[go: up one dir, main page]

WO2019117589A1 - Système de récupération de phosphore et d'azote dans lequel une cuve de formation de cristaux de type à flottation à air double et un appareil de récupération de cristal pouvant séparer des tailles de grain sont introduits, et procédé de récupération de phosphore et d'azote l'utilisant - Google Patents

Système de récupération de phosphore et d'azote dans lequel une cuve de formation de cristaux de type à flottation à air double et un appareil de récupération de cristal pouvant séparer des tailles de grain sont introduits, et procédé de récupération de phosphore et d'azote l'utilisant Download PDF

Info

Publication number
WO2019117589A1
WO2019117589A1 PCT/KR2018/015681 KR2018015681W WO2019117589A1 WO 2019117589 A1 WO2019117589 A1 WO 2019117589A1 KR 2018015681 W KR2018015681 W KR 2018015681W WO 2019117589 A1 WO2019117589 A1 WO 2019117589A1
Authority
WO
WIPO (PCT)
Prior art keywords
phosphorus
crystal
nitrogen
untreated water
crystals
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/KR2018/015681
Other languages
English (en)
Korean (ko)
Inventor
김원재
정진홍
임현만
안광호
장향연
박나리
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.)
Korea Institute of Civil Engineering and Building Technology KICT
Original Assignee
Korea Institute of Civil Engineering and Building Technology KICT
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 Korea Institute of Civil Engineering and Building Technology KICT filed Critical Korea Institute of Civil Engineering and Building Technology KICT
Priority to CN201880054964.0A priority Critical patent/CN111051249B/zh
Publication of WO2019117589A1 publication Critical patent/WO2019117589A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
    • 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
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • 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
    • C02F1/5263—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using natural chemical 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
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
    • C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
    • 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
    • C02F2001/5218—Crystallization
    • 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
    • C02F2209/02—Temperature
    • 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 system capable of simultaneously recovering phosphorus and nitrogen by introducing a crystal-forming vessel and a crystal-recovering apparatus capable of separating the grain size of the two-stage air floating system, and a method for recovering phosphorus and nitrogen using the same.
  • Phosphorus and nitrogen in the water are generated from human or animal manure, synthetic detergents, etc., and these nitrogen or phosphorus are released into the water by raw sewage, livestock wastewater or plant wastewater, It causes problems such as eutrophication, ammonia fish toxin and dissolved oxygen in the water, and when it enters the water source, it causes discomfort due to the generation of taste and odor due to overproduction of algae, and the importance of the management is increasing.
  • phosphorus is one of the three major nutrients in plants, but it is a very rare nutrient on the planet and it is used as a raw material for fertilizer, feed, and chemicals.
  • P phosphorus
  • its production and reserves are limited, Technology to recover phosphorus and nitrogen is known as a sustainable technology that uses resources recursively.
  • the water quality of the return water produced in the sewage treatment process is as shown in Table 1 below.
  • Korean Patent Publication No. 10-2013-0031477 Publication date: 2013.03.29
  • Korean Patent Publication No. 10-2017-0099190 Publication date: 2017.08.31
  • Patent No. 10-1184795 Publication date: 2012.09.20
  • Korean Patent Publication No. 10-1184795 Publication date: 2012.09.20
  • the present invention has been conceived to solve the problems of the prior art as described above, and it is an object of the present invention to provide a crystal formation tank for forming crystals by a two-stage air floating system and a crystal recovery apparatus capable of particle size separation, And to provide a description of a system that can be recovered.
  • an untreated water supply device comprising: an untreated water supply pipe, a first air supply pipe, and a chemical supply pipe, And the second air supply pipe is provided at the lower part to supply fine bubbles, and the growth of the crystal nuclei is promoted, so that the phosphorus and nitrogen crystals are grown
  • a sedimentation separation section for providing a space in which the sludge including the sediment is deposited, an outer partition wall section for separating the crystal growth section and the sedimentation separation section, The precipitated crystals are formed on one side storage portion and the storage portion that is precipitated precipitate formed is stored in the embedded precipitate and the crystal growing unit containing crystalline tone discharge portion for discharging the crystals produced in the crystal growing portion;
  • a pretreatment tank connected to the untreated water supply pipe to supply untreated
  • the crystal forming bath may further include a carrier unit located below the air floating admission unit.
  • the first air supply pipe supplies air at a pressure of 0.5 to 5.0 kg f / cm 2 to generate a large bubble having an average diameter of 1 mm or more
  • the second air supply pipe the average diameter of from 1.0 to supplying air at a pressure of 4.0 kg f / cm 2 can generate fine bubbles of less than 1 mm.
  • the crystal forming bath may supply the chemical to maintain the pH of the mixture of the chemical and the untreated water at a pH of 8.5 to 10, and the crystal forming bath senses temperature, pH and hardness And may further include a sensing unit.
  • the crystal growing unit may further include a sludge collecting unit for removing the sludge floated upward by fine bubbles.
  • the drug may comprise magnesium oxide (MgO).
  • the chemical reservoir may supply the MgO to the air floating admixture so that the molar ratio (Mg / P) of magnesium ions and phosphorus contained in the untreated water is 1.0 to 2.0, the drug reservoir is ammonium nitrogen concentration compared to the moles of magnesium ion and the molar ratio of phosphorus contained in the raw water (Mg 2+ and PO 4 -P / NH 4 + -N) wherein the MgO to be 1.2 to 1.5 air flotation miscible Can be supplied.
  • the pretreatment tank may contain untreated water that has been removed by coagulation and sedimentation of a solid material by injection of a polymeric natural coagulant.
  • the crystal recovers can separate and recover crystals having an average grain size of 300 mu m or more.
  • the crystal recovers include an inlet that can introduce a fluid containing crystals and sludge into a high pressure in a tangential direction, a centrifugal separator that allows the fluid to form a swirling flow, And an outflow section for forming an inverse swirling flow in the direction opposite to the swirling flow through the inner cylinder of the crystal recovers to allow the treated water to flow out, and a crystal discharge section for discharging the separated crystals
  • the diameter of the outlet is formed to be larger than the diameter of the inlet and the diameter of the crystal outlet is smaller than the diameter of the inlet so that selective separation of the crystal can be induced according to the particle diameter and specific gravity,
  • the effluent can be returned to the crystal formation tank.
  • the crystal recovers further include a hopper including a strainer at a lower portion thereof to recover crystals having a particle size of 300 mu m or more contained in the drain water discharged from the crystal recovers, And the filtrate is transported to the crystal formation tank can be formed.
  • a method of recovering phosphorus and nitrogen using the system described above comprising the steps of: (a) supplying untreated water, macropores and chemicals to an air floating admission portion to form crystal nuclei; (b) supplying fine bubbles to a crystal growth portion to react the crystal nuclei to grow crystals; (c) precipitating the aggregate and the crystals contained in the untreated water; And (d) recovering the crystals.
  • the present invention also provides a method for recovering phosphorus and nitrogen crystals.
  • the untreated water subjected to the method of recovering phosphorus and nitrogen crystals is characterized in that a solid natural substance (SS) is removed by injecting a polymer natural coagulant, and the polymer natural coagulant has a deacetylation degree of 80% Or more and a molecular weight (MW) of 10,000 to 1,500,000.
  • SS solid natural substance
