WO2004071970A1 - Procede pour eliminer le phosphore d'eaux usees - Google Patents

Procede pour eliminer le phosphore d'eaux usees Download PDF

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Publication number
WO2004071970A1
WO2004071970A1 PCT/JP2004/001417 JP2004001417W WO2004071970A1 WO 2004071970 A1 WO2004071970 A1 WO 2004071970A1 JP 2004001417 W JP2004001417 W JP 2004001417W WO 2004071970 A1 WO2004071970 A1 WO 2004071970A1
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WO
WIPO (PCT)
Prior art keywords
crystallization
crystallization tank
tank
slurry
wastewater
Prior art date
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PCT/JP2004/001417
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English (en)
Japanese (ja)
Inventor
Rokurou Aoki
Hajime Inagaki
Original Assignee
Nippon Chemical Industrial Co., Ltd
Hipotech Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Nippon Chemical Industrial Co., Ltd, Hipotech Inc filed Critical Nippon Chemical Industrial Co., Ltd
Publication of WO2004071970A1 publication Critical patent/WO2004071970A1/fr

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Classifications

    • 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
    • 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
    • C02F1/5209—Regulation methods for flocculation or precipitation
    • 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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH

Definitions

  • the present invention relates to a method for dephosphorizing wastewater, and more particularly, to a method for dephosphorizing wastewater in which sedimentation and separation of hydroxyapatite from a phosphoric acid-containing wastewater without using a flocculant.
  • Patent Document 1 discloses that after contacting water containing phosphate with a crystal seed containing calcium phosphate in the presence of calcium ions, A method for treating phosphate-containing water in contact with activated alumina is disclosed.
  • Patent Document 2 discloses a method of removing organic solid wastewater in a biological treatment step, and then removing a particulate solid phosphorus containing calcium phosphate. A method for contact treatment is disclosed.
  • Japanese Patent Application Laid-Open No. 62-382921 of Patent Document 3 discloses that in removing a phosphorus compound contained in wastewater, a cement pretreated with ion phosphate as a dephosphorizing crystallization material is disclosed.
  • a dephosphorization treatment method using is disclosed. Any of these methods is a dephosphorization treatment method by a crystallization separation method by contact.
  • wastewater from chemical plants that produce or use yellow phosphorus, phosphoric acid, phosphates, and phosphorus compounds, and wastewater from electroless plating plants that use hypophosphorous acid as a reducing agent are, for example, oxidized.
  • the wastewater containing orthophosphate ions will be treated.
  • the concentration of phosphoric acid in the water to be treated is as high as 300 to 30,000 ppm.
  • JP-A-56-33082 (Claims 1 to 3)
  • Patent Document 3 Patent Document 3
  • Patent Document 4 Patent Document 4
  • JP-A-2001-70951 of Patent Document 4 discloses that a calcium compound and sludge are mixed in a sludge preparation tank, for example, for 5 days or more, particularly for 7 to 50 days. After a long residence time as described above, the mixture is mixed with phosphorus-containing water in a reaction tank consisting of one tank to obtain a calcium salt of phosphorus, and a coagulant such as polyacrylamide is added to perform coagulation sedimentation treatment.
  • a method has been developed for treating phosphorus-containing water that is returned after a part of the sludge obtained by solid-liquid separation is adjusted to pH 7 to 12.
  • the use of a flocculant increases the processing cost, and also has a problem that sludge excellent in filterability cannot be obtained.
  • an object of the present invention is to remove phosphoric acid in wastewater without using a flocculant and to produce a hydroxyapatite having excellent filterability and dewaterability from wastewater containing phosphoric acid.
  • An object of the present invention is to provide a dephosphorization method. Disclosure of the invention
  • the present invention uses a treatment apparatus arranged in series in the order of a first crystallization tank, a second crystallization tank, and a sedimentation tank, and uses a treatment apparatus for crystallizing and separating a hydroxy oxyaluminate from a phosphoric acid-containing wastewater.
  • the pH of the phosphoric acid-containing wastewater, calcium chloride, and the returned hydroxyapatite slurry returned from the settling tank are adjusted with a pH adjusting agent.
  • the slurry obtained in the first crystallization step and the slurry obtained in the first crystallization step are flowed into the second crystallization tank, and calcium chloride and a pH adjuster are added to the first crystallization tank. Further reaction crystallization was carried out at a pH higher than PT / JP2004 / 001417
  • the slurry obtained in the second crystallization step is flowed into a settling tank, sedimentation and separation are performed, the supernatant liquid is treated as treated water, and discharged out of the system. It is intended to provide a method for dephosphorizing waste water, which is characterized by using the returned hydroxyapatite slurry.
  • FIG. 1 is an example of a treatment apparatus used in the method for dephosphorizing waste water of the present invention
  • FIG. 2 is a graph showing a dissolution curve of hydroxyapatite.
  • the method for dephosphorizing wastewater according to the present invention comprises a first crystallization step, a second crystallization step, a second crystallization step, and a treatment apparatus arranged in series in the order of a first crystallization tank, a second crystallization tank, and a sedimentation tank. Sedimentation is performed sequentially, and hydroxyapatite is separated by crystallization from the wastewater containing phosphoric acid to be treated.
