CN215250276U - Old leachate treatment system - Google Patents
Old leachate treatment system Download PDFInfo
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- CN215250276U CN215250276U CN202121302936.1U CN202121302936U CN215250276U CN 215250276 U CN215250276 U CN 215250276U CN 202121302936 U CN202121302936 U CN 202121302936U CN 215250276 U CN215250276 U CN 215250276U
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Abstract
The utility model discloses an aging leachate treatment system, which comprises a nitrosation tank, an anaerobic ammonia oxidation tank, a denitrification tank, an ultrafiltration membrane unit and an electrolytic treatment tank which are arranged in sequence along the water flow direction; an aeration device is arranged at the bottom of the nitrosation tank, and a first stirring device is arranged in the nitrosation tank; the bottom of the anaerobic ammonia oxidation tank is provided with a water distributor, the tank is internally provided with a second stirring device, and the anaerobic ammonia oxidation tank is communicated with the denitrification tank through a first pipeline; a third stirring device is arranged in the denitrification tank and is communicated with the ultrafiltration membrane unit through a second pipeline; the ultrafiltration membrane unit is provided with a return pipe and is communicated with the electrolytic treatment tank through a third pipeline; a plurality of electrolysis units are arranged in the electrolysis treatment tank, and the electrolysis treatment tank is provided with a circulating pipe; the utility model discloses an old leachate treatment system can high-efficient denitrogenation and high-efficient COD of getting rid of, can effectively get rid of the humic acid of difficult degradation, does not produce the concentrate of high concentration pollutant.
Description
Technical Field
The utility model relates to a sewage treatment technical field, in particular to old leachate treatment system.
Background
The C/N (carbon nitrogen ratio) in the aged percolate is extremely unbalanced, the ammonia nitrogen concentration is high, most COD (chemical oxygen demand) in the aged percolate is humic acid which is difficult to degrade, and the integral water quality has poor biochemical treatment performance. The common biochemical treatment, such as the conventional activated sludge process, has low removal efficiency on COD and ammonia nitrogen. The biochemical treatment performance of the aged percolate is generally improved by additionally supplementing a large amount of carbon sources, so that the denitrification efficiency is improved, and the running treatment cost is greatly improved.
At present, membrane method is still adopted as deep treatment technology in many landfill sites. The essence of the membrane method is physical separation by osmotic pressure, and although effluent can be effectively ensured to reach the standard, the recovery rate of the membrane method can only reach within 75 percent, so that a large amount of concentrated solution which is more difficult to treat is generated.
The flocculation precipitation process has poor effect of treating the humic acid which is difficult to degrade, and the removal rate is only 5-15%.
COD, i.e. chemical oxygen demand, is the amount of reducing substances that need to be oxidized in a water sample measured chemically.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving one of the technical problem that exists among the prior art at least. Therefore, the utility model provides an old leachate treatment system can high-efficient denitrogenation and high-efficient COD of getting rid of, can effectively get rid of the humic acid of difficult degradation, does not produce the concentrate of high concentration pollutant.
According to the utility model discloses old leachate treatment system, include: the device comprises a nitrosation tank, an anaerobic ammonia oxidation tank, a denitrification tank, an ultrafiltration membrane unit and an electrolytic treatment tank which are sequentially arranged along the water flow direction;
an aeration device is arranged at the bottom of the nitrosation tank, a first stirring device is arranged in the nitrosation tank, a water outlet pipe is arranged in the nitrosation tank, and the other end of the water outlet pipe extends into the anaerobic ammonia oxidation tank;
a water distributor is arranged at the bottom of the anaerobic ammonia oxidation tank and is communicated with the water outlet pipe, a second stirring device is arranged in the anaerobic ammonia oxidation tank, and the anaerobic ammonia oxidation tank is communicated with the denitrification tank through a first pipeline;
a third stirring device is arranged in the denitrification tank, and the denitrification tank is communicated with the ultrafiltration membrane unit through a second pipeline;
the ultrafiltration membrane unit is provided with a return pipe, the outlet of the return pipe is communicated to the denitrification tank, and the ultrafiltration membrane unit is communicated with the electrolytic treatment tank through a third pipeline;
the electrolytic treatment cell comprises an inlet end and an outlet end, a plurality of electrolytic units are arranged in the electrolytic treatment cell, each electrolytic unit comprises an anode and a cathode, the electrolytic treatment cell is provided with a circulating pipe, and the inlet end and the outlet end are communicated through the circulating pipe.