  • MW molecular weight
  • the drug used to carry out the method of recovering phosphorus and nitrogen crystals may comprise MgO.
  • the pH, the temperature and the hardness of the untreated water and the MgO mixture are monitored after the MgO is injected into the untreated water to control the proper pH and the magnesium ion concentration . ≪ / RTI >
  • the present invention provides a method of determining the optimum concentration of the drug injection of MgO for supplying to recover phosphorus and nitrogen by using the system described in the above, (i) in the raw water pH, water temperature, a magnesium ion (Mg 2+ ) basis including the concentration and alkalinity (alkalinity) of the concentration of total phosphorus (TP) concentration and phosphate (PO 4 -P) concentration of ammonia nitrogen (NH 3 -N) concentration of solids (SS) of the Identifying the constellation; (ii) determining the concentration of magnesium ions according to pH until the equilibrium state is reached after injecting MgO into the untreated water; (iii) calculating an injection amount of MgO to achieve a predetermined target pH and a molar ratio (Mg / P) of magnesium ion (Mg2 + ) to phosphorus (P); (iv) injecting the MgO into the untreated water according to the injection amount calculated in the step (iii), and monitoring the
  • step (iv) when the pH of the mixture of the untreated water and MgO is monitored and the pH of the mixture does not reach a predetermined target pH, And further injecting MgO into the mixture to reach a set target pH.
  • step (iv) the pH and hardness of the untreated water and the MgO mixture are monitored, and then the pH and hardness of the mixture reach a preset target pH and hardness
  • the method may further include the step of re-injecting MgO into the mixture so that the pH and hardness of the mixture reach a preset target pH and hardness.
  • the phosphorus and nitrogen recovery system comprises a crystal form; Pretreatment tank; air blower; A drug reservoir; And crystal recovers can be performed to perform the processes of mixing, crystal nucleation, crystal growth, aggregation, precipitation, and crystal recovery, respectively, so that phosphorus and nitrogen contained in the untreated water can be crystallized and removed.
  • the phosphorus and nitrogen recovery system can remove phosphorus and nitrogen with high efficiency, it can prevent water pollution such as eutrophication of public water bodies and green tide, and can reduce the amount of sludge of untreated water, It is possible to reduce the operation load of the process occurring in the subsequent process of the process.
  • crystals of phosphorus and nitrogen crystallized by using the above system can be immediately recycled as a slow-release fertilizer, which can replace phosphorus imports, can achieve high economic efficiency through fertilizer resource utilization, Can be saved.
  • FIG. 1 is a block diagram showing a typical sewage treatment process used in the Republic of Korea.
  • FIG. 2 is a conceptual diagram showing a system for recovering phosphorus and nitrogen according to the present invention.
  • FIG. 3 is a process diagram showing each step of a method for determining an optimum injection concentration of MgO supplied from a chemical reservoir so as to simultaneously satisfy a range of an optimum magnesium concentration and a pH within a crystal form by a method according to an embodiment of the present invention.
  • FIG. 4 is a graph showing the total phosphorus (TP), phosphorus phosphate (PO 4 -P) and ammonia nitrogen (FIG. 4A ) by pH to determine the proper pH for removing phosphorus contained in untreated water (A) concentration of NH 3 -N) and (b) removal efficiency.
  • TP total phosphorus
  • PO 4 -P phosphate
  • ammonia molar ratio
  • FIG. 6 is a result of X-ray diffraction spectroscopy (XRD) of sediments contained in a dehydrated filtrate in which MgO is injected so that the Mg / P molar ratio is 2.0 by operating the recovery system according to the present invention.
  • XRD X-ray diffraction spectroscopy
  • FIG. 7 is a graph showing the results of (a) total phosphorus (TP), total phosphorus (TP), and total phosphorus phosphate (PO 4 -P) and ammonium concentration of nitrogen (NH 3 -N), (b ) a phosphate (PO 4 -P) and the efficiency of removal of ammonium nitrogen (NH 3 -N), (c ) The results of Jar-test analysis of dry weight per volume of sludge.
  • FIG. 8 is a graph showing changes in the removal efficiency due to the adjustment of the molar ratio of magnesium and phosphate (PO 4 -P) to the ammonia nitrogen concentration in order to remove the ammonia nitrogen contained in the untreated water by operating the recovery system according to the present invention. This is a result.
  • the untreated water supply pipe, the first air supply pipe and the chemical supply pipe are provided at the lower part to supply untreated water, macro bubbles and chemicals, and the untreated water and the chemicals are mixed by the large bubbles,
  • a second air supply pipe provided at a lower portion thereof to supply fine bubbles and to accelerate the growth of the crystal nuclei to provide a space for growing phosphorus and nitrogen crystals
  • a center partition wall for separating the air floating admixture and the crystal growth portion, a space formed by the outer periphery of the crystal growth portion and containing the phosphorus and nitrogen crystals contained in the chemical mixture water passing through the crystal growth portion and the suspended material,
  • An outer partition wall for separating the crystal growth part and the precipitate separation part, a precipitate contained in the untreated water, Standing the precipitated crystals are formed is formed on one side of the storage unit and the precipitate settled storage portion that stores tone crystal form comprising discharging portion for discharging the crystals produced in the crystal growing portion;
  • a pretreatment tank connected to the untreated
  • first and second components are intended to distinguish one element from another, and the scope of the right should not be limited by these terms.
  • first component may be referred to as a second component, and similarly, the second component may also be referred to as a first component.
  • the identification code (e.g., a, b, c, etc.) is used for convenience of explanation, the identification code does not describe the order of each step, Unless otherwise stated, it may occur differently from the stated order. That is, each step may occur in the same order as described, may be performed substantially concurrently, or may be performed in reverse order.
  • the present invention is intended for raw water pH, such as a solid substance (SS), total phosphorus (TP), phosphate (PO 4 -P) and the ammonium nitrogen (NH 3 -N) concentration is high waste water, sewage, can be transported in A phosphorus and nitrogen recovery system capable of crystallizing phosphorus and nitrogen by injecting a controlling agent and a magnesium source and recovering crystallized phosphorus and nitrogen crystals.
  • SS solid substance
  • TP total phosphorus
  • PO 4 -P phosphate
  • NH 3 -N ammonium nitrogen
  • &quot untreated water " used in the present invention is a generic term for various kinds of wastewater and sewage, such as dehydrated filtrate, digested symbol number, concentrated filtrate, and the like, which occur after sewage and sludge treatment processes.
  • FIG. 2 is a conceptual diagram schematically showing a phosphorus and nitrogen recovery system 10 according to the present invention.
  • a phosphorus and nitrogen recovery system 10 includes a crystal structure 100, a pretreatment vessel 200, a blower 300, a chemical reservoir 400, and a crystal recovers 500 .
  • the crystal growth tank 100 includes an air floating admission portion 110, a crystal growth portion 120, a central partition wall portion 130, a deposition storage portion 140, a discharge portion 150, and a precipitation separation portion 180
  • the mixed crystals of untreated water and chemicals, the crystal growth of phosphorus and nitrogen contained in the untreated water, and the precipitation and separation of the crystallized crystals and the sludge are simultaneously carried out to crystallize phosphorus and nitrogen contained in the untreated water and precipitate the crystals and the sludge
  • the crystal is recovered, and the sludge is removed.
  • the central partition wall 130 formed in the inner space of the crystalline structure 100 separates the air floating mixer 110 and the crystal growth part 120 to form separate independent spaces .
  • the air flotation adhering portion 110 is provided with a first air supply pipe 111, an untreated water supply pipe 113 and a chemical supply pipe 115 at a lower portion thereof and a macro-bubble, And serves to provide a space in which the untreated water and the chemicals are mixed by the large bubbles to form crystal nuclei.