  • the phosphoric acid-containing wastewater is not particularly limited, and includes, for example, wastewater containing phosphoric acid from several ppm to several weight%, and among them, the phosphoric acid concentration is particularly preferably 100 ppm to 100,000. Suitable for dephosphorization of wastewater containing high concentration of 0 ppm. Specifically, wastewater from a phosphoric acid production plant, a fertilizer plant, a metal surface treatment plant, an electroless plating plant, or a semiconductor component production process, general household wastewater, and sewage treatment wastewater.
  • the calcium chloride is not particularly limited, and industrially available calcium chloride may be used.
  • Returned HAP slurry refers to HAP slurry concentrated in the sedimentation tank, and the amount supplied per unit time to the first crystallization tank is supplied to the first crystallization tank.
  • the amount of phosphoric acid-containing wastewater supplied per unit time is 100 parts by volume or more, preferably 50 parts by volume or more, and more preferably 100 parts by volume or more.
  • the supply amount per unit time converted to the solid content of the returned HAP slurry supplied to the first crystallization tank was calculated by converting the phosphoric acid contained in the phosphoric acid-containing wastewater supplied to the first crystallization tank to HAP.
  • the amount is 2500 parts by weight or more, preferably 4000 parts by weight or more, per 100 parts by weight of the supply amount per unit time.
  • the HAP produced in the first crystallization tank is brought into contact with a large amount of HAP seed crystals that are 25 times or more the weight of HAP to precipitate HAP crystals on the HAP particles, and the increased HAP is used in the equipment. By circulating 25 times or more through the inside, HAP with a large particle size of Stokes diameter of 10 zm or more and excellent sedimentation and filtration properties can be obtained.
  • the concentration of the solid content of the returned HAP slurry is preferably always 2% by weight or more. If the concentration is less than 2% by weight, the amount of seed crystals is too small and HAP is not crystallized on the seed crystals of the returned HAP slurry.
  • the supply amount of calcium chloride supplied to the first crystallization tank per unit time is determined by converting the phosphoric acid in the phosphoric acid-containing wastewater supplied to the first crystallization tank to HAP. It is to be less than the theoretical equivalent.
  • the reason for keeping the stoichiometric equivalent or less is that in the first crystallization tank, the reaction crystallization is performed in a state where the phosphate ion concentration is high, so the calcium ion, which is the other substance in the reaction, is reduced to reduce the HAP. This is because the solubility increases and the degree of supersaturation can be reduced, and the generation of primary nuclei, which are fine crystals, can be suppressed.
  • the pH in the first crystallization tank is adjusted to 5.5 to 8.0, preferably to 6.5 to 7.5.
  • the pH adjustment in this case is different from that of pure water, and is between the first and second neutralization points containing phosphate ions. Therefore, pH can be adjusted relatively easily. If the pH is adjusted to 5.5 to 8.0 in the first crystallization tank, the solubility of HAP in the first crystallization tank increases and the supersaturation decreases, so the primary nucleus Generation is suppressed. If the pH is less than 5.5, the crystallized HAP is easily dissolved, which is not preferable.
  • Examples of the pH adjusting agent used in the first crystallization tank include a basic solution such as sodium hydroxide and a hydrolyzate, and an acidic solution such as hydrochloric acid and nitric acid.
  • a basic solution such as sodium hydroxide and a hydrolyzate
  • an acidic solution such as hydrochloric acid and nitric acid.
  • Sodium hydroxide is preferable as the basic solution
  • hydrochloric acid is preferable as the acidic solution.
  • calcium hydroxide which is a basic solution, is inexpensive, it affects calcium ion concentration as well as pH adjustment. Therefore, when used, it is preferable to use it in combination with sodium hydroxide.
  • the pH adjuster used in the first crystallization tank is a basic solution
  • the basic solution is preferably mixed with the returned hydroxyapatite slurry and then supplied to the first crystallization tank.
  • the returned HAP slurry has the lowest phosphate ion concentration in the apparatus and is highly alkaline and is optimal as a diluent for basic solutions. This is because the water is supplied to the first crystallization tank, and the pH is not too high locally in the first crystallization tank, and it is difficult to generate fine HAP.
  • the acidic solution is preferably mixed with the phosphoric acid-containing wastewater and then supplied to the first crystallization tank.
  • the acidic solution which is a pH adjuster
  • the acidic solution is diluted, increased, and dispersed in a large amount of wastewater containing phosphoric acid before it is supplied to the first crystallization tank. This is because the pH does not locally decrease and HAP does not dissolve.
  • the phosphoric acid-containing wastewater mixed with the acidic solution no change such as precipitation of crystals was observed.
  • the location where calcium chloride is added in the first crystallization tank is not particularly limited. JP2004 / 001417
  • the mixed solution with the phosphoric acid-containing wastewater it is preferable to supply the mixed solution with the phosphoric acid-containing wastewater to the first crystallization tank.
  • the reason for this is diluted, ⁇ amount of calcium chloride, when dispersed in advance phosphoric acid-containing waste water, there can be the C a HP 0 4 ⁇ 2 H 2 0 crystals (second phosphate calcium-'dihydrate)
