JP5211432B2 - Method for treating water containing suspended matter and chromaticity components - Google Patents
Method for treating water containing suspended matter and chromaticity components Download PDFInfo
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- JP5211432B2 JP5211432B2 JP2006076992A JP2006076992A JP5211432B2 JP 5211432 B2 JP5211432 B2 JP 5211432B2 JP 2006076992 A JP2006076992 A JP 2006076992A JP 2006076992 A JP2006076992 A JP 2006076992A JP 5211432 B2 JP5211432 B2 JP 5211432B2
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 47
- 238000000034 method Methods 0.000 title claims description 7
- 238000001914 filtration Methods 0.000 claims description 17
- 239000012320 chlorinating reagent Substances 0.000 claims description 12
- 239000008235 industrial water Substances 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 8
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical group Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 6
- 229920003002 synthetic resin Polymers 0.000 claims description 4
- 239000000057 synthetic resin Substances 0.000 claims description 4
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical group [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 claims description 3
- 239000006260 foam Substances 0.000 claims 1
- 239000002351 wastewater Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 7
- 238000011001 backwashing Methods 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 6
- 238000009287 sand filtration Methods 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 229910052801 chlorine Inorganic materials 0.000 description 5
- 239000003673 groundwater Substances 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 239000004576 sand Substances 0.000 description 4
- 239000004793 Polystyrene Substances 0.000 description 3
- 230000015271 coagulation Effects 0.000 description 3
- 238000005345 coagulation Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- -1 iron ions Chemical class 0.000 description 3
- 229920002223 polystyrene Polymers 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000011324 bead Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 239000004021 humic acid Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005339 levitation Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Filtration Of Liquid (AREA)
Description
本発明は、懸濁物質及び色度成分を含んだ工業用水を処理する方法に関する。 The present invention relates to how to handle industrial water containing suspended solids and chromaticity components.
河川水、地下水などの工業用水や集塵排水、冷却水などの水中の懸濁物質濃度が比較的高い場合、砂やアンスラサイトを濾材とした濾過装置によって濾過処理することは周知である。 When the concentration of suspended solids in industrial water such as river water and groundwater, dust collection wastewater, and cooling water is relatively high, it is well known to perform filtration using a filtration device using sand or anthracite as a filter medium.
なお、特開２００２−３２６０９１号には、地下水を処理して水道水を製造するに際し、地下水中にフミン酸や鉄イオンなどの色度成分が含まれている場合、塩素水を添加した後、ＰＡＣなどの凝集剤を添加し、次いでマンガン砂などの濾材を充填した濾過層に通水して色度成分を除去することが記載されている。
このような濾過装置にあっては、通水に伴って目詰りしてくるので、定期的に逆洗を行う必要があり、逆洗の都度逆洗排水が発生する。 In such a filtering device, it becomes clogged with water flow, so it is necessary to regularly perform backwashing, and backwash drainage is generated each time backwashing is performed.
しかも、本発明のように懸濁物質と共に色度成分を一緒に濾過装置で除去しようとして凝集剤に加えて塩素剤も併用すると、特に砂濾過の場合、極めて微細な懸濁粒子まで捕捉されてしまうので、発生する逆洗排水の量が膨大なものとなる。 In addition, when a chlorinating agent is used in combination with a flocculant to remove chromaticity components together with a suspended substance together with a suspended substance as in the present invention, even in the case of sand filtration, extremely fine suspended particles are trapped. As a result, the amount of backwash wastewater generated is enormous.
特に、工場の立地条件が総量規制のかかった水域にある場合、このような大量の逆洗排水はそのまま系外に放流することができず、きちんと処理を施した後に放流しなければならない。 In particular, when the location of the factory is in a water area where the total amount is regulated, such a large amount of backwash wastewater cannot be discharged out of the system as it is, and must be discharged after it has been properly treated.