According to the utility model discloses old leachate treatment system has following technological effect at least: the treatment system adopts a nitrosation, anaerobic ammonia oxidation and denitrification coupling process, all strains do not interfere with each other, efficient denitrification is effectively realized, and the denitrification efficiency can reach more than 96%; the adding amount of the carbon source is reduced by about 70 percent compared with the conventional biochemical treatment, the aeration rate is reduced by about 63 percent compared with the conventional biochemical treatment, and the operation cost is greatly reduced; the electrolytic treatment tank adopts an electrocatalytic oxidation technology, so that humic acid which is difficult to degrade can be effectively removed, the COD removal efficiency can reach more than 98 percent, and the removal efficiency on chromaticity is extremely high; the whole treatment system does not produce concentrated solution of high-concentration pollutants, and has simple process, low construction cost and small occupied area.
In some embodiments of the utility model, still be equipped with the equalizing basin before the nitrosation pond, the export of equalizing basin with nitrosation pond intercommunication.
In some embodiments of the present invention, a first regulation tank is further disposed between the anammox tank and the denitrification tank, and the first regulation tank communicates the anammox tank with the denitrification tank, so that the water in the anammox tank passes through the first regulation tank and then enters the denitrification tank.
In some embodiments of the present invention, a second regulation tank is further disposed between the ultrafiltration membrane unit and the electrolytic treatment tank, and the second regulation tank communicates the ultrafiltration membrane unit with the electrolytic treatment tank, so that water in the ultrafiltration membrane unit passes through the second regulation tank and then enters the electrolytic treatment tank.
In some embodiments of the present invention, a sand filter is further disposed behind the electrolytic treatment tank, and the outlet end of the electrolytic treatment tank is communicated with the sand filter.
In some embodiments of the present invention, the bottom of the nitrosation tank is provided with a first sludge discharge port.
In some embodiments of the present invention, a second sludge discharge port is disposed at the bottom of the denitrification tank.
In some embodiments of the present invention, pH monitoring devices are disposed in the nitrosation tank, the anammox tank and the denitrification tank.
In some embodiments of the invention, the anode is a coated titanium anode and the cathode is a copper cathode in the electrolysis cell.
In some embodiments of the present invention, the number of the electrolysis units is 3 to 5.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic structural diagram of a first embodiment of the present invention;
fig. 2 is a schematic structural diagram of a second embodiment of the present invention.
Reference numerals:
a nitrosation tank 100, an aeration device 110 and a first stirring device 120;
the anaerobic ammonia oxidation tank 200, the water distributor 210 and the second stirring device 220;
a denitrification tank 300 and a third stirring device 310;
an ultrafiltration membrane unit 400, a return pipe 410, an electrolytic treatment cell 500, and a circulation pipe 520;
a regulating tank 600, a first regulating and storing tank 700, a second regulating and storing tank 800 and a sand filter tank 900.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention.
In the description of the present invention, it should be understood that the orientation or positional relationship indicated with respect to the orientation description, such as up, down, front, rear, left, right, etc., is based on the orientation or positional relationship shown in the drawings, and is only for convenience of description and simplification of description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, a plurality of means are one or more, a plurality of means are two or more, and the terms greater than, less than, exceeding, etc. are understood as not including the number, and the terms greater than, less than, within, etc. are understood as including the number. If the first and second are described for the purpose of distinguishing technical features, they are not to be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated or implicitly indicating the precedence of the technical features indicated.
