JPH0347592A - Removal of hydrogen peroxide - Google Patents
Removal of hydrogen peroxideInfo
- Publication number
- JPH0347592A JPH0347592A JP18258889A JP18258889A JPH0347592A JP H0347592 A JPH0347592 A JP H0347592A JP 18258889 A JP18258889 A JP 18258889A JP 18258889 A JP18258889 A JP 18258889A JP H0347592 A JPH0347592 A JP H0347592A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- water
- treated
- liquid
- tank
- 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.)
- Granted
Links
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 229910001868 water Inorganic materials 0.000 claims abstract description 40
- 239000010802 sludge Substances 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000001301 oxygen Substances 0.000 claims abstract description 5
- 238000005273 aeration Methods 0.000 abstract description 13
- 239000002351 wastewater Substances 0.000 abstract description 5
- 238000004062 sedimentation Methods 0.000 abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 239000003513 alkali Substances 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- FLTRNWIFKITPIO-UHFFFAOYSA-N iron;trihydrate Chemical compound O.O.O.[Fe] FLTRNWIFKITPIO-UHFFFAOYSA-N 0.000 abstract 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 239000003638 chemical reducing agent Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- -1 iron ions Chemical class 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- QIVUCLWGARAQIO-OLIXTKCUSA-N (3s)-n-[(3s,5s,6r)-6-methyl-2-oxo-1-(2,2,2-trifluoroethyl)-5-(2,3,6-trifluorophenyl)piperidin-3-yl]-2-oxospiro[1h-pyrrolo[2,3-b]pyridine-3,6'-5,7-dihydrocyclopenta[b]pyridine]-3'-carboxamide Chemical compound C1([C@H]2[C@H](N(C(=O)[C@@H](NC(=O)C=3C=C4C[C@]5(CC4=NC=3)C3=CC=CN=C3NC5=O)C2)CC(F)(F)F)C)=C(F)C=CC(F)=C1F QIVUCLWGARAQIO-OLIXTKCUSA-N 0.000 description 1
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 1
- 235000017491 Bambusa tulda Nutrition 0.000 description 1
- 241001330002 Bambuseae Species 0.000 description 1
- 102000016938 Catalase Human genes 0.000 description 1
- 108010053835 Catalase Proteins 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 101100081970 Mus musculus Otog gene Proteins 0.000 description 1
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 1
- 241000282330 Procyon lotor Species 0.000 description 1
- 238000010420 art technique Methods 0.000 description 1
- 239000011425 bamboo Substances 0.000 description 1
- 238000003421 catalytic decomposition reaction Methods 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 159000000014 iron salts Chemical class 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 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
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- XULSCZPZVQIMFM-IPZQJPLYSA-N odevixibat Chemical compound C12=CC(SC)=C(OCC(=O)N[C@@H](C(=O)N[C@@H](CC)C(O)=O)C=3C=CC(O)=CC=3)C=C2S(=O)(=O)NC(CCCC)(CCCC)CN1C1=CC=CC=C1 XULSCZPZVQIMFM-IPZQJPLYSA-N 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Physical Water Treatments (AREA)
- Removal Of Specific Substances (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明はＨ２Ｏ，を使用する廃水処理における残留Ｈ２
０□の除去やＨ２Ｏ２含有水からのＨ２０□除去方法に
関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention is directed to the treatment of residual H2 in wastewater treatment using H2O.
The present invention relates to a method for removing 0□ and H20□ from H2O2-containing water.
従来からの■２０．除去方法としては次の方法がある。 Conventional ■20. The following methods are available for removal.
■ 亜硫酸ソーダ等の還元剤で還元処理。■ Reduction treatment with a reducing agent such as sodium sulfite.
■ アルカリ性で充填塔内に充填した活性炭と接触させ
て分解。■ Decomposed by contacting with alkaline activated carbon packed in a packed tower.
