CN112897675B - Device for synchronously recovering nitrogen source in carbon-nitrogen separation treatment of high-salt landfill leachate concentrated solution - Google Patents
Device for synchronously recovering nitrogen source in carbon-nitrogen separation treatment of high-salt landfill leachate concentrated solution Download PDFInfo
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
Abstract
The invention provides a device for synchronously recovering nitrogen sources in carbon-nitrogen separation treatment of high-salt landfill leachate concentrated solution, which comprises an ozone oxidation stripping tower, and an automatic defoaming agent feeding module, a leachate concentrated solution external circulation module and a negative pressure nitrogen source recovery module which are respectively connected with the ozone oxidation stripping tower; the inside of ozone oxidation air stripping tower is provided with: a first stirring device; the percolate concentrate spraying device is connected with the output end of the percolate concentrate external circulation module; the micro-bubble aeration disc is connected with an external ozone source; the input end of the percolate concentrated solution external circulation module is connected with the lower part of the ozone oxidation stripping tower, and the automatic defoaming agent feeding module and the negative pressure nitrogen source recovery module are connected with the upper part of the ozone oxidation stripping tower. The invention realizes the carbon-nitrogen separation treatment and the nitrogen source recovery of the percolate concentrate, has the advantages of high operation efficiency and small occupied area, and is an environment-friendly technology with good development prospect.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a treatment device for landfill leachate, and particularly relates to a device for synchronously recovering a nitrogen source in the carbon-nitrogen separation treatment of high-salt landfill leachate concentrated solution.
Background
The standard-reaching treatment of the landfill leachate becomes an important measurement index of the sanitary landfill at the present stage, and the application of the membrane technology in the treatment of the leachate effectively solves the problem that the effluent reaches the standard (the pollutant control standard of the domestic landfill site GB 16889-2008). However, the resultant concentrated percolate has become a bottleneck restricting the application of membrane technology due to its characteristics such as complex water quality, high salt content and poor biodegradability. The recharge is used as a concentrated solution treatment mode most applied to actual engineering in China, organic matters and nitrogen pollutants are obviously removed, but salt and heavy metals in the concentrated solution are gradually accumulated, after the concentrated solution enters a treatment system of percolate, the performance of microorganisms in a normal biochemical treatment process is influenced, further vicious circle is achieved, and a large amount of concentrated solution with high salt, high ammonia nitrogen and high organic matters needs to be solved urgently.
Aiming at the concentrated solution with high salt, high ammonia nitrogen and high organic matter, the main treatment process at the present stage comprises the following steps: (1) The evaporation technology can effectively and synchronously remove ammonia nitrogen and crystallized salt, but the evaporation efficiency can be greatly reduced due to the high organic matter content, the operation cost is improved, meanwhile, the evaporator is seriously corroded, and the operation is difficult to continue and stabilize. (2) The ion exchange technology can selectively perform enrichment on organic matters, ammonia nitrogen and inorganic salt ions in the concentrated solution, but the treatment of the organic matters and heavy metals in the regenerated waste liquid is also a difficult problem of the ion exchange technology. (3) The back-spraying incineration technology is mainly applied to the condition that a landfill site is adjacent to a garbage incineration facility, has simple operation and less early investment, is suitable for occasions with low concentrated solution yield and high garbage heat value, and can be subjected to acid corrosion and salt corrosion like the evaporation technology. (4) The advanced oxidation technology has certain advantages for the treatment of substances which are difficult to degrade or toxic to organisms, and opens up a new idea for the treatment of the percolation concentrate. Common advanced oxidation technologies comprise a Fenton method, a photocatalytic oxidation method, an ozone oxidation method and the like, the advantages and the disadvantages of different advanced oxidation technologies are different, the ozone oxidation method has the characteristics of high efficiency, easy control, environmental friendliness and the like, is feasible in economy and technology, and is an advanced technology which has development prospect and accords with green environmental protection.
Patent document CN111606457A discloses an advanced oxidation treatment device and process for leachate concentrate, which can improve the utilization efficiency of ozone by improving the contact between ozone and leachate, and can effectively improve the degradation of organic matters in the concentrate by ozone, but does not consider the removal and conversion of ammonia nitrogen therein, so that there is a need for an advanced oxidation treatment device for leachate concentrate, which can synchronously solve the problems of removal of high organic matters and removal/recovery of ammonia nitrogen.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a device for synchronously recovering a nitrogen source in the carbon-nitrogen separation treatment of a high-salt landfill leachate concentrated solution.