既存の排水処理装置の能力があれば、この逆洗排水をその装置を用いて処理することも考えられるが、通常このような排水処理装置の能力は、発生する排水量に応じて処理能力や水バランスが決められているため、新たに上記濾過装置を増設すると、逆洗排水処理装置まで新設する必要があった。 If the capacity of the existing wastewater treatment equipment is available, it is conceivable to treat this backwash wastewater using that equipment. Usually, the capacity of such wastewater treatment equipment depends on the amount of wastewater generated and the capacity of water. Since the balance has been determined, it was necessary to newly install a backwash wastewater treatment device when the filtration device was newly added.
本発明は上記濾過装置の濾材として、浮上性濾材を採用することにより、極力発生する逆洗排水量を少量におさえることを狙ったものである。 The present invention aims to minimize the amount of backwash wastewater generated as much as possible by adopting a floatable filter medium as the filter medium of the filtration device.
すなわち、本発明は、原水に凝集剤及び塩素剤を添加して濾過する水処理方法及び装置において、濾過装置の逆洗排水量を減少させることができ、しかも処理水の水質も良好なものとすることができる水処理方法を提供することを目的とする。 That is, according to the present invention, in a water treatment method and apparatus for filtering by adding a flocculant and a chlorinating agent to raw water, the amount of backwash drainage of the filtration device can be reduced, and the quality of the treated water is also good. an object of the present invention is to provide a water treatment how that can be.
本発明の具体的な手段は以下の通りである。
請求項１の水処理方法は、懸濁物質及び色度成分を含む原水に凝集剤及び塩素剤を添加した後、浮上性濾材によって濾過する水処理方法であって、原水は懸濁物質濃度８〜２３ｍｇ／Ｌ、色度３〜１１度の工業用水であり、該凝集剤がアルミニウム塩であり、塩素剤が次亜塩素酸塩であり、凝集剤の添加量を８〜１２ｍｇ／Ｌとし、塩素剤の添加量を０．４〜０．６ｍｇ／Ｌとし、前記浮上性濾材は粒径５〜１０ｍｍの球状又は円柱状の発泡合成樹脂よりなり、その層厚みを９００〜１２００ｍｍとし、この浮上性濾材の層へＬＶ１１〜２０ｍ／Ｈｒにて通水することにより、該工業用水の懸濁物質及び色度を除去することを特徴とするものである。
Specific means of the present invention are as follows.
Water treatment method according to
本発明では、原水に対し凝集剤及び塩素剤を添加した後、浮上性濾材によって濾過する。この凝集剤によって懸濁物質が除去され、塩素剤によって色度成分が除去される。凝集処理によって生じたフロックは、浮上性濾材に捕捉されて除去される。 In this invention, after adding a flocculant and a chlorine agent with respect to raw | natural water, it filters with a floating filter medium. Suspended substances are removed by the flocculant, and chromaticity components are removed by the chlorine agent. The floc generated by the coagulation process is captured by the floating filter medium and removed.
この浮上性濾材は、砂と違って、水質に影響を与えない微細な懸濁物質を捕捉しないので、砂濾過に比べて逆洗排水量が少ない。なお、一般に、浮上性濾材による濾過は砂濾過に比べて水中の微粒子の捕捉効率が低いが、本発明では、微粒子を凝集させたり、この浮上性濾材層への通水ＬＶを２０ｍ／Ｈｒ以下と小さくすることにより、この捕捉効率を十分に高いものとすることができる。 Unlike the sand, this floatable filter medium does not capture fine suspended solids that do not affect the water quality, and therefore has less backwash drainage than sand filtration. In general, filtration with a floatable filter medium has a lower trapping efficiency of fine particles in water than sand filtration. However, in the present invention, the fine particles are aggregated, or the water flow LV to the floatable filter medium layer is 20 m / Hr or less. By making it small, this capture efficiency can be made sufficiently high.
以下、図面を参照して実施の形態について説明する。図１は実施の形態に係る水処理装置を示す系統図である。 Hereinafter, embodiments will be described with reference to the drawings. FIG. 1 is a system diagram showing a water treatment apparatus according to an embodiment.