この方法の一例として第８図に示したフローでは、Ｈ２
０□含有水１にＮａＯＨを添加してアルカリ性とし活性
炭を充填した第１活性炭塔１２および第２活性炭塔１３
に順次通過させて該Ｈ！０．を水と酸素に分解処理し、
次いでこの処理水は中和槽１０で中和処理され処理水１
１を得る。In the flow shown in FIG. 8 as an example of this method, H2
0□ First activated carbon tower 12 and second activated carbon tower 13 which are made alkaline by adding NaOH to water 1 and filled with activated carbon.
The H! 0. is decomposed into water and oxygen,
Next, this treated water is neutralized in a neutralization tank 10 and becomes treated water 1.
Get 1.
■ 酵素（カタラーゼ）による分解除去、（例えば特開
昭６４−１１６８９）
上記従来技術■〜■の問題点を次に示す。(2) Decomposition and removal by enzymes (catalase) (for example, JP-A-64-11689) Problems with the above-mentioned prior art techniques (1) to (2) are shown below.
■については還元剤が高価であることや還元処理を完全
に行うには過剰の還元剤が必要となるために処理水に還
元剤が残留する。Regarding (2), the reducing agent remains in the treated water because the reducing agent is expensive and an excessive amount of reducing agent is required to completely perform the reduction treatment.
■については原水のＨｔｏｚｉ４度の変動や原水性状（
懸濁物質）により処理性能が安定しない。Regarding ■, the fluctuation of Htozi 4 degrees of raw water and the raw water properties (
Treatment performance is unstable due to suspended solids).
使用する活性炭が高価である。The activated carbon used is expensive.
■については原水のｏｔｏｇ１度の変動、原水性状（毒
性物質等）により処理が不安定。反応速度が遅いために
反応容器が過大になる。Regarding (①), treatment is unstable due to fluctuations in raw water otog of 1 degree and raw water properties (toxic substances, etc.). The reaction vessel becomes too large due to the slow reaction rate.
〔発明が解決しようとする課題］
前記したように従来技術ではＨ２Ｏ□を除去するのに過
大な設備や高価な薬品が必要であった。[Problems to be Solved by the Invention] As described above, in the conventional technology, excessive equipment and expensive chemicals were required to remove H2O□.
本発明はＨｇｏ□を容易にかつ低コストで完全に除去す
る方法を提供することを解決課題とする。An object of the present invention is to provide a method for completely removing Hgo□ easily and at low cost.
本発明はＨ２Ｏ，含有被処理水をアルカリ剤でｐＨ１０
〜１２に維持しつつエアレーションすることにより該Ｈ
２０！を水と酸素に分解する脱Ｈ１Ｏｇ工程、該脱Ｈｚ
Ｏｔ工程で脱ＨｔＯｚされた該被処理水を液部とＦｅ
（ＯＨ） ｓ主体の汚泥に分離する固液分離工程、およ
び該固液分離工程のＦｅ（ＯＨ） ３主体の汚泥の一部
または全量を該脱ｈＯ□工程に返送する返送工程からな
ることを特徴とする過酸化水素の除去方法である。In the present invention, the water to be treated containing H2O is adjusted to pH 10 using an alkaline agent.
By aerating while maintaining the H
20! The de-H1Og step decomposes into water and oxygen, the de-Hz
The treated water from which HtOz was removed in the Ot process is transferred to the liquid part and the Fe
(OH) It consists of a solid-liquid separation step in which the sludge is separated into s-based sludge, and a return step in which part or all of the Fe(OH) 3-based sludge from the solid-liquid separation step is returned to the de-HO□ step. This is a unique method for removing hydrogen peroxide.
即ち、本発明はエアレーションを行う脱Ｈ！０８工程と
その後段の固液分離工程および返送工程で構成する。That is, the present invention performs aeration to remove H! It consists of the 08 step, the subsequent solid-liquid separation step, and the return step.