  • the air blast mixer 110 may mix chemicals and untreated water sufficiently to form a chemical mixture containing crystal nuclei within a short residence time, and circulate untreated water flowing into the inside.
  • the air floating mixer 110 chemicals and untreated water are mixed to form chemical mixture water, the formation of crystal nuclei is induced in the chemical mixture water, the upward flow of the chemical mixture water is formed,
  • the chemical mixing water may be allowed to flow over the crystal growth unit 120, which will be described later, at the upper end of the mixing unit 110.
  • the crystalline structure 100 may further include a transport section 117 positioned below the air floating type admixture section 110, and may be a crystal of a small size and a small amount of untreated liquid Or the like to the air floating mixer 110 again.
  • the crystal growth unit 120 is provided with a second air supply pipe 121 at the lower part thereof.
  • the crystal nuclei formed in the air floating admission unit 110 are suspended and circulated for a long residence time, .
  • the second air supply pipe 121 is connected to the air diffuser 123 so as to form micro bubbles having a size smaller than that of the large air bubbles formed in the first air supply pipe 111, have.
  • the mixed chemical water containing the crystal nucleus is allowed to stay for 30-120 minutes of residence time while stirring at an appropriate stirring strength, and the mixed chemical water containing the crystal nuclei is continuously stirred and wound During the collision of the rising effect of the fine bubbles supplied from the second air supply pipe 121 and the descending flow of the sludge, the fine crystal nuclei do not sink but continuously collide with other crystal nuclei And the growth of crystals can be promoted.
  • the microbubbles are supplied to float the sludge in the crystal growth unit 120 and the floated sludge is removed by using a sludge collecting unit 190 to be described later so that the concentration of the solid matter SS in the crystal growth tank 100 (CO 2 ) is removed from untreated water having a high alkalinity, thereby increasing the pH and reducing the amount of the drug injected.
  • the growth rate of the crystal is the second air supply can be adjusted by the feed rate of air supplied from the pipe 121 and the second air supply pipe 121 is 1.0 to 4.0, a pressure of kg f / cm 2 To promote the growth of the crystal.
  • the precipitation storage part 140 is located below the air floating type admixture part 110 and the crystal growth part 120 so that the precipitate such as sludge contained in the untreated water and the crystals formed in the crystal growth part 120 And serves to provide space for sedimentation and storage.
  • a first discharge pipe 151 is provided in the discharge unit 150 to discharge crystals and sludge generated in the crystal growth unit 120 formed in the lower part of the deposition storage unit 140,
  • the first discharge pipe 151 may be connected to a crystal recovery machine 500 to be described later to form a structure for recovering crystals.
  • the crystal growth unit 100 may include a sensing unit 160 capable of sensing the pH, hardness, and temperature of the drug mixed water in order to control the supply amount of the supplied chemical to the crystal growth unit 120 And it is also possible to constitute the pH sensor, the hardness sensor, the temperature sensor, or the composite sensor thereof to minimize the consumption of the supplied chemicals. It is also possible to inject chemicals into untreated water, measure the pH of a mixture of untreated water and chemicals, measure the hardness by magnesium ion (Mg 2+ ) concentration, or simultaneously monitor pH and hardness, It is possible to control the concentration of magnesium ions (Mg 2+ ).
  • the chemical when the chemical is injected into the crystal structure 100, the untreated water and the chemical are mixed, floated, and circulated in the crystal structure 100, so that the dissolution and crystallization of the chemical reaches the equilibrium state, And the pH of the mixed water of the drug mixed with the untreated solution is stably maintained. At this time, it is necessary to grasp the point at which the pH reaches the equilibrium state by continuously monitoring the pH until the mixed water count reaches the equilibrium state in the crystal growth tank 100. At this time, in the chemical reservoir 400, It is preferable to adjust the pH of the water to be in the range of pH 8.5 to 10.0, which is an appropriate range for the crystallization of struvite (MAP).
  • MAP crystallization of struvite
  • the sensing unit 160 preferably further includes a hardness sensor capable of monitoring whether an appropriate range of magnesium concentrations has been reached.
  • the crystal forming tank 100 according to the present invention can form phosphorus and nitrogen crystals by adjusting the supplied chemicals and pH, and the process will be described in more detail later.
  • the crystal growth chamber 100 is provided with an outer partition wall portion 170 fixed to the outer periphery of the crystal growth portion 120 and a plurality of outer barrier rib portions 170 provided on the crystal growth portion 120 located between the central partition wall portions 130 And a sludge collecting unit 190 may be further included.
  • the crystal growth part 120 and the precipitate separation part 180 are separated from each other to form an independent space.
  • the outer growth part wall part 170 is formed by the crystal growth part 120,
  • the number of the chemical mixture in which the phosphorus and nitrogen are removed is increased in the upward flow of the outer partition wall portion 170.
  • a floc containing phosphorus and nitrogen crystals of a predetermined size or larger, suspensions, organic substances, microorganisms, etc. may be precipitated and moved to and removed from the precipitation storage unit 140.
  • a sludge collecting unit 190 may be disposed above the crystal growth unit 120 located between the outer partition wall 170 and the central partition wall 130.
  • the sludge collecting unit 190 may be formed by fixing a tubular metal structure or a sludge collecting unit. Accordingly, the solid material SS in the crystal growth tank 100 is supplied with fine bubbles to the crystal growth unit 120 to float, and is collected and discharged by using the sludge collecting unit 190, Can be prevented.
  • the sediment separating unit 180 may further include an outflow unit 185 formed at an upper end thereof.
  • the sediment separating unit 180 may be configured to discharge the treated water, which has been overflowed through the outflow unit 185, And the treated water to be discharged may be stored in a storage tank 600 to be described later.
  • the precipitate separation unit 180 is located at the outer periphery of the crystal growth unit 120, and precipitates crystals and flocs grown in the chemical mixture water of the crystal growth unit 120, and the supernatant is supplied to the upper part of the precipitate separation unit 120 And a part of the crystals and the sludge having reached a certain size and specific gravity in the mixed water of the crystal growth part 120 can be treated to flow into the precipitation storage part 140 at the lower stage And the sludge floated on top of the crystal growth part 120 may be removed via the sludge collecting part 190.
  • the crystalline structure 100 may have a structure (not shown) that can directly discharge the sludge collected by the sludge collection unit 190.
  • the crystal structure 100 may be a composite structure having a cylindrical structure at the upper portion and a conical structure at the lower portion.
  • the air floating mixture portion 110, the crystal growth portion 120, And the sludge collecting unit 190 are disposed in the conical structure, and the sediment storage unit 140 and the sludge collecting unit 160 are disposed in the conical structure,
  • the discharge unit 150 may be disposed so that the sludge is separated and discharged and a system capable of recovering crystals of phosphorus and nitrogen formed is formed.
  • the conical structure of the conical structure maintains the angle formed by the outer wall formed on both sides of the tip portion from 30 to 65 °, so that the precipitate and the phosphorus and nitrogen crystals slip down to the lowermost end,
  • the outer partition wall portion 170 of the sedimentation separation portion is spaced from the lower end by a predetermined distance or more so that it is preferable not to affect the quality of the supernatant liquid during the inflow of the chemical mixture passing through the crystal growth portion 120 from the lower end .
