JP5906892B2 - Calcium / magnesium-containing water treatment method and treatment apparatus - Google Patents
Calcium / magnesium-containing water treatment method and treatment apparatus Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 105
- 229910001868 water Inorganic materials 0.000 title claims description 105
- 239000011777 magnesium Substances 0.000 title claims description 34
- 239000011575 calcium Substances 0.000 title claims description 33
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims description 32
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims description 32
- 229910052791 calcium Inorganic materials 0.000 title claims description 32
- 229910052749 magnesium Inorganic materials 0.000 title claims description 32
- 238000000034 method Methods 0.000 title claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 238000000926 separation method Methods 0.000 claims description 32
- 238000001471 micro-filtration Methods 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 25
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 18
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 11
- 238000001556 precipitation Methods 0.000 claims description 11
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 10
- 239000000347 magnesium hydroxide Substances 0.000 claims description 10
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 10
- 239000003513 alkali Substances 0.000 claims description 8
- 239000012295 chemical reaction liquid Substances 0.000 claims description 8
- 239000002244 precipitate Substances 0.000 claims description 8
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 2
- 125000005587 carbonate group Chemical group 0.000 claims 1
- 239000010802 sludge Substances 0.000 description 26
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 238000001914 filtration Methods 0.000 description 9
- 229920000642 polymer Polymers 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 238000005345 coagulation Methods 0.000 description 5
- 230000015271 coagulation Effects 0.000 description 5
- 238000007796 conventional method Methods 0.000 description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000006228 supernatant Substances 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 238000002407 reforming Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 235000011181 potassium carbonates Nutrition 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
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- Removal Of Specific Substances (AREA)
Description
本発明は、カルシウム及びマグネシウムを含有する水に炭酸根を添加してアルカリ条件下にカルシウムを炭酸カルシウムとして、また、マグネシウムを水酸化マグネシウムとして析出させて固液分離するカルシウム・マグネシウム含有水の処理方法及び処理装置に関する。 The present invention is a treatment of calcium / magnesium-containing water in which carbonate radicals are added to water containing calcium and magnesium, and calcium is precipitated as calcium carbonate under alkaline conditions, and magnesium is precipitated as magnesium hydroxide for solid-liquid separation. The present invention relates to a method and a processing apparatus.
カルシウム及びマグネシウムを含有する排水を、蒸発装置等で加熱処理する場合や、樹脂を用いた吸着処理装置で処理する場合、排水中のカルシウムやマグネシウムは、加熱装置や吸着処理装置内でスケール障害を引き起こしたり、吸着阻害の要因となったりするため、予め除去する必要がある。 When wastewater containing calcium and magnesium is heat-treated with an evaporation device, etc., or treated with an adsorption treatment device using a resin, calcium and magnesium in the wastewater can cause a scale failure in the heating device or adsorption treatment device. It is necessary to remove it in advance because it may cause the cause or cause the adsorption inhibition.
排水中のカルシウムは、ｐＨ９以上のアルカリ条件下、炭酸ナトリウム等の炭酸根との反応で以下の反応式（１）に従って炭酸カルシウムの沈殿として除去することが知られている（コールドライム法）。また、マグネシウムは水酸化ナトリウム等のアルカリを添加してｐＨ１１以上のアルカリ性とすることにより、以下の反応式（２）に従って、水酸化マグネシウムの沈殿として除去することが知られている。
Ｃａ２＋＋Ｎａ２ＣＯ３ → ＣａＣＯ３↓＋２Ｎａ＋ …（１）
Ｍｇ２＋＋２ＮａＯＨ → Ｍｇ（ＯＨ）２↓＋２Ｎａ＋ …（２）
It is known that calcium in wastewater is removed as a calcium carbonate precipitate according to the following reaction formula (1) by reaction with carbonate radicals such as sodium carbonate under alkaline conditions of pH 9 or more (cold dry method). Further, it is known that magnesium is removed as a magnesium hydroxide precipitate according to the following reaction formula (2) by adding an alkali such as sodium hydroxide to make it alkaline at pH 11 or higher.