In the description of the present invention, unless there is an explicit limitation, the words such as setting, installation, connection, etc. should be understood in a broad sense, and those skilled in the art can reasonably determine the specific meanings of the above words in combination with the specific contents of the technical solution.
Referring to fig. 1, the aged leachate treatment system according to an embodiment of the present invention includes: the device comprises a nitrosation tank 100, an anaerobic ammonia oxidation tank 200, a denitrification tank 300, an ultrafiltration membrane unit 400 and an electrolytic treatment tank 500 which are sequentially arranged along the water flow direction; the bottom of the nitrosation tank 100 is provided with an aeration device 110, the tank is internally provided with a first stirring device 120, the nitrosation tank 100 is provided with a water outlet pipe, and the other end of the water outlet pipe extends into the anaerobic ammonia oxidation tank 200; the bottom of the anaerobic ammonia oxidation tank 200 is provided with a water distributor 210, the water distributor 210 is communicated with a water outlet pipe, a second stirring device 220 is arranged in the anaerobic ammonia oxidation tank 200, and the anaerobic ammonia oxidation tank 200 is communicated with the denitrification tank 300 through a first pipeline; a third stirring device 310 is arranged in the denitrification tank 300, and the denitrification tank 300 is communicated with the ultrafiltration membrane unit 400 through a second pipeline; the ultrafiltration membrane unit 400 is provided with a return pipe 410, the outlet of the return pipe 410 is communicated to the denitrification tank 300, and the ultrafiltration membrane unit 400 is communicated with the electrolytic treatment tank 500 through a third pipeline; the electrolytic treatment cell 500 comprises an inlet end and an outlet end, a plurality of electrolytic units are arranged in the cell, each electrolytic unit comprises an anode and a cathode, the electrolytic treatment cell 500 is provided with a circulating pipe 520, the inlet end and the outlet end are communicated through the circulating pipe 520, water is conveyed to the electrolytic units again for circulating treatment, and the outlet end can supply water to the outside.
The nitrosation tank 100 is operated in a sequencing batch mode. The aeration device 110 stops aeration, the first stirring device 120 starts stirring, the anaerobic operation lasts for 12 hours for denitrification, then the aeration device 110 starts aeration, the anaerobic operation lasts for 8 hours, the dissolved oxygen in the nitrosation tank 100 is kept at about 1-1.5 mg/L, and finally the anaerobic ammonia oxidation tank 200 discharges the water in the nitrosation tank 100 through a water outlet pipe and a water distributor 210.
Anaerobic ammonia oxidation pond 200 also adopts the operation of preface batch formula, and second agitating unit 220 stirs pond water, and the water that the outlet pipe was carried simultaneously evenly gets into anaerobic ammonia oxidation pond 200 through water-locator 210, makes the matrix distribution in the pond even, prevents that local ammonia nitrogen and nitrite nitrogen concentration are too high, and local high-concentration ammonia nitrogen and nitrite nitrogen can produce the inhibitory action to the bacterial. After 2 days of operation, the pond water is transported to the denitrification pond 300 through the first pipeline.
The denitrification tank 300 operates in a continuous flow mode, and the third stirring device 310 is used for stirring the tank water, so that the matrix in the tank is uniformly distributed, and further denitrification treatment is performed. The pond water is conveyed to the ultrafiltration membrane unit 400 through the second pipeline, mud and water are separated in the ultrafiltration membrane unit 400, the mud is returned to the denitrification pond 300 through the return pipe 410 to be continuously treated, and the separated water is conveyed to the electrolytic treatment pond 500 through the third pipeline.
The electrolytic treatment tank 500 is operated in a sequencing batch mode, the water in the tank is firstly subjected to oxidative degradation, and the current density is 30-50 mA/cm in the oxidative degradation process2Oxidizing and degrading for 15-20 minutes to oxidize ammonia nitrogen into nitrogen and degrade COD; then, carrying out reduction degradation on the pond water, wherein in the reduction degradation process, the current density is 5-10 mA/cm2The time of reduction and degradation is 15-20 minutes; finally, the current density is 40mA/cm2For 30 minutes. The circulation pipe 520 re-delivers the treated pond water to the electrolysis unit for reciprocating circulation treatment.