脱ＨｔＯｚ工程のｐ）Ｉをアルカリ剤でｐＨｌ０〜１２
に維持しつつエアレーションを行うと共にその後段の固
液分離工程で固液分離されたＦｅ （ＯＨ） ｓ主体の
汚泥の一部または全量を前記脱ＨｔＯ□工程に返送する
ことによりＨ，０□の接触分解除去を行う。p)I in the HtOz removal step is adjusted to pH 0 to 12 with an alkaline agent.
H,0□ is removed by performing aeration while maintaining the temperature at Perform catalytic decomposition removal.
本発明において、Ｆｅ （０）１） ｓ主体の汚泥とは
Ｆｅ （０）１） ｘを主成分とする無機成分とそれ以
外の有機成分、例えば汚水成分であるＣＯＤ、色度等と
化合した難溶解性塩類、汚水中のＳＳ、からなる汚泥を
意味する。ここで、該無機成分としては、Ｆｅ （Ｏ）
ｌ） ｘの他、例えば、Ａｌ （ＯＨ） ！、Ｍｎ （
ＯＨ） ｚ等を含有してかまわない。In the present invention, Fe (0) 1) s-based sludge is a mixture of inorganic components mainly composed of Fe (0) 1) x and other organic components, such as sewage components such as COD and chromaticity. It means sludge consisting of hardly soluble salts and SS in sewage. Here, the inorganic component is Fe (O)
l) In addition to x, for example, Al (OH)! , Mn (
OH) may contain z, etc.
脱Ｈ２０，工程（エアレーション槽）の汚泥濃度はＦｅ
（ＯＨ） ３として５００ｍｇ／ １．以上、好まし
くは５００＋ｗｇ／ｌ〜２０００ｍｇ／ ｊ！になるよ
うにその後段の固液分離工程の汚泥の一部または全量を
返送して調整する。The sludge concentration in the deH20 process (aeration tank) is Fe
(OH) 500mg/1 as 3. Above, preferably 500+wg/l to 2000mg/j! Some or all of the sludge from the subsequent solid-liquid separation process is returned and adjusted so that
処理設備の試運転、本運転等の立ち上げ時には必要によ
り上記汚泥および／又は鉄塩（塩化第２鉄、硫酸第１鉄
、硫酸第２鉄、鉄イオンを含む廃水等）等を添加して脱
Ｈ２０，工程が上記汚泥濃度になるように調整するのが
好ましいが、被処理水に鉄イオンが含有されていれば特
に添加する必要はない。At the time of trial run or start-up of the treatment equipment, the above sludge and/or iron salts (ferric chloride, ferrous sulfate, ferric sulfate, wastewater containing iron ions, etc.), etc. are added as necessary to remove the water. It is preferable to adjust the H20 step so that the sludge concentration is as described above, but if the water to be treated contains iron ions, it is not necessary to add iron ions.
本発明における固液分離工程の固液分離手段としては、
沈殿池等を利用する自然沈降、ｔｌＦｌｌｌ等による膜
分離等が挙げられ、被処理水の種類、処理目的に応じて
適宜選択できる。As the solid-liquid separation means in the solid-liquid separation step in the present invention,
Examples include natural sedimentation using a sedimentation tank or the like, membrane separation using tlFlll, etc., and can be selected as appropriate depending on the type of water to be treated and the purpose of treatment.
次にアルカリ剤を加えてｐＨ１０〜１２に調整しつつエ
アレーションを行いＨｚＯｔを水と酸素に接触分解させ
る。Next, an alkaline agent is added to adjust the pH to 10 to 12 while aeration is performed to catalytically decompose HzOt into water and oxygen.
１１．０□の分解反応式は次の通り。The decomposition reaction formula for 11.0□ is as follows.
２１１２０、→２Ｈｉｏ ＋ｏ、↑
アルカリ剤はＮａＯＨ，ＮａｚＣＯｓ＋ Ｃａ（０１１
）ｚ等、いずれのアルカリ剤でも使用できるが難溶解性
塩によるＣＯＤ除去が期待できることや価格面よりＣａ
（ＯＨ） ｚの使用が望ましい。21120, →2Hio +o, ↑ Alkaline agents include NaOH, NazCOs+ Ca (011
Although any alkaline agent can be used, such as Ca
(OH) It is preferable to use z.