  • the chemical mixture passing through the crystal growth part 120 flows into the precipitation separation part 180 from the lower end of the outer partition wall part 170 and flows upward
  • the mixture of the crystals and the sludge precipitated in the sediment storage unit 140 formed in the lower part of the crystal growth tank 100 is introduced into the crystal collecting unit 500 And only the crystals grown sufficiently to exceed the specific particle size are collected and the remaining crystals are returned to the crystal growth vessel 100 to achieve high treatment efficiency, stability of the treated water quality and economical efficiency, as well as high quality phosphorus and nitrogen crystals To be recovered.
  • the preprocessing tank 200 is connected to an untreated water supply pipe 113 provided at the one end of the crystallization tank 100 to supply untreated water to the air floating adhering portion 110 of the crystal growth tank 100 And the other end is connected to the untreated water conveying pipe 201 to supply and store the untreated water.
  • the pretreatment tank 200 provides a place where the untreated water flowing through the untreated water conveying pipe 201 is stored for a certain period of time to precipitate solid components such as sludge, and the untreated water conveying pipe 203 may be provided to convey the solid component such as the precipitated sludge to be stored in a storage tank 600 to be described later.
  • the untreated water stored in the pretreatment tank 200 may include dehydrated filtrate, digested symbol count, concentrated filtrate, and various wastewater and sewage generated after the sewage and sludge treatment process, but is not limited thereto.
  • the pretreatment tank 200 can inject the polymer natural coagulant into the untreated water to aggregate and remove the high concentration solid material SS, thereby improving the operation and treatment efficiency of the subsequent crystal growth tank 100.
  • the polymeric natural coagulant may include chitosan having a deacetylation degree of 80% or more and a molecular weight (MW) in the range of 10,000 to 1,500,000.
  • Polymer natural coagulants including chitosan have a mechanism of selective flocculation, sedimentation and removal of high solids (SS) without reacting with nutrients such as phosphorus and nitrogen in untreated water.
  • the blower 300 may be connected to the first air supply pipe 111 and the second air supply pipe 121 to supply air to generate the large bubbles and minute bubbles in the crystal growth tank 100.
  • the drug reservoir 400 may be connected to the drug supply pipe 115 to supply the drug to the crystalline type drug reservoir 100.
  • the drug may include various conventional drug materials capable of controlling pH and supplying a magnesium source And supply it to the crystal form set 100.
  • the drug may be preferably a drug including magnesium oxide (MgO) which is excellent in economical efficiency, easily adjustable in pH, and can simultaneously supply a magnesium source.
  • MgO magnesium oxide
  • the chemicals used to crystallize phosphorus contained in the raw water may include MgO and a pH adjusting agent, and the chemicals used to crystallize and remove nitrogen include MgO and potassium phosphate (K 2 HPO 4 ), Etc., and a drug including only MgO may be used.
  • the drug storage tank 400 can store MgO in a slurry state capable of adjusting the pH and supplying the magnesium source at the same time. Since the solubility of MgO is very low at 6.2 mg / L (20 DEG C) (H + ), such as carbonate ion (HCO 3 - ), can be supplied continuously, even if the raw water is not completely dissolved, MgO is slowly converted to Mg 2+ and OH - , the pH adjusting agent and the magnesium source can be simultaneously performed.
  • the chemical storage tank 400 is provided with agitating means so that the completely dissolved MgO does not settle down but can be sufficiently agitated.
  • An air mixing method using an air blower can be applied to the agitating means. Since the system of the present invention can be used in connection with a blower for supplying air to the system, it is not necessary to introduce additional stirring means such as an agitator, and thus a compact structure can be formed.
  • the drug reservoir 400 can control the amount of the drug to be supplied to the crystal growth tank 100 by monitoring the magnesium ions and pH in the crystal growth tank 100,
  • the optimum molar ratio can be determined on the basis of the phosphorus contained in the magnesium ions and the untreated water, so that the medicine can be supplied. More preferably, the drug can be injected so as to have a Mg / P molar ratio of 1.0 to 2.0.
  • the drug when MgO is used as the above-mentioned medicine, the drug is poured into the chemical storage tank 400, and then, until the equilibrium state determined by the dissolution rate of MgO and the crystallization reaction rate in the crystal form bath 100 It is preferable to monitor the pH and the magnesium ion (Mg 2+ ) in the crystal structure 100. It is possible to supply the drug by determining the amount of MgO to be injected so as to have a pH of 8.5 to 10.0.
  • the concentration of magnesium ions (Mg 2+ ) in the crystal structure 100 can be monitored using a hardness sensor since most of the hardness components are composed of magnesium ions (Mg 2+ ).
  • the crystal recovers 500 may be connected to the first conveying pipe 151 provided in the discharging unit 150 of the crystal forming tank to recover crystals generated in the crystal forming tank 100.
  • the crystal recovers 500 can be configured to recover crystals having an average grain size of 300 ⁇ m or more, preferably 500 ⁇ m or more, by inducing a sufficient crystallization reaction in the crystal growth vessel 100,
  • the fine crystal transferring piping 561 may be provided to transport crystals and filtrate having a size of less than 300 ⁇ m to the crystal growth tank 100.
  • the crystal recovers 500 may use a wet cyclone (hydrocyclone) having a composite structure of a lower cone structure and an upper cylindrical structure.
  • the crystal recovers 500 are connected to the first discharge pipe 151 provided in the discharge unit 150 of the crystal form set 100, and the crystals precipitated in the tangential direction of the crystal recovers 500
  • a crystal separator 520 for separating the crystals and the sludge having a predetermined size or more by a centrifugal force so as to form a swirling flow
  • an outflow portion 530 for forming a new swirling flow in the opposite direction of the swirling flow through the inner cylinder of the honeycomb structure 500 to allow the treated water to flow out
  • a crystal discharge portion 540 for discharging separated crystals .
  • a strainer 550 for separating and recovering the separated crystals and the sludge according to the particle diameters and the filtrate having passed through the strainer 550 are stored in the crystal form tank 100 And a hopper 560 provided with a second conveying pipe 561 for conveying the same.
  • the crystal recovers 500 may be formed by separating the mixture of the crystals and the sludge precipitated in the discharging part 150 of the crystal formers 100 according to their particle diameters, And the remaining filtrate can be conveyed.
  • the drainage water discharged from the crystal collecting machine 500 is again separated by the hopper 560 including the lower strainer so that the particle size is 300 mu m or more
  • the particles are recovered by the strainer 550, and particles smaller than this and the filtrate can be transported to the crystal growth tank 100.
  • the outlet 530 formed in the crystal collecting machine 500 is formed to have a diameter larger than the diameter of the inlet 510 so that the flow rate in the outlet 530 is reduced,
  • the crystal discharge unit 540 is formed to have a diameter smaller than the diameter of the inlet 510 to induce selective separation according to the particle diameter and specific gravity and the effluent of the crystal collector 500 is conveyed to the crystal growth vessel 100, It is possible to constitute the microcrystalline to induce a rapid crystallization reaction by repeatedly acting as a crystal nucleus.
  • the crystal having the above-mentioned crystal size can be used as a slow-release fertilizer that can be immediately introduced into the soil by filtering it through a strainer such as a strainer 550 located at the lower end of the crystal collecting machine 500, filtering and filtering.
  • a strainer such as a strainer 550 located at the lower end of the crystal collecting machine 500, filtering and filtering.
  • the dried crystals in the above process may preferably include struvite (MAP), and may include crystals in the form of white or pale brown or gray powder having a specific gravity of 1.7.