In some embodiments of the utility model, still be equipped with equalizing basin 600 before nitrosation pond 100, the export and the nitrosation pond 100 intercommunication of equalizing basin 600.
Before entering the nitrosation tank 100, the aged percolate is conveyed into the regulating tank 600 for water quality balancing and tempering treatment, so that the treatment efficiency of the subsequent process is improved, the concentration of various pollutants in the treatment system is prevented from changing sharply, and the flow fluctuation is slowed down.
In some embodiments of the present invention, a first regulation tank 700 is further disposed between the anammox tank 200 and the denitrification tank 300, and the first regulation tank 700 communicates the anammox tank 200 and the denitrification tank 300, so that water in the anammox tank 200 passes through the first regulation tank 700 and then enters the denitrification tank 300.
The first regulation and storage tank 700 can accumulate the tank water output by the anaerobic ammonia oxidation tank 200, so that ammonia nitrogen, nitrite nitrogen and nitrate nitrogen values in the tank water can be conveniently monitored, and whether a carbon source and the feeding amount are required to be fed in the denitrification tank 300 subsequently can be determined.
In some embodiments of the present invention, a second storage tank 800 is further disposed between the ultrafiltration membrane unit 400 and the electrolytic treatment tank 500, and the second storage tank 800 communicates the ultrafiltration membrane unit 400 and the electrolytic treatment tank 500, so that water in the ultrafiltration membrane unit 400 passes through the second storage tank 800 and then enters the electrolytic treatment tank 500.
The second storage tank 800 can store the tank water output from the ultrafiltration membrane unit 400, and can maintain the flow rate of water during the operation of the electrolytic treatment tank 500 constant.
In some embodiments of the present invention, a sand filter 900 is further disposed behind the electrolytic treatment tank 500, and the outlet end of the electrolytic treatment tank 500 is communicated with the sand filter 900.
The electrolytic treatment tank 500 is connected with a sand filter 900 at the back, and solid suspended substances in water are removed.
In some embodiments of the present invention, the bottom of the nitrosation tank 100 is provided with a first sludge discharge opening.
The first sludge discharge port is arranged to discharge sludge accumulated at the bottom of the nitrosation tank 100 periodically.
In some embodiments of the present invention, a second sludge discharge port is disposed at the bottom of the denitrification tank 300.
And a second sludge discharge port is arranged, so that sludge accumulated at the bottom of the denitrification tank 300 can be discharged periodically.
In some embodiments of the present invention, pH monitoring devices are disposed in the nitritation tank 100, the anammox tank 200 and the denitrification tank 300.
Arranging pH monitoring devices in the anaerobic ammonia oxidation tank 200 and the denitrification tank 300 to monitor the pH value and control the pH value in the nitrosation tank 100 to be 6.8-7.8; the pH value in the anaerobic ammonia oxidation tank 200 is 7.2-8.2; the pH value in the denitrification tank 300 is between 6.8 and 7.8.
In some embodiments of the invention, the anode is a coated titanium anode and the cathode is a copper cathode in the electrolysis cell.
The titanium anode with the coating is adopted for chemical ammonia oxidation, so that the titanium anode has excellent electro-catalytic activity and chemical stability; the copper cathode is used for catalyzing the nitrate to be reduced into nitrogen.
In some embodiments of the present invention, the number of the electrolysis units is 3 to 5.
If the number of the electrolysis units is less than 3, the electrolysis efficiency is not high; if the number of the carbon nanotubes is more than 5, the energy consumption is large.
