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WO2003097540A1 - Appareil et procede de traitement d'eau residuaire organique permettant de recuperer le phosphore - Google Patents

Appareil et procede de traitement d'eau residuaire organique permettant de recuperer le phosphore Download PDF

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Publication number
WO2003097540A1
WO2003097540A1 PCT/JP2003/006393 JP0306393W WO03097540A1 WO 2003097540 A1 WO2003097540 A1 WO 2003097540A1 JP 0306393 W JP0306393 W JP 0306393W WO 03097540 A1 WO03097540 A1 WO 03097540A1
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WO
WIPO (PCT)
Prior art keywords
sludge
phosphorus
biological treatment
liquid
tank
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/JP2003/006393
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English (en)
Japanese (ja)
Inventor
Takuya Kobayashi
Shigeki Yamashita
Kazuaki Shimamura
Toshihiro Tanaka
Norio Yamada
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ebara Corp
Original Assignee
Ebara Corp
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 Ebara Corp filed Critical Ebara Corp
Priority to JP2004505276A priority Critical patent/JPWO2003097540A1/ja
Publication of WO2003097540A1 publication Critical patent/WO2003097540A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1221—Particular type of activated sludge processes comprising treatment of the recirculated sludge
    • 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
    • C02F1/34—Treatment of water, waste water, or sewage with mechanical oscillations
    • C02F1/36—Treatment of water, waste water, or sewage with mechanical oscillations ultrasonic vibrations
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present invention relates to a technique for reducing the amount of excess sludge generated in a process for biologically treating organic wastewater such as sewage and organic industrial wastewater.
  • Sewage and organic industrial wastewater are usually treated by various biological treatment methods such as aerobic biological treatment, nitrification and denitrification, and anaerobic biological treatment.
  • biological treatment of organic water is an excellent treatment method, a large amount of excess sludge is generated during the treatment process, and the amount of generated sludge is over 1,000,000 tons per year in Japan as a whole.
  • excess sludge is dewatered and then landfilled or incinerated, but its disposal costs are increasing every year, which is one of the factors that increase the overall cost of wastewater treatment. For this reason, in recent years, attention has been focused on technologies for controlling the amount of excess sludge generated.
  • the cell membrane of microorganisms in the surplus sludge is destroyed, the contents are converted into liquefied organic matter, and then the liquefied organic matter is returned to the biological treatment tank for biological treatment.
  • the present invention has been devised in order to solve the above-described problems, and provides a technology capable of reducing the amount of excess sludge discharged and simultaneously removing phosphorus in excess sludge. The purpose is to do so. Disclosure of the invention The present inventor has found the following processing method and apparatus as means for solving the above problems.
  • a method for treating excess sludge generated from an organic wastewater treatment process consisting of a biological treatment step and a solid-liquid separation step, wherein part or all of the excess sludge is concentrated to remove liquid and concentrate.
  • Sludge is generated, and the generated desorbed nights are treated as phosphorus and returned to the biological treatment process as waste gas or discharged into the biological treatment process.
  • the sludge is discharged out of the system, and the concentrated sludge generated by the concentration of excess sludge is subjected to ultrasonic treatment. And return it to the biological treatment process.
  • the phosphorus recovery treatment of the above desorption is performed by adding a flocculant to the desorbed solution to coagulate and precipitate phosphate ions to separate and remove phosphorus from the solution.
  • the phosphorus recovery process from the departure night is carried out by adding a force for adding ammonium ions and magnesium to the desorbed solution and maintaining the ⁇ 9 at 9 or more while adding phosphorus to the desorbed solution.
  • a method for treating organic water comprising subjecting the concentrated sludge generated by the method to ultrasonic treatment and returning the sludge to a biological treatment step.
  • Phosphorus recovery from tf! T self-removal is carried out by adding ammonium ion and magnesium at the desorption night or by adding calcium and maintaining the pH at 9 or more to recover phosphorus. 5. The method according to the above item 4, wherein the method is carried out by separating phosphorus from the liquid by praying. 7. An apparatus for treating excess sludge generated from a treatment process for organic '
  • Sludge concentrator to produce desorbed liquid and concentrated sludge by distillation, phosphorus recovery tank for phosphorus recovery treatment of desorbed liquid generated by sludge concentrator, ultrasonic treatment for ultrasonically treating concentrated sludge generated by sludge concentrator
  • An apparatus comprising: an apparatus, and a pipe for returning sludge treated by the ultrasonic treatment apparatus to the biological treatment step.