  • 2 mol of hydrochloric acid is generated at the same time, it is better to handle it in the same way as the above-mentioned acidic solution.Also, it is possible to avoid a local high concentration of calcium ion in the first crystallization tank, This is because the generation of an HAP crystal can be suppressed.
  • the HAP slurry obtained in the first crystallization tank is flowed into the second crystallization tank, calcium chloride is added, and the pH is at least higher than the pH of the first crystallization tank, and p H 11 or less, preferably 8.7 or less further causes reaction crystallization. That is, in the second crystallization tank, the concentration of phosphoric acid in the treated water is reduced as much as possible by controlling the region to a high pH region and a high calcium ion concentration region. If the pH exceeds 11 in the second crystallization tank, calcium carbonate and calcium hydroxide are generated, which results in increased consumption of calcium chloride, which is not preferable.
  • Examples of the pH adjusting agent used to keep the pH in the second crystallization tank within the above range include those similar to those used in the first crystallization tank.
  • sodium hydroxide is preferable as the pH adjuster for changing the liquidity to the basic side.
  • the amount of calcium chloride supplied to the second crystallization tank per unit time is the amount required to convert the equivalent of calcium chloride used in the first crystallization tank and the phosphoric acid in the phosphoric acid-containing wastewater into apatite.
  • the excess is at least 10% by weight or more, preferably 20% by weight or more based on the theoretical equivalent. If the added amount of calcium chloride is insufficient, the unreacted phosphoric acid corresponding to the insufficient amount will flow out.
  • the slurry obtained in the second crystallization tank is flowed into the sedimentation tank, sedimentation and separation are performed, the supernatant liquid is treated water, discharged out of the system, and concentrated.
  • the specific amount of the returned HAP slurry is appropriately selected depending on the pH and average reaction time in the first crystallization tank, the concentration of the returned HAP slurry, the particle size of the HAP, and the like, within a range where the treated water does not become cloudy.
  • the supply amount of the returned HAP slurry to be supplied to the first crystallization tank per unit time is as described above, but preferably the phosphorus supplied to the first crystallization tank is not limited.
  • the amount is 50 to 400 parts by volume, preferably 100 to 200 parts by volume, per 100 parts by volume of supply of acid-containing wastewater per unit time.
  • the returned HAP slurry does not sufficiently act as seed crystals in the first crystallized layer, and fine HAP crystals are generated other than the seed crystals to cause sedimentation and separation. Difficult and undesired because the treated water is easily clouded. Also, if the returned amount exceeds 400 parts by volume, the surface area of the HAP seed crystal increases, but the concentration of phosphoric acid in the first crystallization tank becomes too low due to excessive dilution, and the crystallization rate of HAP decreases. However, the average reaction time is shortened and the concentration of phosphoric acid in the treated water is increased, so it seems that there is an appropriate range.
  • one or more crystallization tanks can be further provided between the first crystallization tank and the sedimentation tank, and the pH in the crystallization tank is the pH in the second crystallization tank. It is preferably higher or the same as it goes downstream, and it is preferably within the range of PH 11 or less.
  • the crystallization action in the method for dephosphorizing waste water of the present invention is to control so as not to generate fine HAP having poor sedimentation such as a Stokes diameter of 1 zm or less in the first crystallization tank.
  • HAP is deposited on the surface of the returned HAP particles, and the HAP particles are grown.
  • the Stokes diameter here is the equivalent diameter of a particle obtained by assuming that the particle is spherical based on the measured sedimentation velocity according to Stokes' law of resistance.
  • the sedimentation velocity is 3.2 mm / h at l ⁇ m and 3201 at 10 ⁇ 111] [1111 / h.
  • HAP seed crystals which are more than 25 times as large as HAP produced per unit time under the control of pH and calcium, and HAP particles are generated.
  • HAP deposited on the top and slightly increased in particle size makes it possible to obtain HAP with a large particle size of 10 m or more and good sedimentation and filtration properties by circulating in the tank. .
  • FIG. 2 shows the vertical axis phosphoric acid concentration (phosphorus content), and the horizontal axis: shows the dissolution curve of Hydro O carboxymethyl ⁇ Pas tie bets in the case of the pH [Ca 5 (OH) ( P 0 4) 3] .
  • A is the dissolution curve of HAP at the calcium ion concentration Omg / l in the aqueous solution
  • B is the dissolution curve of HAP at 4 Omg / l
  • C is the dissolution curve of HAP at 10 Omg / l. It is a curve. That is, FIG. 2 shows the relationship between the phosphate concentration, calcium ion concentration and pH in the production and dissolution of HAP.
  • a crystallization treatment that does not produce finer crystals is performed (approximately X region in FIG. 2). Then, in the crystallization treatment after the second crystallization tank, a high pH region and a high calcium ion concentration region are selected ( (Approximately Y region in Fig. 2) This is to reduce the concentration of phosphoric acid in the treated water sufficiently. It should be noted that the X region and the Y region in FIG. 2 are merely described for convenience of explanation, and are not strict or limit the present invention.
  • FIG. 10 An example of a processing apparatus for performing the wastewater dephosphorization method of the present invention is shown by a flow sheet in FIG.
