CN113800720A - Leachate treatment method and leachate treatment system - Google Patents
Leachate treatment method and leachate treatment system Download PDFInfo
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/048—Purification of waste water by evaporation
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C—CHEMISTRY; METALLURGY
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Abstract
The invention provides a percolate treatment method and a system, wherein the percolate treatment method comprises the first step of carrying out biodegradation reaction on percolate through anaerobic microorganisms to remove partial organic matters in the percolate; secondly, biologically denitrifying the penetrating fluid through anaerobic microorganisms to remove part of nitrogen in the penetrating fluid; thirdly, filtering the penetrating fluid; fourthly, further degrading organic matters in the penetrating fluid through the first advanced oxidation treatment; fifthly, treating the penetrating fluid through reversed electrodialysis to obtain first fresh water and first concentrated water; sixthly, evaporating and crystallizing the first concentrated water to obtain inorganic salt; seventhly, filtering the first fresh water to obtain second fresh water and second concentrated water, wherein the second fresh water is discharged as produced water; eighthly, further degrading organic matters in the second concentrated water through second advanced oxidation treatment; and ninthly, repeatedly executing the third step to the eighth step on the second concentrated water treated in the eighth step. The invention can treat the percolate in full quantity and realize zero emission.
Description
Technical Field
The invention relates to the field of liquid purification, in particular to a leachate treatment method and a leachate treatment system.
Background
In recent years, along with the acceleration of the urbanization process of China, the living standard of people is steadily improved, the production amount of garbage is increased year by year, a large amount of garbage incineration plants are built, garbage collected by a garbage power plant needs to be fermented in a garbage pit for 5-7 days, in the fermentation process, moisture in the garbage can seep out to form garbage leachate, and the garbage leachate is high-concentration, high-ammonia-nitrogen and high-pollution liquid and can have great influence on the environment.
The existing technology for treating leachate in a waste incineration plant generally adopts a process of 'pretreatment + anaerobic + aerobic + advanced treatment system', the advanced treatment generally adopts a membrane separation system, 60-70% of leachate in the existing process can be recycled in the whole plant after being treated, but 30-40% of residual leachate membrane concentrated solution needs to be further treated, and the full treatment of the concentrated solution is directly related to whether the leachate treatment can realize zero emission.
The problems of large amount of concentrated water, incapability of treating the concentrated water, high total treatment operation cost and the like in the treatment process of the percolate at present are difficult problems in the industry. Although the concentrated water can be treated in a full amount by adopting an evaporation and solidification mode, because the concentration of organic matters in the percolate is high, the organic matters which are difficult to biodegrade exist in an evaporation mother liquor form finally, and the percolate cannot achieve zero emission in a real sense.
Disclosure of Invention
The embodiment of the invention provides a leachate treatment method and a leachate treatment system, which at least solve the problem that zero emission of full treatment is difficult to realize in the related art.
According to an embodiment of the present invention, there is provided a leachate treatment method, comprising:
firstly, performing biodegradation reaction on penetrating fluid through anaerobic microorganisms to remove partial organic matters in the penetrating fluid;
secondly, biologically denitrifying the penetrating fluid through anaerobic microorganisms to remove part of nitrogen in the penetrating fluid;
thirdly, filtering the penetrating fluid;
fourthly, further degrading organic matters in the penetrating fluid through the first advanced oxidation treatment;
fifthly, treating the penetrating fluid through reversed electrodialysis to obtain first fresh water and first concentrated water;
sixthly, evaporating and crystallizing the first concentrated water to obtain inorganic salt;
seventhly, filtering the first fresh water to obtain second fresh water and second concentrated water, wherein the second fresh water is discharged as produced water;
eighthly, further degrading organic matters in the second concentrated water through second advanced oxidation treatment;
and ninthly, repeatedly executing the third step to the eighth step on the second concentrated water treated in the eighth step.
And further, collecting the gas produced by the biodegradation reaction in the first step, desulfurizing and dehydrating the gas, feeding the gas into a biogas hot water boiler for combustion to generate hot water, evaporating and crystallizing the first concentrated water by using the hot water in the fifth step, and returning the hot water to the biogas boiler for reheating after the hot water is contacted with the first concentrated water for cooling.
Further, the first advanced oxidation treatment comprises one or more combinations of Fenton oxidation, ozone/hydrogen peroxide oxidation and electron beams, and the second advanced oxidation treatment comprises one or more combinations of electro-catalytic oxidation, supercritical oxidation and wet oxidation.
Further, in the first step, the permeate is subjected to biodegradation reaction using one or a combination of more of an upflow anaerobic sludge blanket reactor (UASB), an internal circulation anaerobic reactor (IC), an upflow anaerobic sludge blanket filter (UBF), and an internal and external circulation anaerobic reactor (IOC).
Further, in the second step, one or more of an anoxic and aerobic process, a short-cut nitrification and denitrification process and an anaerobic ammonia oxidation process are adopted to carry out biological denitrification on the penetrating fluid.
Further, in the third step, an ultrafiltration membrane device is adopted for filtering, and the range of the cut-off molecular weight is 1000-50000 Da; in the seventh step, a nanofiltration membrane is adopted for filtering, and the range of the molecular weight cut-off is 100-400 Da.
Further, in the fifth step, a homogeneous phase ionic membrane is adopted, a continuous pole-reversing operation mode is adopted, and the pole-reversing period is 20-180 min.
