WO2016063581A1 - Procédé de traitement et appareil de traitement pour eaux usées contenant de l'ammoniac - Google Patents

Procédé de traitement et appareil de traitement pour eaux usées contenant de l'ammoniac Download PDF

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Publication number
WO2016063581A1
WO2016063581A1 PCT/JP2015/069438 JP2015069438W WO2016063581A1 WO 2016063581 A1 WO2016063581 A1 WO 2016063581A1 JP 2015069438 W JP2015069438 W JP 2015069438W WO 2016063581 A1 WO2016063581 A1 WO 2016063581A1
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Prior art keywords
ammonia
containing wastewater
separation membrane
gas
liquid separation
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PCT/JP2015/069438
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English (en)
Japanese (ja)
Inventor
江口　正浩
敬介 村上
彰 恵良
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オルガノ株式会社
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Publication of WO2016063581A1 publication Critical patent/WO2016063581A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/24—Dialysis ; Membrane extraction
    • B01D61/30—Accessories; Auxiliary operation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/24—Dialysis ; Membrane extraction
    • B01D61/32—Controlling or regulating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • B01D65/06—Membrane cleaning or sterilisation ; Membrane regeneration with special washing compositions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/24—Sulfates of ammonium
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis

Definitions

  • the present invention relates to an ammonia-containing wastewater treatment method and treatment apparatus for treating ammonia-containing wastewater discharged from an electronics industry factory, chemical factory, etc. and recovering it as ammonium sulfate.
  • a relatively high concentration of ammonia-containing wastewater discharged from an electronic industry factory such as a semiconductor factory, a chemical factory, a thermal power plant, etc. is, for example, an ammonia stripping method (see, for example, Patent Document 1), an evaporation concentration method (for example, it is processed by a catalyst wet oxidation method (for example, see Patent Document 3) or the like.
  • the ammonia containing waste water of comparatively low concentration is processed by the biological treatment method etc., for example.
  • Ammonia stripping method is a treatment method in which ammonia in wastewater is moved to the gas side by adding an alkaline solution to ammonia-containing wastewater, heating it, passing it through a diffusion tower filled with packing, and bringing it into contact with steam and air. It is. Although this method is a comparatively simple process, there exists a subject that the installation of a stripping tower is large. In addition, it is necessary to treat the ammonia that has moved to the gas side using heat energy such as warming and steam, by catalytic oxidation at a higher temperature, resulting in a problem of high processing costs. Further, NO x , N 2 O, etc. may be generated during catalytic oxidation.
  • the evaporative concentration method is a treatment method in which ammonia-containing wastewater is heated and evaporated, and the generated ammonia-containing vapor is condensed and recovered as ammonia water.
  • This method has problems such as heating energy cost for evaporation and scale adhesion on the heat transfer surface of the evaporator.
  • the catalytic wet oxidation method is a method of treating ammonia-containing wastewater by applying a temperature and pressure of 100 to 370 ° C. in the presence of a catalyst. This method has problems in safety and cost due to high temperature and high pressure processing.
  • the ammonia-containing wastewater is economically treated with a simple facility and can be reused through the ammonium sulfate solution.
  • the magnesium compound contained in the ammonia-containing wastewater As a result of the occurrence of a scale due to the above, etc., the gas-liquid separation membrane is clogged, and the ammonia removal rate decreases with the lapse of processing time.
  • Japanese Patent No. 39987896 JP 2011-153043 A Japanese Patent No. 3272859 Japanese Patent No. 3240694 JP 2013-202475 A
  • An object of the present invention is to suppress a decrease in the ammonia removal rate that occurs with the lapse of treatment time in the treatment of ammonia-containing wastewater using a gas-liquid separation membrane.
  • the present invention removes ammonia from ammonia-containing wastewater using a gas-liquid separation membrane in a state where the concentration of magnesium ions in the ammonia-containing wastewater is less than the value obtained by the following formula (1). It is the processing method of the wastewater containing ammonia including the ammonia removal process which makes a sulfuric acid solution contact and collect
  • Magnesium ion concentration (unit: mg / L) 4.69 ⁇ 10 21 ⁇ (2 ⁇ pH) (1) (In formula (1), pH is the pH of the ammonia-containing wastewater to be treated in the ammonia removal step.)
  • the pH of the ammonia-containing wastewater to be treated is preferably 11 or more.
  • a softening treatment step for softening the ammonia-containing wastewater is included before the ammonia removing step.
  • the gas-liquid separation membrane is preferably subjected to acid cleaning at a predetermined time.
  • the ammonia-containing wastewater is caused to flow in a first liquid chamber provided adjacent to one surface of the gas-liquid separation membrane, and adjacent to the other surface of the gas-liquid separation membrane.