Ca 2+ + Na 2 CO 3 → CaCO 3 ↓ + 2Na + (1)
Mg 2+ + 2NaOH → Mg (OH) 2 ↓ + 2Na + (2)
図２は、従来のカルシウム・マグネシウム含有排水の処理方法を示す系統図であって、原水は、反応槽１１でアルカリと炭酸根が添加され、その後凝集槽１２でポリマー（高分子凝集剤）が添加されて凝集処理され、凝集処理水は沈殿槽１３で固液分離される。沈殿槽の上澄水は更に濾過装置１４で濾過され処理水として系外へ排出される。 FIG. 2 is a system diagram showing a conventional method for treating calcium / magnesium-containing wastewater. In raw water, alkali and carbonate radicals are added in a reaction tank 11, and then a polymer (polymer flocculant) is added in a coagulation tank 12. The flocculated water is added and flocculated, and the flocculated water is solid-liquid separated in the settling tank 13. The supernatant water of the precipitation tank is further filtered by the filtration device 14 and discharged out of the system as treated water.
図２に示すように、固液分離手段として沈殿槽１３を用いる従来法では、沈殿槽１３での固液分離性を高めてＳＳを十分に低減した処理水を得るために、ポリマーを添加して凝集処理する必要があり、更に、沈殿槽１３の上澄水を濾過装置１４で濾過してＳＳを除去する必要があった。このため、ポリマー添加の薬剤コストが嵩む上に処理工程が多く、装置も煩雑で大型化するという欠点があった。 As shown in FIG. 2, in the conventional method using the precipitation tank 13 as a solid-liquid separation means, a polymer is added in order to obtain treated water in which the solid-liquid separation property in the precipitation tank 13 is enhanced and SS is sufficiently reduced. In addition, it was necessary to perform a coagulation treatment, and it was necessary to remove the SS by filtering the supernatant water of the precipitation tank 13 with the filtration device 14. For this reason, there are disadvantages that the cost of adding the polymer is increased, the number of processing steps is large, and the apparatus is complicated and large.
本発明は、後工程のスケール成分となる排水中のカルシウム及びマグネシウムを、ポリマーによる凝集処理を必要とすることなく、比較的簡易な装置で高度に除去して高水質の処理水を得るカルシウム・マグネシウム含有水の処理方法及び処理装置を提供することを課題とする。 In the present invention, calcium / magnesium in waste water, which is a scale component in the subsequent process, is highly removed with a relatively simple device without requiring a coagulation treatment with a polymer to obtain high-quality treated water. It is an object of the present invention to provide a method and apparatus for treating magnesium-containing water.
本発明者らは、上記課題を解決すべく鋭意検討を重ねた結果、カルシウム及びマグネシウムを含有する水に炭酸根を添加してアルカリ条件下で反応させて炭酸カルシウム及び水酸化マグネシウムを析出させた反応液を、精密濾過膜で固液分離することにより、ポリマーによる凝集処理を行うことなく、ＳＳ濃度１０ｍｇ／Ｌ以下の高水質の処理水を安定して得ることができること、更に、精密濾過膜分離装置の濃縮水を循環させて析出汚泥を改質することにより、高濃度汚泥を得ることができ、排出汚泥の処理効率も高めることができることを見出した。 As a result of intensive studies to solve the above-mentioned problems, the present inventors added carbonate root to water containing calcium and magnesium and reacted under alkaline conditions to precipitate calcium carbonate and magnesium hydroxide. By separating the reaction liquid into solid and liquid with a microfiltration membrane, it is possible to stably obtain high-quality treated water with an SS concentration of 10 mg / L or less without performing an agglomeration treatment with a polymer. It was found that by recirculating the concentrated water of the separator and reforming the precipitated sludge, a high-concentration sludge can be obtained and the treatment efficiency of the discharged sludge can be increased.