  • the processing apparatus 10 is arranged in series in the order of a first crystallization tank 1, a second crystallization tank 2, and a settling tank 3.
  • the tandem arrangement means that the phosphoric acid-containing wastewater is treated in the order of the first crystallization tank, the second crystallization tank, and the sedimentation tank, and specifically, treated in the first crystallization tank. It means that the treatment liquid treated in the second crystallization tank is supplied to the settling tank while the treatment liquid is supplied to the second crystallization tank.
  • FIG. 10 An example of a processing apparatus for performing the wastewater dephosphorization method of the present invention is shown by a flow sheet in FIG.
  • the processing apparatus 10 is arranged in series in the order of a first crystallization tank 1, a second crystallization tank 2, and a settling tank 3.
  • the tandem arrangement means that the phosphoric acid-containing wastewater is treated in the order of the
  • the pipe for supplying the processing solution treated in the first crystallization tank 1 to the second crystallization tank 2 is denoted by 21 as a first overflow pipe
  • the second crystallization tank 2 A pipe for supplying the processing solution treated in the above only to the settling tank 3 is denoted by 31 as a second overflow pipe.
  • the first crystallization tank and the second crystallization tank are preferably complete mixing tanks that can stir the liquid in the entire tank up and down so that the crystallization reaction can proceed relatively smoothly.
  • a return pipe 14 connected to the first crystallization tank 1 is provided below the settling tank 3, and a slurry pump 16 is provided in the set pipe 14. The lowered HAP slurry is supplied to the first crystallization tank 1 by a slurry pump 16.
  • the slurry is extracted into the slurry tank, and the HAP cake is taken out once a day or three days by a fill and press machine.
  • the first crystallizer 1 and the second crystallization vessel 2 has a diameter 2 4 0 0 thigh, height 4 2 0 0 mm, an effective volume 1 6 m 3, and diameter under water at the center of the vessel
  • a complete mixing tank capable of vertically flowing the liquid or slurry was used.
  • raw water of phosphoric acid-containing wastewater discharged from a plurality of facilities was introduced into raw water tank 4 via pipe 41, and mixed in raw water tank 4 to make the concentration uniform.
  • the wastewater containing phosphoric acid in the raw water tank 4 had the composition shown in Table 1.
  • the calcium chloride slurry in the calcium chloride storage tank 8 and the sodium hydroxide aqueous solution in the sodium hydroxide storage tank 7 were prepared to have the compositions shown in Table 1, respectively. The operation in this example was performed in a steady state.
  • the phosphoric acid-containing wastewater was supplied from the raw water tank 4 to the liquid surface of the first crystallization tank 1 via the pipe 11 using the pump 15 under the conditions shown in Table 2 “Phosphoric acid-containing wastewater”.
  • the pipe 12 connected to the calcium chloride storage tank 8 was connected just before the pipe 11 to the first crystallization tank, and the phosphoric acid-containing wastewater and the chloride slurry were mixed before the first crystallization tank was mixed.
  • the calcium chloride slurry was supplied using a pump 24 under the conditions shown in Table 2 “Calcium chloride solution”.
  • the returned HAP slurry was supplied onto the liquid surface of the first crystallization tank 1 via the pump 16 and the return pipe 14 under the conditions shown in Table 2.
  • sodium hydroxide solution It was supplied appropriately from the storage tank 7 and adjusted so that the pH in the first crystallization tank 1 became the value shown in Table 2.
  • the pipe 22 leading to the sodium hydroxide storage tank 7 was connected to the return pipe 14 so as to join immediately before the first crystallization tank, and the aqueous sodium hydroxide solution and the returned HAP slurry were mixed. After that, it was supplied to the first crystallization tank.
  • the average residence time in the first crystallization tank 1 was about 1.1 hours.
  • the obtained slurry in the first crystallization tank was continuously transferred to the second crystallization tank via the first overflow pipe 21.
  • HAP was crystallized under the conditions shown in Table 3.
  • the sodium hydroxide and calcium chloride solutions of the pH adjusters were each diluted with 100 L / h of water, increased in volume, and dispersed and supplied.
  • the slurry of the second crystallization tank treated in the second crystallization tank was continuously transferred to the settling tank via the second overflow pipe 31.
  • HAP was settled under the conditions shown in Table 4. After the sedimentation treatment, the obtained supernatant was continuously discharged through the third overflow pipe 32 and used as treated water. Table 5 shows the composition of the treated water.
  • the HAP slurry settled in the lower part of the settling tank 3 is returned to the first crystallization tank 1 through the return pipe 14 via the pump 16 via the pump 16 to form a returned HAP slurry.
  • the slurry was transferred from the receiving tank 5 to the filter press 6 via the pump 17 and separated into cake and filtered water. Since the cake did not contain a coagulant and did not stick, it could be easily separated and separated from the film, and the cake after separation could be easily dried.
  • Treated water Table 5 shows the amount of phosphoric acid and the dephosphorization rate.
  • phosphoric acid in wastewater can be removed without using a coagulant.
  • the cake obtained by pressing the filter after settling and separation does not contain coagulant and does not stick, so it can be easily separated from the filter and separated, and the cake after separation can be easily dried. Cost can be reduced.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

