JPS6339309B2 - - Google Patents
Info
- Publication number
- JPS6339309B2 JPS6339309B2 JP55091429A JP9142980A JPS6339309B2 JP S6339309 B2 JPS6339309 B2 JP S6339309B2 JP 55091429 A JP55091429 A JP 55091429A JP 9142980 A JP9142980 A JP 9142980A JP S6339309 B2 JPS6339309 B2 JP S6339309B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- chemical oxidation
- tank
- hydrogen peroxide
- added
- 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.)
- Expired
Links
- 239000010802 sludge Substances 0.000 claims description 65
- 238000011282 treatment Methods 0.000 claims description 51
- 238000000034 method Methods 0.000 claims description 46
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 38
- 239000000126 substance Substances 0.000 claims description 32
- 230000003647 oxidation Effects 0.000 claims description 24
- 238000007254 oxidation reaction Methods 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 21
- 239000002351 wastewater Substances 0.000 claims description 13
- 239000007800 oxidant agent Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 229910052742 iron Inorganic materials 0.000 claims description 6
- -1 iron ions Chemical class 0.000 claims description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 4
- 239000011707 mineral Substances 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 2
- 238000003672 processing method Methods 0.000 claims 2
- 230000003472 neutralizing effect Effects 0.000 claims 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 10
- 238000003756 stirring Methods 0.000 description 10
- 239000002002 slurry Substances 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000005273 aeration Methods 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 150000002500 ions Chemical class 0.000 description 6
- 229910000358 iron sulfate Inorganic materials 0.000 description 6
- 238000004062 sedimentation Methods 0.000 description 6
- 229920006317 cationic polymer Polymers 0.000 description 5
- 239000010800 human waste Substances 0.000 description 5
- 238000006386 neutralization reaction Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000010306 acid treatment Methods 0.000 description 4
- 239000005708 Sodium hypochlorite Substances 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- 239000011790 ferrous sulphate Substances 0.000 description 3
- 235000003891 ferrous sulphate Nutrition 0.000 description 3
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 3
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000009264 composting Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 150000002505 iron Chemical class 0.000 description 2
- 238000010169 landfilling Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 2
- 239000000347 magnesium hydroxide Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- OXIKLRTYAYRAOE-CMDGGOBGSA-N (e)-3-(1-benzyl-3-pyridin-3-ylpyrazol-4-yl)prop-2-enoic acid Chemical compound N1=C(C=2C=NC=CC=2)C(/C=C/C(=O)O)=CN1CC1=CC=CC=C1 OXIKLRTYAYRAOE-CMDGGOBGSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 229920006318 anionic polymer Polymers 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229960004887 ferric hydroxide Drugs 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 238000002604 ultrasonography Methods 0.000 description 1
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、下水、し尿、し尿浄化槽汚泥、ゴミ
埋立滲出汚水、各種産業廃水などの有機性廃水の
革新的な処理プロセスに関するものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to an innovative treatment process for organic wastewater such as sewage, human waste, human waste septic tank sludge, landfill leachate, and various industrial wastewaters.
最近、活性汚泥法などの種々の生物処理を行つ
ても除去されない色度成分や、難生物分解性の
COD成分を除去するための方法として、鉄塩ま
たはアルミニウム塩と、過酸化水素またはオゾン
との併用の化学酸化処理法が知られている。（な
お、これら酸化剤と光、超音波の併用法もよく知
られている）
例えば、古くからフエントン法として知られて
いる、鉄塩と過酸化水素の併用法では第１図に示
すように希釈水で10〜20倍希釈された廃水１は活
性汚泥法の曝気槽２ａにおいて曝気用空気３２で
充分生成処理され、曝気槽２ａからの流出スラリ
ー３は、沈殿池４で固液分離され、スラツジ５の
一部は返送汚泥６として曝気槽２ａに返送され、
残部は余剰汚泥１６ａとなる。沈殿池４の越流水
７（この中には、BODは殆どないが、色度と難
生物分解性CODが多量に含まれている）は化学
酸化処理槽８に流入し、前記鉄イオンを解離する
物質としての硫酸鉄９と前記酸化剤としての過酸