The device for synchronously recovering the nitrogen source by the carbon-nitrogen separation treatment of the high-salt landfill leachate concentrated solution comprises an ozone oxidation stripping tower, and an automatic defoaming agent feeding module, a leachate concentrated solution external circulation module and a negative pressure nitrogen source recovery module which are respectively connected with the ozone oxidation stripping tower;
the inside of ozone oxidation air stripping tower is provided with:
a first stirring device;
the percolate concentrate spraying device is connected with the output end of the percolate concentrate external circulation module;
the micro-bubble aeration disc is connected with an external ozone source;
the input end of the percolate concentrated solution external circulation module is connected with the lower part of the ozone oxidation stripping tower, and the automatic defoaming agent feeding module and the negative pressure nitrogen source recovery module are connected with the upper part of the ozone oxidation stripping tower.
Preferably, the first stirring device comprises a first stirring shaft;
the percolate concentrate spray device comprises: the circular guide pipe and the umbrella-shaped spray header;
the annular guide pipe is arranged around the periphery of the first stirring shaft, and the umbrella-shaped spray headers are distributed on the annular guide pipe.
Preferably, the automatic defoaming agent adding module comprises: the system comprises a time relay, a vacuum pump, a defoaming agent tank and a defoaming agent spray header;
the spray header is arranged in the ozone oxidation stripping tower, the defoaming agent tank is connected with the defoaming agent spray header through the vacuum pump, and the time relay is electrically connected with the vacuum pump.
Preferably, the percolate concentrate external circulation module comprises: an external circulation tank for percolate;
the leachate external circulation tank is connected with the lower part of the ozone oxidation stripping tower through a first guide pipe, and is connected with the leachate concentrated solution spraying device through a second guide pipe;
a sludge-water separation inclined plate, a second stirring device and a pH regulating device are arranged in the percolate external circulation tank;
the lower end of the mud-water separation sloping plate is provided with a mud pipe.
Preferably, the pH adjusting means comprises: a pH probe, a pH determinator, an automatic switch, a pH regulation spray head, a pH regulation pump and a pH regulation liquid tank;
the pH probe and the pH regulation spray header are arranged in the leachate external circulation tank, the pH regulation liquid tank is connected with the pH regulation spray header through the pH regulation pump, the pH regulation pump is electrically connected with the automatic switch, the automatic switch is electrically connected with the pH tester, and the pH tester is connected with the pH probe.
Preferably, the negative pressure nitrogen source recovery module comprises: a nitrogen source recovery tank, a negative pressure fan and a second micro-bubble aeration head;
the second micro-bubble aeration head is positioned in the nitrogen source recovery tank, the second micro-bubble aeration head is connected with the ozone oxidation stripping tower through an air outlet pipe, and the negative pressure fan is arranged on the air outlet pipe;
and the nitrogen source recovery tank is provided with an air outlet and a water outlet.
Preferably, the ozone oxidation stripping tower is of a cylindrical structure, is made of organic glass, polyvinyl chloride, polytetrafluoroethylene or perfluoroalkoxy resin, and is set to be 8/1-12/1 in height-diameter ratio.
Preferably, the microbubble aeration disc is made of titanium, the plurality of umbrella-shaped parallel aeration heads with the aperture of 0.20-0.45 μm are connected, and the size of the generated microbubbles is less than 100nm.
Preferably, the percolate concentrate spraying device is arranged at 1/5-1/4 of the upper part of the ozone oxidation stripping tower.
Preferably, the defoamer is ejected from the defoamer self-dosing module in a parabolic pattern.
Compared with the prior art, the invention has the following beneficial effects:
1. the treatment device has the advantages of high operation efficiency and small occupied area, and can effectively remove organic matters in the concentrated solution and recycle the nitrogen source in the concentrated solution by synchronously utilizing the oxidation and stripping capabilities of ozone.
2. The pH value is controlled to be 10.5, which is not only beneficial to converting ozone into strong oxidability, \96794, effectively improving the oxidation capacity by OH conversion, but also beneficial to blowing off ammonia nitrogen.
Drawings
Other features, objects and advantages of the invention will become more apparent upon reading of the detailed description of non-limiting embodiments with reference to the following drawings:
FIG. 1 is a schematic view of the present invention.
