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WO2014132887A1 - Method and apparatus for treating borofluoride-containing water - Google Patents

Method and apparatus for treating borofluoride-containing water Download PDF

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Publication number
WO2014132887A1
WO2014132887A1 PCT/JP2014/054155 JP2014054155W WO2014132887A1 WO 2014132887 A1 WO2014132887 A1 WO 2014132887A1 JP 2014054155 W JP2014054155 W JP 2014054155W WO 2014132887 A1 WO2014132887 A1 WO 2014132887A1
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Prior art keywords
borofluoride
containing water
water
concentration
solid
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PCT/JP2014/054155
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French (fr)
Japanese (ja)
Inventor
周平 伊澤
石塚　諭
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栗田工業株式会社
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Publication date
Application filed by 栗田工業株式会社 filed Critical 栗田工業株式会社
Priority to JP2015502895A priority Critical patent/JP6269651B2/en
Priority to SG11201506360QA priority patent/SG11201506360QA/en
Priority to KR1020157021768A priority patent/KR101990179B1/en
Priority to CN201480011099.3A priority patent/CN105026320A/en
Publication of WO2014132887A1 publication Critical patent/WO2014132887A1/en

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/12—Halogens or halogen-containing compounds
    • C02F2101/14—Fluorine or fluorine-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Definitions

  • the present invention relates to a method and apparatus for treating borofluoride-containing water, and more particularly, to a method and apparatus for treating water containing borofluoride to obtain treated water in which borofluoride, fluorine and boron are significantly reduced.
  • Patent Documents 1 and 2 A method of treating fluorine and boron by adding an aluminum compound to borofluoride-containing water, reacting under acidic and warm conditions to decompose the borofluoride, and further adding a calcium compound has been proposed ( Patent Documents 1 and 2).
  • Patent Document 1 an aluminum compound is added to borofluoride-containing water so that the Al / F molar ratio is 0.3 to 1.05, the borofluoride is decomposed at pH 2 to 3, and then a calcium compound is added. After insolubilization was generated at pH 9-10, solid-liquid separation was performed, and an aluminum compound was further added to the separated water so that the Al / F molar ratio was 5 or more. A method for liquid separation is described. In the method of Patent Document 1, these series of steps are performed at 50 to 80 ° C. in order to improve the reactivity and precipitation.
  • Patent Document 2 a polyvalent metal compound such as an aluminum compound is added to borofluoride-containing water at a pH of 3 or less, heated to 35 ° C. or more, preferably 40 ° C. or more to decompose borofluoride, and then added with slaked lime Insoluble materials are produced at a pH of 10 or higher, and after cooling to 35 ° C. or lower, aggregation and solid-liquid separation are described.
  • a polyvalent metal compound such as an aluminum compound is added to borofluoride-containing water at a pH of 3 or less, heated to 35 ° C. or more, preferably 40 ° C. or more to decompose borofluoride, and then added with slaked lime Insoluble materials are produced at a pH of 10 or higher, and after cooling to 35 ° C. or lower, aggregation and solid-liquid separation are described.
  • the present invention solves the above-mentioned conventional problems, and treats borofluoride-containing water at a low temperature (room temperature), so that not only fluorine but also boron can be removed to a high degree and a treatment method and treatment of borofluoride-containing water. It is an object to provide an apparatus.
  • the present inventors have optimized the addition amount of the aluminum compound and the addition amount of the calcium compound and solved the above-mentioned problem by performing the treatment at room temperature. I found out that I can.
  • the present invention has been achieved on the basis of such knowledge, and the gist thereof is as follows.
  • the amount of calcium compound added in the second step is equivalent to Al in the aluminum compound.
  • Ca / Al 2.5 to 4.0 (molar ratio) in terms of Ca with respect to the value
  • the treatment temperature of the first and second steps is 10 to 35 ° C.
  • [2] having a fourth step of producing the insolubilized product by treating the separated water obtained in the third step with a pH of 6 to 7, and a fifth step of solid-liquid separating the insolubilized product.
  • a first reaction vessel for decomposing borofluoride at pH 1 to 4 by adding an aluminum compound to borofluoride-containing water, and adding calcium compound to treated water in the first reaction vessel at pH 7 to 13 In a treatment apparatus for borofluoride-containing water having a second reaction tank for producing an insolubilized product by reaction and a first solid-liquid separation means for solid-liquid separation of the insolubilized substance,
  • the treatment temperature of the first and second reaction vessels is 10 to 35 ° C. It is characterized by being That borofluoride compound containing water of the processing apparatus.
  • the present invention by controlling the addition amount of the aluminum compound and the addition amount of the calcium compound and treating at a room temperature of 10 to 35 ° C., not only fluorine but also boron can be removed to a high degree.
  • the treatment of the present invention basically does not require heating, the operating cost can be reduced. Since the present invention reacts at room temperature, it may be heated in some cases in the winter, but even in this case, the operation cost can be reduced as compared with the prior art because it may be kept at room temperature.
  • 6 is a graph showing the relationship between the BF 4 concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4.
  • 6 is a graph showing the relationship between the F concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4.
  • 6 is a graph showing the relationship between the B concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4.
  • 6 is a graph showing the relationship between the Al concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4.
  • 6 is a graph showing the relationship between the SO 4 concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4.
  • FIG. 1 is a system diagram showing an embodiment of a treatment apparatus for water containing borofluoride according to the present invention.
  • 1 is a first reaction tank (first reaction tank), 2 is a second reaction tank (second reaction tank), 3 is a coagulation tank, and 4 is a solid-liquid separation tank (first solid-liquid separation). Means), 5 is a third reaction tank (third reaction tank), 6 is a coagulation tank, and 7 is a solid-liquid separation tank (second solid-liquid separation means).
  • first reaction tank 1 the raw water is added with an aluminum compound (Al compound) and an acid, and the borofluoride in the raw water is decomposed at pH 1 to 4 (first step).
  • the treated water in the first reaction tank 1 is then fed to the second reaction tank 2 and added with a calcium compound (Ca compound) and an alkali as necessary, and treated at pH 7 to 13 to obtain calcium fluoride or the like.
  • the insolubilized product is produced (second step).
  • the treated water in the second reaction tank 2 is then agglomerated by adding a polymer flocculant in the agglomeration tank 3 and then solid-liquid separated in the solid-liquid separation tank 4 (third step).
  • the separated sludge in the solid-liquid separation tank 4 is discharged to the outside of the system, and the separated water is sent to the third reaction tank (third reaction tank) 5, and an aluminum compound and an acid are added as necessary to adjust the pH to 6-7.
  • Insolubilization treatment (fourth step).
  • the treated water in the third reaction tank 5 is then subjected to a coagulation treatment by adding a polymer flocculant in the coagulation tank 6 and then solid-liquid separation in the solid-liquid separation tank 7 (fifth step).
  • the separated sludge in the solid-liquid separation tank 7 is discharged out of the system, and the separated water is taken out as treated water.
  • Examples of water (raw water) containing borofluoride to be treated in the present invention include glass products, pharmaceuticals, cosmetics, resin products, manufacturing wastewater of plating products, flue gas desulfurization wastewater from coal-fired power plants, waste incineration smoke cleaning wastewater, nickel Examples include plating factory wastewater.
  • fluorine and boron in the form of F ⁇ and BO 3 3 ⁇ are also present instead of BF 4 ⁇ .
  • BF 4 concentration BF 4 dissolved in water -..
  • the ionic concentration present invention referred to as "BF 4 concentration” 5 ⁇ 2000mg / L
  • F concentration Fluorine concentration dissolved in water.
  • B concentration concentration of boron dissolved in water.
  • B concentration concentration of boron dissolved in water.
  • the F concentration can be measured by the method defined in JIS K0102 34.1 (lanthanum-azarin complexone spectrophotometry), and the B concentration can be analyzed by the method defined in JIS K0102 47.3 (ICP emission spectrometry).
  • the aluminum compound to be added to the raw water may be any aluminum compound that dissolves aluminum ions under the pH conditions during the reaction.
  • any aluminum compound that dissolves aluminum ions under the pH conditions during the reaction For example, one or two of aluminum sulfate, aluminum chloride, polyaluminum chloride (PAC), sulfate band, etc. The above can be used.
  • the amount of aluminum compound added to the raw water is such that the amount added in terms of Al is 1.2 to 2.5, preferably 1.5 to 2.5 in terms of Al / F (molar ratio) with respect to the F concentration of the raw water.
  • the addition amount in terms of Al with respect to the B concentration is preferably in the range of 2.0 to 4.5 in terms of Al / B (molar ratio). If the addition amount of the aluminum compound is less than the above lower limit, the borofluoride cannot be sufficiently decomposed, and if it is more than the above upper limit, an effect commensurate with the addition amount cannot be obtained, and the use amount of the aluminum compound increases easily. As a result.
  • the pH of the first step is 1 to 4, preferably 1.5 to 2.5. Accordingly, if necessary, an acid (for example, sulfuric acid, hydrochloric acid, more preferably sulfuric acid) is added to the raw water together with an aluminum compound to adjust the pH to 1 to 4, preferably 1.5 to 2.5.
  • an acid for example, sulfuric acid, hydrochloric acid, more preferably sulfuric acid
  • the liquid temperature can be treated at room temperature of 10 to 35 ° C., preferably 15 to 30 ° C. There is no need.