  • the sulfuric acid solution is preferably caused to flow in a counter flow with the ammonia-containing wastewater in a second liquid chamber provided.
  • the present invention removes ammonia from the ammonia-containing wastewater using a gas-liquid separation membrane in a state where the concentration of magnesium ions in the ammonia-containing wastewater is less than the value obtained by the following formula (1).
  • An ammonia-containing wastewater treatment apparatus comprising ammonia removal means for bringing a sulfuric acid solution into contact with ammonia and recovering it as ammonium sulfate.
  • Magnesium ion concentration (unit: mg / L) 4.69 ⁇ 10 21 ⁇ (2 ⁇ pH) (1)
  • pH is the pH of the ammonia-containing waste water to be treated in the ammonia removing means.
  • the pH of the ammonia-containing wastewater to be treated is preferably 11 or more.
  • a softening treatment means for softening the ammonia-containing wastewater is provided before the ammonia removal means.
  • the ammonia-containing wastewater treatment apparatus preferably includes an acid cleaning means for performing acid cleaning of the gas-liquid separation membrane at a predetermined time.
  • the ammonia removing means is adjacent to the first liquid chamber provided adjacent to one surface of the gas-liquid separation membrane and the other surface of the gas-liquid separation membrane.
  • a second liquid chamber provided, the ammonia-containing wastewater is allowed to flow through the first liquid chamber, and the sulfuric acid solution is allowed to flow through the second liquid chamber in a counterflow with the ammonia-containing wastewater. preferable.
  • FIG. 1 It is a schematic block diagram which shows an example of the processing apparatus of the ammonia containing waste_water
  • the ammonia-containing wastewater treatment apparatus 1 includes an ammonia removal device 16 as an ammonia removal unit and a circulation tank 18.
  • the ammonia-containing wastewater treatment apparatus 1 includes a raw water tank 10, a softening device 12 as a softening treatment means, a pH adjustment tank 14, a sulfuric acid storage tank 20, a pH adjusting agent storage tank 22, and an acid storage tank 24 as an acid cleaning means. May be provided.
  • the ammonia removing device 16 has a gas-liquid separation membrane 26, and a first liquid chamber 25a and a second liquid chamber 25b partitioned by the gas-liquid separation membrane 26.
  • the gas-liquid separation membrane 26 is a membrane such as a hollow fiber membrane that does not pass liquid but passes gaseous ammonia.
  • the first liquid chamber 25 a is provided adjacent to one surface of the gas-liquid separation membrane 26, and the second liquid chamber 25 b is provided adjacent to the other surface of the gas-liquid separation membrane 26.
  • Ammonia-containing wastewater is supplied to the first liquid chamber 25a, and a sulfuric acid solution is supplied to the second liquid chamber 25b.
  • the softening device 12 replaces cations such as calcium ions and magnesium ions contained in water with sodium ions with an ion exchange resin such as a cation exchange resin.
  • the raw water pipe 30 is connected to the inlet of the raw water tank 10.
  • the outlet of the raw water tank 10 and the inlet of the softening apparatus 12 are connected by a raw water supply pipe 32, and the outlet of the softening apparatus 12 and the inlet of the pH adjustment tank 14 are connected by a softened water pipe 34.
  • the outlet of the pH adjusting tank 14 and the inlet of the first liquid chamber 25 a provided at one end of the ammonia removing device 16 are connected by a pH adjusting water pipe 36, and the first provided at the other end of the ammonia removing device 16.
  • a treated water pipe 38 is connected to the outlet of one liquid chamber 25a.
  • the outlet of the circulation tank 18 and the inlet of the second liquid chamber 25 b provided on the other end side of the ammonia removing device 16 are connected by a circulation pipe 40, and the second liquid provided on one end side of the ammonia removing device 16.
  • the outlet of the chamber 25 b and the inlet of the circulation tank 18 are connected by a circulation pipe 42.
  • a recovered ammonium sulfate solution pipe 50 is connected to the recovery outlet of the circulation tank 18.
  • the outlet of the sulfuric acid storage tank 20 is connected to the circulation tank 18 by a sulfuric acid pipe 44.
  • the outlet of the pH adjusting agent storage tank 22 is connected to the pH adjusting tank 14 by a pH adjusting agent pipe 46.
  • the outlet of the acid storage tank 24 is connected to the pH adjustment water pipe 36 by an acid pipe 48.
  • Raw ammonia-containing wastewater is stored in the raw water tank 10 as needed through the raw water pipe 30 and then sent to the softening device 12 as needed through the raw water supply pipe 32.
  • the softening device 12 contains the ammonia Magnesium ions in the waste water are removed (softening treatment step), and the value is less than the value obtained by the following formula (1).
  • the softening treatment process may not be performed.
  • Magnesium ion concentration (unit: mg / L) 4.69 ⁇ 10 21 ⁇ (2 ⁇ pH) (1) (In formula (1), pH is the pH of the ammonia-containing wastewater to be treated in the ammonia removal step.)
  • the softened water that has been softened as necessary is sent to the pH adjusting tank 14 through the softened water pipe 34 as necessary.
  • the pH adjusting agent is supplied from the pH adjusting agent storage tank 22 through the pH adjusting agent piping 46 as necessary, and the pH of the softened water is adjusted to a predetermined value (pH adjusting step).
  • the pH adjusting agent used in the pH adjusting step is, for example, an alkali such as a sodium hydroxide solution or an acid such as hydrochloric acid.