Cette invention se rapporte à un procédé d'élimination du phosphore d'eaux usées, qui comprend une première étape de cristallisation consistant à mettre en réaction, dans une premier récipient de cristallisation, une eau usée contenant du phosphore, du chlorure de calcium et une boue d'hydroxyapatite recyclée, provenant d'une cuve de précipitation, et à cristalliser ce mélange, tout en réglant son pH au moyen d'un agent de réglage du pH, une seconde étape de cristallisation consistant à introduire la boue formée dans la première étape de cristallisation dans un second récipient de cristallisation, à ajouter du chlorure de calcium à cette boue, pour entraîner une réaction ultérieure et une cristallisation à un pH supérieur à celui présent dans le premier récipient de cristallisation, à un niveau égal ou inférieur à 11, et une étape consistant à introduire la boue formée dans la seconde étape de cristallisation dans une cuve de précipitation, à effectuer une précipitation et une séparation, à décharger le surnageant qui en résulte à l'extérieur du système sous la forme d'une eau traitée, et à recycler la majeure partie de la boue concentrée qui en résulte sous la forme de boue d'hydroxyapatite mentionnée ci-dessus. Ce procédé permet d'éliminer le phosphore contenu dans une eau usée, sans qu'il soit nécessaire d'utiliser un coagulant, et également de former une hydroxyapatite ayant d'excellentes caractéristiques de filtrage et de déshydratation à partir d'une eau usée contenant du phosphore.
PCT/JP2004/001417 2003-02-12 2004-02-10 Procede pour eliminer le phosphore d'eaux usees WO2004071970A1 (fr)