  • the reaction time in the first step is preferably about 0.5 to 10 hours from the viewpoint of securing the decomposition time of borofluoride in the raw water.
  • ⁇ Second step> a calcium compound is added to the treated water of the first step to precipitate calcium fluoride by the reaction of the following formula, and further, adsorption and removal of boron is performed as described later.
  • a calcium compound 1 type, or 2 or more types, such as slaked lime, calcium chloride, calcium carbonate, can be used, for example.
  • the amount of calcium compound added is 2.5 to 4.0 in terms of Ca / Al (molar ratio) with respect to the amount of Al converted to the aluminum compound added in the first step, preferably 2.
  • the range is 7 to 3.8.
  • the addition amount of the calcium compound within the above range By making the addition amount of the calcium compound within the above range, the adsorption and removal efficiency of boron can be enhanced. Further, by making the addition amount of the calcium compound within the above range, the Al concentration remaining in the treated water in the second step (the aluminum concentration dissolved in the water. In the present invention, it is described as “Al concentration”). And can be effectively used for fluorine removal in the fourth step described later.
  • the Al concentration can be analyzed by the method defined in JIS K0102 58.4 (ICP emission spectroscopy).
  • the second step is carried out under conditions of pH 7 to 13, if necessary, an alkali such as sodium hydroxide or an acid such as sulfuric acid is added to the treated water of the first step together with the calcium compound.
  • an alkali such as sodium hydroxide or an acid such as sulfuric acid is added to the treated water of the first step together with the calcium compound.
  • an alkali such as sodium hydroxide or an acid such as sulfuric acid is added to the treated water of the first step together with the calcium compound.
  • an alkali such as sodium hydroxide or an acid such as sulfuric acid
  • a pH of 10 to 12.5 is more preferable. This is because calcium aluminate (CaO.Al 2 O 3 ) is precipitated by a reaction of the following formula under a highly alkaline condition of pH 10 or higher, and boron is simultaneously adsorbed and removed during this precipitation reaction. Therefore, a more preferable pH condition is 10 to 12 in terms of simultaneous removal of fluorine and boron. 6Ca (OH) 2 + Al 2 (SO 4 ) 3 ⁇ 3CaO ⁇ Al 2 O 3 ⁇ 3CaSO 4 ⁇ 6H 2 O
  • the second step is a liquid temperature of 10 to 35 ° C., preferably 15 to 30 ° C. Process at room temperature of °C. For this reason, heating is not necessary in this step.
  • the reaction time in the second step is preferably about 0.5 to 4 hours from the viewpoint of securing the reaction time of fluorine and calcium compound in raw water.
  • ⁇ Third step> the insolubilized matter (sludge containing calcium fluoride and calcium aluminate) precipitated in the second step is subjected to solid-liquid separation to obtain separated water.
  • a step of aggregating by adding a polymer flocculant may be performed between the second step and the third step.
  • polymer flocculant those used in wastewater treatment can be applied, such as polyacrylamide partial hydrolysates, sodium polyacrylate, and copolymers of acrylamide and acrylic acid (salt).
  • nonionic polymer flocculants such as a molecular flocculant or polyacrylamide can be used.
  • the amount of the polymer flocculant added is usually about 0.1 to 20 mg / L, although it varies depending on the quality of the raw water to be treated and the polymer flocculant used.
  • a membrane separation apparatus for the solid-liquid separation in the third step, a membrane separation apparatus, a filtration apparatus, a dehydrator, etc. can be used in addition to a solid-liquid separation tank such as a precipitation tank.
  • the F concentration is about 3 to 15 mg / L
  • the B concentration is about 1 to 10 mg / L
  • BF 4 is varied depending on the quality of the raw water to be treated, the amount of aluminum compound and calcium compound added, and the like.
  • Treated water having a concentration of 0.1 mg / L or less can be obtained.
  • the Al concentration of this treated water is usually about 30 to 70 mg / L.
  • the solid-liquid separated water in the third step may be treated water, but a fourth step of further removing fluorine by treating the solid-liquid separated water may be performed. That is, although fluorine is insolubilized as calcium fluoride in the second step, a slight amount of fluorine remains in the solid-liquid separated water in the third step due to the solubility of calcium fluoride. Therefore, the remaining fluorine may be further removed by performing the fourth step.
  • aluminum hydroxide is precipitated by adjusting the pH to 6 to 7 by adding an alkali depending on the amount of the aluminum compound, acid, and aluminum compound as required. Fluorine in water is insolubilized and removed by coprecipitation when aluminum hydroxide is precipitated.
  • the calcium compound is added in the above-mentioned Ca / Al (molar ratio) in the second step, thereby obtaining the solid-liquid separation obtained in the third step.
  • About 30 to 70 mg / L of aluminum can be left in water.
  • the amount of aluminum necessary for the fourth step can be covered by the amount of residual aluminum.
  • an acid is added for about 5 to 30 minutes at room temperature (10 to 35 ° C.). It is also possible to remove fluorine only by reacting with stirring.
  • an aluminum compound may be added in this fourth step as necessary.
  • this aluminum compound those exemplified as the aluminum compound used in the first step can be used.
  • the insolubilized matter (fluorine coprecipitation sludge containing aluminum hydroxide) precipitated in the fourth step is subjected to solid-liquid separation to obtain treated water.
  • a step of aggregating by adding a polymer flocculant may be performed between the fourth step and the fifth step.
  • the polymer flocculant one kind or two or more kinds of anionic polymer flocculants such as polyacrylamide partial hydrolyzate, sodium polyacrylate and polyvinylamidine can be used.
  • the amount of the polymer flocculant added is usually about 0.1 to 5 mg / L, although it varies depending on the quality of the raw water to be treated and the polymer flocculant used.
  • a membrane separation apparatus for the solid-liquid separation in the fifth step, a membrane separation apparatus, a filtration apparatus, etc. can be used in addition to a solid-liquid separation tank such as a precipitation tank.
  • the F concentration is 1.1 mg / L or less
  • the B concentration is 3.5 mg / L or less
  • BF 4 although it varies depending on the quality of the raw water to be treated, the addition amount of the aluminum compound and the calcium compound, and the like.
  • High-quality treated water having a concentration of 0.1 mg / L or less and an Al concentration of 1 mg / L or less can be obtained.
  • a part of the fluorine in the raw water Prior to the treatment of the raw water in the first step, a part of the fluorine in the raw water can be removed in advance by solid-liquid separation of the insolubilized matter that is precipitated by adding a calcium compound and reacting at pH 4-10. Good.
  • the F concentration of water flowing into the first step is reduced and the amount of aluminum compound added in the first step is reduced. be able to.
  • a part of the separated sludge obtained by solid-liquid separation in the third step may be returned to the second step and added.
  • the calcium compound added in the second step may be added to and mixed with the returned sludge to modify the sludge, and the modified sludge may be added in the second step.
  • calcium fluoride is newly deposited on the surface of the sludge.
  • a sulfate band (8 wt%, Al 2 O 3 ) was used as the aluminum compound, and slaked lime (Ca (OH) 2 ) was used as the calcium compound.
  • slaked lime (Ca (OH) 2 ) was used as the calcium compound.
  • an anionic polymer flocculant “Clifarm (registered trademark) PA823” manufactured by Kurita Kogyo Co., Ltd. was used, and the amount added was 10 mg / L.
  • FIG. 5 shows that when the Ca / Al (molar ratio) is in the range of 2.5 to 4.0, the amount of Al remaining in the treated water increases and can be effectively used for further fluorine treatment. .
  • the sulfuric acid band was added to the boron in the raw water by variously changing the addition amount in terms of Al with Al / B (molar ratio). Since the fluorine concentration of the raw water is about 1.7 times the boron concentration, if the Al / B (molar ratio) is in the range of about 2.0 to 4.0, the Al / F (molar ratio) is 1. 2 to 2.5.
  • FIG. 8 shows that the boron removal rate is much higher when the treatment temperature is 20 ° C. than when the treatment temperature is 60 ° C. It can be seen that when the Al / B (molar ratio) is in the range of 2.0 to 4.5, the boron removal effect is excellent.
  • F concentration 1.1 mg / L
  • B concentration 3.5 mg / L
  • BF 4 concentration ⁇ 0.1 mg / L
  • Al concentration ⁇ 1 mg / L.

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Abstract

Borofluoride-containing water is treated without carrying out warming so as to highly remove boron as well as fluorine therefrom. A method for treating borofluoride-containing water, which comprises: a first step of adding an aluminum compound to the borofluoride-containing water to decompose a borofluoride at pH 1 to 4; a second step of adding a calcium compound to treated water obtained in the first step to react the treated water with the calcium compound at pH 7 to 13, thereby producing an insoluble substance; and a third step of separating the insoluble substance into a solid material and a liquid material. The aluminum compound is added in such a manner that the Al/F ratio becomes 1.2 to 2.5 (by mole). The calcium compound is added in such a manner that the Ca/Al ratio becomes 2.5 to 4.0 (by mole). Each of the treatment temperature employed in the first step and the treatment temperature employed in the second step is 10 to 35˚C.

