CN114853235A - Electric nitrogen and phosphorus double-anode cooperative recovery device and method for drainage pore water - Google Patents
Electric nitrogen and phosphorus double-anode cooperative recovery device and method for drainage pore water Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 181
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 239000011148 porous material Substances 0.000 title claims abstract description 94
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 61
- 239000011574 phosphorus Substances 0.000 title claims abstract description 61
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 52
- 238000011084 recovery Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000007689 inspection Methods 0.000 claims abstract description 40
- 239000010865 sewage Substances 0.000 claims abstract description 40
- 238000005189 flocculation Methods 0.000 claims abstract description 38
- 230000016615 flocculation Effects 0.000 claims abstract description 36
- 238000002425 crystallisation Methods 0.000 claims abstract description 29
- 230000008025 crystallization Effects 0.000 claims abstract description 28
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 26
- SNAAJJQQZSMGQD-UHFFFAOYSA-N aluminum magnesium Chemical compound [Mg].[Al] SNAAJJQQZSMGQD-UHFFFAOYSA-N 0.000 claims abstract description 25
- 229910000838 Al alloy Inorganic materials 0.000 claims abstract description 24
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 13
- 231100000719 pollutant Toxicity 0.000 claims abstract description 13
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000010992 reflux Methods 0.000 claims abstract description 9
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000004062 sedimentation Methods 0.000 claims description 51
- 230000002572 peristaltic effect Effects 0.000 claims description 30
- 229910052567 struvite Inorganic materials 0.000 claims description 25
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 claims description 22
- 238000007599 discharging Methods 0.000 claims description 17
- 239000002244 precipitate Substances 0.000 claims description 17
- 150000002500 ions Chemical class 0.000 claims description 16
- 238000005273 aeration Methods 0.000 claims description 14
- 239000013078 crystal Substances 0.000 claims description 9
- 238000001556 precipitation Methods 0.000 claims description 9
- 239000013049 sediment Substances 0.000 claims description 9
- -1 ammonium ions Chemical class 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 8
- 239000011347 resin Substances 0.000 claims description 8
- 229920005989 resin Polymers 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 230000001376 precipitating effect Effects 0.000 claims description 7
- 239000011777 magnesium Substances 0.000 claims description 6
- 238000001514 detection method Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 claims description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 4
- 238000004088 simulation Methods 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 230000002195 synergetic effect Effects 0.000 claims description 4
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 238000000265 homogenisation Methods 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 230000003311 flocculating effect Effects 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000002253 acid Substances 0.000 abstract description 2
- 238000005496 tempering Methods 0.000 abstract description 2
- 238000010791 quenching Methods 0.000 abstract 1
- 230000000171 quenching effect Effects 0.000 abstract 1
- 239000000203 mixture Substances 0.000 description 6
- 230000005684 electric field Effects 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000008394 flocculating agent Substances 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 229910000861 Mg alloy Inorganic materials 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 239000013043 chemical agent Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005370 electroosmosis Methods 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 229910001069 Ti alloy Inorganic materials 0.000 description 1
- VONLASUMRVUZLY-UHFFFAOYSA-N [Ir].[Ti].[Ta] Chemical compound [Ir].[Ti].[Ta] VONLASUMRVUZLY-UHFFFAOYSA-N 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 238000009297 electrocoagulation Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000001962 electrophoresis Methods 0.000 description 1
- 238000009393 electroremediation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000005067 remediation Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/45—Phosphates containing plural metal, or metal and ammonium
- C01B25/451—Phosphates containing plural metal, or metal and ammonium containing metal and ammonium
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/18—Alkaline earth metal compounds or magnesium compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F7/00—Aeration of stretches of water
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Hydrology & Water Resources (AREA)
- Life Sciences & Earth Sciences (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention provides an electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device and a method, the device comprises a pretreatment tank, a conical double-anode electrolytic tank and an inspection tank which are sequentially connected, wherein the pretreatment tank is respectively connected with an electric repair anode drainage pore water collection device and an electric repair cathode drainage pore water collection device through two water inlets; the upper part of the conical double-anode electrolytic cell is provided with an aluminum anode electrode plate, an inert cathode electrode plate and a magnesium-aluminum alloy anode electrode plate from the outside to the inside in sequence; the pretreatment tank adjusts the acid quenching and tempering to electronic drainage pore water, and toper double anode electrolytic cell carries out the flocculation separation of particulate form and dissolves attitude nitrogen phosphorus crystallization to electronic drainage pore water and retrieves in coordination, and the inspection pond detects quality of water, through feedback control sewage reflux ratio and regulation DC power supply voltage, realizes drainage pore water's purification. The invention realizes the classified removal of granular and dissolved pollutants in the electric drainage pore water and the cooperative recovery of nitrogen and phosphorus resources.
Description
Technical Field
The invention relates to the field of water resource protection and water environment treatment, in particular to an electric device and a method for recovering nitrogen and phosphorus from pore water through double anodes.
Background
Electrokinetic remediation is an in-situ remediation technology for sediments, which is gradually developed in recent years, and pollutants are subjected to electromigration, electroosmosis and other processes by applying an electric field, are gathered to two ends of an electrode and are then removed.