In some embodiments of the present invention, the aged leachate first enters the adjusting tank 600 to perform water quality equalization conditioning. The effluent of the adjusting tank 600 enters the nitrosation tank 100, and the nitrosation tank 100 operates in a sequencing batch mode. Firstly, the aeration device 110 stops aeration, the first stirring device 120 stirs, the anoxic operation lasts for 12 hours for denitrification, then the aeration device 110 carries out aeration operation for 8 hours, the aeration device 110 can adopt micropore aeration to keep the dissolved oxygen in the pool at about 1-1.5 mg/L, and finally the pool is kept still for precipitating and yielding water, a submersible pump can be added to the water yielding structure, a submersible pump is arranged in the nitrosation pool 100, and the submersible pump is connected with a water outlet pipe. The submersible pump can be arranged at a proper position at the middle upper part of the nitrosation tank 100 according to the treatment capacity of the aged percolate, so that only supernatant liquid of the nitrosation tank 100 is pumped out when water is discharged, and the mixed bacteria entering the anaerobic ammonia oxidation tank 200 is reduced as much as possible. The bottom of the nitrosation pond 100 is provided with a first sludge discharge port, which can discharge sludge regularly. Monitoring the pH value in the pool through a pH monitoring device, controlling the pH value to be 6.8-7.8, and adding sodium carbonate to supplement alkalinity at proper time. The effluent water treated by the nitrosation tank 100 is sent to an anaerobic ammonia oxidation tank 200.
The anaerobic ammonia oxidation tank 200 runs in a sequencing batch mode, the second stirring device 220 is used for stirring, water is fed from the bottom water distributor 210 of the anaerobic ammonia oxidation tank 200, the matrix in the tank is uniformly distributed, and the local ammonia nitrogen and nitrite nitrogen are prevented from being too high in concentration. Monitoring the pH value, controlling the pH value to be 7.2-8.2, and adding dilute hydrochloric acid or sodium carbonate at a proper time to supplement acid and alkali. The denitrification efficiency of the anaerobic ammonia oxidation tank 200 can reach more than 83 percent, and no additional carbon source is required to be added. The effluent of the anaerobic ammonia oxidation tank 200 enters a first regulation and storage tank 700, and the ammonia nitrogen, nitrite nitrogen and nitrate nitrogen values of the effluent can be monitored in the first regulation and storage tank 700.
The first regulation and storage tank 700 discharges water to the denitrification tank 300, the denitrification tank 300 operates in a continuous flow mode, the third stirring device 310 stirs the water, and meanwhile, a proper amount of carbon source is added according to indexes such as ammonia nitrogen, nitrite nitrogen and nitrate nitrogen values of the inlet water, so that denitrification treatment is further performed. Monitoring the pH value, controlling the pH value to be 6.8-7.8, and supplementing an appropriate amount of acid and alkali. The bottom of the denitrification tank 300 is provided with a second sludge discharge port for discharging sludge regularly.
The effluent of the denitrification tank 300 flows into the ultrafiltration membrane unit 400, mud and water are effectively separated, meanwhile, mud flows back into the denitrification tank 300 through the return pipe 410, and the separated water continuously flows out to the second regulation and storage tank 800.
The second storage tank 800 discharges water to the electrolytic processing tank 500. A coated titanium anode and a coated copper cathode are arranged in the electrolytic treatment tank 500, the electrolytic treatment tank 500 operates in a sequencing batch mode, the water in the tank is firstly subjected to oxidative degradation, and the current density is 30-50 mA/cm in the oxidative degradation process2Oxidizing and degrading for 15-20 minutes to oxidize ammonia nitrogen into nitrogen and degrade COD; then, carrying out reduction degradation on the pond water, wherein in the reduction degradation process, the current density is 5-10 mA/cm2The time of reduction and degradation is 15-20 minutes; finally, the current density is 40mA/cm2For 30 minutes. The circulation pipe 520 re-delivers the treated pond water to the electrolysis unit for reciprocating circulation treatment. The effluent of the electrolytic treatment cell 500 is sent to a sand filter 900 for filtration treatment.
After being treated by an aged leachate treatment system, the chroma of the effluent is less than 4, the COD is 10.16mg/L, the ammonia nitrogen is 0.77mg/L, and the total nitrogen is 4.04mg/L, which meets the discharge standard of GB 16889-2008.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an illustrative embodiment," "an example," "a specific example," or "some examples" or the like mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
While embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.