Description

ホウフッ化物含有水の処理方法及び処理装置Method and apparatus for treating borofluoride-containing water
　本発明はホウフッ化物含有水の処理方法及び処理装置に係り、特に、ホウフッ化物を含有する水を処理して、ホウフッ化物、フッ素及びホウ素が著しく低減された処理水を得る方法及び装置に関する。 The present invention relates to a method and apparatus for treating borofluoride-containing water, and more particularly, to a method and apparatus for treating water containing borofluoride to obtain treated water in which borofluoride, fluorine and boron are significantly reduced.
　従来、フッ素含有水の処理方法としては、カルシウム化合物を添加してフッ素をフッ化カルシウムとして析出させて固液分離する方法が広く知られている。フッ素含有水にホウ素が含まれていると、ホウ素の一部がホウフッ化物の形態として存在する。ホウフッ化物はカルシウム化合物とは反応しない。そのため、このようなフッ素含有水の処理方法では処理することができない（非特許文献１）。 Conventionally, as a method for treating fluorine-containing water, a method of solid-liquid separation by adding a calcium compound to precipitate fluorine as calcium fluoride is widely known. When boron is contained in the fluorine-containing water, a part of boron is present in the form of borofluoride. Boron fluoride does not react with calcium compounds. Therefore, it cannot treat with such a processing method of fluorine content water (nonpatent literature 1).
　ホウフッ化物含有水に、アルミニウム化合物を添加し、酸性かつ加温条件下で反応させてホウフッ化物を分解し、さらにカルシウム化合物を添加することで、フッ素とホウ素を処理する方法が提案されている（特許文献１，２）。 A method of treating fluorine and boron by adding an aluminum compound to borofluoride-containing water, reacting under acidic and warm conditions to decompose the borofluoride, and further adding a calcium compound has been proposed ( Patent Documents 1 and 2).
　特許文献１には、ホウフッ化物含有水にアルミニウム化合物をＡｌ／Ｆモル比が０．３～１．０５となるように添加し、ｐＨ２～３でホウフッ化物を分解した後、カルシウム化合物を添加してｐＨ９～１０で不溶化物を生成させた後固液分離し、更に分離水にアルミニウム化合物をＡｌ／Ｆモル比が５以上となるように添加し、ｐＨ６～７で不溶化物を生成させて固液分離する方法が記載されている。この特許文献１の方法では、反応性と沈殿性を向上させるために、これらの一連の工程は５０～８０℃で行われる。 In Patent Document 1, an aluminum compound is added to borofluoride-containing water so that the Al / F molar ratio is 0.3 to 1.05, the borofluoride is decomposed at pH 2 to 3, and then a calcium compound is added. After insolubilization was generated at pH 9-10, solid-liquid separation was performed, and an aluminum compound was further added to the separated water so that the Al / F molar ratio was 5 or more. A method for liquid separation is described. In the method of Patent Document 1, these series of steps are performed at 50 to 80 ° C. in order to improve the reactivity and precipitation.
　特許文献２には、ホウフッ化物含有水にｐＨ３以下でアルミニウム化合物等の多価金属化合物を添加して、３５℃以上、好ましくは４０℃以上に加熱してホウフッ化物を分解した後、消石灰を添加してｐＨ１０以上で不溶化物を生成させ、３５℃以下に冷却後、凝集、固液分離を行うことが記載されている。 In Patent Document 2, a polyvalent metal compound such as an aluminum compound is added to borofluoride-containing water at a pH of 3 or less, heated to 35 ° C. or more, preferably 40 ° C. or more to decompose borofluoride, and then added with slaked lime Insoluble materials are produced at a pH of 10 or higher, and after cooling to 35 ° C. or lower, aggregation and solid-liquid separation are described.
特許第４９５４１３１号公報Japanese Patent No. 4954131 特許第４３３８７０５号公報Japanese Patent No. 4338705
　従来のホウフッ化物含有水の処理方法では、ホウ素の除去を十分に行うことができず、また、高温で反応させるため、運転コストも高くなるという問題がある。 In the conventional method for treating borofluoride-containing water, there is a problem that boron cannot be sufficiently removed and the operation cost is increased because the reaction is performed at a high temperature.
　本発明は上記従来の問題点を解決し、ホウフッ化物含有水を、低温（常温）で処理して、フッ素のみならずホウ素をも高度に除去することができるホウフッ化物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。 The present invention solves the above-mentioned conventional problems, and treats borofluoride-containing water at a low temperature (room temperature), so that not only fluorine but also boron can be removed to a high degree and a treatment method and treatment of borofluoride-containing water. It is an object to provide an apparatus.
　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、アルミニウム化合物の添加量とカルシウム化合物の添加量を最適化すると共に、常温で処理を行うことにより、上記課題を解決す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 have optimized the addition amount of the aluminum compound and the addition amount of the calcium compound and solved the above-mentioned problem by performing the treatment at room temperature. I found out that I can.
　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 knowledge, and the gist thereof is as follows.
［１］　ホウフッ化物含有水にアルミニウム化合物を添加してｐＨ１～４でホウフッ化物を分解する第一の工程と、該第一の工程の処理水にカルシウム化合物を添加してｐＨ７～１３で反応させることにより不溶化物を生成させる第二の工程と、該不溶化物を固液分離する第三の工程とを有するホウフッ化物含有水の処理方法において、前記第一の工程のアルミニウム化合物の添加量が、該ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、前記第二の工程のカルシウム化合物の添加量が、該アルミニウム化合物のＡｌ換算値に対するＣａ換算値でＣａ／Ａｌ＝２．５～４．０（モル比）であり、前記第一及び第二の工程の処理温度が１０～３５℃であることを特徴とするホウフッ化物含有水の処理方法。 [1] First step of adding an aluminum compound to borofluoride-containing water and decomposing the borofluoride at pH 1 to 4, and adding calcium compound to the treated water of the first step to react at pH 7 to 13 In the method for treating borofluoride-containing water having a second step of generating an insolubilized product and a third step of solid-liquid separation of the insolubilized product, the amount of aluminum compound added in the first step is: Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and the amount of calcium compound added in the second step is equivalent to Al in the aluminum compound. Ca / Al = 2.5 to 4.0 (molar ratio) in terms of Ca with respect to the value, and the treatment temperature of the first and second steps is 10 to 35 ° C. Method of processing.
［２］　前記第三の工程で得られた分離水をｐＨ６～７で処理して不溶化物を生成させる第四の工程と、該不溶化物を固液分離する第五の工程とを有することを特徴とする［１］に記載のホウフッ化物含有水の処理方法。 [2] having a fourth step of producing the insolubilized product by treating the separated water obtained in the third step with a pH of 6 to 7, and a fifth step of solid-liquid separating the insolubilized product. The method for treating borofluoride-containing water as described in [1], which is characterized by the following.
［３］　前記第一の工程のアルミニウム化合物の添加量が、前記ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、かつ、
　前記ホウフッ化物含有水のホウ素濃度に対するＡｌ換算値でＡｌ／Ｂ＝２．０～４．５（モル比）であることを特徴とする［１］又は［２］に記載のホウフッ化物含有水の処理方法。 [3] The addition amount of the aluminum compound in the first step is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and
The borofluoride-containing water according to [1] or [2], wherein Al / B = 2.0 to 4.5 (molar ratio) in terms of Al with respect to the boron concentration of the borofluoride-containing water Processing method.
［４］　前記第三の工程で得られる分離水のアルミニウム濃度が３０～７０ｍｇ／Ｌであることを特徴とする［１］ないし［３］のいずれかに記載のホウフッ化物含有水の処理方法。 [4] The method for treating borofluoride-containing water according to any one of [1] to [3], wherein the aluminum concentration of the separated water obtained in the third step is 30 to 70 mg / L.
［５］　ホウフッ化物含有水にアルミニウム化合物を添加してｐＨ１～４でホウフッ化物を分解する第一の反応槽と、該第一の反応槽の処理水にカルシウム化合物を添加してｐＨ７～１３で反応させることにより不溶化物を生成させる第二の反応槽と、該不溶化物を固液分離する第一の固液分離手段とを有するホウフッ化物含有水の処理装置において、前記第一の反応槽のアルミニウム化合物の添加量が、該ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、前記第二の反応槽のカルシウム化合物の添加量が、該アルミニウム化合物のＡｌ換算値に対するＣａ換算値でＣａ／Ａｌ＝２．５～４．０（モル比）であり、前記第一及び第二の反応槽の処理温度が１０～３５℃であることを特徴とするホウフッ化物含有水の処理装置。 [5] A first reaction vessel for decomposing borofluoride at pH 1 to 4 by adding an aluminum compound to borofluoride-containing water, and adding calcium compound to treated water in the first reaction vessel at pH 7 to 13 In a treatment apparatus for borofluoride-containing water having a second reaction tank for producing an insolubilized product by reaction and a first solid-liquid separation means for solid-liquid separation of the insolubilized substance, The addition amount of the aluminum compound is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and the addition amount of the calcium compound in the second reaction tank Is Ca / Al = 2.5 to 4.0 (molar ratio) in terms of Ca relative to the Al equivalent of the aluminum compound, and the treatment temperature of the first and second reaction vessels is 10 to 35 ° C. It is characterized by being That borofluoride compound containing water of the processing apparatus.