The patent with publication number CN207671889U discloses an in-situ reduction and decontamination device for polluted bottom mud of rivers and lakes based on drainage of pore water, which applies a low-voltage direct-current electric field to the bottom mud, makes pollutants migrate along with the pore water under the combined action of a gravity field, and collects the drained pore water. The electric drainage guide pore water has the following characteristics: (1) the ion composition is complex, and the ion composition not only contains ammonium ions and phosphate ions, but also contains a small amount of heavy metal ions and the like; (2) the dissolved nitrogen and phosphorus concentration in the discharged pore water is high, the pH difference of the two-pole discharged pore water is large, the pore water discharged by the anode is acidic, the pH value is less than 5, the total phosphorus concentration is 20-30mg/L, the total nitrogen concentration is 16-24mg/L, the pore water discharged by the cathode is alkaline, the pH value is more than 12, the total phosphorus concentration is 1-2mg/L, and the total nitrogen concentration is 140-170 mg/L; (3) due to electroosmosis, more pore water is drained by cathode conduction than by anode conduction, and the ion composition and concentration difference in the water in the cathode and anode conduction gaps are large, so that the quality of the sewage is difficult to adjust by simple mixing; (4) part of the particulate matter can migrate with the pore water under the action of electrophoresis, so that the content of particulate nitrogen and phosphorus in the drainage gap water is also higher. In conclusion, the electric drainage pore water has complex components and high nitrogen and phosphorus content, and needs a special process to treat the pore water so as to meet the requirement of environmental management.
For the recovery of nitrogen and phosphorus contaminants in water, patent publication No. CN213679897U discloses a device for recovering nitrogen and phosphorus from wastewater by struvite crystallization by adding chemical agents, such as MgO, Mg (OH) 2 The magnesium reacts with nitrogen and phosphorus in the sewage to generate magnesium ammonium phosphate, and nitrogen and phosphorus are recycled, so that the cost of the magnesium source is high. Go back toAnother method for collecting nitrogen and phosphorus in sewage is to apply an electric field, use metals such as aluminum, iron and the like as anodes, sacrifice the anodes to generate metal cation flocculants, and separate pollutants from water bodies in the modes of aggregating flocs, floating and the like. The patent with publication number CN210481103U discloses a wastewater treatment and purification system based on an electric flocculation technology, which adopts an integrated device, and the main purification principle is to sacrifice a metal anode to flocculate the pollutants, and to remove the pollutants through an inclined plate sedimentation tank under the action of a coagulation-assisting agent. The system has no special pretreatment tank, is difficult to solve the problem of complex water quality of drainage guide pore water, and has higher impurities in the sediment generated by flocculation. The patent of publication No. CN105174672A discloses a double-layer double-anode device for electrochemically removing and recovering sludge heavy metals, wherein a stainless steel electrode is adopted as a cathode, an iridium tantalum titanium alloy electrode is adopted as an anode, the device adopts double anodes to increase the reaction contact area, and the main technology is electromigration and ion selective permeation, so that the device is not suitable for sewage treatment; for the patent with publication number CN110357219A, an efficient nitrogen and phosphorus recovery electrochemical reaction system is disclosed, the device adopts a magnesium alloy rod-shaped anode and a stainless steel cathode design, electrodes are parallel and staggered and are vertical to the sewage flow direction, the main technical principle is that magnesium ions are provided for anode electrolysis for generating magnesium ammonium phosphate precipitate, but the device does not consider the problem of complex ion interference in sewage and cannot meet the requirements of the coordinated recovery of granular substances of drainage pore water and dissolved nitrogen, phosphorus.
The inventor of the application finds that the conventional electrocoagulation nitrogen and phosphorus cooperative recovery method has some problems through research in the process of implementing the invention: the method has higher requirements on the treatment of water quality, and is difficult to treat sewage with large pH change and complex ion composition; the pretreatment measures are single, classification treatment is not carried out according to the forms of pollutants, flocs are easily accumulated in an electric flocculation reaction zone, and the use efficiency of the electrode plate is influenced; the recovery method of crystallization precipitation can not be cooperated with the electric flocculation process, so that the purity of the recovered substances is low, and the dissolved nitrogen, nitrogen and phosphorus in the sewage are not fully utilized. Therefore, the sewage composition characteristics need to be fully considered for the treatment of the electric drainage and guide pore water, and the problems of acid regulation and tempering, particle separation, nitrogen and phosphorus cooperative recovery and the like are solved.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides the device and the method for recovering the nitrogen and phosphorus in the pore water through the cooperation of the double anodes of the electric drainage and guide, a flocculating agent is not required to be added, an electric field is applied to sacrifice the anodes to generate a metal cation flocculating agent, a sedimentation tank is arranged below an electrolytic tank, flocculation is effectively prevented from being deposited on a plate electrode, the electric energy utilization efficiency is improved, meanwhile, magnesium ammonium phosphate which can be recycled as a slow release fertilizer and aluminum phosphate with wide application are generated, the discharge problem of the pore water through electric drainage and guide is effectively solved, the operation cost is low, the maintenance is simple, and no chemical agent pollution exists.