化水素１０が添加され、PH２〜４の酸性条件下で
所定時間撹拌されCOD、色度などが分解された
のち、中和槽１１において苛性ソーダなどのアル
カリ剤１２が添加され、PH６前後に中和される。
この中和処理によつて、水酸化第２鉄Fe（OH）3
を主体とするスラツジ１３ａが析出するので、こ
れを沈殿池１４にて分離して処理水１５とするも
のである。
Recently, chromatic components that cannot be removed even with various biological treatments such as activated sludge method, and those that are difficult to biodegrade
As a method for removing COD components, a chemical oxidation treatment method using a combination of iron salt or aluminum salt and hydrogen peroxide or ozone is known. (In addition, the combined use of these oxidizing agents, light, and ultrasound is also well known.) For example, in the combined use of iron salt and hydrogen peroxide, which has long been known as the Fuenton method, as shown in Figure 1. Wastewater 1 diluted 10 to 20 times with dilution water is sufficiently generated and treated with aeration air 32 in an aeration tank 2a of the activated sludge method, and slurry 3 flowing out from the aeration tank 2a is separated into solid and liquid in a settling tank 4. A part of the sludge 5 is returned to the aeration tank 2a as return sludge 6,
The remainder becomes surplus sludge 16a. The overflow water 7 of the settling tank 4 (there is almost no BOD in it, but it contains a large amount of chromatic and non-biodegradable COD) flows into the chemical oxidation treatment tank 8, where the iron ions are dissociated. Iron sulfate (9) as a substance to be oxidized and hydrogen peroxide (10) as an oxidizing agent are added, stirred for a predetermined time under acidic conditions of pH 2 to 4 to decompose COD, chromaticity, etc., and then mixed with caustic soda in a neutralization tank 11. An alkaline agent 12 such as the following is added to neutralize the pH to around 6.
Through this neutralization treatment, ferric hydroxide Fe(OH) 3
A sludge 13a mainly composed of is precipitated, and this is separated in a sedimentation tank 14 and used as treated water 15.
一方、前記生物処理工程からの余剰汚泥１６ａ
と前記化学酸化処理工程から排出されるスラツジ
１７は、混合されたのちカチオンポリマーなど汚
泥脱水用の凝集剤１８が撹拌槽１９に添加混合さ
れたのち、遠心脱水機２０などの脱水機により脱
水ケーキ２１と脱水分離水２２とに分離される。 On the other hand, surplus sludge 16a from the biological treatment process
The sludge 17 discharged from the chemical oxidation treatment process is mixed, and then a flocculant 18 for sludge dewatering such as a cationic polymer is added and mixed in a stirring tank 19, and then a dewatered cake is formed by a dehydrator such as a centrifugal dehydrator 20. 21 and dehydrated separated water 22.
この従来法は、次のような重大な問題点を生じ
ている。
This conventional method has the following serious problems.
生物処理工程から発生する有機性汚泥の脱水
性が悪いため、カチオンポリマーなどの凝集剤
を多量に使用しても、低含水率の脱水ケーキが
得られない。 Because the organic sludge generated from the biological treatment process has poor dewatering properties, a dehydrated cake with a low water content cannot be obtained even if a large amount of flocculant such as a cationic polymer is used.
しかも、化学酸化処理工程からも多量のFe
（OH）3を主体とする難脱水性のスラツジが発
生するので、一層、汚泥発生量が増大し、脱水
ケーキの含水率も高くなる。 Moreover, a large amount of Fe is also produced in the chemical oxidation process.
Since a sludge containing (OH) 3 that is difficult to dehydrate is generated, the amount of sludge generated further increases and the moisture content of the dehydrated cake also increases.
したがつて、脱水ケーキの埋立て、コンポス
ト化、焼却などの汚泥処分工程に不都合を生ず
る。 Therefore, this causes inconvenience in sludge disposal processes such as landfilling, composting, and incineration of the dehydrated cake.
化学酸化処理工程と前記汚泥脱水工程に、そ
れぞれ多量の薬剤を使用するので、運転経費が
著しく高額となる。 Since large amounts of chemicals are used in each of the chemical oxidation treatment step and the sludge dewatering step, operating costs become extremely high.
本発明は、これらの従来プロセスの問題点を解
決することができる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り、生物処理工
程、化学酸化処理工程、汚泥処理工程の各工程を
著しく合理化し、省資源化することを可能にする
ものである。 The purpose of the present invention is to provide a method for treating organic wastewater that can solve the problems of these conventional processes. This makes it possible to significantly streamline the process and save resources.