［６］　前記固液分離手段で得られた分離水をｐＨ６～７で処理して不溶化物を生成させる第三の反応槽と、該不溶化物を固液分離する第二の固液分離手段とを有することを特徴とする［５］に記載のホウフッ化物含有水の処理装置。 [6] A third reaction tank for producing an insolubilized product by treating the separated water obtained by the solid-liquid separating unit at pH 6 to 7, and a second solid-liquid separating unit for solid-liquid separating the insolubilized product. The apparatus for treating borofluoride-containing water according to [5], comprising:
［７］　前記第一の反応槽のアルミニウム化合物の添加量が、前記ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、かつ、前記ホウフッ化物含有水のホウ素濃度に対するＡｌ換算値でＡｌ／Ｂ＝２．０～４．５（モル比）であることを特徴とする［５］又は［６］に記載のホウフッ化物含有水の処理方法。 [7] The addition amount of the aluminum compound in the first reaction tank is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and The borofluoride-containing water according to [5] or [6], wherein Al / B = 2.0 to 4.5 (molar ratio) in terms of Al with respect to the boron concentration of the borofluoride-containing water Processing method.
［８］　前記第一の固液分離手段で得られる分離水のアルミニウム濃度が３０～７０ｍｇ／Ｌであることを特徴とする［５］ないし［７］のいずれかに記載のホウフッ化物含有水の処理装置。 [8] The borofluoride-containing water according to any one of [5] to [7], wherein the aluminum concentration of the separation water obtained by the first solid-liquid separation means is 30 to 70 mg / L Processing equipment.
　本発明によれば、アルミニウム化合物の添加量とカルシウム化合物の添加量を制御すると共に、１０～３５℃の常温で処理することにより、フッ素のみならずホウ素をも高度に除去することができる。 According to the present invention, by controlling the addition amount of the aluminum compound and the addition amount of the calcium compound and treating at a room temperature of 10 to 35 ° C., not only fluorine but also boron can be removed to a high degree.
　本発明の処理は、基本的に加温を必要としないため、運転コストを削減することができる。本発明は常温で反応させるため、冬期においては場合により加温する場合があるが、この場合においても常温に保てば良いため運転コストは従来技術より削減できる。 Since the treatment of the present invention basically does not require heating, the operating cost can be reduced. Since the present invention reacts at room temperature, it may be heated in some cases in the winter, but even in this case, the operation cost can be reduced as compared with the prior art because it may be kept at room temperature.
　処理水中にアルミニウムを残留させて、更なる高度処理でフッ素を極低濃度にまで除去することもできる。 It is possible to leave aluminum in the treated water and remove fluorine to a very low concentration by further advanced treatment.
本発明のホウフッ化物含有水の処理装置の実施の形態を示す系統図である。It is a systematic diagram which shows embodiment of the processing apparatus of the borofluoride containing water of this invention. 実験例１～４における処理水のＢＦ４濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the BF 4 concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例１～４における処理水のＦ濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the F concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例１～４における処理水のＢ濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the B concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例１～４における処理水のＡｌ濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the Al concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例１～４における処理水のＳＯ４濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the SO 4 concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例１～４における処理水のＣａ濃度とＣａ／Ａｌ（モル比）との関係を示すグラフである。6 is a graph showing the relationship between the Ca concentration of treated water and Ca / Al (molar ratio) in Experimental Examples 1 to 4. 実験例５，６における処理水のＢ濃度とＡｌ／Ｂ（モル比）との関係を示すグラフである。It is a graph which shows the relationship between B density | concentration of the treated water in Experiment Example 5, 6, and Al / B (molar ratio).
　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。 Embodiments of the present invention will be described below in detail with reference to the drawings.
　図１は、本発明のホウフッ化物含有水の処理装置の実施の形態を示す系統図である。 FIG. 1 is a system diagram showing an embodiment of a treatment apparatus for water containing borofluoride according to the present invention.
　図１において、１は第１反応槽（第一の反応槽）、２は第２反応槽（第二の反応槽）、３は凝集槽、４は固液分離槽（第一の固液分離手段）、５は第３反応槽（第三の反応槽）、６は凝集槽、７は固液分離槽（第二の固液分離手段）をそれぞれ示す。原水は、第１反応槽１において、アルミニウム化合物（Ａｌ化合物）と酸が添加されてｐＨ１～４で原水中のホウフッ化物が分解処理される（第一の工程）。 In FIG. 1, 1 is a first reaction tank (first reaction tank), 2 is a second reaction tank (second reaction tank), 3 is a coagulation tank, and 4 is a solid-liquid separation tank (first solid-liquid separation). Means), 5 is a third reaction tank (third reaction tank), 6 is a coagulation tank, and 7 is a solid-liquid separation tank (second solid-liquid separation means). In the first reaction tank 1, the raw water is added with an aluminum compound (Al compound) and an acid, and the borofluoride in the raw water is decomposed at pH 1 to 4 (first step).
　第１反応槽１の処理水は次いで第２反応槽２に送給され、カルシウム化合物（Ｃａ化合物）と必要に応じてアルカリが添加され、ｐＨ７～１３で処理されることにより、フッ化カルシウム等の不溶化物が生成する（第二の工程）。 The treated water in the first reaction tank 1 is then fed to the second reaction tank 2 and added with a calcium compound (Ca compound) and an alkali as necessary, and treated at pH 7 to 13 to obtain calcium fluoride or the like. The insolubilized product is produced (second step).
　第２反応槽２の処理水は、次いで凝集槽３で高分子凝集剤が添加されて凝集処理された後、固液分離槽４で固液分離される（第三の工程）。 The treated water in the second reaction tank 2 is then agglomerated by adding a polymer flocculant in the agglomeration tank 3 and then solid-liquid separated in the solid-liquid separation tank 4 (third step).
　固液分離槽４の分離汚泥は系外へ排出され、分離水は第３反応槽（第三の反応槽）５に送給され、必要に応じてアルミニウム化合物と酸が添加されてｐＨ６～７で不溶化処理される（第四の工程）。 The separated sludge in the solid-liquid separation tank 4 is discharged to the outside of the system, and the separated water is sent to the third reaction tank (third reaction tank) 5, and an aluminum compound and an acid are added as necessary to adjust the pH to 6-7. Insolubilization treatment (fourth step).
　この第３反応槽５の処理水は、次いで凝集槽６で高分子凝集剤が添加されて凝集処理された後、固液分離槽７で固液分離される（第五の工程）。 The treated water in the third reaction tank 5 is then subjected to a coagulation treatment by adding a polymer flocculant in the coagulation tank 6 and then solid-liquid separation in the solid-liquid separation tank 7 (fifth step).
　固液分離槽７の分離汚泥は系外へ排出され、分離水は処理水として取り出される。 The separated sludge in the solid-liquid separation tank 7 is discharged out of the system, and the separated water is taken out as treated water.
　以下、原水及び各工程の処理について説明する。 Hereinafter, the raw water and each process will be described.
＜原水＞
　本発明で処理するホウフッ化物を含む水（原水）としては、ガラス製品、医薬品、化粧品、樹脂製品、めっき製品の製造排水、石炭火力発電所の排煙脱硫排水、ごみ焼却場洗煙排水、ニッケルめっき工場排水などが挙げられる。通常、これらのホウフッ化物含有排水中には、ＢＦ４ －とならずにＦ－、ＢＯ３ ３－の形態となったフッ素及びホウ素も存在する。 <Raw water>
Examples of water (raw water) containing borofluoride to be treated in the present invention include glass products, pharmaceuticals, cosmetics, resin products, manufacturing wastewater of plating products, flue gas desulfurization wastewater from coal-fired power plants, waste incineration smoke cleaning wastewater, nickel Examples include plating factory wastewater. In these borofluoride-containing wastewaters, fluorine and boron in the form of F − and BO 3 3− are also present instead of BF 4 − .
　本発明で処理するこれらの原水の水質は、通常ＢＦ４濃度（水中に溶解しているＢＦ４ －イオン濃度。本発明では「ＢＦ４濃度」と記載する。）５～２０００ｍｇ／Ｌ、Ｆ濃度（水中に溶解しているフッ素濃度。本発明では「Ｆ濃度」と記載する。）５～１００００ｍｇ／Ｌ、Ｂ濃度（水中に溶解しているホウ素の濃度。本発明では「Ｂ濃度」と記載する。）１～５００ｍｇ／Ｌで、ｐＨ０．５～１１．５である。 These raw water quality to be processed by the present invention is generally BF 4 concentration (BF 4 dissolved in water -.. The ionic concentration present invention referred to as "BF 4 concentration") 5 ~ 2000mg / L, F concentration (Fluorine concentration dissolved in water. In the present invention, described as “F concentration.”) 5 to 10,000 mg / L, B concentration (concentration of boron dissolved in water. In the present invention, described as “B concentration”) 1) 500 mg / L and pH 0.5-11.5.
　Ｆ濃度はＪＩＳ　Ｋ０１０２の３４．１（ランタン－アザリンコンプレキソン吸光光度法）に定める方法によって測定でき、Ｂ濃度はＪＩＳ　Ｋ０１０２の４７．３（ＩＣＰ発光分光分析法）に定める方法で分析できる。 The F concentration can be measured by the method defined in JIS K0102 34.1 (lanthanum-azarin complexone spectrophotometry), and the B concentration can be analyzed by the method defined in JIS K0102 47.3 (ICP emission spectrometry).