本発明はこのような知見に基いて達成されたものであり、以下を要旨とする。 The present invention has been achieved on the basis of such findings, and the gist thereof is as follows.
［１］ カルシウム及びマグネシウムを含有する水（以下「原水」という。）に、反応槽で炭酸根を添加してｐＨ１１以上のアルカリ条件下に炭酸カルシウム及び水酸化マグネシウムを析出させ、該反応槽からの該析出物を含む反応液を固液分離するカルシウム・マグネシウム含有水の処理方法において、該析出物を精密濾過膜分離装置で固液分離する方法であって、該反応槽からの反応液を循環槽に受け入れ、該循環槽の流出液を該精密濾過膜分離装置で固液分離し、該精密濾過膜分離装置の濃縮水の一部を循環水として前記反応槽に返送して前記原水と混合して処理すると共に、残部を循環槽に返送することを特徴とするカルシウム・マグネシウム含有水の処理方法。 [1] To a water containing calcium and magnesium (hereinafter referred to as “raw water”), a carbonate radical is added in a reaction tank to precipitate calcium carbonate and magnesium hydroxide under an alkaline condition of pH 11 or higher. of the processing method of the calcium-magnesium-containing water to the reaction solution to solid-liquid separation comprising the precipitates, a method of solid-liquid separation of the precipitation distillate with microfiltration membrane separation apparatus, the reaction liquid from the reaction vessel The effluent from the circulation tank is solid-liquid separated by the microfiltration membrane separator, a part of the concentrated water from the microfiltration membrane separator is returned to the reaction tank as circulation water, and the raw water and A method for treating calcium / magnesium-containing water, characterized by mixing and treating, and returning the remainder to a circulation tank .
［２］ ［１］において、前記原水に混合する循環水量が原水量の０．５〜１．５倍であることを特徴とするカルシウム・マグネシウム含有水の処理方法。 [ 2 ] The method for treating calcium / magnesium-containing water according to [ 1 ], wherein the amount of circulating water mixed with the raw water is 0.5 to 1.5 times the amount of raw water.
［３］ カルシウム及びマグネシウムを含有する水（以下「原水」という。）に炭酸根を添加してｐＨ１１以上のアルカリ条件下に炭酸カルシウム及び水酸化マグネシウムを析出させ、該析出物を含む反応液を固液分離するカルシウム・マグネシウム含有水の処理装置において、該原水にアルカリと炭酸根を添加する反応槽と、該反応槽からの反応液を受け入れる循環槽と、該循環槽の流出液を固液分離する精密濾過膜分離装置と、該精密濾過膜分離装置の濃縮水を前記反応槽及び循環槽に返送する手段とを有することを特徴とするカルシウム・マグネシウム含有水の処理装置。 [ 3 ] Carbonate is added to water containing calcium and magnesium (hereinafter referred to as “raw water”) to precipitate calcium carbonate and magnesium hydroxide under alkaline conditions of pH 11 or higher, and a reaction solution containing the precipitate is obtained. In a calcium / magnesium-containing water treatment apparatus for solid-liquid separation, a reaction tank for adding alkali and carbonate radicals to the raw water, a circulation tank for receiving the reaction liquid from the reaction tank, and an effluent from the circulation tank A treatment apparatus for calcium / magnesium-containing water, comprising: a microfiltration membrane separation device for separation; and means for returning the concentrated water of the microfiltration membrane separation device to the reaction tank and the circulation tank.
本発明によれば、後工程のスケール成分となる排水中のカルシウム及びマグネシウムを、ポリマーによる凝集処理を必要とすることなく、比較的簡易な装置で高度に除去して高水質の処理水を安定に得ることができる。
また、精密濾過膜分離装置の濃縮水を循環させて析出汚泥を改質することにより、高濃度汚泥を得ることができ、排出汚泥の処理効率も改善され、汚泥処理コストの削減を図ることも可能となる。
According to the present invention, calcium and magnesium in the waste water, which is a scale component in the subsequent process, is highly removed with a relatively simple device without the need for a coagulation treatment with a polymer, thereby stabilizing high-quality treated water. Can get to.