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JP2003-033510 2003-02-12
JP2003033510A JP3977757B2 (ja) 2003-02-12 2003-02-12 排水の脱リン方法

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JP4600865B2 (ja) * 2005-03-31 2010-12-22 株式会社日立プラントテクノロジー リン含有水の晶析処理方法
JP2009226250A (ja) 2008-03-19 2009-10-08 Toshiba Corp リン回収方法及びリン回収システム
JP5058129B2 (ja) * 2008-11-06 2012-10-24 オルガノ株式会社 晶析反応方法
KR101309565B1 (ko) * 2010-12-08 2013-09-17 서울시립대학교 산학협력단 Ｐ-ｃ ｓｗｒｏ 시스템에서 발생한 결정을 이용한 하수내 인 제거방법
CN102826640A (zh) * 2011-06-17 2012-12-19 中国石油化工股份有限公司 一种处理有机磷生产废水的方法
CN103521155B (zh) * 2013-10-08 2014-12-31 中国农业大学 一种畜禽废水磷素结晶成肥反应器及其应用
CN105016523B (zh) * 2015-07-06 2017-07-28 重庆泰克环保科技股份有限公司 一种含磷废水处理净化系统
KR102114634B1 (ko) * 2020-03-03 2020-05-25 주식회사 지이테크 선택성 흡착모듈을 이용한 하수의 인 처리 및 회수 공정

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JPH02164493A (ja) * 1988-12-19 1990-06-25 Osaka Gas Co Ltd 排水の脱リン方法
JPH04150996A (ja) * 1990-10-12 1992-05-25 Agency Of Ind Science & Technol リン酸イオン含有排水の処理方法
JP2001129560A (ja) * 1999-11-02 2001-05-15 Kurita Water Ind Ltd リン含有水の処理方法及び装置
JP2002348106A (ja) * 2001-05-29 2002-12-04 Kiyoshi Suzuki リン回収方法及び装置

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105540770A (zh) * 2015-12-19 2016-05-04 湖南科技大学 一种磁诱导结晶去除及回收污水中磷的方法及装置
CN105540770B (zh) * 2015-12-19 2018-06-29 湖南科技大学 一种磁诱导结晶去除及回收污水中磷的方法及装置

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JP3977757B2 (ja) 2007-09-19
JP2004261640A (ja) 2004-09-24

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