  • a biological treatment tank that receives the organic water and performs biological treatment, a solid-liquid separation that separates the activated sludge mixture discharged from the biological treatment tank into solid and liquid to form sedimentation sludge and treatment
  • a sludge concentrator for concentrating part or all of the settled sludge discharged from the solid-liquid separator to generate desorption night and concentrated sludge
  • a phosphorus recovery tank for performing a phosphorus recovery treatment of the desorbed liquid generated by the sludge concentrator
  • An ultrasonic treatment apparatus for ultrasonically treating the concentrated sludge generated by the sludge concentrator, and a pipe for returning the sludge treated by the ultrasonic treatment apparatus to the biological treatment tank.
  • FIG. 1 is a schematic diagram of a treatment port for subjecting excess sludge discharged from a biological treatment process of organic water to ultrasonic treatment and phosphorus recovery treatment according to the method of the present invention.
  • FIG. 2 is a flow diagram of a biological treatment system for organic wastewater, which is a combination of a sludge volume reduction treatment and a phosphorus recovery treatment according to the present invention, used in an embodiment of the present invention.
  • FIG. 3 is a graph showing the progress of the amount of sludge in the biological treatment tank in Example 1.
  • FIG. 4 is a graph showing the progress of the amount of sludge in the biological treatment tank in Example 2.
  • FIG. 5 is a flow diagram of a biological treatment system of organic wastewater combined with sludge treatment by ultrasonic treatment used in a comparative example.
  • FIG. 6 is a graph showing the progress of the amount of sludge in the biological treatment tank in the comparative example.
  • reference numerals refer to the following components. 1 Organic 'ft ⁇ 7_R; 2 Biological treatment tank; 3 Activated sludge mixture; 4 Solid-liquid separation;
  • FIG. 1 is a schematic diagram of a treatment flow according to the present invention in which an ultrasonic reaction step and a phosphorus recovery step are provided in a system for treating excess sludge discharged from a biological treatment process of organic and water.
  • the organic ', water 1 is supplied to the biological treatment tank 2, and the organic substances in the organic' water 1 are mineralized by biological treatment with activated sludge.
  • the biological treatment tank 2 may be any biological treatment tank used in this technology such as a standard activated sludge method, an anaerobic aerobic method, an anaerobic anoxic aerobic method, a nitrification denitrification method, and a biofilm method. Applicable.
  • the activated sludge mixture 3 discharged from the biological treatment tank 2 is supplied to a solid-liquid separation device (for example, a settling tank) 4 and separated into treated water 5 and settled sludge 6.
  • the settled sludge 6 is returned to the biological treatment tank 2 as returned sludge 7, and at least a part 8 of the returned sludge is supplied to the sludge concentrator 11 to be separated into concentrated sludge 12 and desorption night 17.
  • a phosphorus release tank 9 is provided in front of the sludge concentrator 11 to release the polyphosphoric acid in the sludge by, for example, stirring in an anaerobic state. Phosphorus concentration can be increased.
  • the desorption night 17 discharged from the sludge concentrator is supplied to the phosphorus recovery step 18.
  • MAP magnesium phosphate ammonium
  • HAP hydrodoxyapatite
  • the desorbed solution 17 is formed by a phosphorus recovery method known in the art such as the HAP method.
  • the soluble phosphorus is fixed and separated and recovered as phosphorus-containing crystals 20 or the like.
  • the processing solution 19 from which phosphorus has been separated and recovered is returned to the biological treatment tank 2. If the phosphorus concentration and the organic matter concentration of the phosphorus-recovered treatment solution 19 are sufficiently low and the discharge standards are satisfied, it can be discharged outside the system as a treatment STR.
  • the concentrated sludge 12 obtained from the sludge concentrator 11 is supplied to the ultrasonic reaction tank 13 and subjected to ultrasonic treatment. By increasing the concentration of the concentrated sludge 12 supplied to the ultrasonic reactor 13, the amount of liquid sludge can be reduced and liquid sludge can be obtained efficiently.