Detailed Description
The present invention will be described in detail with reference to specific examples. The following examples will aid those skilled in the art in further understanding the present invention, but are not intended to limit the invention in any manner. It should be noted that it would be obvious to those skilled in the art that various changes and modifications can be made without departing from the spirit of the invention. All falling within the scope of the present invention.
As shown in figure 1, the invention provides a device for synchronously recovering a nitrogen source in carbon-nitrogen separation treatment of landfill leachate concentrate, which comprises an ozone oxidation stripping tower 1, an automatic defoaming agent feeding module 2, a leachate concentrate external circulation module and a negative pressure nitrogen source recovery module. The system comprises an ozone stripping tower 1, an automatic defoaming agent adding module 2, an leachate concentrated solution external circulation module, a negative pressure nitrogen source recovery module and a control module, wherein the ozone stripping tower 1 is used for degrading organic matters in leachate and separating and converting ammonia nitrogen, the automatic defoaming agent adding module is used for preventing a large amount of foams generated by introducing ozone from overflowing, the leachate concentrated solution external circulation module is used for adjusting the pH value under the optimal efficiency of ozone oxidation and ammonia nitrogen stripping, and the negative pressure nitrogen source recovery module is used for collecting ammonia nitrogen after stripping and converting. The treated garbage seepsThe ammonia nitrogen of the filtrate concentrate is 3000-10000mg/L and the COD is Cr Is 5000-20000mg/L.
Ozone oxidation blows and takes off tower 1 and is hollow cylinder structure, and inside is provided with: a first stirring device, a concentrate fountain of the diafiltration solution, and a micro-bubble aeration basin 106.
The first stirring device comprises a first stirring shaft 102. The first stirring shaft 102 extends into the ozone oxidation stripping tower 1 from top to bottom, the first stirring shaft 102 is driven by the first motor 101, and the first stirring shaft 102 is provided with a stirring paddle 105.
The concentrate sprinkler of infiltration liquid connects the output of the concentrate extrinsic cycle module of infiltration liquid, includes: a circular guide pipe 103 and an umbrella-shaped spray header 104; the circular guide pipe 103 is arranged around the periphery of the first stirring shaft 102, and the umbrella-shaped spray headers 104 are distributed on the circular guide pipe 103.
The micro-bubble aeration disc 106 is arranged at the bottom in the ozone oxidation stripping tower 1, and the micro-bubble aeration disc 106 is connected with an external ozone generator through an air inlet pipe 107.
The automatic defoaming agent adding module 2 comprises: a time relay 201, a vacuum pump 202, an antifoaming agent tank 203 and an antifoaming agent shower head 204. The spray header 204 is arranged in the ozone oxidation stripping tower 1, the defoaming agent tank 203 is connected with the defoaming agent spray header 204 through the defoaming agent vacuum pump 202, and the time relay 201 is electrically connected with the defoaming agent vacuum pump 202. The spray header 204 is arranged on the side wall of the ozone oxidation stripping tower 1, and the defoaming agent is sprayed out from the spray header in a parabolic form.
The percolate concentrate external circulation module comprises a percolate external circulation tank 3. The percolate external circulation tank 3 is connected with the lower part of the ozone oxidation stripping tower 1 through a first guide pipe 301, and the percolate external circulation tank 3 is connected with a percolate concentrate spraying device through a second guide pipe 312; a mud-water separation inclined plate 314, a second stirring device and a pH regulation device are arranged in the percolate external circulation tank 3; the lower end of the mud-water separation sloping plate 314 is provided with a mud pipe 303. The first draft tube 301 is provided with a first vacuum pump 302, and the second draft tube 312 is provided with a second vacuum pump 313.
Specifically, the pH adjusting device includes: a pH probe 304, a pH determinator 305, an automatic switch 306, a pH regulation spray head 307, a pH regulation pump 308 and a pH regulation liquid tank 309. The pH probe 304 and the pH regulation spray header 307 are arranged in the leachate external circulation tank 3, the pH regulation liquid tank 309 is connected with the pH regulation spray header 307 through a pH regulation pump 308, the pH regulation pump 308 is electrically connected with an automatic switch 306, the automatic switch 306 is electrically connected with a pH tester 305, and the pH tester 305 is connected with the pH probe 304. The second stirring device comprises a second stirring shaft 311, which is driven by a second motor 310.