本発明は、有機性廃水を生物反応槽にて生物処
理する工程と、該生物処理工程の前段及び／又は
後段に化学酸化処理工程を組合わせて処理する方
法において、前記化学酸化処理工程で酸化剤と、
水溶液中で鉄イオンを解離する物質を添加し、生
成する酸化スラツジを直接又は予め濃縮したのち
前記生物処理工程に添加し、前記生物処理工程か
ら排出される、生物処理スラツジと前記酸化スラ
ツジとの混合スラツジに鉱酸を添加したのち、さ
らに過酸化水素を添加し、機械脱水することを特
徴とする有機性廃水の処理方法である。
The present invention provides a method for treating organic wastewater by combining a step of biologically treating organic wastewater in a biological reaction tank and a chemical oxidation treatment step before and/or after the biological treatment step. agent and
A substance that dissociates iron ions in an aqueous solution is added, and the resulting oxidized sludge is added to the biological treatment process either directly or after being concentrated in advance, and the biological treatment sludge discharged from the biological treatment process is combined with the oxidized sludge. This method of treating organic wastewater is characterized by adding mineral acid to the mixed sludge, then further adding hydrogen peroxide, and mechanically dewatering the sludge.
本発明の実施態様を図面を参照しながら説明す
ると、第２図において、し尿、ゴミ滲出汚水など
の（有機性）廃水１は、活性汚泥法など、任意の
生物処理工程の生物反応槽２ｂに流入し、生物処
理によつて、BOD、CODの除去、NH4−Ｎの硝
化脱窒素を受ける。なお、この生物処理工程に生
物学硝化脱窒素プロセス、生物学的脱リンプロセ
スを採用する場合、廃水１は一般に嫌気部に流入
される。生物反応槽２ｂからの流出スラリー３は
沈殿池４に流入し、ここで活性汚泥が分離された
のち、沈殿池４の越流水７は化学酸化処理槽８に
導入され、スリツジ５の一部は返送汚泥６として
生物反応槽２ｂに返送される。前記化学酸化処理
槽８においては越流水７は前記鉄イオンを解離す
る物質として硫酸鉄９と前記酸化剤として過酸化
水素１０が添加、撹拌され、CODと色度が分解
される。
An embodiment of the present invention will be described with reference to the drawings. In Fig. 2, (organic) wastewater 1 such as human waste and garbage-leaching sewage is fed into a biological reaction tank 2b of any biological treatment process such as an activated sludge method. The inflow is subjected to biological treatment to remove BOD and COD, and to nitrify and denitrify NH 4 -N. Note that when a biological nitrification denitrification process or a biological dephosphorization process is employed in this biological treatment step, the wastewater 1 generally flows into an anaerobic section. The outflow slurry 3 from the biological reaction tank 2b flows into the settling tank 4, where the activated sludge is separated, and then the overflow water 7 of the settling tank 4 is introduced into the chemical oxidation treatment tank 8, and a part of the sludge 5 is The sludge is returned to the biological reaction tank 2b as return sludge 6. In the chemical oxidation treatment tank 8, to the overflow water 7, iron sulfate 9 as a substance for dissociating the iron ions and hydrogen peroxide 10 as the oxidizing agent are added and stirred to decompose the COD and chromaticity.
次で、化学酸化処理槽８のスラリーは中和槽１
１に流入し、ここで水酸化マグネシウムなどのア
ルカリ剤１２が添加され、析出するFe（OH）3を
主体とする沈殿物を含むスラリーは沈殿池１４に
て沈殿スラツジとしての酸化スラツジ１３ｂと処
理水１５に沈降分離され、酸化スラツジ１３ｂは
生物反応槽２ｂ又は前記流出スラリー３にリサイ
クルされる。 Next, the slurry in chemical oxidation treatment tank 8 is transferred to neutralization tank 1.
1, an alkaline agent 12 such as magnesium hydroxide is added thereto, and the precipitated slurry containing a precipitate mainly composed of Fe(OH) 3 is processed in a settling tank 14 as an oxidized sludge 13b as a precipitated sludge. The oxidized sludge 13b is separated by sedimentation into water 15 and recycled to the biological reaction tank 2b or the effluent slurry 3.
このような方法によると、緻密な酸化スラツジ
１３ｂが流出スラリー３中の活性汚泥フロツクに
よつて取り込まれるため、前記活性汚泥の沈降性
が向上し、沈殿池４における懸濁物質のキヤリオ
ーバーが著しく少なくなり、また、バルキングも
発生しにくくなる。 According to such a method, since the dense oxidized sludge 13b is taken up by the activated sludge flocs in the effluent slurry 3, the settling properties of the activated sludge are improved, and the carryover of suspended solids in the settling tank 4 is significantly reduced. In addition, bulking becomes less likely to occur.