In order to achieve the purpose, the invention adopts the technical scheme that:
an electric nitrogen and phosphorus double-anode collaborative recovery device for drainage pore water comprises a pretreatment tank, a conical double-anode electrolytic tank and an inspection tank which are sequentially connected, wherein the pretreatment tank is respectively connected with an electric restoration anode drainage pore water collection device and an electric restoration cathode drainage pore water collection device through two water inlets, and a first mechanical stirrer, a first pH sensor, an aerator pipe and ion selective adsorption resin are arranged in the pretreatment tank; the upper part of the conical double-anode electrolytic cell consists of three concentric annular electrode plates, namely an aluminum anode electrode plate, an inert cathode electrode plate and a magnesium-aluminum alloy anode electrode plate from outside to inside in sequence, and the lower part of the conical double-anode electrolytic cell is provided with a flocculation sedimentation tank and a crystallization sedimentation tank which are respectively arranged below the aluminum anode electrode plate and the inert cathode electrode plate; be equipped with third pH sensor, nitrogen phosphorus sensor, sewage reflux unit in the inspection pond, sewage reflux unit is arranged in will inspecting the sewage backward flow in the pond to toper double anode electrolytic cell according to the pH value and total nitrogen, total phosphorus concentration that third pH sensor, nitrogen phosphorus sensor detected.
Furthermore, two water inlets are including locating first water inlet and second water inlet on pretreatment tank upper portion, and first water inlet front end is led through first peristaltic pump and electronic restoration positive pole and is arranged pore water collection device and link to each other, and second water inlet front end is led through second peristaltic pump and electronic restoration negative pole and is arranged pore water collection device and link to each other.
Further, the pretreatment tank is provided with a pretreatment tank water outlet, the conical double-anode electrolytic tank is provided with an electrolytic tank water inlet, and the pretreatment tank water outlet is communicated with the electrolytic tank water inlet through a rubber hose; the conical double-anode electrolytic cell is provided with an electrolytic cell water outlet which is communicated with the inspection cell through an electrolytic cell water outlet conduit.
Further, the aluminum anode electrode plate is used for generating flocculated substances, and removing particulate pollutants in the sewage through electric flocculation; the inert cathode electrode plate is used for generating OH through electrolytic reaction - Providing a suitable alkaline environment for the electrolytic cell; the magnesium-aluminum alloy anode plate electrode is used for providing Mg 2+ Reacting with dissolved phosphate and ammonium ions in sewage to generate magnesium ammonium phosphate crystals, and dissolving Al from the electrode plates 3+ Flocs are generated under the action of the magnesium ammonium phosphate, and the magnesium ammonium phosphate is promoted to crystallize and precipitate.
Furthermore, the aluminum anode electrode plate and the magnesium-aluminum alloy anode electrode plate are respectively connected with the positive electrode of the direct-current stabilized power supply through a first lead and a second lead, the inert cathode electrode plate is connected with the negative electrode of the direct-current stabilized power supply through a third lead, and the voltage and the current of the direct-current stabilized power supply can be adjusted.
Furthermore, the conical double-anode electrolytic cell is provided with an electrolytic cell secondary treatment water inlet between the inert cathode electrode plate and the magnesium-aluminum alloy anode electrode plate, an electrolytic cell water outlet is arranged above the magnesium-aluminum alloy anode electrode plate, and the electrolytic cell water outlet is communicated with the inspection cell through an electrolytic cell water outlet conduit.
Furthermore, an inspection pool water outlet is formed in the rear end of the upper part of the inspection pool, and an inspection pool secondary sedimentation discharge port is formed below the inspection pool; and after the detection of the third pH sensor and the nitrogen and phosphorus sensor, the required pH value is between 6 and 9 and the total nitrogen and phosphorus concentrations are lower than the electric flocculation recovery threshold value, the pore water is discharged from a water outlet of the inspection pool, and if the total nitrogen and phosphorus concentrations are higher than the electric flocculation recovery threshold value, the pore water is guided to flow back from a secondary treatment water inlet of the electrolytic pool to enter the electrolytic pool again through a sewage return pipe by using a third peristaltic pump.