＜第一の工程＞
　第一の工程では、原水にアルミニウム化合物を添加して下式の反応によりホウフッ化物を分解する。
　　３ＢＦ４ －＋２Ａｌ３＋＋９Ｈ２Ｏ→２ＡｌＦ６ ３－＋３Ｈ３ＢＯ３＋９Ｈ＋ <First step>
In the first step, an aluminum compound is added to raw water and borofluoride is decomposed by the reaction of the following formula.
3BF 4 − + 2Al 3+ + 9H 2 O → 2AlF 6 3 − + 3H 3 BO 3 + 9H +
　原水に添加するアルミニウム化合物としては、反応時のｐＨ条件においてアルミニウムイオンが溶解するものであればよく、例えば、硫酸アルミニウム、塩化アルミニウム、ポリ塩化アルミニウム（ＰＡＣ）、硫酸バンドなどの１種又は２種以上を用いることができる。 The aluminum compound to be added to the raw water may be any aluminum compound that dissolves aluminum ions under the pH conditions during the reaction. For example, one or two of aluminum sulfate, aluminum chloride, polyaluminum chloride (PAC), sulfate band, etc. The above can be used.
　原水へのアルミニウム化合物添加量は、原水のＦ濃度に対してＡｌ換算の添加量がＡｌ／Ｆ（モル比）で１．２～２．５、好ましくは１．５～２．５で、原水のＢ濃度に対してＡｌ換算の添加量がＡｌ／Ｂ（モル比）で好ましくは２．０～４．５の範囲となるような添加量とする。アルミニウム化合物の添加量が上記下限よりも少ないと、ホウフッ化物を十分に分解させることができず、上記上限より多くても、添加量に見合う効果は得られず、アルミニウム化合物使用量が徒に増大する結果となり好ましくない。 The amount of aluminum compound added to the raw water is such that the amount added in terms of Al is 1.2 to 2.5, preferably 1.5 to 2.5 in terms of Al / F (molar ratio) with respect to the F concentration of the raw water. The addition amount in terms of Al with respect to the B concentration is preferably in the range of 2.0 to 4.5 in terms of Al / B (molar ratio). If the addition amount of the aluminum compound is less than the above lower limit, the borofluoride cannot be sufficiently decomposed, and if it is more than the above upper limit, an effect commensurate with the addition amount cannot be obtained, and the use amount of the aluminum compound increases easily. As a result.
　アルミニウム化合物によるホウフッ化物の分解反応は、酸性条件で迅速に反応が進むことから、第一の工程のｐＨは１～４、好ましくは１．５～２．５とする。従って、必要に応じて原水にアルミニウム化合物と共に酸（例えば硫酸、塩酸、より好ましくは硫酸）を添加してｐＨ１～４、好ましくは１．５～２．５にｐＨ調整する。 Since the decomposition reaction of borofluoride with an aluminum compound proceeds rapidly under acidic conditions, the pH of the first step is 1 to 4, preferably 1.5 to 2.5. Accordingly, if necessary, an acid (for example, sulfuric acid, hydrochloric acid, more preferably sulfuric acid) is added to the raw water together with an aluminum compound to adjust the pH to 1 to 4, preferably 1.5 to 2.5.
　本発明においては、上記アルミニウム化合物添加量及びｐＨ条件を採用することにより、液温１０～３５℃、好ましくは１５～３０℃の常温で処理が可能であるため、第一の工程における加温の必要はない。 In the present invention, by adopting the above-mentioned aluminum compound addition amount and pH conditions, the liquid temperature can be treated at room temperature of 10 to 35 ° C., preferably 15 to 30 ° C. There is no need.
　第一の工程の反応時間は、原水中のホウフッ化物の分解時間を確保する点から０．５～１０時間程度とすることが好ましい。 The reaction time in the first step is preferably about 0.5 to 10 hours from the viewpoint of securing the decomposition time of borofluoride in the raw water.
＜第二の工程＞
　第二の工程では、第一の工程の処理水にカルシウム化合物を添加して、下式の反応によりフッ化カルシウムを析出させると共に、更に後述の通り、ホウ素の吸着除去を行う。
　　ＡｌＦ６ ３－＋３Ｃａ２＋＋３ＯＨ－→３ＣａＦ２＋Ａｌ（ＯＨ）３ <Second step>
In the second step, a calcium compound is added to the treated water of the first step to precipitate calcium fluoride by the reaction of the following formula, and further, adsorption and removal of boron is performed as described later.
AlF 6 3− + 3Ca 2+ + 3OH − → 3CaF 2 + Al (OH) 3
　カルシウム化合物としては、例えば消石灰、塩化カルシウム、炭酸カルシウムなどの１種又は２種以上を用いることができる。 As a calcium compound, 1 type, or 2 or more types, such as slaked lime, calcium chloride, calcium carbonate, can be used, for example.
　カルシウム化合物の添加量は、第一の工程で添加したアルミニウム化合物のＡｌ換算量に対して、Ｃａ換算の添加量がＣａ／Ａｌ（モル比）で２．５～４．０、好ましくは２．７～３．８の範囲となるようにする。 The amount of calcium compound added is 2.5 to 4.0 in terms of Ca / Al (molar ratio) with respect to the amount of Al converted to the aluminum compound added in the first step, preferably 2. The range is 7 to 3.8.
　カルシウム化合物の添加量を上記範囲内とすることにより、ホウ素の吸着除去効率を高めることができる。また、カルシウム化合物の添加量を上記範囲内とすることにより、第二の工程の処理水中に残留するＡｌ濃度（水中に溶解しているアルミニウム濃度。本発明では「Ａｌ濃度」と記載する。）を高め、後述の第四の工程でのフッ素除去に有効利用することが可能となる。 By making the addition amount of the calcium compound within the above range, the adsorption and removal efficiency of boron can be enhanced. Further, by making the addition amount of the calcium compound within the above range, the Al concentration remaining in the treated water in the second step (the aluminum concentration dissolved in the water. In the present invention, it is described as “Al concentration”). And can be effectively used for fluorine removal in the fourth step described later.
　Ａｌ濃度はＪＩＳ　Ｋ０１０２の５８．４（ＩＣＰ発光分光分析法）に定める方法で分析することができる。 The Al concentration can be analyzed by the method defined in JIS K0102 58.4 (ICP emission spectroscopy).
　本発明において、この第二の工程はｐＨ７～１３の条件で行うため、必要に応じて、第一の工程の処理水にカルシウム化合物と共に、水酸化ナトリウム等のアルカリまたは硫酸などの酸を添加してｐＨ調整する。なお、カルシウム化合物として消石灰を用い、消石灰の添加により、所望のｐＨとなる場合は、このｐＨ調整は不要である。 In the present invention, since the second step is carried out under conditions of pH 7 to 13, if necessary, an alkali such as sodium hydroxide or an acid such as sulfuric acid is added to the treated water of the first step together with the calcium compound. To adjust the pH. When slaked lime is used as the calcium compound and the desired pH is obtained by adding slaked lime, this pH adjustment is not necessary.
　一般的に、フッ化カルシウムの析出はｐＨ４～１０の条件とすることが好ましいが、特に、フッ素の除去を優先する場合はｐＨ９～１１がより好ましい。これは、アルミニウムとフッ素の結合がアルカリ条件下で切れやすいため、フッ化カルシウムの析出が促進されるためである。 In general, it is preferable to deposit calcium fluoride under conditions of pH 4 to 10, but pH 9 to 11 is more preferable particularly when priority is given to removal of fluorine. This is because the precipitation of calcium fluoride is promoted because the bond between aluminum and fluorine is easily broken under alkaline conditions.
　ホウ素の除去を優先する場合はｐＨ１０～１２．５がより好ましい。これは、ｐＨ１０以上の高アルカリ条件において、下式の反応によりアルミン酸カルシウム（ＣａＯ・Ａｌ２Ｏ３）が析出し、この析出反応の際に、同時にホウ素が吸着・除去されるためである。従って、フッ素とホウ素の同時除去の点において、より好ましいｐＨ条件は１０～１２である。
　　６Ｃａ（ＯＨ）２＋Ａｌ２（ＳＯ４）３→３ＣａＯ・Ａｌ２Ｏ３・３ＣａＳＯ４・６Ｈ２Ｏ When priority is given to removal of boron, a pH of 10 to 12.5 is more preferable. This is because calcium aluminate (CaO.Al 2 O 3 ) is precipitated by a reaction of the following formula under a highly alkaline condition of pH 10 or higher, and boron is simultaneously adsorbed and removed during this precipitation reaction. Therefore, a more preferable pH condition is 10 to 12 in terms of simultaneous removal of fluorine and boron.
6Ca (OH) 2 + Al 2 (SO 4 ) 3 → 3CaO · Al 2 O 3 · 3CaSO 4 · 6H 2 O
　この第二の工程におけるホウ素の除去は吸着反応であり、液温が低い方が吸着量が高くなるため、本発明では、第二の工程は、液温１０～３５℃、好ましくは１５～３０℃の常温で処理する。このため、この工程においても加温の必要はない。 The removal of boron in the second step is an adsorption reaction, and the lower the liquid temperature, the higher the amount of adsorption. Therefore, in the present invention, the second step is a liquid temperature of 10 to 35 ° C., preferably 15 to 30 ° C. Process at room temperature of ℃. For this reason, heating is not necessary in this step.