  • the softened water is preferably adjusted to pH 11 or higher in order to dissociate ammonium ions in the ammonia-containing wastewater into ammonia gas and increase the ammonia removal rate in the ammonia removal step described below. Further, considering the influence on the membrane, piping material, etc., it is more preferable to adjust the pH within the range of 11-12. If the pH of the softened water is a predetermined value, the pH adjustment step may not be performed.
  • the pH-adjusted water whose pH has been adjusted as necessary is fed to the first liquid chamber 25a through the pH-adjusted water pipe 36 from an inlet provided on one end side of the ammonia removing device 16.
  • ammonia is removed from the ammonia-containing wastewater by using a gas-liquid separation membrane 26 that allows ammonia to pass through without passing through a liquid.
  • the treated water from which ammonia has been removed is discharged through the treated water pipe 38 from the outlet of the first liquid chamber 25 a provided on the other end side of the ammonia removing device 16.
  • the sulfuric acid solution stored in the circulation tank 18 from the sulfuric acid storage tank 20 through the sulfuric acid pipe 44 is supplied to the second liquid chamber 25b from the inlet provided on the other end side of the ammonia removing device 16 through the circulation pipe 40.
  • the ammonia-containing waste water in the liquid chamber 25a may be allowed to flow outside the hollow fiber membrane (first liquid chamber 25a), and a sulfuric acid solution may be allowed to flow inside the hollow fiber membrane (second liquid chamber 25b).
  • the ammonia that has passed through the gas-liquid separation membrane 26 comes into contact with the sulfuric acid solution flowing through the second liquid chamber 25b of the ammonia removing device 16 to produce ammonium sulfate (the ammonia removing step).
  • the produced ammonium sulfate is sent to the circulation tank 18 through the circulation pipe 42 from the outlet of the second liquid chamber 25b provided on one end side of the ammonia removing device 16 while being dissolved in the sulfuric acid solution.
  • the sulfuric acid solution is circulated through the circulation tank 18, the circulation pipe 40, and the circulation pipe 42 until the ammonium sulfate has a predetermined concentration.
  • the sulfuric acid solution is supplied from the sulfuric acid storage tank 20 through the sulfuric acid pipe 44 to the circulation tank 18, and the pH of the circulated sulfuric acid solution is adjusted to a predetermined value.
  • the recovered ammonium sulfate solution is discharged from the circulation tank 18 through the recovered ammonium sulfate solution pipe 50.
  • the magnesium ion concentration (unit: mg / L) of the ammonia-containing wastewater to be treated is obtained from the above formula (1) with respect to pH.
  • the magnesium ion concentration (unit: mg / L) of the ammonia-containing wastewater to be treated is obtained from the above formula (1) with respect to pH.
  • the pH of the ammonia-containing wastewater to be treated is preferably 11 or more from the viewpoint of the ammonia removal rate.
  • the magnesium ion concentration of the ammonia-containing wastewater to be treated is less than 0.469 mg / L determined by the above formula (1).
  • the ammonia-containing wastewater to be treated is, for example, ammonia-containing wastewater discharged from an electronic industry factory such as a semiconductor factory, a chemical factory, or a thermal power plant.
  • ammonia-containing wastewater contains an oxidant such as hydrogen peroxide, such as ammonia-containing wastewater discharged from an electronic industry factory such as a semiconductor factory
  • an oxidant removal treatment such as activated carbon treatment is performed before the ammonia removal device 16. May remove the oxidizing agent. Thereby, the fall of the ammonia removal rate in the ammonia removal process resulting from oxidizing agents, such as hydrogen peroxide, and the deterioration of a gas-liquid separation membrane can be suppressed.
  • the ammonia concentration in the ammonia-containing waste water of the raw water is not particularly limited, but in order to make the concentration of ammonium sulfate in the recovered ammonium sulfate solution 25% by mass or more and to make the ammonium sulfate hardly precipitate, 900 mg / L It is preferable to operate at 2,200 mg / L or less.
  • ammonia concentration in the ammonia-containing wastewater is low (for example, less than 900 mg / L)
  • ammonia may be concentrated by reverse osmosis membrane treatment or the like before the ammonia removal device 16.
  • concentration may be returned to the raw
  • At least one of the raw water tank 10, the raw water pipe 30 and the raw water supply pipe 32 is equipped with a heat exchangeable, heating and other equipment that can be heated, and the temperature of the raw water is heated, for example, in the range of 35 to 55 ° C. to remove ammonia.
  • the ammonia-containing wastewater may be sent to 16.
  • the temperature of the raw water is less than 35 ° C., the ammonia in the ammonia-containing wastewater becomes difficult to gasify, and the ammonia removal rate in the ammonia removal device 16 tends to decrease.
  • the treated water may be circulated to the raw water tank 10 or the like for keeping the raw water warm or adjusting the ammonia concentration.
  • Examples of the cation exchange resin used in the softening device 12 include strong acid cation exchange resin, weak acid cation exchange resin, aminophosphate chelate resin, iminodiacetic acid chelate resin, and the like. It is preferable to use at least one of aminophosphate-type chelate resin and iminodiacetic acid-type chelate resin from the selectivity of magnesium ion and calcium ion.