エアレーシッン時間は１５分〜６０分で良い。Air racing time may be 15 to 60 minutes.
空気量は単位槽容量、単位時間当り３０〜３００１／−
３・分が良い。The amount of air is 30 to 3001/- per unit tank capacity and unit time.
3 minutes is good.
以下、本発明の一実施態様を第１図のフローチャートを
参照して説明する。Hereinafter, one embodiment of the present invention will be described with reference to the flowchart of FIG.
フェントン処理等により生じた廃水のＨ！０８含有水１
は、まず、脱Ｈ！０８工程のエアレーシッン槽２に移送
され、ここで、散気設備５からの空気により本発明の該
Ｆｅ（ＯＨ）を主体の汚泥とＨ２Ｏ２とを接触反応させ
てｕｔｏｔをＨｔＯと０８に分解する。該エアレーショ
ン槽２はアルカリ剤Ｃａ （ＯＮ） ｔを含有し槽内の
ｐｉを該所定の値ｔｏ−１２に保持している。エアレー
ション槽２から排出された処理液は、必要により凝集槽
３に送られ、高分子凝集剤と処理液とを攪拌機４により
混合し、脱Ｉ１８島工程でＬＯｚが分解された処理液は
、固液分離工程の沈殿池７にて液部りとＦｅ（Ｏｌｌ）
ｓ主体の汚泥Ｓに分離し、該汚泥Ｓは返送汚泥ポンプ８
により返送管６を通じて脱ＨｘＯｔ工程ヘリサイクルさ
れる。一方、余剰な汚泥Ｓは排泥管９により排出される
。又、液部りは中和槽１０に送られＨ，ＳＯ，等により
中和され処理水１１となる。処理水１１はそのまま放流
されるか、更に別の図示していない処理工程へ回される
。H! of wastewater generated from Fenton treatment, etc. 08 containing water 1
Well, first of all, get rid of sex! The sludge is transferred to the air lacing tank 2 in the 08 step, where the Fe(OH)-based sludge of the present invention and H2O2 are brought into contact reaction with the air from the aeration equipment 5 to decompose utot into HtO and 08. The aeration tank 2 contains an alkaline agent Ca (ON) t to maintain pi in the tank at the predetermined value to-12. The treated liquid discharged from the aeration tank 2 is sent to the flocculation tank 3 if necessary, and the polymer flocculant and the treated liquid are mixed by the stirrer 4. In the settling tank 7 of the liquid separation process, the liquid part and Fe (Oll)
The sludge S is separated into sludge S mainly composed of
It is recycled to the HxOt removal process through the return pipe 6. On the other hand, excess sludge S is discharged through the sludge pipe 9. Further, the liquid portion is sent to a neutralization tank 10, where it is neutralized with H, SO, etc., and becomes treated water 11. The treated water 11 is either discharged as is or sent to another treatment step (not shown).
（実施例−１）
本発明を実施例を用いて説明するが、本発明はこれに限
定されるものではない。(Example-1) The present invention will be explained using Examples, but the present invention is not limited thereto.
本発明の実施例に使用した廃水は冷間圧延スラッジの浸
出水でその性状は次の通りである。The wastewater used in the examples of the present invention was leachate of cold-rolled sludge, and its properties were as follows.
上記廃水を次に示す処理条件でフェントン処理した。The above wastewater was subjected to Fenton treatment under the following treatment conditions.
上記処理条件で得られたフェントン処理水に試薬のＨ７
０□を加えてｈＯ□濃度を２００ｐｐ−に調整後、ｐＨ
によるＨ２Ｏ２除去性能を試験した。The reagent H7 was added to the Fenton-treated water obtained under the above treatment conditions.
