JPS63185493A - Water treatment - Google Patents
Water treatmentInfo
- Publication number
- JPS63185493A JPS63185493A JP1648887A JP1648887A JPS63185493A JP S63185493 A JPS63185493 A JP S63185493A JP 1648887 A JP1648887 A JP 1648887A JP 1648887 A JP1648887 A JP 1648887A JP S63185493 A JPS63185493 A JP S63185493A
- Authority
- JP
- Japan
- Prior art keywords
- treated water
- water
- treatment
- sludge
- flocculation
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000010802 sludge Substances 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 238000005189 flocculation Methods 0.000 claims abstract description 11
- 230000016615 flocculation Effects 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 13
- 238000000108 ultra-filtration Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 8
- 238000009287 sand filtration Methods 0.000 abstract description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 abstract description 3
- 239000008213 purified water Substances 0.000 abstract 2
- 238000007599 discharging Methods 0.000 abstract 1
- 239000007787 solid Substances 0.000 abstract 1
- 239000012498 ultrapure water Substances 0.000 abstract 1
- 238000005345 coagulation Methods 0.000 description 9
- 230000015271 coagulation Effects 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- 230000003472 neutralizing effect Effects 0.000 description 4
- 230000008719 thickening Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000004576 sand Substances 0.000 description 3
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000010800 human waste Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、生物処理後の処理水に凝集剤を混入し、処理
水中の汚泥を凝集処理し、凝集処理後の処理水を固液分
離処理する水処理方法に関する。Detailed Description of the Invention [Field of Industrial Application] The present invention involves mixing a flocculant into treated water after biological treatment, flocculating sludge in the treated water, and separating the treated water after the flocculation treatment into solid-liquid. The present invention relates to a water treatment method.
従来、第３図に示すように、生物処理装置（１）からの
処理水に凝集混和槽（２）で凝集剤と中和剤を混入して
、処理水のｐＨを６．５程度に調整した状態で処理水中
の汚泥を凝集処理し、凝集処理後の処理水を沈澱池（７
）で固液分離処理し、沈澱池（７）の上澄水を砂ろ過槽
（８）で処理して清浄水を取出し、沈澱池（７）の沈降
汚泥を濃縮槽（９）で濃縮処理し、濃縮槽（９）の上澄
液を生物処理装置（１）に戻し、濃縮槽（９）から濃縮
汚泥を取出していた。Conventionally, as shown in Figure 3, a flocculant and a neutralizing agent are mixed into the treated water from the biological treatment device (1) in the coagulation mixing tank (2) to adjust the pH of the treated water to about 6.5. The sludge in the treated water is flocculated in this state, and the treated water after the flocculation treatment is sent to a settling tank (7
), the supernatant water in the settling tank (7) is processed in a sand filter tank (8) to extract clean water, and the settled sludge in the settling tank (7) is concentrated in a thickening tank (9). The supernatant liquid of the thickening tank (9) was returned to the biological treatment device (1), and the thickened sludge was taken out from the thickening tank (9).
しかし、砂ろ過槽（８）からの清浄水はＳＳが少ないも
ののＣＯＤ値及び色度の高いものになる欠点があり、ま
た、沈澱池（７）、砂ろ過槽（８）、濃縮槽（９）から
成る固液分離設備が大型になって、設置場所確保の面で
も欠点があった。そして、砂ろ過槽（８）からの清浄水
のＣＯＤ値と色度を低下させるためにオゾンや活性炭に
よる高度処理する場合、運転経費が高くなる欠点があっ
た。However, although the clean water from the sand filter tank (8) has a low SS content, it has a high COD value and chromaticity. ), the solid-liquid separation equipment became large, and there were also drawbacks in terms of securing space for installation. Further, when performing advanced treatment with ozone or activated carbon to reduce the COD value and chromaticity of clean water from the sand filter tank (8), there is a drawback that operating costs are high.
本発明の目的は、固液分離によって得られる清浄水を、
高度処理すること無く、ＳＳの無いかつＣＯＤ値及び色
度の低いものにでき、かつ、固液分離設備を小型なもの
で済ませられる水処理方法を提供することにある。The purpose of the present invention is to use clean water obtained by solid-liquid separation.
It is an object of the present invention to provide a water treatment method that can produce water without SS and low COD value and chromaticity without requiring advanced treatment, and which can be completed with small solid-liquid separation equipment.