　第二の工程の反応時間は、原水中のフッ素とカルシウム化合物との反応時間等を確保する点から０．５～４時間程度とすることが好ましい。 The reaction time in the second step is preferably about 0.5 to 4 hours from the viewpoint of securing the reaction time of fluorine and calcium compound in raw water.
＜第三の工程＞
　第三の工程では、第二の工程で析出した不溶化物（フッ化カルシウム及びアルミン酸カルシウムを含む汚泥）を固液分離して分離水を得る。固液分離性能を高めるために、第二の工程と第三の工程との間に、高分子凝集剤を添加して凝集する工程を行ってもよい。 <Third step>
In the third step, the insolubilized matter (sludge containing calcium fluoride and calcium aluminate) precipitated in the second step is subjected to solid-liquid separation to obtain separated water. In order to improve the solid-liquid separation performance, a step of aggregating by adding a polymer flocculant may be performed between the second step and the third step.
　高分子凝集剤としては、排水処理で使用されているものが適用可能であり、ポリアクリルアミド部分加水分解物、ポリアクリル酸ナトリウム、アクリルアミドとアクリル酸（塩）との共重合物等のアニオン系高分子凝集剤あるいはポリアクリルアミド等のノニオン性の高分子凝集剤の１種又は２種以上を用いることができる。高分子凝集剤の添加量は、処理対象原水の水質や用いる高分子凝集剤によっても異なるが、通常０．１～２０ｍｇ／Ｌ程度である。 As the polymer flocculant, those used in wastewater treatment can be applied, such as polyacrylamide partial hydrolysates, sodium polyacrylate, and copolymers of acrylamide and acrylic acid (salt). One kind or two or more kinds of nonionic polymer flocculants such as a molecular flocculant or polyacrylamide can be used. The amount of the polymer flocculant added is usually about 0.1 to 20 mg / L, although it varies depending on the quality of the raw water to be treated and the polymer flocculant used.
　第三の工程における固液分離には、沈殿槽等の固液分離槽の他、膜分離装置、濾過装置、脱水機等を用いることができる。 For the solid-liquid separation in the third step, a membrane separation apparatus, a filtration apparatus, a dehydrator, etc. can be used in addition to a solid-liquid separation tank such as a precipitation tank.
　この第三の工程においては、処理対象原水の水質、アルミニウム化合物及びカルシウム化合物の添加量等によっても異なるが、通常、Ｆ濃度３～１５ｍｇ／Ｌ程度、Ｂ濃度１～１０ｍｇ／Ｌ程度、ＢＦ４濃度０．１ｍｇ／Ｌ以下の処理水を得ることができる。後述の如く、この処理水のＡｌ濃度は通常３０～７０ｍｇ／Ｌ程度である。 In this third step, the F concentration is about 3 to 15 mg / L, the B concentration is about 1 to 10 mg / L, and BF 4 is varied depending on the quality of the raw water to be treated, the amount of aluminum compound and calcium compound added, and the like. Treated water having a concentration of 0.1 mg / L or less can be obtained. As will be described later, the Al concentration of this treated water is usually about 30 to 70 mg / L.
＜第四の工程＞
　本発明においては、上記の第三の工程の固液分離水を処理水としてもよいが、更にこの固液分離水を処理してフッ素を除去する第四の工程を行ってもよい。即ち、第二の工程でフッ素はフッ化カルシウムとして不溶化されるが、フッ化カルシウムの溶解度の関係から、第三の工程の固液分離水中にはわずかながらフッ素が残留する。従って、第四の工程を行って、残留するフッ素を更に除去してもよい。 <Fourth process>
In the present invention, the solid-liquid separated water in the third step may be treated water, but a fourth step of further removing fluorine by treating the solid-liquid separated water may be performed. That is, although fluorine is insolubilized as calcium fluoride in the second step, a slight amount of fluorine remains in the solid-liquid separated water in the third step due to the solubility of calcium fluoride. Therefore, the remaining fluorine may be further removed by performing the fourth step.
　第四の工程では、必要に応じてアルミニウム化合物と酸、アルミニウム化合物の添加量によってはアルカリを添加してｐＨ６～７に調整することにより、水酸化アルミニウムを析出させる。この水酸化アルミニウムが析出する際の共沈作用により水中のフッ素を不溶化させて除去する。 In the fourth step, aluminum hydroxide is precipitated by adjusting the pH to 6 to 7 by adding an alkali depending on the amount of the aluminum compound, acid, and aluminum compound as required. Fluorine in water is insolubilized and removed by coprecipitation when aluminum hydroxide is precipitated.
　本発明においては、第一の工程でアルミニウム化合物を添加した後、第二の工程でカルシウム化合物を前述のＣａ／Ａｌ（モル比）で添加することにより、第三の工程で得られる固液分離水中にアルミニウムを３０～７０ｍｇ／Ｌ程度残留させることができる。このため、この第四の工程に必要なアルミニウム量を、この残留アルミニウム量で賄うことができ、第四の工程では、酸を添加して５～３０分程度、常温（１０～３５℃）の攪拌下に反応させるのみで、フッ素を除去することも可能である。ただし、必要に応じてこの第四の工程でアルミニウム化合物を添加してもよい。このアルミニウム化合物としては、第一の工程で用いるアルミニウム化合物として例示したものを用いることができる。 In the present invention, after the aluminum compound is added in the first step, the calcium compound is added in the above-mentioned Ca / Al (molar ratio) in the second step, thereby obtaining the solid-liquid separation obtained in the third step. About 30 to 70 mg / L of aluminum can be left in water. For this reason, the amount of aluminum necessary for the fourth step can be covered by the amount of residual aluminum. In the fourth step, an acid is added for about 5 to 30 minutes at room temperature (10 to 35 ° C.). It is also possible to remove fluorine only by reacting with stirring. However, an aluminum compound may be added in this fourth step as necessary. As this aluminum compound, those exemplified as the aluminum compound used in the first step can be used.
＜第五の工程＞
　第五の工程では、第四工程で析出した不溶化物（水酸化アルミニウムを含むフッ素の共沈汚泥）を固液分離して処理水を得る。ここで、固液分離性能を高めるために、第四の工程と第五の工程との間に、高分子凝集剤を添加して凝集する工程を行ってもよい。 <Fifth process>
In the fifth step, the insolubilized matter (fluorine coprecipitation sludge containing aluminum hydroxide) precipitated in the fourth step is subjected to solid-liquid separation to obtain treated water. Here, in order to improve the solid-liquid separation performance, a step of aggregating by adding a polymer flocculant may be performed between the fourth step and the fifth step.
　この場合、高分子凝集剤としては、ポリアクリルアミド部分加水分解物、ポリアクリル酸ナトリウム、ポリビニルアミジン等のアニオン系高分子凝集剤の１種又は２種以上を用いることができる。高分子凝集剤の添加量は、処理対象原水の水質や用いる高分子凝集剤によっても異なるが、通常０．１～５ｍｇ／Ｌ程度である。 In this case, as the polymer flocculant, one kind or two or more kinds of anionic polymer flocculants such as polyacrylamide partial hydrolyzate, sodium polyacrylate and polyvinylamidine can be used. The amount of the polymer flocculant added is usually about 0.1 to 5 mg / L, although it varies depending on the quality of the raw water to be treated and the polymer flocculant used.
　第五の工程における固液分離には、沈殿槽等の固液分離槽の他、膜分離装置、濾過装置等を用いることができる。 For the solid-liquid separation in the fifth step, a membrane separation apparatus, a filtration apparatus, etc. can be used in addition to a solid-liquid separation tank such as a precipitation tank.
　この第五の工程においては、処理対象原水の水質、アルミニウム化合物及びカルシウム化合物の添加量等によっても異なるが、通常、Ｆ濃度１．１ｍｇ／Ｌ以下、Ｂ濃度３．５ｍｇ／Ｌ以下、ＢＦ４濃度０．１ｍｇ／Ｌ以下、Ａｌ濃度１ｍｇ／Ｌ以下の高水質の処理水を得ることができる。 In the fifth step, the F concentration is 1.1 mg / L or less, the B concentration is 3.5 mg / L or less, BF 4 , although it varies depending on the quality of the raw water to be treated, the addition amount of the aluminum compound and the calcium compound, and the like. High-quality treated water having a concentration of 0.1 mg / L or less and an Al concentration of 1 mg / L or less can be obtained.
＜その他の工程＞
　本発明においては、更に、以下の工程を付加してもよい。 <Other processes>
In the present invention, the following steps may be further added.
　原水を第一の工程で処理するに先立ち、カルシウム化合物を添加してｐＨ４～１０で反応させて析出した不溶化物を固液分離することにより、原水中のフッ素の一部を予め除去してもよい。このような前処理工程を付加して原水中のフッ素を予め粗取りすることにより、第一の工程に流入する水のＦ濃度を低減して第一の工程におけるアルミニウム化合物の添加量を削減することができる。 Prior to the treatment of the raw water in the first step, a part of the fluorine in the raw water can be removed in advance by solid-liquid separation of the insolubilized matter that is precipitated by adding a calcium compound and reacting at pH 4-10. Good. By adding such a pretreatment step and pre-roughening the fluorine in the raw water in advance, the F concentration of water flowing into the first step is reduced and the amount of aluminum compound added in the first step is reduced. be able to.