In addition, by recirculating the concentrated water from the microfiltration membrane separation device and reforming the precipitated sludge, high-concentration sludge can be obtained, the treatment efficiency of the discharged sludge can be improved, and the sludge treatment cost can be reduced. It becomes possible.
以下に図面を参照して本発明の実施の形態を詳細に説明する。 Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.
図１は本発明のカルシウム・マグネシウム含有水の処理装置の実施の形態の一例を示す系統図であり、１は反応槽、２は循環槽、３は精密濾過（ＭＦ）膜分離装置である。反応槽１及び循環槽２には、撹拌手段が設けられ、また反応槽１にはｐＨ計が設けられている。Ｐはポンプである。 FIG. 1 is a system diagram showing an example of an embodiment of a treatment apparatus for calcium / magnesium-containing water according to the present invention, wherein 1 is a reaction tank, 2 is a circulation tank, and 3 is a microfiltration (MF) membrane separation apparatus. The reaction tank 1 and the circulation tank 2 are provided with stirring means, and the reaction tank 1 is provided with a pH meter. P is a pump.
図１において、原水（カルシウム・マグネシウム含有水）は反応槽１に導入されて、ＭＦ膜分離装置３から返送されたＭＦ膜分離装置３の濃縮水と共に、アルカリと炭酸根が添加され、ｐＨ１１以上のアルカリ条件下、原水中のカルシウムが炭酸カルシウムとして、またマグネシウムが水酸化マグネシウムとして析出し、析出物を含む反応液は次いで循環槽２を経てポンプＰによりＭＦ膜分離装置３にて固液分離され、ＭＦ膜の透過水が処理水として系外へ排出される。一方、濃縮水は、その一部が反応槽１に返送され、残部は循環槽２に循環される。この循環槽２からは、必要に応じて余剰汚泥が排出される。 In FIG. 1, raw water (calcium / magnesium-containing water) is introduced into a reaction tank 1, and alkali and carbonate radicals are added together with the concentrated water of the MF membrane separation device 3 returned from the MF membrane separation device 3. Under the alkaline conditions, calcium in the raw water is precipitated as calcium carbonate and magnesium is precipitated as magnesium hydroxide, and the reaction liquid containing the precipitate is then separated into solid and liquid by the MF membrane separator 3 by the pump P through the circulation tank 2. Then, the permeated water of the MF membrane is discharged out of the system as treated water. On the other hand, part of the concentrated water is returned to the reaction tank 1 and the remaining part is circulated to the circulation tank 2. Excess sludge is discharged from the circulation tank 2 as necessary.
本発明で処理する原水は、カルシウムとマグネシウムを含有する水であり、そのカルシウム濃度、マグネシウム濃度には特に制限はないが、カルシウム濃度５０〜２０００ｍｇ／Ｌ、マグネシウム濃度５０〜２０００ｍｇ／Ｌ程度の鉱山排水、排煙脱硫排水、下水などが挙げられる。 The raw water to be treated in the present invention is water containing calcium and magnesium, and the calcium concentration and magnesium concentration are not particularly limited, but the mine has a calcium concentration of about 50 to 2000 mg / L and a magnesium concentration of about 50 to 2000 mg / L. Examples include wastewater, flue gas desulfurization wastewater, and sewage.
原水に添加するアルカリとしては、水酸化ナトリウム、水酸化カリウム等を用いることができ、アルカリ添加により反応液のｐＨを１１以上、好ましくは１１〜１３に調整する。このｐＨが１１未満では、マグネシウムを水酸化マグネシウムとして十分に析出させることができず、処理水のマグネシウム濃度が高くなり、好ましくない。ｐＨが１３を超えると、アルカリ使用量が徒に多くなり、不経済である。 As the alkali added to the raw water, sodium hydroxide, potassium hydroxide or the like can be used, and the pH of the reaction solution is adjusted to 11 or more, preferably 11 to 13 by adding the alkali. If this pH is less than 11, magnesium cannot be sufficiently precipitated as magnesium hydroxide, and the magnesium concentration of the treated water becomes high, which is not preferable. If the pH exceeds 13, the amount of alkali used is increased, which is uneconomical.