An electric pore water nitrogen and phosphorus double-anode collaborative recovery method is implemented by applying the device, and comprises the following steps:
s1, adding the cathode and anode electric drainage pore water into a pretreatment tank by using a first peristaltic pump and a second peristaltic pump, opening a first mechanical stirrer for homogenization, opening an aeration pipe, continuously aerating in the subsequent treatment process to promote uniform mixing of sewage, and properly adjusting pH;
s2, after the pH value of drainage guide pore water in the pretreatment tank is detected by the first pH sensor to be between 8 and 10.5, the drainage guide pore water passes through ion selective adsorption resin and is discharged into an electrolytic tank through a water outlet of the pretreatment tank;
s3, enabling drainage pore water to pass through an aluminum anode electrode plate in an electrolytic cell, flocculating particle suspended matters, precipitating in a flocculation sedimentation tank, discharging precipitates through a precipitation discharge port, enabling the precipitates to reach a magnesium-aluminum alloy anode electrode plate through an inert cathode electrode plate, reacting to generate magnesium ammonium phosphate and flocculates, precipitating in a crystallization sedimentation tank below, stirring slowly by a second mechanical stirrer in the crystallization sedimentation tank, and discharging the precipitates through a crystallization sedimentation discharge port;
s4, discharging pore water from a water outlet of the electrolytic cell, allowing the pore water to enter an inspection pool through a water outlet conduit of the electrolytic cell, detecting by a third pH sensor and a nitrogen and phosphorus sensor, when the pH value is within the range of 6-9 and the total nitrogen and phosphorus concentration flocculation recovery threshold value is reached, discharging the pore water from the water outlet of the inspection pool, if the pH value is higher than the threshold value, guiding the discharged pore water to flow back again from a secondary treatment water inlet of the electrolytic cell through a sewage return pipe by using a peristaltic pump to enter the electrolytic cell, fully reacting until the discharge requirement is met, discharging a small amount of sediment in the inspection pool through a secondary sedimentation discharge outlet of the inspection pool, and drying the sediment discharged from the sedimentation discharge outlet and the secondary sedimentation discharge outlet to obtain struvite crystals;
and S5, determining appropriate reaction time and electrolytic voltage under different nitrogen and phosphorus concentration conditions through an indoor simulation experiment, and changing the water inlet flow and the reflux ratio to realize the synergistic removal of nitrogen and phosphorus by adjusting the first peristaltic pump, the second peristaltic pump and the third peristaltic pump according to the detection results of the third pH sensor and the nitrogen and phosphorus sensor.
Due to the adoption of the scheme, the invention has the following beneficial effects:
(1) the pretreatment of the drainage guide pore water greatly improves the quality of sewage and the efficiency of subsequent reaction. The anode pore water which is electrically drained is acidic, the cathode pore water is alkaline, and the cathode drainage pore water is more than the anode pore water, so that the two-pole pore water is combined and then stirred and uniformly mixed to facilitate uniform treatment;
(2) according to the form classification control of the pollutants in the drainage guide pore water, the treatment efficiency of the device is improved. Removing granular impurities through the aluminum anode and then passing through the magnesium aluminum alloy anode, so that the purity of magnesium ammonium phosphate in the flocculation precipitate generated by the subsequent reaction is improved; through the magnesium-aluminum alloy anode, the synergistic effect of the recovery of dissolved nitrogen and phosphorus from magnesium ammonium phosphate crystals and flocs generated by electric flocculation is realized, and the crystallization and precipitation rate of magnesium ammonium phosphate is accelerated;
(3) through technical parameter optimization such as voltage and sewage reflux ratio, can realize that nitrogen phosphorus is high-efficient to be retrieved, adopt feedback control system, improved device degree of automation.
Drawings
Fig. 1 is a schematic structural diagram of one embodiment of the electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device.
In the figure: 1-a first peristaltic pump, 1-2-a second peristaltic pump, 1-3-a third peristaltic pump, 2-1-a first pretreatment tank water inlet, 2-a second pretreatment tank water inlet, 3-1-a first mechanical stirrer, 3-2-a second mechanical stirrer, 4-1-a first pH sensor, 4-2-a second pH sensor, 5-an overflow tank, 6-a pretreatment tank water outlet, 7-a rubber hose, 8-an electrolytic tank water inlet, 9-an electrolytic tank water outlet conduit, 10-an aluminum anode plate, 11-1-a first lead, 11-2-a second lead, 11-2-a third lead, 12-a direct current stabilized voltage power supply, 13-an inert cathode plate, 14-a magnesium aluminum alloy anode plate, 15-1-a flocculation sedimentation tank, 15-2-a crystallization sedimentation tank, 16-1-flocculation precipitation discharge port, 16-2-crystallization precipitation discharge port, 17-electrolytic cell water outlet, 18-nitrogen and phosphorus sensor, 19-inspection cell water outlet, 20-inspection cell secondary precipitation discharge port, 21-electrolytic cell secondary treatment water inlet, 22-aeration pipe, 23-secondary treatment water inlet conduit, 24-sewage return pipe, 25-pretreatment cell, 26-conical double anode electrolytic cell, 27-inspection cell, and 28-ion selective adsorption resin.
Detailed Description
The technical scheme of the invention is clearly and completely described below by combining the attached drawings.
Referring to fig. 1, an embodiment of the apparatus for recovering nitrogen and phosphorus by double anode cooperation for drainage and drainage of pore water of the present invention includes a pretreatment tank 25, a tapered double anode electrolytic cell 26, and an inspection tank 27, wherein the tapered double anode electrolytic cell 26 is connected to the pretreatment tank 25 and the inspection tank 27. Specifically, the pretreatment tank 25 is provided with a pretreatment tank water outlet 6, the conical double-anode electrolytic tank 26 is provided with an electrolytic tank water inlet 8, and the pretreatment tank water outlet 6 is communicated with the electrolytic tank water inlet 8 through a rubber hose 7; the conical double-anode electrolytic cell 26 is provided with an electrolytic cell water outlet 17, and the electrolytic cell water outlet 17 is communicated with the inspection cell 27 through an electrolytic cell water outlet conduit 9.