本発明特徴手段は、生物処理後の処理水の凝集処理に際
して処理水のｐＨを４〜６の範囲に調整し、凝集処理後
の処理水の固液分離処理に際して、限外ろ過装置と循環
槽とにわたって処理水を強制循環させて、前記限外ろ過
装置から清浄水をかつ前記循環槽から濃縮汚泥を夫々取
出すことにあり、その作用効果は次の通りである。The characteristic means of the present invention is to adjust the pH of the treated water to a range of 4 to 6 during coagulation treatment of the treated water after biological treatment, and to use an ultrafiltration device and a circulation tank during solid-liquid separation treatment of the treated water after flocculation treatment. The purpose is to forcefully circulate the treated water over the ultrafiltration device and take out the concentrated sludge from the circulation tank, respectively, and its effects are as follows.
つまり、凝集処理に際しての処理水のｐ）（を変化させ
て、凝集処理後の処理水の色度とｐＨとの相関を調べた
ところ、第３図に示すように、ｐＨが４〜６、望まし−
くは４．５〜５．５の範囲で色度を十分に低くできるこ
とが判明し、また、ＣＯＤ値についても同様にｐＨが４
〜６、望ましくは４．５〜５．５の範囲で十分に低くで
きることが判明した。In other words, when we investigated the correlation between the chromaticity and pH of the treated water after the flocculation treatment by changing the p) of the treated water during the flocculation treatment, we found that the pH was between 4 and 6, as shown in Figure 3. Desirable-
It was found that the chromaticity could be sufficiently lowered within the range of pH 4.5 to 5.5, and the COD value was similarly reduced within the range of pH 4.5 to 5.5.
It has been found that it can be made sufficiently low in the range of ~6, preferably 4.5 ~ 5.5.
他方、生物処理後の処理水中にはＨＣＯ３−などのアル
カリが存在するため、ｐ）Ｉを４〜６の範囲とする。On the other hand, since alkali such as HCO3- is present in the treated water after biological treatment, p)I is set in the range of 4 to 6.
ＨＣＯ＋−→ｃｏｔ ＋ ｏｎ−
の分解が生じて、多量のＣＯ２が発生し、゛そのＣＯ２
が汚泥に付着して汚泥が浮上するため、沈澱池での固液
分離が困難であった。The decomposition of HCO+-→cot+on- occurs, and a large amount of CO2 is generated.
solid-liquid separation in the settling tank was difficult because the sludge adhered to the sludge and the sludge rose to the surface.
そこで、凝集処理後の処理水を、限外ろ過装置と循環槽
にわたって強制循環させると、ＣＯ８による悪影響を受
けること無く、ＳＳが無くてＣＯＤ値及び色度の低い清
浄水を限外ろ過装置から取出せ、かつ、１５０００〜２
５０００＋＋＋ｇ／ １程度の高濃度汚泥を循環槽から
取出せることが判った。Therefore, if the treated water after coagulation treatment is forcedly circulated through the ultrafiltration device and the circulation tank, clean water with no SS and low COD value and color can be obtained from the ultrafiltration device without being adversely affected by CO8. Take out and 15000~2
It was found that high concentration sludge of about 5000+++g/1 could be taken out from the circulation tank.
ちなみに、本発明方法と従来方法によって得られる清浄
水の比較実験を行ったところ、以下に示すようになり、
本発明方法のＣＯＤと色度の除去率は従来方法よりも１
０〜２０％も高くなった。By the way, when we conducted a comparative experiment on clean water obtained by the method of the present invention and the conventional method, the following results were obtained:
The removal rate of COD and chromaticity of the method of the present invention is 1 higher than that of the conventional method.
It has increased by 0-20%.
し尿処理場で高濃度二段活性汚泥方式で生物処理した処
理水を使用した。We used treated water that was biologically treated using a high-concentration two-stage activated sludge method at a human waste treatment plant.
従来方法としては、凝集処理、沈澱池による固液分離処
理、砂ろ過処理、活性炭による吸着処理をその順に行っ
た。In the conventional method, coagulation treatment, solid-liquid separation treatment using a sedimentation tank, sand filtration treatment, and adsorption treatment using activated carbon were performed in that order.
凝集剤は硫酸バンドを使用し、Ａ ｊ！ ｇｏｓ換算で
本発明方法では４００ｔｓｇ／ ｌを、かつ、従来方法
では６００ｍｇ／ ｌを夫々添加した。A sulfuric acid band is used as a flocculant, and A j! In terms of gos, 400 tsg/l was added in the method of the present invention, and 600 mg/l in the conventional method.
尚、０内は除去率、ＮＤは不検出である。Note that 0 indicates the removal rate, and ND indicates non-detection.
その結果、砂ろ過、オゾンや活性炭による高度処理を必
要としない運転経費が十分に少ない状態で、ＳＳが無く
てＣＯＤ値及び色度が十分に低い極めて清浄度の高い処
理水を得られるようになった。As a result, it has become possible to obtain extremely clean treated water with no SS and sufficiently low COD values and chromaticity, without the need for advanced treatment using sand filtration, ozone or activated carbon, and with sufficiently low operating costs. became.