炭酸根、即ち、炭酸イオンを生成させる物質としては、炭酸ナトリウム、炭酸カリウムの炭酸塩の他、炭酸水素ナトリウム（重曹）や炭酸ガス等を用いることもできる。これらは１種を単独で用いてもよく、２種以上を併用してもよい。 As a carbonate radical, that is, a substance that generates carbonate ions, sodium bicarbonate, potassium carbonate, sodium hydrogen carbonate (sodium bicarbonate), carbon dioxide gas, and the like can be used. These may be used alone or in combination of two or more.
炭酸根の添加量は、原水中のカルシウムを炭酸カルシウムとして析出させるに必要な理論量の１倍以上、特に１〜１０倍であることが好ましい。この炭酸根の添加量が上記下限よりも少ないと、原水中のカルシウムを炭酸カルシウムとして十分に析出させることができず、処理水のカルシウム濃度が高くなり好ましくない。炭酸根の添加量が多過ぎても不経済である。 The amount of carbonate radical added is preferably at least 1 times, especially 1 to 10 times the theoretical amount required to precipitate calcium in raw water as calcium carbonate. When the amount of the carbonate radical added is less than the above lower limit, calcium in the raw water cannot be sufficiently precipitated as calcium carbonate, which is not preferable because the calcium concentration of the treated water increases. It is uneconomical to add too much carbonate.
本発明において、ＭＦ膜分離装置の濃縮水の原水側への循環は必ずしも必要ではないが、濃縮水を原水側に循環させて原水と混合して反応を行うことにより、濃縮水中の析出物を核として更に炭酸カルシウム及び水酸化マグネシウムの析出が進行することにより、高濃度の汚泥が得られるようになり好ましい。 In the present invention, it is not always necessary to circulate the concentrated water to the raw water side of the MF membrane separation device, but the concentrated water is circulated to the raw water side and mixed with the raw water to carry out the reaction, whereby the precipitate in the concentrated water is removed. Further precipitation of calcium carbonate and magnesium hydroxide as a nucleus is preferable because a high-concentration sludge can be obtained.
この場合、原水側へ返送する濃縮水量（循環水量）は、原水量の０．５〜１．５倍程度とすることが好ましい。この返送濃縮水量が少な過ぎると、濃縮水を返送することによる上記効果を十分に得ることができず、多過ぎると反応槽容量が過大となり、経済性が損なわれ、実用的でなくなる。 In this case, the concentrated water amount (circulated water amount) to be returned to the raw water side is preferably about 0.5 to 1.5 times the raw water amount. If the amount of the concentrated water to be returned is too small, the above-mentioned effect by returning the concentrated water cannot be obtained sufficiently. If the amount of the concentrated water is too large, the reaction tank capacity becomes excessive, the economic efficiency is impaired, and it becomes impractical.
このような本発明の方法によれば、処理水（ＭＦ膜分離装置３の透過水）として、ＳＳ濃度１０ｍｇ／Ｌ以下の高水質の処理水を、従来法のようにポリマー添加や、沈殿槽と濾過装置の２段の固液分離処理を行うことなく、ＭＦ膜分離装置による１段の固液分離処理で安定に得ることができ、また、濃縮水の返送により、後述の実施例に示すように、高濃度汚泥を得ることができる。 According to such a method of the present invention, high-quality treated water having an SS concentration of 10 mg / L or less as treated water (permeated water of the MF membrane separation device 3) is added to a polymer as in the conventional method, or a precipitation tank. And the filtration device can be stably obtained by a single-stage solid-liquid separation process using an MF membrane separation apparatus, and by returning the concentrated water, it will be described in the examples below. Thus, a high concentration sludge can be obtained.