原水は、配管１を流れる間に凝集剤タンク２及び塩素剤タンク３からそれぞれ薬注用ポンプ２ａ，３ａを介して凝集剤の溶液及び塩素剤の溶液が添加され、次いでラインミキサ４にて攪拌された後、浮上性濾材６を収容した濾過槽５に導入され、該浮上性濾材６によって濾過される。濾過処理水が配管７から取り出される。
The raw water is added with the flocculant solution and the chlorinating agent solution from the
原水としては、河川水、地下水などの工業用水が例示される。集塵排水としては、転炉循環水系統における固形分濃度の高い排水が例示される。 The raw water, river water, the industrial water such as ground water is illustrated. Examples of the dust collection wastewater include wastewater having a high solid content concentration in the converter circulating water system.
上記の凝集剤としては、ＰＡＣ、硫酸バンドなどのアルミニウム塩などが好適である。その添加量はアルミニウムに換算して３〜２５ｍｇ−Ａｌ／Ｌ程度が好適であるが、特にこれに限定されるものではない。 As the above-mentioned flocculant, aluminum salts such as PAC and sulfuric acid band are suitable. The amount added is preferably about 3 to 25 mg-Al / L in terms of aluminum, but is not particularly limited thereto.
塩素剤としては、次亜塩素酸ソーダなどの次亜塩素酸塩が好適である。その添加量はＣｌ２に換算して０．１〜１．５ｍｇ−Ｃｌ２／Ｌ程度が好適であるが、特にこれに限定されるものではない。 As the chlorinating agent, hypochlorite such as sodium hypochlorite is suitable. The addition amount is preferably about 0.1 to 1.5 mg-Cl 2 / L in terms of Cl 2 , but is not particularly limited thereto.
図１ではラインミキサ４を用いているが、凝集撹拌槽を設置してもよい。この場合、凝集撹拌槽に凝集剤やさらには塩素剤を薬注してもよい。また、凝集槽とフロック成長槽とを併設してもよい。 Although the line mixer 4 is used in FIG. 1, a coagulation stirring tank may be installed. In this case, a flocculant or further a chlorine agent may be poured into the flocculent stirring tank. Further, a coagulation tank and a floc growth tank may be provided side by side.
上記濾過槽５内に収容する浮上性濾材６としては、粒径が５〜１０ｍｍであり、比重が０．０１〜０．９５特に０．０２〜０．８とりわけ約０．０５程度の合成樹脂製のものが好適である。合成樹脂としてはポリエチレン、ポリプロピレン、ポリスチレン、ポリスチロール、ポリウレタンなどが好適であり、中でもポリスチレンが好適である。浮上性濾材の形状は、球状又は円柱状のものが、角部が少なく撹拌効率が良いので好適である。
The floatable filter medium 6 accommodated in the
なお、浮上性濾材の粒径が過大であると、逆洗水量が多く必要となるおそれがある。また、比重が過大であると、濾材の攪拌洗浄動力も大きくなる。 If the particle size of the floatable filter medium is excessive, a large amount of backwash water may be required. Further, if the specific gravity is excessive, the stirring and cleaning power of the filter medium also increases.
濾過槽５は、浮上性濾材６の層厚みが９００〜１２００ｍｍとなるように浮上性濾材を収容するのが好ましい。
It is preferable that the
この浮上性濾材６の層への通水ＬＶは１１〜２０ｍ／Ｈｒとすることが好ましい。このようにＬＶを低目にすることにより、凝集フロックの捕捉効率を高め、処理水質を向上させることができる。 The water passing LV onto a layer of floating filter media 6 is preferably set to 1 1-20 m / Hr. By lowering the LV in this way, it is possible to improve the capture efficiency of the aggregated flocs and improve the quality of the treated water.