The upper part of the pretreatment tank 25 is provided with a first water inlet 2-1 and a second water inlet 2-2, the front end of the first water inlet 2-1 is connected with an electric restoration anode drainage pore water collection device through a first peristaltic pump 1-1, and the front end of the second water inlet 2-2 is connected with an electric restoration cathode drainage pore water collection device through a second peristaltic pump 1-2.
The pretreatment tank 25 is internally provided with a first mechanical stirrer 3-1, a first pH sensor 4-1 and an aeration pipe 22, the aeration pipe 22 can be designed to be vertically inserted, the aeration pipe 22 is provided with a small hole, and the top end of the aeration pipe 22 is connected with an air supply device. The outer side of the pretreatment tank 25 is provided with an overflow tank 5, and the overflow tank 5 is used for containing redundant pore water during slow aeration treatment. And a pretreatment tank water outlet 6 is arranged below the side edge of the pretreatment tank 25 and communicated with an electrolytic tank water inlet 8 of the conical double-anode electrolytic tank 26. The front end of the water outlet 6 of the pretreatment tank is provided with ion selective adsorption resin 28.
The coneThe double-anode electrolytic cell 16 is designed into a structure that the lower part is a cone and the upper part is a cylinder, the upper cylinder is composed of three concentric annular electrode plates, wherein the outermost layer is an aluminum anode electrode plate 10 which is mainly used for generating flocculation substances and removing granular pollutants in sewage through electric flocculation; the inert cathode electrode plate 13 is arranged in the middle, OH < - > is generated mainly through electrolytic reaction, and a proper alkaline environment is provided for the electrolytic cell 26; the inner layer is a magnesium-aluminum alloy anode electrode plate 14 which mainly provides Mg 2+ Reacting with dissolved phosphate and ammonium ions in sewage to generate magnesium ammonium phosphate crystals, and dissolving Al from the electrode plates 3+ Flocs are generated under the action of the magnesium ammonium phosphate, and the magnesium ammonium phosphate is promoted to crystallize and precipitate. Electrode plates with different diameters can be properly replaced according to the sewage composition for adjusting the distance between the electrode plates. The aluminum anode electrode plate 10 and the magnesium-aluminum alloy anode electrode plate 14 are respectively connected with the positive electrode of a direct current stabilized power supply 12 through a first lead 11-1 and a second lead 11-2, the inert cathode electrode plate 13 is connected with the negative electrode of the direct current stabilized power supply 12 through a third lead 11-3, and the voltage and the current of the direct current stabilized power supply 12 are adjustable.
The lower cone of the conical double-anode electrolytic cell 26 is a funnel-shaped sedimentation tank and is positioned below the corresponding electrode plate, specifically, a flocculation sedimentation tank 15-1 and a crystallization sedimentation tank 15-2 are respectively arranged below the aluminum anode electrode plate 10 and the inert cathode electrode plate 13 in the conical double-anode electrolytic cell 26, namely, the crystallization sedimentation tank 15-2 is arranged between the innermost aluminum-magnesium alloy anode electrode plate 14 and the inert cathode electrode plate 13, the flocculation sedimentation tank 15-1 is arranged between the outermost aluminum anode electrode plate 10 and the inert cathode electrode plate 13, and the flocculation sedimentation tank 15-1 and the crystallization sedimentation tank 15-2 are respectively used for collecting particle pollutants and ammonium magnesium phosphate crystal sediment.
The crystallization and sedimentation tank 15-2 is internally provided with a second mechanical stirrer 3-2 and a second pH sensor 4-2, the second mechanical stirrer 3-2 runs at a low speed, a flocculation and sedimentation discharge port 16-1 and a crystallization and sedimentation discharge port 16-2 are respectively arranged below the flocculation and sedimentation tank 15-1 and the crystallization and sedimentation tank 15-2, and valves are respectively arranged at the sedimentation discharge ports.
The conical double-anode electrolytic cell 26 is provided with an electrolytic cell secondary treatment water inlet 21 between the inert cathode electrode plate 13 and the magnesium-aluminum alloy anode electrode plate 14, and an electrolytic cell water outlet 17 is arranged above the magnesium-aluminum alloy anode electrode plate 14. The electrolytic cell water outlet 17 is arranged at the top of the innermost cylinder of the conical double-anode electrolytic cell 26 and is used for connecting the inspection cell 27.
The inspection tank 27 is also provided with a sewage return pipe 24, the sewage return pipe 24 is connected with the secondary treatment water inlet 21 of the electrolytic tank through a conduit 23, and the conduit 23 is provided with a third peristaltic pump 1-3.
The embodiment of the invention also provides an electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery method, which is carried out by adopting the device shown in FIG. 1, and the method comprises the following steps:
s1, adding the cathode and anode electric drainage pore water into the pretreatment tank 25 by using the first peristaltic pump 1-1 and the second peristaltic pump 1-2, starting the first mechanical stirrer 3-1 for homogenization, starting the aeration pipe 22 and continuously aerating in the subsequent treatment process to promote uniform mixing of the sewage and properly adjust the pH.