一方、生物処理スラツジと酸化スラツジ１３ｂ
との混合スラツジ１６ｂは汚泥処理工程に流入
し、酸処理槽２３において硫酸などの鉱酸２４が
添加され、酸化スラツジ１３ｂ中のFe（OH）3が
溶解し、Fe3+イオン状となる。酸処理槽２３か
らのスラリーは次で撹拌槽２５に流入し、ここで
過酸化水素２６が添加され、Fe3+イオンの触媒
効果によりスラツジが改質され、脱水性が著しく
改善される。撹拌槽２５内の処理液のPHは２〜４
に設定することが好ましく、これにより過酸化水
素２６の酸化力を充分に向上することができる。 On the other hand, biologically treated sludge and oxidized sludge 13b
The mixed sludge 16b flows into the sludge treatment process, where a mineral acid 24 such as sulfuric acid is added in an acid treatment tank 23, and Fe(OH) 3 in the oxidized sludge 13b is dissolved to form Fe 3+ ions. The slurry from the acid treatment tank 23 then flows into the stirring tank 25, where hydrogen peroxide 26 is added and the sludge is reformed by the catalytic effect of Fe 3+ ions, significantly improving the dewatering properties. The pH of the processing liquid in the stirring tank 25 is 2 to 4.
It is preferable to set the oxidizing power of the hydrogen peroxide 26 to a sufficient value.
かくて改質されたスラツジはフイルタープレス
などの機械脱水機２７により脱水され、脱水ケー
キ２８と脱水分離水２９に分離され、脱水分離水
２９は前記化学酸化処理槽８にリサイクルされ、
新品の硫酸鉄９の添加量を不要にするか、又はこ
れが大幅に減少できるようになつている。この場
合、脱水分離水２９中に多量のFe3+イオンを回
収するには前記機械脱水工程をPH２〜３の範囲に
設定することが重要である。 The thus modified sludge is dehydrated by a mechanical dehydrator 27 such as a filter press, separated into a dehydrated cake 28 and dehydrated separated water 29, and the dehydrated separated water 29 is recycled to the chemical oxidation treatment tank 8.
The amount of new iron sulfate 9 added is now unnecessary or can be significantly reduced. In this case, in order to recover a large amount of Fe 3+ ions in the dehydrated separated water 29, it is important to set the mechanical dehydration step to a pH range of 2 to 3.
なお、撹拌槽２５におけるスラツジの改質処理
用のFe3+イオンが、酸化スラツジ１３ｂから溶
出するFe3+イオンの量では不足する場合は硫酸
鉄３０を補充添加してもよい。 Note that if the amount of Fe 3+ ions for the sludge reforming treatment in the stirring tank 25 is insufficient in the amount of Fe 3+ ions eluted from the oxidized sludge 13b, iron sulfate 30 may be supplemented.
また、酸処理槽２３において、酸化スラツジ１
３ｂとのFe（OH）3の溶解に伴つて、残留する
COD成分も溶出してくる場合には、このCOD成
分が処理系内にリサイクルされるのを防止するた
めに、COD除去槽３１に酸化剤として過酸化水
素３３が添加される。この場合、Fe3+イオンは
過酸化水素３３の酸化力向上の触媒として作用す
る。 In addition, in the acid treatment tank 23, the oxidized sludge 1
As Fe(OH) 3 dissolves with 3b, the remaining
When COD components are also eluted, hydrogen peroxide 33 is added to the COD removal tank 31 as an oxidizing agent in order to prevent this COD component from being recycled into the treatment system. In this case, Fe 3+ ions act as a catalyst to improve the oxidizing power of hydrogen peroxide 33.
次に、第３図の実施態様は生物処理工程の前に
化学酸化処理工程を設けた場合である。第３図示
例は、BODよりもCODが高く、かつ、COD成分
が難生物分解性である廃水を処理するのに好適で
ある。すなわち、COD成分が化学酸化処理の結
果、生物分解され易いものに変化し、後続する生
物処理工程で効果的に除去される。また、この場
合、第１図の従来例における沈殿池１４を省略で
きる利点もある。 Next, the embodiment shown in FIG. 3 is a case where a chemical oxidation treatment step is provided before the biological treatment step. The example shown in the third figure is suitable for treating wastewater in which the COD is higher than the BOD and the COD component is hardly biodegradable. That is, as a result of the chemical oxidation treatment, the COD component changes into something that is easily biodegradable, and is effectively removed in the subsequent biological treatment process. Further, in this case, there is an advantage that the sedimentation tank 14 in the conventional example shown in FIG. 1 can be omitted.
