170A4 (en) * | 2003-07-14 | 2010-01-13 | Ebara Corp | PROCESS FOR USING DOUBLE AMMONIUM PHOSPHATE AND MAGNESIUM AND APPARATUS THEREOF |
| EP1698595A4 (en) * | 2003-11-21 | 2010-03-17 | Ebara Corp | METHOD FOR FORMING / RECOVERING MAGNESIUM / AMMONIUM PHOSPHATE, AND APPARATUS THEREFOR |
| JP2006289168A (en) * | 2005-04-06 | 2006-10-26 | Maezawa Ind Inc | Wastewater treatment equipment |
| WO2007023170A1 (en) * | 2005-08-23 | 2007-03-01 | Thomas Dockhorn | Device and method for treating waste waters |
| WO2007076953A1 (en) * | 2005-12-23 | 2007-07-12 | Fraunhofer Gesellschaft zur Förderung der angewandten Forschung e.V. | Anaerobic purification of wastewater |
| WO2013153531A1 (en) | 2012-04-11 | 2013-10-17 | Universidade Do Minho | Nanoporous, aluminium-supported alumina membrane, method for producing same and use thereof |
| CN106976977A (en) * | 2017-05-19 | 2017-07-25 | 上海惠果环境工程有限公司 | Cultivating wastewater purification and recovery system |
| CN106976977B (en) * | 2017-05-19 | 2024-05-17 | 上海惠果环境工程有限公司 | Cultivation wastewater treatment and recovery system |
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