一般に、浮上性濾材は砂濾過に比べて懸濁物質の捕捉効率が低いが、凝集剤を添加して懸濁物質を凝集させているので、懸濁物質は浮上性濾材６によって捕捉される。特に、上記のようにＬＶを小さくすることにより、懸濁物質の凝集フロックが十分に捕捉される。例えば、図１のフローによると、凝集剤の添加量８〜１２ｍｇ／Ｌ、塩素剤の添加量０．４〜０．６ｍｇ／Ｌの条件下で懸濁物質濃度８〜２３ｍｇ／Ｌ、色度３〜１１度の工業用水を平均して懸濁物質除去率６０〜７５％、色度除去率５０〜８０％にて処理することが可能である。 In general, the floatable filter medium has a lower trapping efficiency of suspended substances than sand filtration, but the suspended substances are trapped by the floatable filter medium 6 because the suspended substances are aggregated by adding a flocculant. In particular, by reducing the LV as described above, the aggregated flocs of the suspended matter are sufficiently captured. For example, according to the flow shown in FIG. 1, the suspended solid concentration is 8 to 23 mg / L under the conditions of 8 to 12 mg / L of the flocculant added and 0.4 to 0.6 mg / L of the chlorinating agent. It is possible to treat industrial water at 3 to 11 degrees on average at a suspended matter removal rate of 60 to 75% and a chromaticity removal rate of 50 to 80%.
図１のフローでは、浮上性濾材６を有した濾過槽５を用いているが、前記の通り、この浮上性濾材は砂濾過に比べて逆洗排水量が少ないという長所を有している。
In the flow of FIG. 1, the
この逆洗を行うには、濾過槽５の上方から逆洗用水（例えば、処理水）を下向きに通水し、浮上性濾材６を下方に展開させ、逆洗排水を濾過槽５の下部から槽外に取り出すのが好ましい。この浮上性部材は、比重が小さいので、撹拌洗浄に要する動力が少なく、また、逆洗水量も少量で足りる。なお、逆洗時に撹拌機を用いて濾材を撹拌してもよい。
In order to perform this backwashing, water for backwashing (for example, treated water) is passed downward from above the
以下、実施例及び比較例について説明する。なお、以下の実施例及び比較例で処理した原水は地下水を水源とする工業用水であり、濁度は１．８〜１７．６ｍｇ／Ｌであり、色度は６．２〜１４．６ｍｇ／Ｌであった。 Hereinafter, examples and comparative examples will be described. The raw water treated in the following Examples and Comparative Examples is industrial water using groundwater as a water source, turbidity is 1.8 to 17.6 mg / L, and chromaticity is 6.2 to 14.6 mg / L. L.
実施例１
図１のフローにおいて、原水流量を６０ｍ３／Ｈｒとし、凝集剤としてＰＡＣを２０ｍｇ／Ｌの割合で添加し、塩素剤として次亜塩素酸ソーダを０．５ｍｇ−Ｃｌ２／Ｌの割合で添加した。
Example 1
In the flow of FIG. 1, the raw water flow rate is 60 m 3 / Hr, PAC is added as a flocculant at a rate of 20 mg / L, and sodium hypochlorite is added as a chlorinating agent at a rate of 0.5 mg-Cl 2 / L. did.
濾過槽５の容積は７ｍ３であり、内部には５ｍ３の浮上性濾材６が層厚さ１１７４ｍｍとなるように収容されている。
The volume of the
浮上性濾材としては、平均粒径７ｍｍ（最小粒径５ｍｍ、最大粒径９ｍｍ）、比重０．０５の発泡スチレン製球状ビーズを用いた。 As the floating filter medium, spherical beads made of expanded styrene having an average particle diameter of 7 mm (minimum particle diameter of 5 mm, maximum particle diameter of 9 mm) and a specific gravity of 0.05 were used.