なお、本発明においては、前記生物処理工程と
して、回転円板法、流動触媒生物処理法などの生
物膜法を採用した場合、前記返送汚泥６の返送は
不要となる。また、化学処理槽８、COD除去槽
３１に添加される前記酸化剤としては、過酸化水
素のほかに、オゾン、塩素系酸化剤（次亜塩素酸
ソーダなど）も使用でき、これらの併用も可能で
ある。さらに前記アルカリ剤１２としては、極め
て緻密な酸化スラツジ１３ｂが得られることから
マグネシウム系アルカリ剤が好ましいが、苛性ソ
ーダ、消石灰の使用も可能である。 In addition, in the present invention, when a biofilm method such as a rotating disk method or a fluidized catalyst biological treatment method is employed as the biological treatment step, the return sludge 6 does not need to be returned. In addition, as the oxidizing agent added to the chemical treatment tank 8 and the COD removal tank 31, in addition to hydrogen peroxide, ozone and chlorine-based oxidizing agents (sodium hypochlorite, etc.) can also be used, and these can also be used in combination. It is possible. Further, as the alkaline agent 12, a magnesium-based alkaline agent is preferable because an extremely dense oxidized sludge 13b can be obtained, but caustic soda and slaked lime can also be used.
また、第２図示例では化学酸化処理槽８と、撹
拌槽２５において、同一種類の前記金属イオン解
離物質が添加されているが、互いに異なる種類の
ものを使用してもよく、また、上記各槽で複数種
類のものを使用する場合、その組合わせが異なる
ものであつてもよい。 Further, in the second illustrated example, the same type of metal ion dissociated substance is added to the chemical oxidation treatment tank 8 and the stirring tank 25, but different types of substances may be used. When using a plurality of types in a tank, the combinations may be different.
本発明によれば、次のような工業上重要な利益
を得ることができる。
According to the present invention, the following industrially important benefits can be obtained.
(1) 生物処理工程からの余剰汚泥、酸化スラツジ
の両者を極めて合理的に改質でき、含水率の低
い脱水ケーキが容易に得られる。(1) Both surplus sludge and oxidized sludge from the biological treatment process can be modified in a very rational manner, and a dehydrated cake with a low moisture content can be easily obtained.
(2) 機械脱水工程の前処理工程として、カチオン
ポリマーなどを添加する凝集処理が不要とな
り、残留カチオンポリマーなどによる二次公害
の心配がない。(2) As a pre-treatment step for the mechanical dewatering process, there is no need for agglomeration treatment that involves adding cationic polymers, etc., and there is no need to worry about secondary pollution caused by residual cationic polymers.
(3) 色度成分、難生物分解性のCOD成分を効果
的に除去することができる。(3) Chromaticity components and non-biodegradable COD components can be effectively removed.
(4) 機械脱水工程からの脱水ケーキ量が大幅に減
少でき、しかも、脱水ケーキの埋め立て、コン
ポスト化、焼却などの処分を容易に、低コスト
で行うことができる。(4) The amount of dehydrated cake from the mechanical dewatering process can be significantly reduced, and furthermore, the dehydrated cake can be disposed of by landfilling, composting, incineration, etc. easily and at low cost.
次に本発明の実施例について記す。 Next, examples of the present invention will be described.