After adjusting the hO□ concentration to 200 pp- by adding 0□, the pH
The H2O2 removal performance was tested.
試験条件は次の通りである。The test conditions are as follows.
第２図に結果を示す。Figure 2 shows the results.
Ｈ２０□除去のための至適ｐｕは１０以上であった。The optimal pu for H20□ removal was 10 or more.
（実施例−２）
実施例−１のフェントン処理水に試薬のＨ２Ｏ２を加え
てＨｚＯｔ濃度を２００ｐｐｍに調整したものを１１用
意した。(Example-2) 11 samples were prepared by adding H2O2 as a reagent to the Fenton-treated water of Example-1 to adjust the HzOt concentration to 200 ppm.
これに実施例−１で沈殿分離された汚泥をＦｅ （ＯＨ
） ｓ濃度として各々２００〜２０００ｐｐｍになるよ
うに加えてＣａ （Ｏｉｌ） ｚでｐＨ１１，０〜１１
．２に維持しつつ通気量毎分０．２１で３０分間エアレ
ージジンした。Fe (OH
) s concentration to be 200 to 2000 ppm each, and Ca (Oil) z to pH 11.0 to 11.
．． Airing was carried out for 30 minutes at an air flow rate of 0.21 per minute while maintaining the air flow rate at 0.2.
第３図に結果を示す。The results are shown in Figure 3.
Ｆｅ （ＯＨ） ｓとしてｓｏｏｐｐｍ以上、混合槽に
汚泥として存在すると残留■ｚｏｔの除去性能は非常に
良かった。When sooppm or more of Fe (OH) s was present in the mixing tank as sludge, the removal performance of residual ■zot was very good.
（実施例−３）
実施例−１で沈殿分離された汚泥をＦｅ（ＯＩｌ）ｉ濃
度として５００．１１０００ｐｐになるように加えて実
施例−２と同様に試験してエアレーシッン時間を調べた
。(Example 3) The sludge precipitated and separated in Example 1 was added so that the Fe(OIl)i concentration was 500.11000 pp, and tested in the same manner as in Example 2 to examine the air lacing time.
第４図に結果を示す。Figure 4 shows the results.
Ｆｅ（ＯＲ）ｘ ５００ｐｐ−ならエアレーション時間
は３０分、１１０００ｐｐなら１５分で残留Ｈ２０、が
分解除去できた。For Fe(OR)x 500pp-, the aeration time was 30 minutes, and for 11000pp, residual H20 could be decomposed and removed in 15 minutes.
（実施例−４）
ＮｚＯ＊ ２００ｐｐ−を含有する水溶液、１１にｒｅ
（ＯＲ） ｓとして１０００ｐｐｓ＋になるようにＦ
ｅＣ１，を添加してＣａ （ＯＲ） ｚでｐＨ１１，ｏ
に調整した。(Example-4) Aqueous solution containing 200 pp- of NzO*, re
(OR) F to be 1000pps+ as s
Add eC1, and adjust pH to 11,o with Ca (OR) z.
Adjusted to.
通気量毎分０．２２で３０分間エアレージジンすると処
理水のＩｌ＊Ｏｔ濃度は１ ｐｐｓ＋以下になった。When aeration was performed for 30 minutes at an aeration rate of 0.22 per minute, the Il*Ot concentration of the treated water became 1 pps+ or less.
（実施例−５）
Ｈｏｏｔ ２００ｐｐｍを含有する水溶液１２に実施
例４で沈降分離した汚泥を全量添加し、Ｃａ （ＯＨ）
＊でｐＨ１１，０に調整した。(Example-5) The entire amount of the sludge separated by sedimentation in Example 4 was added to the aqueous solution 12 containing 200 ppm of Hoot, and Ca (OH)
*The pH was adjusted to 11.0.
実施例４と同様にエアレーションすると処理水のＨｚＯ
ｔ濃度はｌｐｐｍ１以下であった。When aerated in the same manner as in Example 4, the HzO of the treated water
The t concentration was less than lppm1.