  • the sludge concentration is preferably 1 to: I 0%, preferably 4 to 8%.
  • the amount of energy consumed by the ultrasonic oscillator used in the ultrasonic reactor 13 is 1 OOO kj Z liters relative to the amount of the liquid to be treated, and that the energy consumed per ultrasonic horn cross-sectional area Is preferably 30 cm 2 or more .
  • the sonicated sludge 14 flowing out of the ultrasonic reaction tank 13 is returned to the biological treatment tank 2.
  • the biological treatment tank includes a denitrification tank, as in the case of the recirculation type nitrification and denitrification method, the soluble organic matter contained in the ultrasonically treated sludge 14 can be used as a hydrogen donor for the denitrification reaction.
  • Supplying the ultrasonically treated sludge 14 to the denitrification tank is an effective method for treating organic water.
  • FIG. 2 shows a processing flow in which excess sludge from the biological treatment process of organic water used in this example was treated using the method of the present invention to reduce sludge volume and recover phosphorus.
  • a nitrification denitrification tank composed of a denitrification tank 31 and a nitrification tank 32 was used as the biological treatment tank 2, and sewage was used as the organic water 1.
  • the sewage to be treated was supplied to the denitrification tank 31 of the biological treatment tank 2 at a flow rate of 10 m 3 / d.
  • the activated sludge concentration in the biological treatment device 2 was about 300 mg—SS / liter.
  • the activated sludge mixture from the nitriding tank 32 of the biological treatment apparatus 2 was supplied to the solid-liquid component 8 4.
  • the solid-liquid Using a sedimentation basin as the separation device 4, the activated sludge mixture 3 was separated into a treatment 5 and a settling sludge 6.
  • the flow rate of the returned sludge 7 of the settling sludge 6 discharged from the solid-liquid component 4 was 4 m 3 , and the sludge concentration was about 1000 Omg_SS / liter.
  • the desorption night 17 obtained by the sludge concentrator 11 was supplied to the phosphorus recovery step 18.
  • PAC polychlorinated aluminum
  • PAC polychlorinated aluminum
  • the concentration of ion phosphate in the treated water 19 from which phosphorus had been recovered was reduced to 0.5 mg liter.
  • SS was as good as 1 mg / liter or less and SzK was obtained, it was discharged out of the system as it was.
  • Table 1 Properties of sludge thickening and deaeration night 17 and phosphorus recovery process 19 in Example 1
  • the concentrated sludge 12 obtained by the sludge concentrator 11 was supplied to an ultrasonic reaction tank 13 and subjected to ultrasonic treatment.
  • the actual power consumption of the ultrasonic transmitter used in the ultrasonic reactor 13 was 700 w (electric power: 1.8 kwh per day).
  • the irradiation intensity per sludge amount was 50 kJZ liter.
  • the sludge 14 after the ultrasonic treatment was returned to the denitrification tank 31 of the biological treatment tank 2.
  • Table 2 shows the properties of the concentrated sludge 12 before the ultrasonic treatment and the sludge 14 after the ultrasonic treatment in the treatment process of Example 1. According to Table 1, in this example, the ultrasonic treatment was performed. The sludge 14 has more soluble components than the stage before the ultrasonic treatment, indicating that the sludge has liquefied. Table 2: Properties of returned sludge and ultrasonically treated sludge in Example 1
  • S—CODC r Solubility COD Table 3 shows the water quality of the treated water 5 of the biological treatment system of Example 1 combined with the excess sludge treatment according to the present invention. From Table 3, it can be seen that in this example, a good S7 water quality of 10 mg liter of SS and 30 mg / liter of COD Cr was obtained. In addition, total phosphorus was as good as 0.5 mgZ liter. Table 3: Water quality of sewage and treatment in Example 1
  • FIG. 3 shows the progress of the amount of sludge in the biological treatment tank 2 in the biological treatment process combined with the excess sludge treatment according to the present embodiment.