比較例（従来例）
Ｆ県Ｉ市Ｋし尿処理場では、20倍希釈したし尿
を、第１図に示したプロセスに従つて活性汚泥法
で処理したのち、沈殿池４からの越流水の色度、
COD、リン酸を除去するため、硫酸第１鉄100
mg／（Feとして）、と過酸化水素H2O2100mg／
を添加して、PH３〜3.5の条件で４時間撹拌し
たのち、消石灰Ca（OH）2を加え、PH６〜７に中
和し、アニオンポリマー1.0mg／を加え沈降分
離させて処理水を得る方法をとつていた。しか
し、活性汚泥の余剰汚泥と、化学酸化処理工程か
ら発生する酸化スラツジとの濃縮、脱水性が極め
て悪く、カチオンポリマーをSS当たり2.0％添加
してベルトプレス型脱水機で脱水しても、脱水ケ
ーキの含水率が85〜86％と高く、乾燥、焼却の燃
料費が非常に高額で、大きな問題となつていた。Comparative Example (Conventional Example) At the human waste treatment plant in City I, F Prefecture, human waste diluted 20 times was treated using the activated sludge method according to the process shown in Figure 1, and then the color of the overflow water from settling tank 4 was changed. Every time,
Ferrous Sulfate 100 to remove COD, phosphoric acid
mg/(as Fe), and hydrogen peroxide H 2 O 2 100 mg/
After stirring for 4 hours at a pH of 3 to 3.5, slaked lime Ca(OH) 2 is added to neutralize the pH to 6 to 7, and 1.0 mg of anionic polymer is added and sedimentation is performed to obtain treated water. I was taking it. However, the concentration and dewatering properties of surplus activated sludge and oxidized sludge generated from the chemical oxidation treatment process are extremely poor, and even when cationic polymer is added at 2.0% per SS and dewatered using a belt press type dehydrator, The moisture content of the cake was as high as 85-86%, and the fuel costs for drying and incineration were extremely high, creating a major problem.
実施例 １
比較例に示した現状を根本的に改善するために
第２図に示す本発明方法を適用した。Example 1 In order to fundamentally improve the current situation shown in the comparative example, the method of the present invention shown in FIG. 2 was applied.
すなわち、沈殿池４の越流水に、硫酸第１鉄を
Feとして100mg／（スタート時のみ）および
H2O2100mg／を添加して、比較例と同様の撹拌
条件、中和条件で化学酸化処理し、酸化スラツジ
を曝気槽にリサイクルさせた。次に、酸化スラツ
ジと生物処理スラツジとの混合スラツジ１６ｂを
シツクナーで濃縮したのち（SS濃度4.0％）、硫酸
を加えてPHを1.5に調整後、２時間撹拌した。次
に、過酸化水素を2500ppmと水酸化マグネシウム
を加えPH２〜2.5の条件で20分間撹拌したのち、
フイルタープレス（供給圧力３Kgｆ／cm2、圧搾圧
力15Kgｆ／cm2）で脱水した結果、含水率65％とい
う著しい低含水率の脱水ケーキが得られた。 That is, ferrous sulfate is added to the overflow water of settling tank 4.
100mg/(starting only) as Fe and
100 mg of H 2 O 2 was added, chemical oxidation treatment was carried out under the same stirring conditions and neutralization conditions as in the comparative example, and the oxidized sludge was recycled to the aeration tank. Next, the mixed sludge 16b of oxidized sludge and biologically treated sludge was concentrated using a thickener (SS concentration: 4.0%), and sulfuric acid was added to adjust the pH to 1.5, followed by stirring for 2 hours. Next, 2500 ppm of hydrogen peroxide and magnesium hydroxide were added and stirred for 20 minutes at a pH of 2 to 2.5.
As a result of dehydration using a filter press (supply pressure 3 Kgf/cm 2 , squeezing pressure 15 Kgf/cm 2 ), a dehydrated cake with a significantly low water content of 65% was obtained.
一方、脱水分離水は、化学酸化処理工程８にリ
サイクルし、脱水分離水中の鉄分を再利用した結
果、新鮮な硫酸第１鉄の所要添加量は比較例の1/
１０の10mg／（Feとして）に減少できた。以上
の結果、従来法（比較例）の問題点はすべて解決
され、脱水ケーキの乾燥、焼却費は節約され、し
かも、化学酸化処理工程から排出されるスラツジ
量は比較例に比べ1/10に減少でき、焼却灰の発生
量も減少し、処分に要する費用も低減化できた。 On the other hand, as a result of recycling the dehydrated separated water to chemical oxidation treatment step 8 and reusing the iron content in the dehydrated separated water, the required amount of fresh ferrous sulfate to be added is 1/1 of that of the comparative example.
It was possible to reduce it to 10 mg/(as Fe) of 10. As a result of the above, all the problems of the conventional method (comparative example) have been solved, the cost of drying and incinerating the dehydrated cake has been saved, and the amount of sludge discharged from the chemical oxidation process has been reduced to 1/10 compared to the comparative example. The amount of incinerated ash generated was also reduced, and the costs required for disposal were also reduced.