The pretreatment tank 25 is used for mixing and adjusting the discharged bipolar pore water, the front end of the first water inlet 2-1 is connected with an electric restoration anode drainage pore water collection device, the front end of the second water inlet 2-2 is connected with an electric restoration cathode drainage pore water collection device, the first water inlet 1-1 and the second water inlet 2-2 are respectively used for adding the drainage pore water into the pretreatment tank 25 through the first peristaltic pump 1-1 and the second peristaltic pump 1-2, the liquid is uniformly mixed through the first mechanical stirrer 3-1, the first pH sensor 4-1 needs to be calibrated before use, a probe is immersed into the liquid in the pretreatment tank 25 during use, aeration holes are formed in the aeration pipe 22, the top end of the aeration pipe is connected with a gas supply device, and the overflow tank 5 is used for containing redundant pore water when aeration treatment is slow.
S2, after the pH value of drainage guide pore water in the pretreatment tank 25 is detected by the first pH sensor 4-1 to be between 8 and 10.5, the drainage guide pore water passes through the ion selective adsorption resin 28 and is discharged into the electrolytic tank (26) through the pretreatment tank water outlet 6; the aerated drainage pore water passes through a specific ion selective adsorption resin 28 to remove a small amount of ions such as redundant heavy metal ions.
S3, conducting and draining pore water in an electrolytic tank 26, enabling the pore water to pass through an aluminum anode electrode plate 10 to flocculate particle suspended matters, precipitating in a flocculation sedimentation tank 15-1, discharging precipitates through a precipitation discharge port 16-1, enabling the precipitates to pass through an inert cathode electrode plate 13 to reach a magnesium aluminum alloy anode electrode plate 14, reacting to generate magnesium ammonium phosphate and flocculates, precipitating in a crystallization sedimentation tank 15-2 below, stirring slowly by a second mechanical stirrer 3-2 in the crystallization sedimentation tank 15-2 to facilitate crystallization of the magnesium ammonium phosphate, and discharging the precipitates through a crystallization sedimentation discharge port 16-2.
In the electrolytic cell 26, the aluminum anode electrode plate 10 and the magnesium-aluminum alloy anode electrode plate 14 are respectively connected with the positive electrode of the direct current stabilized power supply 12 through a first lead 11-1 and a second lead 11-2, the inert cathode electrode plate 13 is connected with the negative electrode of the direct current stabilized power supply 12 through a third lead 11-3, and the direct current stabilized power supply 12 is adjustable in voltage and current and has a digital display function. After entering the electrolytic tank 26, the drainage pore water passes through the outer aluminum anode electrode plate 10, the suspended particles in the sewage and the dissolved aluminum ions generate flocculation reaction, and the generated flocculate is precipitated in the flocculation sedimentation tank 15-1, so that the particulate matters in the sewage are removed. Then leading and draining pore water to reach a magnesium-aluminum alloy electrode plate 14 through an inert cathode electrode plate 13, reacting dissolved nitrogen and phosphorus in sewage with magnesium ions to generate magnesium ammonium phosphate, precipitating to a lower crystallization sedimentation tank 15-2 under the action of floc generated by aluminum ions, arranging a second mechanical stirrer 3-2 in the crystallization sedimentation tank 15-2, stirring at a slow speed to facilitate the formation of crystals, and discharging precipitates in the flocculation sedimentation tank 15-1 and the crystallization sedimentation tank 15-2 through a flocculation sedimentation discharge port 16-1 and a crystallization sedimentation discharge port 16-2 respectively.
S4, discharging pore water from the water outlet 17 of the electrolytic cell, entering the inspection pool 27 through the water outlet conduit 9 of the electrolytic cell, detecting by the third pH sensor 4-3 and the nitrogen and phosphorus sensor 18, discharging from the water outlet 19 of the inspection pool after reaching the flocculation recovery threshold (determined by simulation test) of the required pH value within the range of 6-9 and the total nitrogen and total phosphorus concentration, if the threshold is higher than the threshold, guiding and discharging the pore water, reflowing again from the secondary treatment water inlet 21 of the electrolytic cell into the electrolytic cell (26) through the sewage backflow pipe 24 by the third peristaltic pump 1-3, fully reacting until meeting the discharge requirement, discharging a small amount of sediment in the inspection pool through the secondary sedimentation discharge outlet 20 of the inspection pool, and drying the sediment discharged from the sedimentation discharge outlet 16 and the secondary sedimentation discharge outlet (20) to obtain crystals such as struvite.
And S5, determining appropriate reaction time and electrolytic voltage under different nitrogen and phosphorus concentration conditions through indoor simulation experiments. According to the detection results of the third pH sensor 4-3 and the nitrogen and phosphorus sensor (18), the water inlet flow and the reflux ratio are changed by adjusting the peristaltic pumps (1-1, 1-2 and 1-3) to realize the synergistic removal of nitrogen and phosphorus.