（実施例−６）
実施例−５で沈降分離した汚泥を用い、実施例−５と同
様に試験すると処理水の１１ｚＯｔｉ１１度は１ρｐ■
以下であった。(Example 6) Using the sludge that was sedimented and separated in Example 5, a test was conducted in the same manner as in Example 5. 11zOti11 degrees of the treated water was 1ρp■
It was below.
実施例４〜６の結果を第５図〜第７図に示す。The results of Examples 4 to 6 are shown in FIGS. 5 to 7.
本発明は脱ｌ（！Ｏｔ工程に後段の分離汚泥を戻すこと
によって
■ 短時間に完全な１１□０□除去が可能。The present invention enables complete removal of 11□0□ in a short time by returning the separated sludge in the latter stage to the de-l removal (!Ot process).
■ 残留Ｈ２Ｏ２濃度の変動に対して対応が容易。■ Easily responds to fluctuations in residual H2O2 concentration.
■ 運転管理が容易。■ Easy operation management.
本発明は従来法に比べて残留ＨｔＣｈを容易にかつ完全
、低コストで除去する方法を提供することができる。The present invention can provide a method for removing residual HtCh more easily, completely, and at lower cost than conventional methods.
第１図は本発明の処理フローシートの一例を示す図、第
２図〜第７図は本発明の実施例１〜実施例６に各々に対
応する結果を示すグラフである。
第８図は活性炭を用いた従来法の一例を示す。
符号の説明
１：）ｌｚｏ、含有水、
２：脱Ｈ２Ｏ２工程のエアレーション槽、３：凝集槽、
４；攪拌機、
散気設備、
沈殿汚泥Ｓの返送管、
固液分離工程の沈殿池、
返送汚泥ポンプ、 ９：排泥管、
中和槽、 １１：処理水、
第１活性炭塔、 １３：第２活性炭塔、Ｆｅ （ＯＨ
） ｓ主体の汚泥、 Ｌ：液部。
（ばか３名）
第 ２ 図
ＰＨ（−）
第 １
図
１：丸Ｏ令肩水
３： ン騒、墳ｔｔｒｔ
５、を気録Ａ
７；Ｉ！ＩＪ今讐工１−波灘氾
９・抑泡１
１１゛処狸大
し、涜ｉ！
２：ｆｌＬｔ％Ｏ□工％ｌ＃Ｉｌγレーン、ン埼４、ギ
ｔキを−１
６攪Ｍ汚泥！遁直〒
８：ＶＬ凍８堤ボ′：Ｊ７゜
１０、”？ ％Ｑ埼
Ｓ、Ｆ七（ｏＨ）、１休−汚泥
第 ３
図
第
Ｆａ（ＤＨ＞ｚ
（ＰＰ啼−ン
図
エアレーンーン哨ｑ司（４＋）
第
５
図
第
図
第
第
図
１：ｌ−１，０，令肩本
槽特梅
１０漕ち榎
１
処ａ号永
１２゛ｗＡ１：ｔＩ）ｔ、ｌ ５ｊＬ
１３樋２１竹及寿FIG. 1 is a diagram showing an example of a processing flow sheet of the present invention, and FIGS. 2 to 7 are graphs showing results corresponding to Examples 1 to 6 of the present invention, respectively. FIG. 8 shows an example of a conventional method using activated carbon. Explanation of symbols 1:) lzo, contained water, 2: Aeration tank for deH2O2 process, 3: Coagulation tank,
4: Stirrer, aeration equipment, return pipe for settled sludge S, settling tank for solid-liquid separation process, return sludge pump, 9: Sludge pipe, neutralization tank, 11: Treated water, 1st activated carbon tower, 13: 1st 2 activated carbon towers, Fe (OH
) s-based sludge, L: liquid part. (3 idiots) 2nd figure PH (-) 1st figure 1: Maru Orei shoulder water 3: Noisy, mound ttrt 5, wo kiroku A 7;I! IJ now enemy work 1 - wave flood 9, bubble control 1 11゛It's a raccoon big, sacrilege! 2:flLt%O□工%l#Ilγ Lane, Nsai 4, Gitki -1 6 Stir M sludge! 8: VL frozen 8th embankment: J7゜10, %Q S, F7 (oH), 1st rest - sludge Figure 3 Fa (DH>z (PP sound diagram Air lane guard) q Tsukasa (4+) Fig. 5 Fig. Fig. Fig. 1: l-1, 0, Rei shoulder main tank special plum 10 rowing Enoki 1 place a No. 12゛ wA1: tI) t, l 5jL 13 gutter 21 bamboo longevity
Claims (1)
２に維持しつつエアレーションすることにより該Ｈ＿２
Ｏ＿２を水と酸素に分解する脱Ｈ＿２Ｏ＿２工程、該脱
Ｈ＿２Ｏ＿２工程で脱Ｈ＿２Ｏ＿２された該被処理水を
液部とＦｅ（ＯＨ）＿３主体の汚泥に分離する固液分離
工程、および該固液分離工程のＦｅ（ＯＨ）＿３主体の