The negative pressure nitrogen source recovery module comprises: a nitrogen source recovery tank 4, a negative pressure air blower 401, and a second micro-bubble aeration head 402. The second micro-bubble aeration head 402 is positioned in the nitrogen source recovery tank 4, the second micro-bubble aeration head 402 is connected with the ozone oxidation stripping tower 1 through an air outlet pipe 108, and the negative pressure fan is arranged on the air outlet pipe 108; the nitrogen source recovery tank 4 is provided with a gas outlet 404 and a water outlet 403.
Garbage leachate concentrate continuous outer loop adjusts pH, adopts leachate concentrate shower head 104 downstream in ozone oxidation blows off tower 1, with microbubble ozone that microbubble aeration dish 106 produced the upward movement realizes abundant convection current contact reaction, utilizes the oxidative treatment organic matter of ozone, utilizes ozone to blow off ammonia nitrogen and with its oxidation to nitrogen oxide in step, utilizes negative pressure environment to absorb nitrogen oxide to nitrogen source recovery canning dilute nitric acid, realizes carbon nitrogen separation and nitrogen source recovery and retrieves dilute nitric acid
The ozone oxidation stripping tower 1 is made of organic glass, polyvinyl chloride, polytetrafluoroethylene or perfluoroalkoxy resin, and the height-diameter ratio is set to be 8/1-12/1. The microbubble aeration discs 106 and 402 are made of titanium and are provided with a plurality of umbrella-shaped parallel aeration heads with the aperture of 0.20-0.45 μm, and the size of the generated microbubbles is less than 100nm. The number of the stirring paddles 105 of the stirring device is 4-8, and the types of the stirring paddles are selected from straight blade turbine paddles, inclined blade turbine paddles, folding blade turbine paddles, semicircular pipe type turbine paddles, downward pressing type turbine paddles, boolean Makino paddles and the like. The percolate concentrate spray devices 103 and 104 are arranged at 1/5-1/4 of the upper end of the ozone oxidation stripping tower 1.
The pH value of the landfill leachate concentrated solution is adjusted through continuous external circulation, the leachate concentrated solution spray head moves downwards in the ozone oxidation stripping tower, full convection contact reaction is achieved through microbubble ozone which moves upwards generated by the microbubble aeration disc, organic matters are removed through the oxidizability of the ozone, ammonia nitrogen is stripped through the ozone synchronously and oxidized to nitrogen oxide, and the nitrogen oxide is absorbed to the nitrogen source recovery tank to prepare dilute nitric acid through a negative pressure environment.
In a practical environment, the invention gives practical operation results of 3 examples as follows:
example 1
Concentrated solution (COD) of percolate emergency device of certain refuse landfill Cr 10500mg/L, 3850mg/L of ammonia nitrogen and 80mS/cm of conductivity), and adopting the process device shown in figure 1 for treatment, wherein the main process parameters are as follows: the treated water volume is 5L, the diameter of the ozone oxidation stripping tower is 10cm, the height-diameter ratio is 8, the material of the microbubble aeration disc is titanium, the ozone concentration is 80mg/L, the flow rate is 1L/min, the format of the stirring paddle is set to 4 straight-blade turbine paddles, the rotating speed is 25r/min, the circulating flow rate of the percolate is 5L/min, the pH is automatically controlled and adjusted to 10.5, the reaction time is 120min, the COD removal rate of the final effluent is 62.3%, and the nitrogen recovery rate can reach 70.5%.
Example 2
Percolate Concentrate (COD) of certain refuse landfill Cr 20000mg/L, 8000mg/L ammonia nitrogen and 40mS/cm conductivity) is treated by the process device shown in figure 1, and the main process parameters are as follows: the treated water volume is 5L, the diameter of the ozone oxidation stripping tower is 8cm, the height-diameter ratio is 10, the material of the microbubble aeration disc is titanium, the ozone concentration is 120mg/L, the flow rate is 0.5L/min, the format of the stirring paddle is set to be 6 folding turbine paddles, the rotating speed is 20r/min, the circulating flow rate of the percolate is 5L/min, the pH is automatically controlled and adjusted to 10.5, the reaction time is 120min, the COD removal rate of the final effluent is 50.6%, and the nitrogen recovery rate can reach 68.9%.