実施例 ２
酸化剤としてH2O2の代わりにO3又は次亜塩素
酸ソーダを用いたほかは実施例１と同じ条件で処
理した結果、処理水のCODは（H2O2を使用した
場合5ppmであつたのに対し）O3による場合は
15ppmであり、次亜塩素酸ソーダを用いた場合は
18〜19ppmであつた。Example 2 As a result of treatment under the same conditions as in Example 1 except that O 3 or sodium hypochlorite was used instead of H 2 O 2 as the oxidizing agent, the COD of the treated water was ( 5 ppm) while in the case of O 3
15ppm, and when using sodium hypochlorite
It was 18-19 ppm.
第１図は従来法の系統説明図、第２図及び第３
図は本発明の各実施態様を示す系統説明図であ
る。
１……廃水、２ａ……曝気槽、２ｂ……生物反
応槽、３……流出スラリー、４……沈殿池、５…
…スラツジ、６……返送汚泥、７……越流水、８
……化学酸化処理槽、９……硫酸鉄、１０……過
酸化水素、１１……中和槽、１２……アルカリ
剤、１３ａ……スラツジ、１３ｂ……酸化スラツ
ジ、１４……沈殿池、１５……処理水、１６ａ…
…余剰汚泥、１６ｂ……混合スラツジ、１７……
スラツジ、１８……凝集剤、１９……撹拌槽、２
０……遠心脱水機、２１……脱水ケーキ、２２…
…脱水分離水、２３……酸処理槽、２４……鉱
酸、２５……撹拌槽、２６……過酸化水素、２７
……機械脱水機、２８……脱水ケーキ、２９……
脱水分離水、３０……硫酸鉄、３１……COD除
去槽、３２……空気、３３……過酸化水素。
Figure 1 is a diagram explaining the system of the conventional method, Figures 2 and 3
The figure is a system explanatory diagram showing each embodiment of the present invention. 1... Wastewater, 2a... Aeration tank, 2b... Biological reaction tank, 3... Effluent slurry, 4... Sedimentation tank, 5...
...Sludge, 6...Return sludge, 7...Overflow water, 8
... Chemical oxidation treatment tank, 9 ... Iron sulfate, 10 ... Hydrogen peroxide, 11 ... Neutralization tank, 12 ... Alkali agent, 13a ... Sludge, 13b ... Oxidation sludge, 14 ... Sedimentation tank, 15... Treated water, 16a...
...Excess sludge, 16b...Mixed sludge, 17...
Sludge, 18...Flocculant, 19...Stirring tank, 2
0...Centrifugal dehydrator, 21...Dehydrated cake, 22...
... Dehydrated separated water, 23 ... Acid treatment tank, 24 ... Mineral acid, 25 ... Stirring tank, 26 ... Hydrogen peroxide, 27
... Mechanical dehydrator, 28 ... Dehydrated cake, 29 ...
Dehydrated separated water, 30...iron sulfate, 31...COD removal tank, 32...air, 33...hydrogen peroxide.
Claims (1)
程と、該生物処理工程の前段及び／又は後段に化
学酸化処理工程を組合わせて処理する方法におい
て、前記化学酸化処理工程で酸化剤と、水溶液中
で鉄イオンを解離する物質とを添加し、生成する
酸化スラツジを直接又は予め濃縮したのち前記生
物処理工程に添加し、前記生物処理工程から排出
される、生物処理スラツジと前記酸化スラツジと
の混合スラツジに鉱酸を添加したのち、さらに、
過酸化水素を添加し、機械脱水することを特徴と
する有機性廃水の処理方法。 ２ 前記化学酸化処理工程が、前記機械脱水工程
からの脱水分離水又は脱水分離水に前記過酸化水
素を添加したものを返送添加して処理されるもの
である特許請求の範囲第１項記載の処理方法。 ３ 前記化学酸化処理工程が、その後段に、前記
化学酸化処理工程で生成する前記スラツジの中和
処理工程を含むものである特許請求の範囲第１項
又は第２項記載の処理方法。 ４ 前記機械脱水工程の前段の前記過酸化水素を
添加する工程が、前記鉄イオンを解離する物質を
併用添加して処理されるものである特許請求の範
囲第１〜３項のいずれか一つの項記載の処理方
法。 ５ 前記機械脱水工程の前段の、前記過酸化水素
を添加する工程が、PHを２〜４に設定して処理さ
れるものである特許請求の範囲第１〜４項のいず
れか一つの項記載の処理方法。[Scope of Claims] 1. A method of treating organic wastewater by combining a step of biologically treating organic wastewater in a biological reaction tank and a chemical oxidation treatment step before and/or after the biological treatment step, wherein the chemical oxidation treatment Biological treatment in which an oxidizing agent and a substance that dissociates iron ions in an aqueous solution are added in the process, and the resulting oxidized sludge is added to the biological treatment process either directly or after being concentrated in advance, and is discharged from the biological treatment process. After adding mineral acid to the mixed sludge of the sludge and the oxidized sludge, further