The invention solves the practical problem of electric drainage treatment, uses a conical double-anode electrolytic cell design, utilizes an outer aluminum anode electrode plate to generate an electric flocculation effect to realize the rapid separation of particle pollutants in sewage, then utilizes an inner-measuring magnesium-aluminum alloy anode electrode plate to dissolve out magnesium ions and aluminum ions, leads nitrogen and phosphorus dissolved in water to form magnesium ammonium phosphate precipitate, and rapidly crystallizes and precipitates under the hydrolysis effect of the aluminum ions. The pollution particles of the flocculation precipitation and the recovery products of the crystallization and flocculation are classified and recovered through the inner and outer cone barrels, and the removal of particulate impurities in the drainage guide pore water and the cooperative recovery of nitrogen are realized.
The above description is only an embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (8)
1. The utility model provides an electronic drainage pore water nitrogen phosphorus anodal recovery unit in coordination which characterized in that: the device comprises a pretreatment tank, a conical double-anode electrolytic tank and an inspection tank which are sequentially connected, wherein the pretreatment tank is respectively connected with an electric restoration anode drainage pore water collection device and an electric restoration cathode drainage pore water collection device through two water inlets, and a first mechanical stirrer, a first pH sensor, an aeration pipe and ion selective adsorption resin are arranged in the pretreatment tank; the upper part of the conical double-anode electrolytic cell consists of three concentric annular electrode plates, namely an aluminum anode electrode plate, an inert cathode electrode plate and a magnesium-aluminum alloy anode electrode plate from outside to inside in sequence, and the lower part of the conical double-anode electrolytic cell is provided with a flocculation sedimentation tank and a crystallization sedimentation tank which are respectively arranged below the aluminum anode electrode plate and the inert cathode electrode plate; be equipped with third pH sensor, nitrogen phosphorus sensor, sewage reflux unit in the inspection pond, sewage reflux unit is arranged in will inspecting the sewage backward flow in the pond to toper double anode electrolytic cell according to the pH value and total nitrogen, total phosphorus concentration that third pH sensor, nitrogen phosphorus sensor detected.
2. The electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device of claim 1, characterized in that: the two water inlets comprise a first water inlet and a second water inlet which are arranged on the upper portion of the pretreatment tank, the front end of the first water inlet is connected with the electric repair anode drainage guide pore water collecting device through a first peristaltic pump, and the front end of the second water inlet is connected with the electric repair cathode drainage guide pore water collecting device through a second peristaltic pump.
3. The electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device of claim 1, characterized in that: the pretreatment tank is provided with a pretreatment tank water outlet, the conical double-anode electrolytic tank is provided with an electrolytic tank water inlet, and the pretreatment tank water outlet is communicated with the electrolytic tank water inlet through a rubber hose; the conical double-anode electrolytic cell is provided with an electrolytic cell water outlet which is communicated with the inspection cell through an electrolytic cell water outlet conduit.
4. The electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device of claim 1, characterized in that: the aluminum anode electrode plate is used for generating flocculated substances and removing granular pollutants in the sewage through electric flocculation; the inert cathode electrode plate is used for generating OH through electrolytic reaction - Providing a suitable alkaline environment for the electrolytic cell; the magnesium-aluminum alloy anode plate electrode is used for providing Mg 2+ Reacting with dissolved phosphate and ammonium ions in sewage to generate magnesium ammonium phosphate crystals, and dissolving Al from the electrode plates 3+ Flocs are generated under the action of the magnesium ammonium phosphate, and the magnesium ammonium phosphate is promoted to crystallize and precipitate.
5. The electric double-anode nitrogen and phosphorus cooperative recovery device for drainage and conduction pore water as claimed in claim 1, is characterized in that: the aluminum anode electrode plate and the magnesium-aluminum alloy anode electrode plate are respectively connected with the positive electrode of the direct current stabilized power supply through a first lead and a second lead, the inert cathode electrode plate is connected with the negative electrode of the direct current stabilized power supply through a third lead, and the voltage and the current of the direct current stabilized power supply can be adjusted.
6. The electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device of claim 1, characterized in that: the conical double-anode electrolytic cell is characterized in that an electrolytic cell secondary treatment water inlet is formed between the inert cathode electrode plate and the magnesium-aluminum alloy anode electrode plate, an electrolytic cell water outlet is formed above the magnesium-aluminum alloy anode electrode plate, and the electrolytic cell water outlet is communicated with the inspection cell through an electrolytic cell water outlet conduit.
7. The electric drainage pore water nitrogen and phosphorus double-anode cooperative recovery device of claim 1, characterized in that: the rear end of the upper part of the inspection pool is provided with an inspection pool water outlet, and an inspection pool secondary sedimentation outlet is arranged below the inspection pool; and after the detection of the third pH sensor and the nitrogen and phosphorus sensor, the required pH value is between 6 and 9 and the total nitrogen and phosphorus concentrations are lower than the electric flocculation recovery threshold value, the pore water is discharged from a water outlet of the inspection pool, and if the total nitrogen and phosphorus concentrations are higher than the electric flocculation recovery threshold value, the pore water is guided to flow back from a secondary treatment water inlet of the electrolytic pool to enter the electrolytic pool again through a sewage return pipe by using a third peristaltic pump.