以下に実施例及び比較例を挙げて本発明をより具体的に説明する。 Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples.
なお、以下の実施例及び比較例で処理した原水は、純水にカルシウム濃度５００ｍｇ／Ｌ、マグネシウム濃度１０００ｍｇ／Ｌとなるように塩化カルシウムと塩化マグネシウムを添加して調製した合成排水である。 The raw water treated in the following Examples and Comparative Examples is a synthetic wastewater prepared by adding calcium chloride and magnesium chloride to pure water so that the calcium concentration is 500 mg / L and the magnesium concentration is 1000 mg / L.
［比較例１］
原水を図２に示す従来法に従って処理した。反応槽１１にて、原水に炭酸ナトリウムを理論量の１．３倍（１７００ｍｇ／Ｌ）添加すると共に、水酸化ナトリウムを用いてｐＨ１２．５とした後、凝集槽１２にてアニオンポリマーを３ｍｇ／Ｌ添加して凝集処理を行った。凝集処理水を沈殿槽１３で固液分離し、沈殿槽１３の上澄水を濾過装置１４で濾過した。
沈殿槽１３の上澄水と、処理水（濾過装置１４の濾過水）について、その水質を分析し、結果を表１に示した。
また、沈殿槽１３の分離汚泥の汚泥濃度を調べ、結果を表１に示した。
なお、汚泥濃度は、分離汚泥を２４時間静置した後の汚泥層について測定した汚泥濃度である。
[Comparative Example 1]
Raw water was treated according to the conventional method shown in FIG. In the reaction tank 11, 1.3 times the theoretical amount of sodium carbonate (1700 mg / L) was added to the raw water, and the pH was adjusted to 12.5 using sodium hydroxide. L was added for aggregation treatment. The agglomerated water was subjected to solid-liquid separation in the precipitation tank 13, and the supernatant water of the precipitation tank 13 was filtered with the filtration device 14.
The water quality of the supernatant water of the sedimentation tank 13 and the treated water (filtered water of the filtration device 14) was analyzed, and the results are shown in Table 1.
Moreover, the sludge density | concentration of the separation sludge of the sedimentation tank 13 was investigated, and the result was shown in Table 1.
In addition, a sludge density | concentration is a sludge density | concentration measured about the sludge layer after leaving separation sludge for 24 hours.
［実施例１］
原水を図１に示す本発明法に従って処理した。反応槽１にて、比較例１と同様の条件で原水に炭酸ナトリウムと水酸化ナトリウムを添加した後、循環槽２を経てＭＦ膜分離装置３で固液分離した。ＭＦ膜分離装置３への通水はクロスフローとした。ＭＦ膜分離装置３の濃縮水のうちの一部（原水量と同量）は反応槽１に返送し、残部は循環槽２に循環させた。余剰汚泥は循環槽２から抜き出した。
この処理は２０日間連続して行った。
得られた処理水（ＭＦ膜分離装置の透過水）の水質の分析結果を表１に示す。
また、循環槽２から抜き出した汚泥について、比較例１と同様にして測定した汚泥濃度（処理が安定してからの平均値）を表１に示すと共に、この汚泥濃度の経時変化を図３に示した。
[Example 1]
Raw water was treated according to the method of the present invention shown in FIG. In the reaction tank 1, sodium carbonate and sodium hydroxide were added to the raw water under the same conditions as in Comparative Example 1, and then solid-liquid separation was performed in the MF membrane separator 3 through the circulation tank 2. Water flow to the MF membrane separation device 3 was a cross flow. A part of the concentrated water of the MF membrane separation device 3 (the same amount as the amount of raw water) was returned to the reaction tank 1 and the remainder was circulated to the circulation tank 2. Excess sludge was extracted from the circulation tank 2.
This treatment was performed continuously for 20 days.
Table 1 shows the analysis results of the water quality of the obtained treated water (permeated water of the MF membrane separator).