  • the gas-liquid separation membrane 26 is not particularly limited as long as it does not pass liquid but passes gaseous ammonia.
  • the gas-liquid separation membrane 26 include a hydrophobic porous hollow fiber membrane.
  • a hollow fiber membrane having a hollow fiber diameter of about 300 ⁇ m, a pore size of about 0.03 ⁇ m, and an (average) porosity of about 40 to 50% may be used.
  • circulation pipes 40 and 42 connected to the second liquid chamber 25b of the ammonia removing device 16 through which the sulfuric acid solution is passed have an automatic valve.
  • the sulfuric acid solution from the sulfuric acid storage tank 20 so that the pH of the sulfuric acid solution to be circulated is maintained at 2 or less. If the pH of the circulated sulfuric acid solution exceeds 2, the ammonia removal rate may be reduced.
  • the sulfuric acid solution added from the sulfuric acid storage tank 20 is preferably as high as possible. From the viewpoint of handling and the like, the sulfuric acid concentration of the sulfuric acid solution added from the sulfuric acid storage tank 20 is preferably 50% by mass or more.
  • the concentration of the recovered ammonium sulfate in the circulated sulfuric acid solution is equal to or higher than a predetermined concentration, for example, 25% by mass or higher, the recovered ammonium sulfate solution is discharged from the circulation tank 18 through the recovered ammonium sulfate solution pipe 50. .
  • the concentration of ammonium sulfate in the circulated sulfuric acid solution may be measured using, for example, an ammonium sulfate concentration measuring means such as a hydrometer or a concentration meter. Based on the measured ammonium sulfate concentration, when the ammonium sulfate concentration becomes a predetermined concentration or higher, for example, 25 mass% or higher, the ammonium sulfate may be automatically discharged from the circulation tank 18 through the recovered ammonium sulfate solution pipe 50 as a recovered ammonium sulfate solution.
  • the gas-liquid separation membrane 26 may be subjected to acid cleaning at a predetermined time. preferable. As shown in FIG. 1, for example, the acid solution is sent from the acid storage tank 24 through the acid pipe 48 and the pH adjustment water pipe 36 to the first liquid chamber 25a of the ammonia removing device 16, and the gas-liquid separation membrane 26 is washed. (Acid cleaning step).
  • an acid solution such as sulfuric acid, hydrochloric acid or citric acid can be used.
  • an acid storage tank 24 may be separately installed as shown in FIG. 1, or in the second liquid chamber 25b of the ammonia removing device 16 as in the ammonia-containing waste water treatment device 3 shown in FIG. You may install the sulfuric acid piping 52 which liquid-feeds a part of sulfuric acid solution from the sulfuric acid storage tank 20 currently sending into the 1st liquid chamber 25a.
  • the pH of the ammonia-containing wastewater is preferably 11 or more, so the magnesium ion concentration in the ammonia-containing wastewater is preferably less than 0.469 mg / L.
  • the pH of the ammonia-containing wastewater is preferably 11 or more, so the magnesium ion concentration in the ammonia-containing wastewater is preferably less than 0.328 mg / L.
  • the magnesium ion concentration (unit: mg / L) in the ammonia-containing wastewater to be treated is obtained by the above formula (1) with respect to pH. It may be less than the value.
  • the turbidity in raw water is filtered with a 0.45 ⁇ m filter, and the result of fluorescent X-ray analysis using a fluorescent X-ray analyzer (ZSX100e type, manufactured by Rigaku Corporation) is shown in FIG.
  • Example 1 ammonia treatment was carried out using a gas-liquid separation membrane with the magnesium concentration in the ammonia-containing wastewater being in a state of less than 0.3 mg / L.
  • Comparative Example 1 ammonia treatment was performed using a gas-liquid separation membrane without removing magnesium from the ammonia-containing wastewater.
  • Example 2 the gas-liquid separation membrane having a reduced ammonia removal rate after the treatment in Comparative Example 1 was subjected to immersion cleaning with 0.1% by mass of hydrochloric acid for 1 hour and then subjected to ammonia treatment again.
  • ammonia concentration before and after the treatment was measured by JIS K0102 indophenol blue absorptiometry, and the ammonia removal rate was calculated. The results are shown in Table 2.
  • the ammonia removal rate of Example 2 is a value immediately after cleaning.
  • Example 1 the ammonia removal rate was almost the same as 75% over time. In Comparative Example 1, the ammonia removal rate immediately after the start of the treatment was 75%, but the removal rate gradually decreased with time and became 66% after 14 hours. In Example 2, it was confirmed that the ammonia removal rate recovered to 75% by the acid cleaning.
  • 1,3 Ammonia-containing wastewater treatment device 10 raw water tank, 12 softening device, 14 pH adjustment tank, 16 ammonia removal device, 18 circulation tank, 20 sulfuric acid storage tank, 22 pH adjuster storage tank, 24 acid storage tank, 25a first liquid Chamber, 25b second liquid chamber, 26 gas-liquid separation membrane, 30 raw water piping, 32 raw water supply piping, 34 softened treated water piping, 36 pH adjusted water piping, 38 treated water piping, 40, 42 circulation piping, 44, 52 Sulfuric acid piping, 46 pH adjuster piping, 48 acid piping, 50 recovered ammonium sulfate solution piping.