  • the amount of sludge in the biological treatment tank 2 was stable at about 10 kg during continuous operation for about 60 days, and it can be seen that the amount of excess sludge generated was suppressed by the excess sludge treatment according to the present invention.
  • Example 2 the same system as that of Example 1 shown in FIG. 2 was used, and phosphorus was recovered by the HAP method as a phosphorus recovery step 18.
  • sewage as organic 'ft ⁇ water 1 at a flow rate of 10 m 3 Z d is supplied to the denitrification tank 31 of the biological treatment tank 2.
  • Activity in biological treatment tank 2 The sludge concentration was about 3000 mg—S SZ liter.
  • the activated sludge mixture from the nitrification tank 32 of the biological treatment tank 2 was supplied to the solid-liquid separation device 4.
  • the activated sludge mixture 3 was separated into a treatment 5 and a settled sludge 6 by using a sedimentation basin as the solid-liquid separator 4.
  • the flow rate of the settled sludge 6 discharged from the solid-liquid separation unit 4 was 4 m 3 , and the sludge concentration was about l OOO Omg—S SZ Little.
  • 3.36 m 3 / d is returned to the denitrification tank 31 of the biological treatment tank 2 as returned sludge 7, and the remaining 0.64 m 3 / d is supplied to the phosphorus release tank 9 as treated sludge 8. , it was mixed with a portion of the organic tt ⁇ zK 1 0. 5 m 3 Bruno d.
  • the same treatment as in Example 1 was performed to release polyphosphoric acid in the sludge.
  • the sludge treated in the phosphorus discharge tank 9 was supplied to a sludge concentrator 11 and separated into a desulfurization unit 17 and a concentrated sludge unit 12.
  • the concentrated sludge 12 had a sludge concentration of 5% and the concentrated sludge amount was 0.13 m 3 Zd.
  • the desorbed liquid 17 obtained in the sludge concentrator 11 was supplied to the phosphorus recovery step 18.
  • a phosphorus ram filled with phosphate ore was used as the phosphorus recovery step 18, and slaked lime was added to the desorbed liquid 17 to adjust the power and supply calcium, so that phosphorus was converted to HAP: Ca.
  • the phosphorus recovery was performed by 5 OH (P0 4) HAP method for settling removed by crystallization as 3.
  • Table 4 shows the water qualities of the desorbed solution 17 in the phosphorus recovery step 18 and the treated solution 19 after phosphorus recovery. Table 4 indicates that soluble phosphorus was separated and removed from the desorbent 17 in the phosphorus recovery step 18.
  • the phosphorus-recovered treatment solution 19 was discharged as treated water outside the system.
  • Table 4 Properties of sludge concentration and desorption night 17 and phosphorus recovered SzK 19 in Example 2
  • the concentrated sludge 12 obtained by the sludge concentrator 11 was supplied to the ultrasonic reaction tank 13 in its entirety and subjected to ultrasonic treatment under the same conditions as in Example 1.
  • the sludge 14 after the ultrasonic treatment was returned to the denitrification tank 31 of the biological treatment tank 2.
  • Table 5 shows the properties of the concentrated sludge 12 before the ultrasonic treatment and the sludge 14 after the ultrasonic treatment in the treatment process of Example 2. From Table 5, it can be seen that the ultrasonic treatment The amount of the soluble component of the treated sludge 14 was higher than that before the ultrasonic treatment, indicating that the sludge was liquefied. Table 5: Return sludge and ultrasonically treated sludge in Example 2
  • S—CODC r soluble COD Table 6 shows the water quality of the treated water 5 of the biological treatment system in Example 2 in which the excess sludge treatment according to the present invention is combined. From Table 6, it can be seen that in this example, good treated water quality of 8 mgZ liter for SS and 2 mgZ liter for COD Cr was obtained. Also, the total water content was 0.4 ml and good water quality was obtained. Table 6: Sewage and treated water quality in Example 2
  • FIG. 4 shows the progress of the amount of sludge in the biological treatment tank 2 in the biological treatment process combined with the excess sludge treatment according to the present embodiment.
  • the amount of sludge in the biological treatment tank 10 was stable at about 10 kg, and it can be seen that the amount of excess sludge could be suppressed by the excess sludge treatment according to the present invention.