8. An electric pore water nitrogen and phosphorus double-anode collaborative recovery method, which is implemented by the device of any one of claims 1-7, and is characterized in that: the method comprises the following steps:
s1, adding the cathode and anode electric drainage pore water into a pretreatment tank by using a first peristaltic pump and a second peristaltic pump, opening a first mechanical stirrer for homogenization, opening an aeration pipe, continuously aerating in the subsequent treatment process to promote uniform mixing of sewage, and properly adjusting pH;
s2, after the pH value of drainage guide pore water in the pretreatment tank is detected by the first pH sensor to be between 8 and 10.5, the drainage guide pore water passes through ion selective adsorption resin and is discharged into an electrolytic tank through a water outlet of the pretreatment tank;
s3, enabling drainage pore water to pass through an aluminum anode electrode plate in an electrolytic cell, flocculating particle suspended matters, precipitating in a flocculation sedimentation tank, discharging precipitates through a precipitation discharge port, enabling the precipitates to reach a magnesium-aluminum alloy anode electrode plate through an inert cathode electrode plate, reacting to generate magnesium ammonium phosphate and flocculates, precipitating in a crystallization sedimentation tank below, stirring slowly by a second mechanical stirrer in the crystallization sedimentation tank, and discharging the precipitates through a crystallization sedimentation discharge port;
s4, discharging pore water from a water outlet of the electrolytic cell, allowing the pore water to enter an inspection pool through a water outlet conduit of the electrolytic cell, detecting by a third pH sensor and a nitrogen and phosphorus sensor, when the pH value is within the range of 6-9 and the total nitrogen and phosphorus concentration flocculation recovery threshold value is reached, discharging the pore water from the water outlet of the inspection pool, if the pH value is higher than the threshold value, guiding the discharged pore water to flow back again from a secondary treatment water inlet of the electrolytic cell through a sewage return pipe by using a peristaltic pump to enter the electrolytic cell, fully reacting until the discharge requirement is met, discharging a small amount of sediment in the inspection pool through a secondary sedimentation discharge outlet of the inspection pool, and drying the sediment discharged from the sedimentation discharge outlet and the secondary sedimentation discharge outlet to obtain struvite crystals;
and S5, determining appropriate reaction time and electrolytic voltage under different nitrogen and phosphorus concentration conditions through an indoor simulation experiment, and changing the water inlet flow and the reflux ratio to realize the synergistic removal of nitrogen and phosphorus by adjusting the first peristaltic pump, the second peristaltic pump and the third peristaltic pump according to the detection results of the third pH sensor and the nitrogen and phosphorus sensor.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005177681A (en) * | 2003-12-22 | 2005-07-07 | Bio Carrier Technology:Kk | Air bubble generator and electric floatation method |
| US20140021057A1 (en) * | 2012-07-23 | 2014-01-23 | Abderrazak Berrak | Method for simultaneous elimination of orthophosphate and ammonium using electrolytic process |
| CN105668717A (en) * | 2016-04-12 | 2016-06-15 | 景德镇陶瓷学院 | Magnesium ammonium phosphate-electrooxidation integrated device and simultaneous nitrogen and phosphorus removing method thereof |
| CN107746163A (en) * | 2017-11-22 | 2018-03-02 | 长江水利委员会长江科学院 | A kind of dystrophication sediment in-situ decrement decontamination apparatus based on pore water guide |
| CN109607990A (en) * | 2018-12-29 | 2019-04-12 | 博域环保技术研究院(南京)有限公司 | A kind of heavily contaminated river bottom mud electrolysis nitrogen consolidates the processing method of phosphorus |
| CN112125483A (en) * | 2020-08-31 | 2020-12-25 | 同济大学 | Synchronous recovery processing method for nitrogen and phosphorus in high-solid anaerobic digestion sludge |
| CN212770001U (en) * | 2020-04-16 | 2021-03-23 | 王招 | Electrochemical synchronous denitrification and dephosphorization device |
-
2022
- 2022-04-22 CN CN202210428758.XA patent/CN114853235A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005177681A (en) * | 2003-12-22 | 2005-07-07 | Bio Carrier Technology:Kk | Air bubble generator and electric floatation method |
| US20140021057A1 (en) * | 2012-07-23 | 2014-01-23 | Abderrazak Berrak | Method for simultaneous elimination of orthophosphate and ammonium using electrolytic process |
| CN105668717A (en) * | 2016-04-12 | 2016-06-15 | 景德镇陶瓷学院 | Magnesium ammonium phosphate-electrooxidation integrated device and simultaneous nitrogen and phosphorus removing method thereof |
| CN107746163A (en) * | 2017-11-22 | 2018-03-02 | 长江水利委员会长江科学院 | A kind of dystrophication sediment in-situ decrement decontamination apparatus based on pore water guide |
| CN109607990A (en) * | 2018-12-29 | 2019-04-12 | 博域环保技术研究院(南京)有限公司 | A kind of heavily contaminated river bottom mud electrolysis nitrogen consolidates the processing method of phosphorus |
| CN212770001U (en) * | 2020-04-16 | 2021-03-23 | 王招 | Electrochemical synchronous denitrification and dephosphorization device |
| CN112125483A (en) * | 2020-08-31 | 2020-12-25 | 同济大学 | Synchronous recovery processing method for nitrogen and phosphorus in high-solid anaerobic digestion sludge |
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