　第三の工程で固液分離して得られた分離汚泥の一部を第二の工程に返送して添加してもよい。この場合において、第二の工程で添加するカルシウム化合物をこの返送汚泥に添加混合して汚泥を改質し、改質汚泥を第二の工程で添加するようにしてもよい。このような汚泥返送を行うことにより、この汚泥の表面で新たにフッ化カルシウムが析出する。これにより、第三の工程で得られる固液分離汚泥の脱水性が高められ、この汚泥を脱水処理して得られる脱水ケーキの含水率を低減することができる。 A part of the separated sludge obtained by solid-liquid separation in the third step may be returned to the second step and added. In this case, the calcium compound added in the second step may be added to and mixed with the returned sludge to modify the sludge, and the modified sludge may be added in the second step. By performing such sludge return, calcium fluoride is newly deposited on the surface of the sludge. Thereby, the dehydrating property of the solid-liquid separation sludge obtained in the third step is enhanced, and the moisture content of the dehydrated cake obtained by dehydrating the sludge can be reduced.
　以下に本発明例及び比較例を示す実験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 in more detail with reference to experimental examples showing the present invention and comparative examples.
　なお、以下において、原水としては、下記水質のものを用いた。
＜原水水質＞
　Ｆ濃度：６００ｍｇ／Ｌ（３１．６ミリモル／Ｌ）
　Ｂ濃度：２００ｍｇ－Ｂ／Ｌ（１８．５ミリモル／Ｌ）
　ＢＦ４濃度：２５０ｍｇ／Ｌ In the following, raw water having the following water quality was used.
<Raw water quality>
F concentration: 600 mg / L (31.6 mmol / L)
B concentration: 200 mg-B / L (18.5 mmol / L)
BF 4 concentration: 250 mg / L
　アルミニウム化合物としては硫酸バンド（８重量％、Ａｌ２Ｏ３）を用い、カルシウム化合物としては消石灰（Ｃａ（ＯＨ）２）を用いた。高分子凝集剤としては、栗田工業（株）製アニオン系高分子凝集剤「クリファーム（登録商標）ＰＡ８２３」を用い、その添加量は１０ｍｇ／Ｌとした。 A sulfate band (8 wt%, Al 2 O 3 ) was used as the aluminum compound, and slaked lime (Ca (OH) 2 ) was used as the calcium compound. As the polymer flocculant, an anionic polymer flocculant “Clifarm (registered trademark) PA823” manufactured by Kurita Kogyo Co., Ltd. was used, and the amount added was 10 mg / L.
［実験例１～４］
　原水に硫酸バンドをそれぞれ下記表１に示す量添加し、硫酸でｐＨ２に調整した後、４時間反応させた。その後、消石灰を添加してｐＨ１０で１時間反応させた。消石灰は、硫酸バンド添加量と消石灰添加量とで算出されるＣａ／Ａｌ（モル比）を１～６の範囲で種々変更して添加した。 [Experimental Examples 1 to 4]
A sulfuric acid band was added to the raw water in the amounts shown in Table 1 below, adjusted to pH 2 with sulfuric acid, and reacted for 4 hours. Then, slaked lime was added and reacted at pH 10 for 1 hour. The slaked lime was added by changing the Ca / Al (molar ratio) calculated based on the addition amount of the sulfuric acid band and the addition amount of the slaked lime in the range of 1 to 6.
　消石灰の添加でｐＨが１０にならない場合には、適宜酸（硫酸）又はアルカリ（水酸化ナトリウム）を添加してｐＨ１０に調整した。 When the pH did not reach 10 due to the addition of slaked lime, acid (sulfuric acid) or alkali (sodium hydroxide) was appropriately added to adjust the pH to 10.
Figure JPOXMLDOC01-appb-T000001
Figure JPOXMLDOC01-appb-T000001
　次いで、高分子凝集剤を添加して５分間凝集処理し、凝集処理水を固液分離した。 Next, a polymer flocculant was added and the mixture was agglomerated for 5 minutes, and the agglomerated water was separated into solid and liquid.
　上記一連の処理はいずれも液温２０℃で行った。 All the above series of treatments were performed at a liquid temperature of 20 ° C.
　得られた処理水（固液分離水）の水質を分析し、Ｃａ／Ａｌモル比との関係を調べ、結果を図２～７に示した。 The water quality of the obtained treated water (solid-liquid separation water) was analyzed, the relationship with the Ca / Al molar ratio was examined, and the results are shown in FIGS.
　図２より、Ａｌ／Ｆ（モル比）が１．５以上であると、原水中のホウフッ化物（ＢＦ４）を完全に分解することができることが分かる。 From FIG. 2, it can be seen that the borofluoride (BF 4 ) in the raw water can be completely decomposed when the Al / F (molar ratio) is 1.5 or more.
　図３，４より、Ａｌ／Ｆ（モル比）が１．５以上で、Ｃａ／Ａｌ（モル比）が２．５～４．０の範囲であるとフッ素及びホウ素の除去率が高く、特にホウ素の除去効率が向上することが分かる。 3 and 4, when Al / F (molar ratio) is 1.5 or more and Ca / Al (molar ratio) is in the range of 2.5 to 4.0, the removal rate of fluorine and boron is high. It can be seen that the boron removal efficiency is improved.
　図５より、Ｃａ／Ａｌ（モル比）が２．５～４．０の範囲であると、処理水中に残留するＡｌ量が多くなり、更なるフッ素の処理に有効利用することができることが分かる。 FIG. 5 shows that when the Ca / Al (molar ratio) is in the range of 2.5 to 4.0, the amount of Al remaining in the treated water increases and can be effectively used for further fluorine treatment. .
　図６の通り、Ｃａ／Ａｌ（モル比）が２．５～４．０の範囲であると、処理水中のＳＯ４濃度（ＳＯ４ ２－イオン濃度）が低く、装置後段（処理水配管など）でのＣａＳＯ４スケールトラブルが軽減できる。 As shown in FIG. 6, when the Ca / Al (molar ratio) is in the range of 2.5 to 4.0, the SO 4 concentration (SO 4 2- ion concentration) in the treated water is low, and the latter part of the apparatus (treated water piping, etc.) ) CaSO 4 scale trouble can be reduced.
　図７の通り、Ｃａ／Ａｌ（モル比）が２．５～４．０の範囲であると、処理水中のＣａ濃度（Ｃａ２＋イオン濃度）が低く、装置後段（処理水配管など）でのＣａＳＯ４スケールトラブルが軽減できる。 As shown in FIG. 7, when the Ca / Al (molar ratio) is in the range of 2.5 to 4.0, the Ca concentration (Ca 2+ ion concentration) in the treated water is low, and the latter part of the apparatus (treated water piping, etc.) CaSO 4 scale trouble can be reduced.
［実験例５，６］
　原水に所定量の硫酸バンドを添加し、硫酸でｐＨ２に調整した後４時間反応させた。その後、消石灰を添加してｐＨ１０で１時間反応させた。消石灰は、硫酸バンド添加量と消石灰添加量とで算出されるＣａ／Ａｌ（モル比）が２．５となるように添加した。 [Experimental Examples 5 and 6]
A predetermined amount of sulfuric acid band was added to the raw water, adjusted to pH 2 with sulfuric acid, and then reacted for 4 hours. Then, slaked lime was added and reacted at pH 10 for 1 hour. Slaked lime was added so that the Ca / Al (molar ratio) calculated by the addition amount of sulfuric acid band and the addition amount of slaked lime was 2.5.
　消石灰の添加でｐＨが１０にならない場合には、適宜酸（硫酸）又はアルカリ（水酸化ナトリウム）を添加してｐＨ１０に調整した。 When the pH did not reach 10 due to the addition of slaked lime, acid (sulfuric acid) or alkali (sodium hydroxide) was appropriately added to adjust the pH to 10.
　次いで、高分子凝集剤を添加して５分間凝集処理し、凝集処理水を固液分離した。 Next, a polymer flocculant was added and the mixture was agglomerated for 5 minutes, and the agglomerated water was separated into solid and liquid.
　硫酸バンドは、原水中のホウ素に対して、Ａｌ換算の添加量をＡｌ／Ｂ（モル比）で種々変更して添加した。原水のフッ素濃度は、ホウ素濃度の約１．７倍であるので、Ａｌ／Ｂ（モル比）が約２.０～４.０の範囲であれば、Ａｌ／Ｆ（モル比）は１．２～２．５となる。 The sulfuric acid band was added to the boron in the raw water by variously changing the addition amount in terms of Al with Al / B (molar ratio). Since the fluorine concentration of the raw water is about 1.7 times the boron concentration, if the Al / B (molar ratio) is in the range of about 2.0 to 4.0, the Al / F (molar ratio) is 1. 2 to 2.5.
　上記の一連の処理は、実験例５では液温２０℃で行い、実験例６では液温６０℃で行った。 The series of treatments described above were performed at a liquid temperature of 20 ° C. in Experimental Example 5 and at a liquid temperature of 60 ° C. in Experimental Example 6.
　得られた処理水（固液分離水）のＢ濃度を分析し、Ａｌ／Ｂモル比との関係を図８に示した。 B concentration of the obtained treated water (solid-liquid separated water) was analyzed, and the relationship with the Al / B molar ratio is shown in FIG.