  • the excess sludge generated from the biological treatment process of organic '1 * ⁇ water is liquefied by ultrasonic waves and returned to the denitrification tank 31 of the biological treatment tank 2.
  • Went. Sewage was used as the organic water 1 and supplied at a flow rate of 10 m 3 / d to the denitrification tank 31 of the biological treatment tank 2.
  • the activated sludge concentration in the biological treatment tank 2 was about 300 Omg-S S / liter.
  • the activated sludge mixture 3 from the nitrification tank 32 of the biological treatment tank 2 was supplied to the solid-liquid separation unit 4.
  • the activated sludge mixed solution 3 was separated into the treated SzK 5 and the settled sludge 6 using a sedimentation basin method as the solid-liquid separation device 4.
  • the flow rate of the settled sludge 6 discharged from the solid-liquid separation unit 4 was 4 m d, and the sludge concentration was about 10 OOOmg-SSZ liter.
  • the entire amount of the settled sludge 6 discharged from the solid-liquid separation device 4 was supplied to the ultrasonic reaction tank 13 and subjected to ultrasonic treatment.
  • the conditions for the ultrasonic treatment were the same as in Examples 1 and 2.
  • the sludge 14 after the ultrasonic treatment was returned to the biological treatment tank 2.
  • Table 7 shows the properties of the settled sludge 6 before the ultrasonic treatment and the sludge 14 after the ultrasonic treatment in the treatment process of this comparative example. Table 7 shows that in this comparative example, the sludge was liquefied by the ultrasonic treatment, but the dissolution was less than that in Examples 1 and 2. Table 7: Properties of returned sludge and ultrasonically treated sludge in comparative examples
  • Table 8 shows the quality of treated water 5 of the biological treatment system when the excess sludge treatment of this comparative example is combined. From Table 8, in this comparative example, the SS and C 0 D cr of the treated water were higher than those in Examples 1 and 2, and the deviation was higher than in Examples 1 and 2, indicating that the water quality was inferior. . In addition, the SS in the biological treatment tank was higher than that in the example, and the amount of sludge in the biological treatment tank decreased as can be seen from Fig. 6, so the sludge in the biological treatment tank 2 also flowed out into the treatment tank 5. It is considered that In addition, the phosphorus in Process 5 became higher than the raw water, with the addition of 4, mg Z liter and phosphorus derived from SS. Table 8: Sewage and SzK Water Quality in Comparative Example
  • FIG. 6 shows the progress of the amount of sludge in the biological treatment tank 2 in the biological treatment process combined with the excess sludge treatment according to the present comparative example.
  • the operation was terminated in 35 days because sludge spilled violently.
  • the system of this comparative example could not perform stable biological treatment.
  • the amount of excess sludge generated in the treatment process of organic wastewater by biological treatment can be significantly reduced, and at the same time, phosphorus can be efficiently removed from sludge. It can be carried out. Also, the amount of power required to reduce the amount of excess sludge generated is small. That is, according to the present invention, since the ultrasonic treatment is employed for the treatment of the settled sludge, the power consumption is small and the processing apparatus may be small and simple.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Treatment Of Sludge (AREA)
  • Removal Of Specific Substances (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

Appareil et procédé de traitement d'une boue excédentaire selon lequel il est possible non seulement de réduire le volume excédentaire de boue, mais aussi de récupérer le phosphore de la boue. L'invention porte également sur un appareil et sur un procédé de traitement biologique d'eau résiduaire organique au moyen d'un système de traitement de la boue. L'invention porte également sur un procédé de traitement de la boue excédentaire générée à partir d'un processus de traitement d'eau résiduaire et comprenant une phase de traitement biologique et une phase de séparation des liquides et des solides. Ce procédé se caractérise en qu'une partie ou la totalité de la boue excédentaire est concentrée dans un liquide surnageant et la boue concentrée, le liquide surnageant obtenu est soumis au traitement de récupération du phosphore et recyclé au cours de la phase de traitement biologique ou évacué à l'extérieur du système sous forme d'eau traitée, et la boue concentrée provenant de la concentration de la boue excédentaire est soumise à une sonication et recyclée au cours de la phase de traitement biologique.