A method for treating organic wastewater characterized by adding hydrogen peroxide and mechanical dehydration. 2. The method according to claim 1, wherein the chemical oxidation treatment step is performed by returning and adding the dehydrated separated water from the mechanical dehydration step or the dehydrated separated water to which the hydrogen peroxide has been added. Processing method. 3. The treatment method according to claim 1 or 2, wherein the chemical oxidation treatment step includes a subsequent step of neutralizing the sludge produced in the chemical oxidation treatment step. 4. The method according to any one of claims 1 to 3, wherein the step of adding hydrogen peroxide before the mechanical dehydration step is performed by adding a substance that dissociates the iron ions in combination. Treatment method described in section. 5. The method according to any one of claims 1 to 4, wherein the step of adding hydrogen peroxide before the mechanical dehydration step is performed by setting the pH to 2 to 4. processing method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9142980A JPS5719086A (en) | 1980-07-04 | 1980-07-04 | Disposal of organic waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9142980A JPS5719086A (en) | 1980-07-04 | 1980-07-04 | Disposal of organic waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5719086A JPS5719086A (en) | 1982-02-01 |
| JPS6339309B2 true JPS6339309B2 (en) | 1988-08-04 |
Family
ID=14026124
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9142980A Granted JPS5719086A (en) | 1980-07-04 | 1980-07-04 | Disposal of organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5719086A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107265527A (en) * | 2015-12-01 | 2017-10-20 | 蔡留凤 | Composite water purifying agent and its application are prepared using aluminium scrap lime-ash |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6451200A (en) * | 1987-08-20 | 1989-02-27 | Mitsuo Saito | Treatment of waste |
| JPH0655320B2 (en) * | 1987-09-02 | 1994-07-27 | 満郎 齋藤 | Waste treatment agent and waste treatment method |
| JPH04131188A (en) * | 1990-09-25 | 1992-05-01 | Daiso Co Ltd | Treatment of waste water |
| CN102838201A (en) * | 2012-09-28 | 2012-12-26 | 天津莱特化工有限公司 | Process for treating industrial wastewater by enhanced Fenton method |
| CN117756371B (en) * | 2023-12-15 | 2024-06-25 | 中国科学院重庆绿色智能技术研究院 | Chemical conditioning and dewatering control method for reservoir sediment sludge |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5245582A (en) * | 1975-10-09 | 1977-04-11 | Tokai Denka Kogyo Kk | Solid-liquid separation method of organic waste fluid sludge |
| JPS534356A (en) * | 1976-07-02 | 1978-01-14 | Toho Beslon Co | Drainage treating method |
| JPS5399657A (en) * | 1977-02-14 | 1978-08-31 | Mitsubishi Heavy Ind Ltd | Method of oxidizing waste water |
| JPS5419549A (en) * | 1977-07-14 | 1979-02-14 | Toa Gosei Chem Ind | Method of highly treating nighttsoil secondary treated water |
| JPS5462655A (en) * | 1977-10-26 | 1979-05-19 | Mitsubishi Gas Chemical Co | Method of treating sludge |
-
1980
- 1980-07-04 JP JP9142980A patent/JPS5719086A/en active Granted
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5245582A (en) * | 1975-10-09 | 1977-04-11 | Tokai Denka Kogyo Kk | Solid-liquid separation method of organic waste fluid sludge |
| JPS534356A (en) * | 1976-07-02 | 1978-01-14 | Toho Beslon Co | Drainage treating method |
| JPS5399657A (en) * | 1977-02-14 | 1978-08-31 | Mitsubishi Heavy Ind Ltd | Method of oxidizing waste water |
| JPS5419549A (en) * | 1977-07-14 | 1979-02-14 | Toa Gosei Chem Ind | Method of highly treating nighttsoil secondary treated water |
| JPS5462655A (en) * | 1977-10-26 | 1979-05-19 | Mitsubishi Gas Chemical Co | Method of treating sludge |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107265527A (en) * | 2015-12-01 | 2017-10-20 | 蔡留凤 | Composite water purifying agent and its application are prepared using aluminium scrap lime-ash |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5719086A (en) | 1982-02-01 |
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