Example 3
Percolate Concentrate (COD) of certain refuse landfill Cr 15000mg/L, ammonia nitrogen 10000mg/L, conductivity 55 mS/cm) are treated by the process equipment shown in figure 1, and the main process parameters are as follows: the treated water amount is 5L, the diameter of the ozone oxidation stripping tower is 6cm, the height-diameter ratio is 12, the material of the microbubble aeration disc is titanium, the ozone concentration is 100mg/L, the flow rate is 0.8L/min, the format of the stirring paddle is set to 6 folding turbine paddles, the rotating speed is 30r/min, the circulating flow rate of the percolate is 3L/min, the pH value is automatically controlled to be adjusted to 10.5, the reaction time is 120min, the COD removal rate of the final effluent is 53.6 percent, and the nitrogen recovery rate can reach 66.4 percent.
In the description of the present application, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, merely for convenience of description and simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed in a particular orientation, and be operated, and therefore, are not to be construed as limiting the present application.
The foregoing description of specific embodiments of the present invention has been presented. It is to be understood that the present invention is not limited to the specific embodiments described above, and that various changes or modifications may be made by one skilled in the art within the scope of the appended claims without departing from the spirit of the invention. The embodiments and features of the embodiments of the present application may be combined with each other arbitrarily without conflict.
Claims (7)
1. The device for synchronously recovering the nitrogen source by carbon-nitrogen separation treatment of the high-salt landfill leachate concentrated solution is characterized by comprising an ozone oxidation stripping tower (1), and an automatic defoaming agent feeding module (2), a leachate concentrated solution external circulation module and a negative pressure nitrogen source recovery module which are respectively connected with the ozone oxidation stripping tower (1);
the inside of ozone oxidation blows and takes off tower (1) is provided with:
a first stirring device;
the percolate concentrate spraying device is connected with the output end of the percolate concentrate external circulation module;
a microbubble aeration disc (106), the microbubble aeration disc (106) being connected to an external ozone source;
the input end of the percolate concentrated solution external circulation module is connected with the lower part of the ozone oxidation stripping tower (1), and the defoamer automatic feeding module (2) and the negative pressure nitrogen source recovery module are connected with the upper part of the ozone oxidation stripping tower (1);
the first stirring device comprises a first stirring shaft (102);
the percolate concentrate spray device comprises: a circular guide pipe (103) and an umbrella-shaped spray header (104);
the circular guide pipe (103) is arranged around the periphery of the first stirring shaft (102), and the umbrella-shaped spray headers (104) are distributed on the circular guide pipe (103);
the negative pressure nitrogen source recovery module comprises: a nitrogen source recovery tank (4), a negative pressure fan (401) and a second microbubble aeration head (402);
the second micro-bubble aeration head (402) is positioned in the nitrogen source recovery tank (4), the second micro-bubble aeration head (402) is connected with the ozone oxidation stripping tower (1) through an air outlet pipe (108), and the negative pressure fan is arranged on the air outlet pipe (108);
the nitrogen source recovery tank (4) is provided with an air outlet (404) and a water outlet (403);
the ozone oxidation stripping tower (1) is of a cylindrical structure, is made of organic glass, polyvinyl chloride, polytetrafluoroethylene or perfluoroalkoxy resin, and is set to be 8/1-12/1 in height-diameter ratio.
2. The apparatus for simultaneous recovery of nitrogen source for carbon-nitrogen separation treatment of high-salt landfill leachate concentrate of claim 1, wherein the defoamer module (2) comprises: the system comprises a time relay (201), a vacuum pump (202), an antifoaming agent tank (203) and an antifoaming agent spray header (204);
the spray header (204) is arranged in the ozone oxidation stripping tower (1), the defoaming agent tank (203) is connected with the defoaming agent spray header (204) through the vacuum pump (202), and the time relay (201) is electrically connected with the vacuum pump (202).
3. The apparatus for simultaneous recovery of nitrogen source for carbon-nitrogen separation process of high-salt landfill leachate concentrate of claim 1, wherein the leachate concentrate recirculation module comprises: an external leachate circulation tank (3);
the leachate external circulation tank (3) is connected with the lower part of the ozone oxidation stripping tower (1) through a first guide pipe (301), and the leachate external circulation tank (3) is connected with the leachate concentrated solution spraying device through a second guide pipe (312);
a mud-water separation inclined plate (314), a second stirring device and a pH regulation device are arranged in the leachate external circulation tank (3);
the lower end of the mud-water separation sloping plate (314) is provided with a mud discharge pipe (303).