また、固液分離に要する設備は、限外ろ過装置、循環槽
、強制循環設備であるから、前述の従来技術のように、
いずれも大型になる沈澱池、砂ろ過槽、濃縮槽を設ける
に比して極めて小型にでき、固液分離設備の設置場所を
確保する面で有利になった。In addition, since the equipment required for solid-liquid separation is an ultrafiltration device, a circulation tank, and forced circulation equipment, as in the prior art described above,
Compared to the installation of larger sedimentation tanks, sand filtration tanks, and thickening tanks, these can be made much smaller, which is advantageous in terms of securing space for solid-liquid separation equipment.
次に、第１図により実施例を示す。 Next, an example will be shown with reference to FIG.
し尿系汚水等を生物処理装置（１）で浄化処理 ゛し、
生物処理後の処理水に凝集混合槽（２）で凝集剤と中和
剤を混入して、凝集処理に際して処理水のｐＨを４〜６
、望ましくは４．５〜５．５の範囲に調整して、処理水
中の汚泥を凝集処理する。Purify human waste water, etc. with biological treatment equipment (1),
A flocculant and a neutralizing agent are mixed into the treated water after biological treatment in the flocculation mixing tank (2), and the pH of the treated water is adjusted to 4 to 6 during flocculation treatment.
, preferably in the range of 4.5 to 5.5, to coagulate the sludge in the treated water.
凝集剤としては塩化第２鉄や硫酸バンド等の公知のもの
を適当に選択使用し、凝集剤の添加量は処理水の汚泥濃
度に見合って適当に設定する。As the flocculant, a known flocculant such as ferric chloride or sulfuric acid is appropriately selected and used, and the amount of flocculant added is appropriately set in accordance with the sludge concentration of the treated water.
中和剤としては、水酸化ナトリウム等の適当なアルカリ
を選択使用し、中和剤の添加量は凝集剤の添加量に見合
って処理水のｐＨが４〜６の範囲になるように適宜設定
する。As the neutralizing agent, select and use an appropriate alkali such as sodium hydroxide, and set the amount of the neutralizing agent appropriately so that the pH of the treated water is in the range of 4 to 6, commensurate with the amount of flocculant added. do.
凝集処理後の処理水を循環槽（３）に送り、ポンプ付流
路（４）と還流路（５）によって限外ろ過装置（６）と
循環槽（３）とにわたって処理水を強制循環させる。そ
の時、約５％の清浄水と凝集時に発生したＣＯ□が、限
外ろ過装置（６）の膜（６ａ）を通過し、限外ろ過装置
（６）から取出される。また、循環槽（３）の汚泥濃度
を１５０００〜２５０００ａ＋ｇ／ ！！に維持して、
濃縮汚泥を循環槽（３）から適量ずつ取出し、もって、
凝集処理後の処理水を固液分離処理する。The treated water after the coagulation treatment is sent to the circulation tank (3), and the treated water is forced to circulate through the ultrafiltration device (6) and the circulation tank (3) using the pump-equipped channel (4) and the reflux channel (5). . At that time, about 5% of the clean water and the CO□ generated during coagulation pass through the membrane (6a) of the ultrafiltration device (6) and are taken out from the ultrafiltration device (6). Also, the sludge concentration in the circulation tank (3) should be 15,000 to 25,000a+g/! ! maintain it,
Take out an appropriate amount of thickened sludge from the circulation tank (3), and
The treated water after coagulation treatment is subjected to solid-liquid separation treatment.
尚、第２図に示すように、凝集処理時の処理水のｐＨと
限外ろ過装置（６）からの清浄水の色度との相関は、塩
化第２鉄も硫酸バンドも同様の傾向になり、ｐＨを４〜
６、望ましくは４．５〜５．５の範囲に維持すると色度
が十分に低くなり、また、ｐＨを４未満にすると凝集剤
が清浄水に混入する問題が派生する。As shown in Figure 2, the correlation between the pH of the treated water during coagulation treatment and the chromaticity of the clean water from the ultrafiltration device (6) shows a similar tendency for ferric chloride and sulfuric acid. and the pH is 4~
6. Preferably, if the pH is maintained within the range of 4.5 to 5.5, the chromaticity will be sufficiently low, and if the pH is less than 4, there will be a problem that the flocculant will be mixed into the clean water.
また、凝集処理時の処理水のｐ Ｈと清浄水のＣＯＤ値
との相関も色度と同様であり、ｐＨを４〜６、望ましく
は４．５〜５．５の範囲でＣＯＤ値が十分に低くなる。In addition, the correlation between the pH of treated water during coagulation treatment and the COD value of clean water is similar to chromaticity, and the COD value is sufficient when the pH is in the range of 4 to 6, preferably 4.5 to 5.5. becomes lower.