  • MAP struvite
  • each supply pipe provided in the phosphorus and nitrogen recovery system according to the present invention is provided with a supply pump (pump, p) to smoothly supply untreated water, crystals, and chemicals.
  • a supply pump pump, p
  • a flow rate measuring instrument capable of measuring the flow rate and a valve for controlling the flow rate of the air are provided in the untreated water supply pipe 113, the chemical supply pipe 115, the second air supply pipe 121 and the first discharge pipe 151, a flow meter F is provided to quantify the supply of untreated water, air, chemicals and the like, thereby controlling the phosphorus and nitrogen crystallization reaction precisely.
  • the phosphorus and nitrogen recovery system 10 may include a storage tank 600 capable of discharging sludge, treated water, and the like.
  • the phosphorus and nitrogen recovery system 10 includes a crystal structure 100; A pretreatment tank 200; A blower 300; A drug reservoir 400; And crystal recovery machine 500 can be used to crystallize and remove phosphorus and nitrogen contained in untreated water through 1) admixture, 2) crystal nucleation, 3) crystal growth, and 4) precipitation and crystal recovery processes,
  • the phosphorus and nitrogen crystals formed in the reactor 100 can be recovered, thereby reducing the environmental pollution and achieving recycling of resources, and it is possible to reduce the operating load caused by the return water in various sewage treatment processes.
  • the phosphorus and nitrogen crystals recovered by crystallization through the phosphorus and nitrogen recovery system 10 according to the present invention can be immediately reused as a fertilizer, thereby achieving high economic efficiency through fertilizer resource utilization, The amount of use can be reduced.
  • a preferred process for generating and recovering phosphorus crystals using the phosphorus and nitrogen recovery system 10 according to the present invention can be performed as shown below.
  • the drug and untreated water are mixed so that the Mg / P titration molar ratio of phosphorus (P) contained in MgO and untreated water is 1.2 or more, and the mixed water of the drug and untreated water is adjusted to pH 9.0 or more,
  • the optimum crystallization conditions are such that large bubbles are introduced in the air floating mixer 110 and rapidly stirred within 3 minutes and fine bubbles are supplied from the crystal growth part 120 to be slowly stirred for 20 minutes or more, ) For 30 minutes or more to perform a phosphorus and nitrogen recovery process.
  • a mixture of crystals and sludge precipitated in a sediment storage unit (140) located in the lower part of the crystal structure is supplied to a crystal recovery machine, And the crystals having a size smaller than a certain particle size are recovered and recrystallized to efficiently remove phosphorus and nitrogen contained in the untreated water It can generate.
  • a method of recovering phosphorus and nitrogen using the system described above wherein the phosphorus and nitrogen recovery method comprises the steps of: (a) supplying untreated water, macro bubbles, ; (b) supplying fine bubbles to a crystal growing part and reacting the crystal nuclei to grow crystals; (c) precipitating the aggregate and the crystals contained in the untreated water; And (d) recovering the crystals.
  • step (a) untreated water, macro-bubbles, and chemicals are supplied to the air-floating mixer to form a chemical mixture water containing crystal nuclei, and the large bubbles are uniformly mixed And the crystal nuclei can be formed by reacting the untreated water with the chemical.
  • the chemical may include magnesium, a pH adjusting agent, dipotassium phosphate (K 2 HPO 4 ), and the like.
  • the phosphorus and nitrogen contained in the untreated water are efficiently In this step, the process of removing phosphorus and nitrogen contained in untreated water is divided into a process of recovering mainly phosphorus and a process of recovering mainly nitrogen As shown in FIG.
  • MgO magnesium oxide
  • the MgO implantation amount satisfying the set molar ratio of Mg / P can be calculated and injected.
  • a drug containing a magnesium source is added so that the molar concentration (Mg / P molar ratio) of magnesium contained in the drug relative to phosphorus contained in the untreated water is 1.0 to 2.0
  • the Mg / P molar ratio can be controlled to be 1.2 to 1.5, and in this case, the removal efficiency of the phosphorus phosphate can be attained by 90% or more.
  • a phosphorus magnesium source should be injected so that the molar concentration of phosphorus and magnesium relative to the ammonia nitrogen of untreated water is 1.0 to 2.0, The molar concentration of contrast phosphorus and magnesium may be adjusted to 1.2 to 1.5, respectively.
  • MgO and phosphorous can be used as the magnesium source, and potassium phosphate (K 2 HPO 4 ) can be used.
  • K 2 HPO 4 potassium phosphate
  • the removal efficiency of phosphate phosphorus can be more than 95% and the removal efficiency of ammonia nitrogen can be more than 90% have.
  • the magnesium source and the pH adjuster may not be separately provided, and only the MgO may be supplied as the drug, so that the magnesium concentration and the pH of the inside of the crystal form are adjusted simultaneously to form phosphorus and nitrogen crystals.
  • MAP struvite
  • magnesium chloride hydrate MgCl 2 .6H 2 O, MgSO 4 .7H 2 O, etc.
  • the magnesium supply source and the pH adjusting agent are not separately provided, and MgO alone is used as a medicine to simultaneously perform both of the role of removing phosphorus and nitrogen.
  • MgO is advantageous in that it is very inexpensive as compared with other magnesium sources and has excellent economical efficiency.
  • the MgO is to be hydrolyzed by reaction with water as shown in Scheme 1 a Mg 2+ ion and two OH - ions discharge, and adjusting the pH of the magnesium and alkali supply range is possible only by injection of the MgO .
  • the MgO generally has a very low solubility in water of 6.2 mg / L, but can be used in a solution having a high acidity (such as a solution having high alkalinity or a solution containing ammonia nitrogen) capable of providing H + The solubility increases.
  • MgO can be injected to satisfy the optimum magnesium concentration and pH range simultaneously in the crystal structure through the basic experiment, and the optimum injection concentration will be described in detail in the method of determining the optimum injection concentration of MgO to be described later.
  • the pressure of the blower can be held by and to be large bubbles are supplied, can be sufficient stirring to a large air bubble supply, and is a crystal nucleation through which induce rapid crystallization reaction so that 0.5 to 5.0 kg f / cm 2 .
  • step (b) is a step of supplying fine bubbles to the crystal growth part to react the crystal nuclei to grow crystals, wherein the crystal nuclei formed in the air floating blend part are reacted in the crystal growth part to promote crystal growth .
  • the chemical mixture flowed over the upper end of the air floating admission portion is allowed to stay in the crystal growth portion for 30 to 120 minutes, and stirred and floated during the residence time to grow crystal nuclei in the chemical treatment water So that the fine crystal nucleus does not sink quickly but continuously collides with other crystal nuclei in the process of collision between the rising effect of the air bubbles and the downward flow of the sludge, have.
  • the growth rate of the crystal and can be adjusted by the air supply amount of the micro-bubble diffuser, at this time, the pressure is preferably from 1.0 to 4.0 kg f / cm 2.
  • step (c) comprises the steps of precipitating the aggregate and the crystals contained in the untreated water, removing the sludge contained in the crystals formed in the crystal growth unit and the chemical mixture water by transferring the sludge to the precipitate separation unit,
  • the crystals and floating sludge grown in the mixed water of the growth part of the chemical mixing water at a predetermined size or more are allowed to settle in the sedimentation storage part in a residence time range of 20 to 60 minutes and the sludge floated on the upper part of the crystal growth part is collected in the upper sludge collecting part 190
  • the precipitate separating unit 180 may be configured to discharge the treated water through the outflow unit 185 formed at the upper end.
  • the step (d) may be configured to recover the crystals by separating and recovering crystals having a specific average particle size.