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  • Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Urology & Nephrology (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)
  • Treatment Of Water By Ion Exchange (AREA)

Abstract

　L'invention concerne un procédé de traitement et un appareil de traitement pour eaux usées contenant de l'ammoniac, la diminution du taux d'élimination de l'ammoniac à mesure que le temps de traitement s'écoule étant réduite au minimum lors du traitement d'eaux usées contenant de l'ammoniac à l'aide d'une membrane de séparation vapeur-liquide. Ce procédé de traitement des eaux usées contenant de l'ammoniac comprend une étape d'élimination de l'ammoniac dans laquelle, dans des conditions dans lesquelles la concentration en ions magnésium dans les eaux usées contenant de l'ammoniac est inférieure à une valeur calculée à partir de l'équation (1) et, à l'aide d'un appareil 16 d'élimination de l'ammoniac équipé d'une membrane 26 de séparation vapeur-liquide, l'ammoniac est éliminé des eaux usées contenant de l'ammoniac, et une solution d'acide sulfurique est mise en contact avec l'ammoniac éliminé, qui est récupéré sous la forme de sulfate d'ammonium. Concentration en ions magnésium (unité : mg/L) = 4,69 × 1021 – (2 × pH) (1) (dans l'équation (1), pH représente le pH des eaux usées contenant de l'ammoniac traitées à l'étape d'élimination de l'ammoniac).
PCT/JP2015/069438 2014-10-22 2015-07-06 Procédé de traitement et appareil de traitement pour eaux usées contenant de l'ammoniac WO2016063581A1 (fr)