4. The apparatus for simultaneous recovery of nitrogen source for carbon-nitrogen separation treatment of high-salt landfill leachate concentrate of claim 3, wherein the pH control apparatus comprises: a pH probe (304), a pH determinator (305), an automatic switch (306), a pH regulation spray head (307), a pH regulation pump (308) and a pH regulation liquid tank (309);
the pH probe (304) and the pH regulation spray header (307) are arranged in the leachate external circulation tank (3), the pH regulation liquid tank (309) is connected with the pH regulation spray header (307) through the pH regulation pump (308), the pH regulation pump (308) is electrically connected with the automatic switch (306), the automatic switch (306) is electrically connected with the pH determinator (305), and the pH determinator (305) is connected with the pH probe (304).
5. The apparatus for simultaneous separation of carbon and nitrogen of a concentrated solution of high-salt landfill leachate and recovery of nitrogen source as claimed in claim 1, wherein the micro-bubble aeration disk (106) is made of titanium and has a plurality of umbrella-shaped parallel aeration heads with a pore size of 0.20-0.45 μm, and the size of generated micro-bubbles is less than 100nm.
6. The apparatus for simultaneous recovery of nitrogen source for carbon-nitrogen separation treatment of high-salt landfill leachate concentrate according to claim 1, wherein the leachate concentrate spraying apparatus is disposed at 1/5-1/4 of the upper part of the ozone oxidation stripping tower (1).
7. The apparatus for simultaneous carbon-nitrogen separation treatment of high-salt landfill leachate concentrate and recovery of nitrogen source according to claim 1, wherein the defoamer is ejected from the defoamer dosing module (2) in a parabolic form.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101700930A (en) * | 2009-10-21 | 2010-05-05 | 宁波市鄞州区绿州能源利用有限公司 | Automatic spraying defoaming device for waste leachate treatment |
| CN101781036A (en) * | 2009-12-23 | 2010-07-21 | 新奥科技发展有限公司 | Equipment and method for treating nondegradable wastewater by utilizing catalytic oxidation of ozone |
| CN103274549A (en) * | 2013-06-07 | 2013-09-04 | 中国农业大学 | Cycle closed type filler-free high-efficiency ammonia nitrogen removing and nutrient recovery device of biogas slurry |
| CN105130088A (en) * | 2014-05-28 | 2015-12-09 | 江苏维尔利环保科技股份有限公司 | Ozone oxidation treatment leachate nanofiltration concentrate treatment method |
| CN110372143A (en) * | 2019-07-19 | 2019-10-25 | 中节能工程技术研究院有限公司 | A kind of landfill leachate materialization deamination preprocess method and equipment |
| KR102180129B1 (en) * | 2020-07-03 | 2020-11-17 | 주식회사 한화그린 | 4 no purification method of livestock wastewater |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6734621B2 (en) * | 2014-02-20 | 2020-08-05 | オルガノ株式会社 | Ozone water supply method and ozone water supply device |
-
2021
- 2021-01-20 CN CN202110077071.1A patent/CN112897675B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101700930A (en) * | 2009-10-21 | 2010-05-05 | 宁波市鄞州区绿州能源利用有限公司 | Automatic spraying defoaming device for waste leachate treatment |
| CN101781036A (en) * | 2009-12-23 | 2010-07-21 | 新奥科技发展有限公司 | Equipment and method for treating nondegradable wastewater by utilizing catalytic oxidation of ozone |
| CN103274549A (en) * | 2013-06-07 | 2013-09-04 | 中国农业大学 | Cycle closed type filler-free high-efficiency ammonia nitrogen removing and nutrient recovery device of biogas slurry |
| CN105130088A (en) * | 2014-05-28 | 2015-12-09 | 江苏维尔利环保科技股份有限公司 | Ozone oxidation treatment leachate nanofiltration concentrate treatment method |
| CN110372143A (en) * | 2019-07-19 | 2019-10-25 | 中节能工程技术研究院有限公司 | A kind of landfill leachate materialization deamination preprocess method and equipment |
| KR102180129B1 (en) * | 2020-07-03 | 2020-11-17 | 주식회사 한화그린 | 4 no purification method of livestock wastewater |
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| CN112897675A (en) | 2021-06-04 |
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