  • crystals and sludge precipitated in the lower sedimentation storage unit 140 of the crystal formation tank may be introduced into a crystal recovery device such as a hydrocyclone to separate crystals having a specific particle size. It is preferable to recover particles having a particle size of 300 mu m or more (preferably 500 mu m or more) which is an immediately usable size.
  • the above-mentioned crystal recovers are formed by adjusting the flow rate of the crystals and the sludge mixture separated from the outflow portion (not shown) formed at the lower end to induce generation of strong swirling flow, lowering the flow rate of the outflow portion, (Preferably 500 m or more) can be recovered with high efficiency.
  • the method for recovering phosphorus and nitrogen crystals according to the present invention as described above can effectively recover phosphorus and nitrogen contained in untreated water and recover it, and the recovered crystals can be immediately used as a slow-release fertilizer.
  • the recovery system according to the present invention can be applied to a solid waste (SS), a total waste (TP), or an ammonia nitrogen (NH), such as reflux water 3- N), 1) water treatment chemicals capable of pH adjustment and magnesium source supply, 2) air floating admixture for supplying macro-bubbles, and water supplied with untreated water in a short time (3) a crystal growth part for supplying fine bubbles causes the crystal nucleus to float and circulate for a long residence time to induce crystal growth, and (4) a non-treated water In the process of overflowing from the sedimentation separation part separated by the partition wall, flocs of a predetermined size or larger are precipitated and only the clean treated water is discharged, and 5) The mixture of the crystals and the sludge is introduced into the crystal recovery device, and only the crystals grown with a sufficient particle size separated by particle size are collected, and the remaining crystals are returned to the crystal growth vessel 100 to achieve high treatment efficiency, stability of the treated water quality and economical efficiency And can recover high quality struvite (MAP) crystals
  • FIG. 3 is a process diagram showing each step of a method for determining the optimum injection concentration of MgO from the chemical storage tank so as to simultaneously satisfy the optimum magnesium concentration and the pH range in the crystal structure of the phosphorus and nitrogen recovery system according to the present invention.
  • the optimum injection of the MgO concentration determination method (i) raw water in the pH, the concentration of magnesium ion (Mg 2+), the concentration of total phosphorus (TP), phosphate (PO 4 - P) and the concentration of ammonia nitrogen (NH 3 -N); (ii) determining the concentration of magnesium ions according to pH until the equilibrium state is reached after injecting MgO into the untreated water; (iii) calculating an injection amount of MgO to achieve a predetermined target pH and a molar ratio (Mg / P) of magnesium ion (Mg2 + ) to phosphorus (P); (iv) injecting the MgO into the untreated water according to the injection amount calculated in the step (iii), and monitoring the properties of the mixture of the untreated water and the MgO; And (v) performing the continuous operation at the same injection amount when the mixture reaches a preset target pH.
  • Mg 2+ concentration of total phosphorus
  • TP total phosphorus
  • the MgO is injected into the crystal growth tank 100.
  • the MgO is injected into the crystal growth tank 100.
  • the pH of the untreated water, the water temperature, the concentration of magnesium ion (Mg 2+ ), the concentration of total phosphorus (TP), the concentration of phosphate phosphorus (PO 4 -P), the concentration of ammonia nitrogen (NH 3 -N) (PH 8.5 to 10) and Mg / P on the basis of the basic properties of the untreated water, which is a step of grasping the basic properties including the concentration of the solid substance (SS) and the alkalinity
  • the amount of MgO to be implanted can be determined.
  • the Mg 2+ and pH change according to the amount of MgO injected should be monitored until the equilibrium state is reached after the MgO is injected into the untreated water. After the MgO is injected in an amount necessary for achieving the condition, The nature of the water and the MgO mixture can be monitored.
  • the MgO may be injected by repeating the above steps by further injecting predetermined MgO to measure the pH again.
  • the amount of MgO injected when the pH and hardness of the untreated water and the MgO mixture are monitored at the same time can be determined.
  • the pH of the mixture is adjusted to reach the predetermined target pH
  • the method may further comprise the step of re-injecting MgO into the mixture or monitoring the pH and hardness of the untreated water and the MgO mixture and then adjusting the pH and hardness of the mixture to a predetermined target pH and hardness
  • the method further comprises injecting MgO into the mixture so that the pH and hardness of the mixture reach a preset target pH and hardness.
  • the optimal concentration of MgO can be determined from the chemical storage tank so that the optimum magnesium concentration and the pH range can be simultaneously satisfied in the crystal structure of the phosphorus and nitrogen recovery system according to the present invention, .
  • the dehydrated filtrate was supplied to each of 6 containers Jar by 1 L, and the pH of the dehydrated filtrate was adjusted by adjusting the pH of the dehydrated filtrate (pH 8.0, 8.5, 9.0, 9.5, 10.0 ).
  • the magnesium solution was poured into the dehydrated filtrate with the pH adjusted as described above, stirred at a rate of 100 rpm for 3 minutes, and allowed to stand for 30 minutes to induce precipitation. Thereafter, the dehydrated filtrate was collected to analyze the concentration change and removal efficiency of total phosphorus (TP), phosphorus phosphate (PO 4 -P) and ammonia nitrogen (NH 3 -N) by pH, 4.
  • Jar-test was conducted to determine the proper molar ratio for the sewage treatment by operating the phosphorus and nitrogen recovery system according to the present invention.
  • the molar ratio (Mg / P molar ratio: 0, 0.75, 1.0, 1.25, 1.5, 2.0) of magnesium (Mg 2+ ) to phosphorus (P) was varied using the same dehydration filtrate as in the above- Jar-test was carried out to determine the proper Mg / P molar ratio, and the test was carried out using the method as shown below.
  • the Mg / P molar ratios (Mg / P molar ratios: 0, 0.75, 1.0, 1.25, and 1.5, respectively) were obtained by feeding a dehydrated filtrate to each of six vessels , 2.0) were adjusted.
  • struvite As shown in FIG. 6, it was confirmed that struvite (MAP) was formed from the distribution of the XRD peak in the dehydrated filtrate in which the Mg solution was injected so that the molar ratio was 2.00.
  • a suitable slow stirring time is determined by performing a Jar-test while varying the slow stirring and the sedimentation time using the dehydration filtrate of the sewage treatment facility Tests were conducted and performed in the order shown below.
  • the ammonium nitrogen using the same dewatering the filtrate as in Example 1 to determine the proper molar ratio to remove the (NH 3 -N) ammonium nitrogen contained in the raw water (NH 3 (P) and magnesium (Mg 2+ ) relative to the molar concentration of ammonium and nitrogen, and the removal efficiency change due to the adjustment of the molar ratio of magnesium to the molarity of ammonia nitrogen And the results are shown in FIG.
  • the magnesium to phosphorus molar ratio (Mg 2+ and PO 4 - P / NH 4 + -N) is in the range of 1.2 to 1.5 with respect to the ammonia nitrogen molar concentration
  • the removal efficiency of phosphate phosphorus and ammonia nitrogen And the ammonia nitrogen (NH 3 -N) can be removed with an efficiency of 90% or more.
  • Example 2 The same dehydration filtrate as in Example 1 was used and MgO was injected into the dehydrated filtrate to remove the Mg 2+ concentration and the removal efficiency of phosphate (PO 4 -P) and ammonia nitrogen (NH 3 -N) After reaching the target pH, the mixture was allowed to stand for 3 minutes, and the supernatant was collected and analyzed. The results are shown in FIG.
  • MgO was injected into 2 L of the dehydrated filtrate to obtain a Mg 2+ concentration of 346 mg / L at a pH of 10.0, wherein the Mg / P molar ratio was 1.5 or more And the pH also satisfied the optimum crystallization condition.
  • the present invention relates to a system capable of simultaneously recovering phosphorus and nitrogen by introducing a crystal-forming vessel and a crystal-recovering apparatus capable of separating the grain size of the two-stage air floating system, and a method for recovering phosphorus and nitrogen using the same.