　図８より、処理温度が６０℃の場合よりも、２０℃の場合の方が、ホウ素除去率が格段に高いことが分かる。Ａｌ／Ｂ（モル比）が２．０～４．５の範囲であると、ホウ素除去効果に優れることが分かる。 FIG. 8 shows that the boron removal rate is much higher when the treatment temperature is 20 ° C. than when the treatment temperature is 60 ° C. It can be seen that when the Al / B (molar ratio) is in the range of 2.0 to 4.5, the boron removal effect is excellent.
［実験例７］
　実験例３において、硫酸バンドをＡｌ／Ｆ（モル比）＝１．５、Ａｌ／Ｂ（モル比）＝２．５、Ｃａ／Ａｌ（モル比）＝３．３となるように添加した場合において得られた固液分離水（Ｆ濃度＝９ｍｇ／Ｌ、Ｂ濃度＝３．５ｍｇ／Ｌ、ＢＦ４濃度＜０．１ｍｇ／Ｌ、Ａｌ濃度＝６１ｍｇ／Ｌ）に、硫酸を添加してｐＨ６．５とし、１５分攪拌して不溶化物を析出させた。 [Experimental Example 7]
In Experimental Example 3, when a sulfuric acid band was added so that Al / F (molar ratio) = 1.5, Al / B (molar ratio) = 2.5, and Ca / Al (molar ratio) = 3.3 Was added to the solid-liquid separated water (F concentration = 9 mg / L, B concentration = 3.5 mg / L, BF 4 concentration <0.1 mg / L, Al concentration = 61 mg / L) obtained by adding sulfuric acid to pH 6 And the mixture was stirred for 15 minutes to precipitate an insolubilized product.
　次いで、高分子凝集剤を添加して５分間凝集処理し、凝集処理水を固液分離した。 Next, a polymer flocculant was added and the mixture was agglomerated for 5 minutes, and the agglomerated water was separated into solid and liquid.
　得られた処理水（固液分離水）は、Ｆ濃度＝１．１ｍｇ／Ｌ、Ｂ濃度＝３．５ｍｇ／Ｌ、ＢＦ４濃度＜０．１ｍｇ／Ｌ、Ａｌ濃度＜１ｍｇ／Ｌの高水質の処理水であった。 The obtained treated water (solid-liquid separation water) has high water quality with F concentration = 1.1 mg / L, B concentration = 3.5 mg / L, BF 4 concentration <0.1 mg / L, Al concentration <1 mg / L. Was treated water.
　本発明を特定の態様を用いて詳細に説明したが、本発明の意図と範囲を離れることなく様々な変更が可能であることは当業者に明らかである。
　本出願は、２０１３年２月２８日付で出願された日本特許出願２０１３－０３９１９３に基づいており、その全体が引用により援用される。 Although the present invention has been described in detail using specific embodiments, it will be apparent to those skilled in the art that various modifications can be made without departing from the spirit and scope of the invention.
This application is based on Japanese Patent Application No. 2013-039193 filed on February 28, 2013, which is incorporated by reference in its entirety.

Claims (8)

  1. 　ホウフッ化物含有水にアルミニウム化合物を添加してｐＨ１～４でホウフッ化物を分解する第一の工程と、該第一の工程の処理水にカルシウム化合物を添加してｐＨ７～１３で反応させることにより不溶化物を生成させる第二の工程と、該不溶化物を固液分離する第三の工程とを有するホウフッ化物含有水の処理方法において、
    　前記第一の工程のアルミニウム化合物の添加量が、該ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、
    　前記第二の工程のカルシウム化合物の添加量が、該アルミニウム化合物のＡｌ換算値に対するＣａ換算値でＣａ／Ａｌ＝２．５～４．０（モル比）であり、
    　前記第一及び第二の工程の処理温度が１０～３５℃であることを特徴とするホウフッ化物含有水の処理方法。     Insoluble by adding an aluminum compound to borofluoride-containing water and decomposing the borofluoride at pH 1 to 4, and adding calcium compound to the treated water of the first step and reacting at pH 7 to 13 In a method for treating borofluoride-containing water having a second step of producing a product and a third step of solid-liquid separation of the insolubilized product,
    The amount of the aluminum compound added in the first step is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water,
    The amount of calcium compound added in the second step is Ca / Al = 2.5 to 4.0 (molar ratio) in terms of Ca with respect to Al in terms of the aluminum compound,
    A method for treating borofluoride-containing water, wherein the treatment temperature in the first and second steps is 10 to 35 ° C.
  2. 　前記第三の工程で得られた分離水をｐＨ６～７で処理して不溶化物を生成させる第四の工程と、該不溶化物を固液分離する第五の工程とを有することを特徴とする請求項１に記載のホウフッ化物含有水の処理方法。 Characterized in that it comprises a fourth step of producing an insolubilized product by treating the separated water obtained in the third step with a pH of 6 to 7, and a fifth step of solid-liquid separation of the insolubilized product. The method for treating borofluoride-containing water according to claim 1.
  3. 　前記第一の工程のアルミニウム化合物の添加量が、前記ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、かつ、前記ホウフッ化物含有水のホウ素濃度に対するＡｌ換算値でＡｌ／Ｂ＝２．０～４．５（モル比）であることを特徴とする請求項１又は２に記載のホウフッ化物含有水の処理方法。 The addition amount of the aluminum compound in the first step is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and the borofluoride-containing content is 3. The method for treating borofluoride-containing water according to claim 1, wherein Al / B = 2.0 to 4.5 (molar ratio) in terms of Al with respect to the boron concentration of water.
  4. 　前記第三の工程で得られる分離水のアルミニウム濃度が３０～７０ｍｇ／Ｌであることを特徴とする請求項１ないし３のいずれか１項に記載のホウフッ化物含有水の処理方法。 The method for treating borofluoride-containing water according to any one of claims 1 to 3, wherein the aluminum concentration of the separated water obtained in the third step is 30 to 70 mg / L.
  5. 　ホウフッ化物含有水にアルミニウム化合物を添加してｐＨ１～４でホウフッ化物を分解する第一の反応槽と、該第一の反応槽の処理水にカルシウム化合物を添加してｐＨ７～１３で反応させることにより不溶化物を生成させる第二の反応槽と、該不溶化物を固液分離する第一の固液分離手段とを有するホウフッ化物含有水の処理装置において、
    　前記第一の反応槽のアルミニウム化合物の添加量が、該ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、
    　前記第二の反応槽のカルシウム化合物の添加量が、該アルミニウム化合物のＡｌ換算値に対するＣａ換算値でＣａ／Ａｌ＝２．５～４．０（モル比）であり、
    　前記第一及び第二の反応槽の処理温度が１０～３５℃であることを特徴とするホウフッ化物含有水の処理装置。     A first reaction vessel in which an aluminum compound is added to borofluoride-containing water to decompose the borofluoride at pH 1 to 4, and a calcium compound is added to the treated water in the first reaction vessel to react at pH 7 to 13 In a treatment apparatus for borofluoride-containing water having a second reaction tank for producing an insolubilized product by means of a first solid-liquid separation means for solid-liquid separation of the insolubilized product,
    The addition amount of the aluminum compound in the first reaction tank is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water,
    The addition amount of the calcium compound in the second reaction tank is Ca / Al = 2.5 to 4.0 (molar ratio) as a Ca conversion value with respect to an Al conversion value of the aluminum compound,
    An apparatus for treating borofluoride-containing water, wherein the treatment temperature of the first and second reaction vessels is 10 to 35 ° C.
  6. 　前記固液分離手段で得られた分離水をｐＨ６～７で処理して不溶化物を生成させる第三の反応槽と、該不溶化物を固液分離する第二の固液分離手段とを有することを特徴とする請求項５に記載のホウフッ化物含有水の処理装置。 It has a third reaction tank for producing the insolubilized product by treating the separated water obtained by the solid-liquid separating unit at pH 6-7, and a second solid-liquid separating unit for solid-liquid separating the insolubilized product. The apparatus for treating borofluoride-containing water according to claim 5.
  7. 　前記第一の反応槽のアルミニウム化合物の添加量が、前記ホウフッ化物含有水のフッ素濃度に対するＡｌ換算値でＡｌ／Ｆ＝１．２～２．５（モル比）であり、かつ、前記ホウフッ化物含有水のホウ素濃度に対するＡｌ換算値でＡｌ／Ｂ＝２．０～４．５（モル比）であることを特徴とする請求項５又は６に記載のホウフッ化物含有水の処理方法。 The addition amount of the aluminum compound in the first reaction tank is Al / F = 1.2 to 2.5 (molar ratio) in terms of Al with respect to the fluorine concentration of the borofluoride-containing water, and the borofluoride The method for treating borofluoride-containing water according to claim 5 or 6, wherein Al / B = 2.0 to 4.5 (molar ratio) in terms of Al with respect to the boron concentration of the contained water.
  8. 　前記第一の固液分離手段で得られる分離水のアルミニウム濃度が３０～７０ｍｇ／Ｌであることを特徴とする請求項５ないし７のいずれか１項に記載のホウフッ化物含有水の処理装置。 The apparatus for treating borofluoride-containing water according to any one of claims 5 to 7, wherein the aluminum concentration of the separated water obtained by the first solid-liquid separation means is 30 to 70 mg / L.
PCT/JP2014/054155 2013-02-28 2014-02-21 Method and apparatus for treating borofluoride-containing water WO2014132887A1 (en)

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