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JP2014215622A JP2016078014A (ja) 2014-10-22 2014-10-22 アンモニア含有排水の処理方法および処理装置
JP2014-215622 2014-10-22

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017154393A1 (fr) * 2016-03-09 2017-09-14 オルガノ株式会社 Procédé de traitement et dispositif de traitement d'eaux usées contenant de l'ammoniac
WO2017213050A1 (fr) * 2016-06-07 2017-12-14 オルガノ株式会社 Procédé et dispositif de traitement de l'eau, procédé de modification du dispositif de traitement de l'eau et kit de modification du dispositif de traitement de l'eau
GB2565749A (en) * 2017-06-13 2019-02-27 Univ Cranfield Ammonia Separation

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JPH10137540A (ja) * 1996-11-13 1998-05-26 Mitsui Mining Co Ltd 排煙脱硫装置からの排水処理方法
JPH11510432A (ja) * 1995-08-07 1999-09-14 ゼノン、エンバイロンメンタル、インコーポレーテッド 逆浸透を使用する高純度の水の製造
US20100218573A1 (en) * 2009-02-27 2010-09-02 Victor Van Slyke System and method for producing an organic based fertilizer and usable water from animal waste
JP2010227851A (ja) * 2009-03-27 2010-10-14 Metawater Co Ltd 膜ろ過システムおよびその洗浄方法
JP2010269288A (ja) * 2009-05-25 2010-12-02 Astom:Kk 有機酸の製造方法
US20120315209A1 (en) * 2011-04-20 2012-12-13 Thermoenergy Corporation Methods and systems for treating water streams
JP2013202475A (ja) * 2012-03-28 2013-10-07 Sumitomo Metal Mining Engineering Co Ltd アンモニア含有排水からのアンモニア除去方法

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JPH11510432A (ja) * 1995-08-07 1999-09-14 ゼノン、エンバイロンメンタル、インコーポレーテッド 逆浸透を使用する高純度の水の製造
JPH10137540A (ja) * 1996-11-13 1998-05-26 Mitsui Mining Co Ltd 排煙脱硫装置からの排水処理方法
US20100218573A1 (en) * 2009-02-27 2010-09-02 Victor Van Slyke System and method for producing an organic based fertilizer and usable water from animal waste
JP2010227851A (ja) * 2009-03-27 2010-10-14 Metawater Co Ltd 膜ろ過システムおよびその洗浄方法
JP2010269288A (ja) * 2009-05-25 2010-12-02 Astom:Kk 有機酸の製造方法
US20120315209A1 (en) * 2011-04-20 2012-12-13 Thermoenergy Corporation Methods and systems for treating water streams
JP2013202475A (ja) * 2012-03-28 2013-10-07 Sumitomo Metal Mining Engineering Co Ltd アンモニア含有排水からのアンモニア除去方法

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017154393A1 (fr) * 2016-03-09 2017-09-14 オルガノ株式会社 Procédé de traitement et dispositif de traitement d'eaux usées contenant de l'ammoniac
JP2017159233A (ja) * 2016-03-09 2017-09-14 オルガノ株式会社 アンモニア含有排水の処理方法および処理装置
WO2017213050A1 (fr) * 2016-06-07 2017-12-14 オルガノ株式会社 Procédé et dispositif de traitement de l'eau, procédé de modification du dispositif de traitement de l'eau et kit de modification du dispositif de traitement de l'eau
JP2017217608A (ja) * 2016-06-07 2017-12-14 オルガノ株式会社 水処理方法および装置、水処理装置の改造方法、並びに水処理装置改造用キット
GB2565749A (en) * 2017-06-13 2019-02-27 Univ Cranfield Ammonia Separation

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