Landscapes

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

Abstract

La présente invention concerne un système capable de récupérer simultanément du phosphore et de l'azote par introduction d'une cuve de formation de cristaux de type à flottation à air double pour fournir simultanément des macrobulles et des microbulles et un appareil de récupération de cristaux pouvant séparer des tailles de grain, et un procédé de récupération de phosphore et d'azote l'utilisant.
PCT/KR2018/015681 2017-12-11 2018-12-11 Système de récupération de phosphore et d'azote dans lequel une cuve de formation de cristaux de type à flottation à air double et un appareil de récupération de cristal pouvant séparer des tailles de grain sont introduits, et procédé de récupération de phosphore et d'azote l'utilisant Ceased WO2019117589A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201880054964.0A CN111051249B (zh) 2017-12-11 2018-12-11 磷和氮的回收系统、利用其的磷和氮的回收方法及确定氧化镁的最佳注入浓度的方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020170169498A KR101864178B1 (ko) 2017-12-11 2017-12-11 이단 공기부상 방식의 결정형성조와 입경 분리가 가능한 결정회수장치가 도입된 인과 질소의 회수 시스템 및 이를 이용한 인과 질소의 회수 방법
KR10-2017-0169498 2017-12-11

Publications (1)

Publication Number Publication Date
WO2019117589A1 true WO2019117589A1 (fr) 2019-06-20

Family

ID=62913746

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2018/015681 Ceased WO2019117589A1 (fr) 2017-12-11 2018-12-11 Système de récupération de phosphore et d'azote dans lequel une cuve de formation de cristaux de type à flottation à air double et un appareil de récupération de cristal pouvant séparer des tailles de grain sont introduits, et procédé de récupération de phosphore et d'azote l'utilisant

Country Status (3)

Country Link
KR (1) KR101864178B1 (fr)
CN (1) CN111051249B (fr)
WO (1) WO2019117589A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110386697A (zh) * 2019-08-21 2019-10-29 长沙理工大学 一种疏浚余水处理方法和处理装置