The sludge extracted from the circulation tank 2 was measured in the same manner as in Comparative Example 1, and the sludge concentration (average value after the treatment was stabilized) is shown in Table 1, and the change in sludge concentration with time is shown in FIG. Indicated.
実施例１及び比較例１より、以下のことが分かる。
本発明法による実施例１では、ポリマーを必要とすることなく、また、濾過装置を用いることなく、比較例１の処理水（濾過装置の濾過水）と同等以上の高水質の処理水を得ることができ、しかも、得られる汚泥濃度も比較例１の場合に比べて格段に高い。これは、濃縮水の循環により、汚泥が改質され、汚泥濃度が高くなったことによるものである。なお、図３より、汚泥の改質は１日程度で進行し、初期汚泥濃度１％程度が１日経過後は平均１６％程度まで高くなることが分かる。
From Example 1 and Comparative Example 1, the following can be understood.
In Example 1 according to the method of the present invention, high-quality treated water equal to or higher than the treated water of Comparative Example 1 (filtered water of the filtration device) is obtained without using a polymer and without using a filtration device. In addition, the obtained sludge concentration is much higher than that of Comparative Example 1. This is because the sludge was reformed by the circulation of the concentrated water and the sludge concentration became high. It can be seen from FIG. 3 that the sludge reforming progresses in about one day, and the initial sludge concentration increases to about 16% on average after one day.
１ 反応槽
２ 循環槽
３ ＭＦ膜分離装置
１１ 反応槽
１２ 凝集槽
１３ 沈殿槽
１４ 濾過装置
DESCRIPTION OF SYMBOLS 1 Reaction tank 2 Circulation tank 3 MF membrane separator 11 Reaction tank 12 Coagulation tank 13 Precipitation tank 14 Filtration apparatus
Claims (3)
該析出物を精密濾過膜分離装置で固液分離する方法であって、該反応槽からの反応液を循環槽に受け入れ、該循環槽の流出液を該精密濾過膜分離装置で固液分離し、該精密濾過膜分離装置の濃縮水の一部を循環水として前記反応槽に返送して前記原水と混合して処理すると共に、残部を循環槽に返送することを特徴とするカルシウム・マグネシウム含有水の処理方法。 In water (hereinafter referred to as "raw water".) Containing calcium and magnesium, to precipitate calcium carbonate and magnesium hydroxide pH11 or more alkaline conditions by adding carbonate groups in the reaction vessel, the precipitation from the reaction vessel In the method for treating calcium / magnesium-containing water for solid-liquid separation of reaction liquid containing substances,
A method for solid-liquid separation of the precipitate with a microfiltration membrane separation apparatus , wherein the reaction liquid from the reaction tank is received in a circulation tank, and an effluent from the circulation tank is solid-liquid separated with the microfiltration membrane separation apparatus. In addition, a part of the concentrated water of the microfiltration membrane separation device is returned to the reaction tank as circulating water and mixed with the raw water for treatment, and the remainder is returned to the circulation tank. Water treatment method.
該原水にアルカリと炭酸根を添加する反応槽と、該反応槽からの反応液を受け入れる循環槽と、該循環槽の流出液を固液分離する精密濾過膜分離装置と、該精密濾過膜分離装置の濃縮水を前記反応槽及び循環槽に返送する手段とを有することを特徴とするカルシウム・マグネシウム含有水の処理装置。 Carbonate is added to water containing calcium and magnesium (hereinafter referred to as “raw water”) to precipitate calcium carbonate and magnesium hydroxide under alkaline conditions of pH 11 or higher, and the reaction liquid containing the precipitate is separated into solid and liquid. In the calcium and magnesium containing water treatment equipment
A reaction tank for adding alkali and carbonate radicals to the raw water, a circulation tank for receiving the reaction liquid from the reaction tank, a microfiltration membrane separation apparatus for solid-liquid separation of the effluent of the circulation tank, and the microfiltration membrane separation And a means for returning the concentrated water of the apparatus to the reaction tank and the circulation tank.
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