Claims (10)
1. An aging leachate treatment system, comprising:
the device comprises a nitrosation tank (100), an anaerobic ammonia oxidation tank (200), a denitrification tank (300), an ultrafiltration membrane unit (400) and an electrolytic treatment tank (500) which are sequentially arranged along the water flow direction;
an aeration device (110) is arranged at the bottom of the nitrosation tank (100), a first stirring device (120) is arranged in the nitrosation tank, a water outlet pipe is arranged in the nitrosation tank (100), and the other end of the water outlet pipe extends into the anaerobic ammonia oxidation tank (200);
a water distributor (210) is arranged at the bottom of the anaerobic ammonia oxidation tank (200), the water distributor (210) is communicated with the water outlet pipe, a second stirring device (220) is arranged in the anaerobic ammonia oxidation tank (200), and the anaerobic ammonia oxidation tank (200) is communicated with the denitrification tank (300) through a first pipeline;
a third stirring device (310) is arranged in the denitrification tank (300), and the denitrification tank (300) is communicated with the ultrafiltration membrane unit (400) through a second pipeline;
the ultrafiltration membrane unit (400) is provided with a return pipe (410), the outlet of the return pipe (410) is communicated to the denitrification tank (300), and the ultrafiltration membrane unit (400) is communicated with the electrolytic treatment tank (500) through a third pipeline;
the electrolytic treatment cell (500) comprises an inlet end and an outlet end, a plurality of electrolytic units are arranged in the electrolytic treatment cell, each electrolytic unit comprises an anode and a cathode, the electrolytic treatment cell (500) is provided with a circulating pipe (520), and the inlet end and the outlet end are communicated through the circulating pipe (520).
2. The treatment system for the aged percolate according to claim 1, wherein a regulating tank (600) is further arranged in front of the nitrosation tank (100), and the outlet of the regulating tank (600) is communicated with the nitrosation tank (100).
3. The aging percolate treatment system according to claim 1, wherein a first regulation tank (700) is further arranged between the anaerobic ammonia oxidation tank (200) and the denitrification tank (300), the anaerobic ammonia oxidation tank (200) is communicated with the denitrification tank (300) through the first regulation tank (700), and water in the anaerobic ammonia oxidation tank (200) passes through the first regulation tank (700) and then enters the denitrification tank (300).
4. The aged leachate treatment system according to claim 1, wherein a second storage tank (800) is further disposed between the ultrafiltration membrane unit (400) and the electrolytic treatment tank (500), and the second storage tank (800) communicates the ultrafiltration membrane unit (400) and the electrolytic treatment tank (500), so that water in the ultrafiltration membrane unit (400) passes through the second storage tank (800) and then enters the electrolytic treatment tank (500).
5. The leachate treatment system of claim 1, wherein a sand filter (900) is further disposed after the electrolytic treatment tank (500), and an outlet end of the electrolytic treatment tank (500) is communicated with the sand filter (900).
6. The elderly percolate treatment system according to claim 1, wherein the tank bottom of the nitrosation tank (100) is provided with a first sludge outlet.
7. The aging percolate treatment system according to claim 1, wherein the bottom of the denitrification tank (300) is provided with a second sludge discharge.
8. The elderly leachate treatment system of claim 1, wherein pH monitoring devices are disposed in the nitrosation tank (100), the anammox tank (200), and the denitrification tank (300).
9. The leachate treatment system of claim 1, wherein said anode in said electrolysis unit is a coated titanium anode and said cathode is a copper cathode.
10. The leachate treatment system of claim 1, wherein the number of said electrolysis units is 3 to 5.
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| CN114085012A (en) * | 2022-01-19 | 2022-02-25 | 湖南金旅环保股份有限公司 | Organic wastewater treatment system and organic wastewater treatment method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114085012A (en) * | 2022-01-19 | 2022-02-25 | 湖南金旅环保股份有限公司 | Organic wastewater treatment system and organic wastewater treatment method |
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