次に別実施例を説明する。 Next, another embodiment will be described.
循環槽（３）からの濃縮汚泥の一部を生物処理装置（１
）に還元してもよく、その場合、凝集剤が循環使用され
るために凝集剤の消費量を少なくできる。A portion of the thickened sludge from the circulation tank (3) is transferred to the biological treatment device (1).
), in which case the flocculant is recycled and the consumption amount of the flocculant can be reduced.
生物処理の方式や原水の種類は不問である。The biological treatment method and type of raw water are not important.
限外ろ過装置（６）は生物膜やセラミツタフィルターな
どを利用したものであり、その具体構成は不問である。The ultrafiltration device (6) uses a biofilm, a ceramic ivy filter, or the like, and its specific configuration is not limited.
第１図は本発明の実施例を示すフローシートである。第
２図は実験結果を示すグラフである。
第３図は従来例を示すフローシートである。
（３）・・・・・・循環槽、（６）・・・・・・限外ろ
過装置。FIG. 1 is a flow sheet showing an embodiment of the present invention. FIG. 2 is a graph showing the experimental results. FIG. 3 is a flow sheet showing a conventional example. (3)... Circulation tank, (6)... Ultrafiltration device.
Claims (1)
を凝集処理し、凝集処理後の処理水を固液分離処理する
水処理方法であって、前記凝集処理に際して処理水のｐ
Ｈを４〜６の範囲に調整し、前記固液分離処理に際して
、限外ろ過装置（６）と循環槽（３）とにわたって処理
水を強制循環させて、前記限外ろ過装置（６）から清浄
水をかつ前記循環槽（３）から濃縮汚泥を夫々取出す水
処理方法。A water treatment method in which a flocculant is mixed into treated water after biological treatment, sludge in the treated water is flocculated, and the treated water after flocculation treatment is subjected to solid-liquid separation treatment, the method comprising:
H is adjusted to a range of 4 to 6, and during the solid-liquid separation process, the treated water is forcibly circulated across the ultrafiltration device (6) and the circulation tank (3), and the water is removed from the ultrafiltration device (6). A water treatment method that takes out clean water and thickened sludge from the circulation tank (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1648887A JPS63185493A (en) | 1987-01-26 | 1987-01-26 | Water treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1648887A JPS63185493A (en) | 1987-01-26 | 1987-01-26 | Water treatment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63185493A true JPS63185493A (en) | 1988-08-01 |
Family
ID=11917674
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1648887A Pending JPS63185493A (en) | 1987-01-26 | 1987-01-26 | Water treatment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63185493A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009160567A (en) * | 2007-12-10 | 2009-07-23 | Kobelco Eco-Solutions Co Ltd | Biological treating method and biological treatment apparatus |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4840971A (en) * | 1971-10-01 | 1973-06-15 | ||
| JPS55155798A (en) * | 1979-05-23 | 1980-12-04 | Ebara Infilco Co Ltd | Treating method of organic waste water |
| JPS561959A (en) * | 1979-06-20 | 1981-01-10 | Ricoh Co Ltd | Original feeding method |
| JPS5684697A (en) * | 1979-12-08 | 1981-07-10 | Ebara Infilco Co Ltd | Treatment of high concentration organic waste water |
| JPS5992091A (en) * | 1982-11-19 | 1984-05-28 | Mitsubishi Heavy Ind Ltd | Disposal of waste liquor |
-
1987
- 1987-01-26 JP JP1648887A patent/JPS63185493A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4840971A (en) * | 1971-10-01 | 1973-06-15 | ||
| JPS55155798A (en) * | 1979-05-23 | 1980-12-04 | Ebara Infilco Co Ltd | Treating method of organic waste water |
| JPS561959A (en) * | 1979-06-20 | 1981-01-10 | Ricoh Co Ltd | Original feeding method |
| JPS5684697A (en) * | 1979-12-08 | 1981-07-10 | Ebara Infilco Co Ltd | Treatment of high concentration organic waste water |
| JPS5992091A (en) * | 1982-11-19 | 1984-05-28 | Mitsubishi Heavy Ind Ltd | Disposal of waste liquor |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009160567A (en) * | 2007-12-10 | 2009-07-23 | Kobelco Eco-Solutions Co Ltd | Biological treating method and biological treatment apparatus |
| JP4612078B2 (en) * | 2007-12-10 | 2011-01-12 | 株式会社神鋼環境ソリューション | Biological treatment method and biological treatment apparatus |
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