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102399895B1 (ko) * 2020-12-29 2022-05-20 한국건설기술연구원 산화마그네슘(MgO) 용해도 예측 모듈이 구비된 스트루바이트 결정화 폐수처리 시스템 및 이를 이용한 스트루바이트 결정화 방법

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20020005521A (ko) * 2001-09-13 2002-01-17 서정원 스트루바이트 침전을 이용한 고농도 질소폐수 처리방법 및이를 이용한 폐수 처리장치
KR20020066499A (ko) * 2001-02-12 2002-08-19 코오롱건설주식회사 스트러바이트 침전과 암모니아 스트리핑 결합형 질소, 인동시제거 축산폐수 전처리 방법 및 장치
KR20060102762A (ko) * 2005-03-24 2006-09-28 충청북도 스트루바이트(ｓｔｒｕｖｉｔｅ) 결정화 방법에 의한산업폐수의 질소처리장치 및 방법
KR101268376B1 (ko) * 2012-12-18 2013-05-28 제일산업개발(주) 환경친화형 응집제
KR20160003935A (ko) * 2014-07-01 2016-01-12 주식회사이피에스솔루션 인 제거, 회수 장치 및 그 방법

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100522836C (zh) * 2007-04-17 2009-08-05 哈尔滨工业大学 气提式内循环装置及磷酸铵镁结晶回收氮、磷的方法
US20120031849A1 (en) * 2010-02-05 2012-02-09 Ostara Nutrient Recovery Technologies Inc. Aerated reactor apparatus and methods
CN101817581B (zh) * 2010-04-08 2012-11-07 同济大学 一体化鸟粪石法氮磷回收装置
CN103935974B (zh) * 2014-03-24 2016-11-09 同济大学 一种将污水中高浓度氨氮回收为高纯度大颗粒鸟粪石的方法
KR101624258B1 (ko) * 2014-07-01 2016-05-26 주식회사이피에스솔루션 질소와 인 제거, 회수 장치 및 그 방법
KR101614651B1 (ko) * 2015-03-06 2016-04-22 성균관대학교산학협력단 하이드로싸이클론을 이용한 정수 처리 시스템 및 이를 이용한 정수 처리 방법

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20020066499A (ko) * 2001-02-12 2002-08-19 코오롱건설주식회사 스트러바이트 침전과 암모니아 스트리핑 결합형 질소, 인동시제거 축산폐수 전처리 방법 및 장치
KR20020005521A (ko) * 2001-09-13 2002-01-17 서정원 스트루바이트 침전을 이용한 고농도 질소폐수 처리방법 및이를 이용한 폐수 처리장치
KR20060102762A (ko) * 2005-03-24 2006-09-28 충청북도 스트루바이트(ｓｔｒｕｖｉｔｅ) 결정화 방법에 의한산업폐수의 질소처리장치 및 방법
KR101268376B1 (ko) * 2012-12-18 2013-05-28 제일산업개발(주) 환경친화형 응집제
KR20160003935A (ko) * 2014-07-01 2016-01-12 주식회사이피에스솔루션 인 제거, 회수 장치 및 그 방법

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110386697A (zh) * 2019-08-21 2019-10-29 长沙理工大学 一种疏浚余水处理方法和处理装置

Also Published As

Publication number Publication date
CN111051249B (zh) 2022-03-29
KR101864178B1 (ko) 2018-07-13
CN111051249A (zh) 2020-04-21

Similar Documents

Publication Publication Date Title
WO2019107948A2 (fr) Dispositif de traitement d'eaux d'égout perfectionné ayant un système de gestion intégrée et de commande automatique de bioréacteur et une nouvelle fonction de production d'énergie renouvelable et présentant ainsi un traitement d'eaux d'égout et des rendements énergétiques améliorés, et procédé de traitement d'eaux d'égout perfectionné
JP2019505368A (ja) 廃水からのリン化合物の回収
WO2011139089A2 (fr) Dispositif de traitement de l'eau propre et des eaux d'égout/eaux usées de type à courant descendant naturel permettant d'économiser de l'énergie
WO2013097461A1 (fr) Système de traitement d'égouts et de boues, et procédé pour leur traitement
US20210317016A1 (en) Methods and apparatus for nutrient and water recovery from waste streams
KR101462033B1 (ko) 인 결정화 장치를 갖는 하·폐수처리시설
WO2013048010A1 (fr) Système évolué de traitement de l'eau pour la séparation par membrane basé sur l'élimination des phosphores et des matériaux obstruant la membrane contenus dans un flux latéral
WO2019117589A1 (fr) Système de récupération de phosphore et d'azote dans lequel une cuve de formation de cristaux de type à flottation à air double et un appareil de récupération de cristal pouvant séparer des tailles de grain sont introduits, et procédé de récupération de phosphore et d'azote l'utilisant
ES2252288T3 (es) Procedimiento para la depuracion de aguas residuales y estacion depuradora para la realizacion del procedimiento.
WO2018221970A2 (fr) Système de précipitation/flottation hautement efficace comportant des processus intégrés de précipitation et de flottation/séparation et son procédé de commande
KR101278475B1 (ko) 선회류식 무기슬러지 분리배출장치와 생물반응조를 결합한 슬러지처리장치
WO2014112765A1 (fr) Dispositif de traitement d'eau d'égout et d'eau usée possédant une unité de rétention de boues activées, et procédé de réduction de la teneur en azote pour eau d'égout et eau usée utilisant ledit dispositif
KR100970964B1 (ko) 슬러지 저감 및 인 제거를 위한 슬러지 처리 방법 및 장치
KR100627158B1 (ko) 변성전분 폐수처리 방법
KR100876104B1 (ko) 축산 분뇨 처리장치 및 방법
CN103011462A (zh) 重复利用电厂中水石灰软化法处理循环补充水的废渣的装置及方法
WO2017086701A1 (fr) Procédé automatisé de traitement d'eau de type à récupération de support
CN213388125U (zh) 隧道施工污水一体化处理设备
JP3456022B2 (ja) 汚水処理設備
JP3794736B2 (ja) 高濃度のリン及びアンモニア性窒素含有排水の処理方法
KR101861072B1 (ko) 인 결정화 장치를 갖는 하·폐수처리시설 및 음식물쓰레기·축산분뇨처리시설
KR101956039B1 (ko) 산화프로필렌 생산공정에서 발생하는 폐수처리 장치 및 방법
JPH02277597A (ja) 有機性汚水の処理方法
KR101206941B1 (ko) 조류 제거장치 및 이를 이용한 조류 제거방법
CN103693728A (zh) 一种含磷、镍废水的预处理工艺

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18889601

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 18889601

Country of ref document: EP

Kind code of ref document: A1

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205 DATED 21/01/2021)

122 Ep: pct application non-entry in european phase

Ref document number: 18889601

Country of ref document: EP

Kind code of ref document: A1