汚泥の一部または全量を該脱Ｈ＿２Ｏ＿２工程に返送す
る返送工程からなることを特徴とする過酸化水素の除去
方法。The pH of the water to be treated containing H_2O_2 is adjusted to 10 to 1 using an alkaline agent.
By aerating while maintaining the H_2
A de-H_2O_2 step in which O_2 is decomposed into water and oxygen, a solid-liquid separation step in which the water to be treated that has been de-H_2O_2 in the de-H_2O_2 step is separated into a liquid part and sludge mainly composed of Fe(OH)_3, and the solid-liquid separation. A method for removing hydrogen peroxide, comprising a return step of returning part or all of Fe(OH)_3-based sludge from the process to the H_2O_2 removal step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1182588A JPH0696144B2 (en) | 1989-07-17 | 1989-07-17 | How to remove hydrogen peroxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1182588A JPH0696144B2 (en) | 1989-07-17 | 1989-07-17 | How to remove hydrogen peroxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0347592A true JPH0347592A (en) | 1991-02-28 |
| JPH0696144B2 JPH0696144B2 (en) | 1994-11-30 |
Family
ID=16120918
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1182588A Expired - Fee Related JPH0696144B2 (en) | 1989-07-17 | 1989-07-17 | How to remove hydrogen peroxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0696144B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0707868A1 (en) * | 1993-03-30 | 1996-04-24 | Bovar Inc. | Chemical destruction of toxic organic agent |
| JP2002172384A (en) * | 2000-12-05 | 2002-06-18 | Kurita Water Ind Ltd | Method for treating waste water containing ammonia and hydrogen peroxide |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54112556A (en) * | 1978-02-22 | 1979-09-03 | Kankyo Eng | Disposal method of organic waste water |
| JPS5528720A (en) * | 1978-08-22 | 1980-02-29 | Sankyo Yuki Kk | Method and apparatus for treatment of liquid waste matter |
-
1989
- 1989-07-17 JP JP1182588A patent/JPH0696144B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54112556A (en) * | 1978-02-22 | 1979-09-03 | Kankyo Eng | Disposal method of organic waste water |
| JPS5528720A (en) * | 1978-08-22 | 1980-02-29 | Sankyo Yuki Kk | Method and apparatus for treatment of liquid waste matter |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0707868A1 (en) * | 1993-03-30 | 1996-04-24 | Bovar Inc. | Chemical destruction of toxic organic agent |
| JP2002172384A (en) * | 2000-12-05 | 2002-06-18 | Kurita Water Ind Ltd | Method for treating waste water containing ammonia and hydrogen peroxide |
| JP4524525B2 (en) * | 2000-12-05 | 2010-08-18 | 栗田工業株式会社 | Method for treating wastewater containing ammonia and hydrogen peroxide |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0696144B2 (en) | 1994-11-30 |
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