PCT/JP2003/006393 2002-05-22 2003-05-22 Appareil et procede de traitement d'eau residuaire organique permettant de recuperer le phosphore Ceased WO2003097540A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2004505276A JPWO2003097540A1 (ja) 2002-05-22 2003-05-22 リン回収が可能な有機性廃水の処理方法及び装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2002147805 2002-05-22
JP2002/147805 2002-05-22

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WO2003097540A1 true WO2003097540A1 (fr) 2003-11-27

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PCT/JP2003/006393 Ceased WO2003097540A1 (fr) 2002-05-22 2003-05-22 Appareil et procede de traitement d'eau residuaire organique permettant de recuperer le phosphore

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006087986A (ja) * 2004-09-21 2006-04-06 Kaneka Corp スケール生成防止方法
JP2013215681A (ja) * 2012-04-10 2013-10-24 Hitachi Power Solutions Co Ltd リン酸マグネシウムアンモニウム生成抑制システム及びメタン発酵システム
CN104045213A (zh) * 2014-06-27 2014-09-17 南京信息工程大学 一种污水的处理方法
FR3092105A1 (fr) * 2019-01-28 2020-07-31 Suez Groupe Procédé et installation de récupération de phosphore dans un effluent de boues issues d’eaux usées
CN119874143A (zh) * 2025-02-21 2025-04-25 中机国际工程设计研究院有限责任公司 一种剩余污泥处理方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5186826B2 (ja) * 2007-07-30 2013-04-24 Ｊｆｅスチール株式会社 Ｐを含有する処理液の廃液濃度制御方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02227191A (ja) * 1989-02-28 1990-09-10 Ebara Infilco Co Ltd 有機性汚水の処理方法
JPH0824873A (ja) * 1994-07-21 1996-01-30 Ebara Res Co Ltd 有機性汚水の高度処理方法
JPH09108690A (ja) * 1995-10-17 1997-04-28 Ebara Corp リン含有汚水の処理方法
EP0965566A2 (fr) * 1998-06-15 1999-12-22 Shinko Pantec Kabushika Kaisha installation de traitement d eaux usées organiques
JP2002059190A (ja) * 2000-08-18 2002-02-26 Hitachi Kiden Kogyo Ltd 汚水及び汚泥の処理方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH02227191A (ja) * 1989-02-28 1990-09-10 Ebara Infilco Co Ltd 有機性汚水の処理方法
JPH0824873A (ja) * 1994-07-21 1996-01-30 Ebara Res Co Ltd 有機性汚水の高度処理方法
JPH09108690A (ja) * 1995-10-17 1997-04-28 Ebara Corp リン含有汚水の処理方法
EP0965566A2 (fr) * 1998-06-15 1999-12-22 Shinko Pantec Kabushika Kaisha installation de traitement d eaux usées organiques
JP2002059190A (ja) * 2000-08-18 2002-02-26 Hitachi Kiden Kogyo Ltd 汚水及び汚泥の処理方法

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006087986A (ja) * 2004-09-21 2006-04-06 Kaneka Corp スケール生成防止方法
JP2013215681A (ja) * 2012-04-10 2013-10-24 Hitachi Power Solutions Co Ltd リン酸マグネシウムアンモニウム生成抑制システム及びメタン発酵システム
CN104045213A (zh) * 2014-06-27 2014-09-17 南京信息工程大学 一种污水的处理方法
CN104045213B (zh) * 2014-06-27 2015-09-30 南京信息工程大学 一种污水的处理方法
FR3092105A1 (fr) * 2019-01-28 2020-07-31 Suez Groupe Procédé et installation de récupération de phosphore dans un effluent de boues issues d’eaux usées
WO2020156978A1 (fr) * 2019-01-28 2020-08-06 Suez Groupe Procede et installation de recuperation de phosphore dans un effluent de boues issues d'eaux usees
CN119874143A (zh) * 2025-02-21 2025-04-25 中机国际工程设计研究院有限责任公司 一种剩余污泥处理方法

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TWI298712B (en) 2008-07-11
JPWO2003097540A1 (ja) 2005-09-15
TW200306955A (en) 2003-12-01

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