５ヶ月連続的にＬＶ＝２０ｍ／Ｈｒにて通水し、この間平均して１２Ｈｒに１回の割合で逆洗した。ＬＶを回復させるのに必要な１回の逆洗水量は平均して６ｍ３であった。従って、この５ヶ月の間に発生した逆洗排水量は合計で１８００ｍ３であった。 Water was passed continuously at LV = 20 m / Hr for 5 months, and during this period, the water was backwashed at a rate of once every 12 hours. The average amount of backwash water required to recover LV was 6 m 3 on average. Accordingly, the total amount of backwash wastewater generated during these 5 months was 1800 m 3 .
この結果、濁度は常に５ｍｇ／Ｌ以下で、かつ濁度の除去率は平均して５７％であり、色度の除去率は平均して５２％であった。 As a result, the turbidity was always 5 mg / L or less, the removal rate of turbidity averaged 57%, and the removal rate of chromaticity averaged 52%.
比較例１
図１において、浮上性濾材６の代りに同容積の砂を用い、下向流にて通水したこと以外は同様にして同一の原水を１週間処理した。逆洗の頻度も同じとした。なお、ＬＶを回復させるのに必要な１回当りの逆洗水量は平均して４０ｍ３であり、実施例１の６．７倍であった。
Comparative Example 1
In FIG. 1, the same raw water was treated for 1 week in the same manner except that sand having the same volume was used instead of the floatable filter medium 6 and water was passed in a downward flow. The frequency of backwashing was also the same. In addition, the amount of backwash water per one time required for recovering LV was 40 m 3 on average, which was 6.7 times that of Example 1.
その結果、濁度の除去率は平均して６５％であり、色度の除去率は平均して４７％であった。 As a result, the removal rate of turbidity averaged 65%, and the removal rate of chromaticity averaged 47%.
上記の結果より、浮上性濾材槽を用いた本発明によっても濁度及び色度を十分に除去することができ、しかも逆洗排水量を著しく少なくすることができることが認められた。なお、濁度については、必要とする用水水質に応じて凝集剤の添加量を増加させることにより、砂濾過レベルの性能を得ることが可能である。 From the above results, it was confirmed that the turbidity and chromaticity can be sufficiently removed by the present invention using the floatable filter medium tank, and the backwash drainage can be remarkably reduced. In addition, about turbidity, it is possible to obtain the performance of a sand filtration level by increasing the addition amount of a flocculant according to the required water quality.
４ ラインミキサ
５ 濾過槽
６ 浮上性濾材
4
Claims (1)
原水は懸濁物質濃度８〜２３ｍｇ／Ｌ、色度３〜１１度の工業用水であり、
該凝集剤がアルミニウム塩であり、塩素剤が次亜塩素酸塩であり、
凝集剤の添加量を８〜１２ｍｇ／Ｌとし、塩素剤の添加量を０．４〜０．６ｍｇ／Ｌとし、
前記浮上性濾材は粒径５〜１０ｍｍの球状又は円柱状の発泡合成樹脂よりなり、その層厚みを９００〜１２００ｍｍとし、
この浮上性濾材の層へＬＶ１１〜２０ｍ／Ｈｒにて通水することにより、該工業用水の懸濁物質及び色度を除去することを特徴とする水処理方法。 A water treatment method in which a flocculant and a chlorinating agent are added to raw water containing suspended solids and chromaticity components, followed by filtration with a floatable filter medium ,
Raw water is industrial water with a suspended solids concentration of 8 to 23 mg / L and chromaticity of 3 to 11 degrees.
The flocculant is an aluminum salt, the chlorinating agent is a hypochlorite,
The addition amount of the flocculant is 8 to 12 mg / L, the addition amount of the chlorinating agent is 0.4 to 0.6 mg / L,
The floatable filter medium is made of a spherical or cylindrical foam synthetic resin having a particle size of 5 to 10 mm, and its layer thickness is 900 to 1200 mm.
A water treatment method comprising removing suspended matter and chromaticity of the industrial water by passing water through the floatable filter medium at LV 11 to 20 m / Hr .
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| JP6554862B2 (en) * | 2015-03-27 | 2019-08-07 | 栗田工業株式会社 | Cooling water filtration method |
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