According to another embodiment of the present invention, there is provided a leachate treatment system comprising an anaerobic unit, a biochemical unit, an ultrafiltration unit, a first advanced oxidation unit, a bipolar electrodialysis unit, a nanofiltration unit, a second advanced oxidation unit, an evaporation unit, and a crystallization unit; the anaerobic unit, the biochemical unit, the ultrafiltration unit, the first advanced oxidation unit, the reverse electrode electrodialysis unit and the nanofiltration unit are sequentially connected through pipelines; the second advanced oxidation unit is connected with the nanofiltration unit through a pipeline, and is also connected with a pipeline between the ultrafiltration unit and the first advanced oxidation unit through a pipeline; the evaporation unit is connected to the electrodialysis reversal unit, and the crystallization unit is connected to the evaporation unit.
Further, the leachate treatment system also comprises a biogas purification device and a biogas boiler, wherein the biogas purification device is connected with the anaerobic unit to purify biogas generated by the anaerobic unit, the biogas boiler generates hot water for the evaporation unit by burning the biogas, and the evaporation unit adopts a humidification-dehumidification type evaporator.
Further, the crystallization unit comprises a thickener, a plate-and-frame filter press, a dryer and an automatic packaging machine.
Has the advantages that: compared with the prior art, the invention aims at the water quality characteristics of the percolate, has high system pollutant removal rate and stable operation, and can realize full treatment and zero discharge of the percolate; on the basis of a process for treating percolate by reverse electrodialysis, a first advanced oxidation treatment and a second advanced oxidation treatment are added, the first advanced oxidation treatment can realize open loop and short bond of macromolecular refractory organic matters in the effluent of the ultrafiltration membrane, and meanwhile, the removal rate of COD reaches 40-80%, so that the problem of organic matters of a subsequent EDR membrane is effectively avoided, and the running stability of the EDR membrane is improved; the second advanced oxidation treatment can effectively nanofiltration of various organic matter components in the concentrated water, the removal rate of COD is more than 90%, and the accumulation of organic matters in the system is avoided, so that the continuous operation of the system is ensured; the purposes of considering the treatment cost and reducing the energy consumption are achieved; anaerobic methane is used as a heat source, and a humidifying-dehumidifying evaporator is introduced to treat concentrated water, so that the full-amount treatment of the concentrated water can be realized.
In conclusion, the leachate treatment method related by the invention is an organic combination of a plurality of step units, and each unit is absent, so that zero emission of the leachate in full treatment is finally realized, and no evaporation mother liquor is generated.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:
figure 1 is a schematic block diagram of a leachate treatment system according to an embodiment of the present invention.
Detailed Description
The invention will be described in detail hereinafter with reference to the accompanying drawings in conjunction with embodiments. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
It should be noted that the terms "first," "second," and the like in the description and claims of the present invention and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order.
Referring to fig. 1, an embodiment of the present invention provides a leachate treatment system, including an anaerobic unit, a biochemical unit, an ultrafiltration unit, a first advanced oxidation unit, a reverse electrodialysis unit, a nanofiltration unit, a second advanced oxidation unit, an evaporation unit, and a crystallization unit; the anaerobic unit, the biochemical unit, the ultrafiltration unit, the first advanced oxidation unit, the reverse electrode electrodialysis unit and the nanofiltration unit are sequentially connected through pipelines; the second advanced oxidation unit is connected with the nanofiltration unit through a pipeline, and is also connected with a pipeline between the ultrafiltration unit and the first advanced oxidation unit through a pipeline; the evaporation unit is connected to the electrodialysis reversal unit, and the crystallization unit is connected to the evaporation unit.
In at least one embodiment, the leachate treatment system further comprises a biogas purification device and a biogas boiler, wherein the biogas purification device is connected with the anaerobic unit to purify biogas generated by the anaerobic unit, and the biogas boiler generates hot water for the evaporation unit to use by burning the biogas.
In at least one embodiment, the crystallization unit comprises a thickener, a plate and frame filter press, a dryer, and an automatic packaging machine.
Another embodiment of the present invention provides a method for treating leachate, comprising:
the first step, the penetrating fluid is biologically degraded by anaerobic microbe bacteria to remove partial organic matters in the penetrating fluid.
In at least one embodiment, the permeate is subjected to a biodegradation reaction using an anaerobic unit.
The anaerobic unit comprises one or more of an upflow anaerobic sludge blanket reactor (UASB), an internal circulation anaerobic reactor (IC), an upflow anaerobic sludge blanket filter (UBF) and an internal and external circulation anaerobic reactor (IOC).
In the step, the leachate treatment firstly enters an anaerobic unit, and the leachate treatment is subjected to biodegradation reaction under the action of anaerobic microorganisms to convert organic matters in the wastewater into CO2And CH4And the generated gas containing a certain amount of methane is collected as anaerobic biogas and then discharged out of the anaerobic unit for reuse. The content of the organic matters in the leachate after anaerobic treatment is greatly reduced, and the removal rate of the organic matters is generally 60-90%.
And in the second step, the penetrating fluid is subjected to biological denitrification through anaerobic microorganisms, and partial nitrogen in the penetrating fluid is removed.
In at least one embodiment, the permeate is biodenitrified using one or more combinations of anoxic-aerobic processes (a/O), partial nitrification-denitrification, and anaerobic ammonia oxidation processes (Anammox).
In the step, anaerobic effluent enters a biochemical unit, the biochemical unit mainly realizes the function of biological denitrification by the action of microorganisms, and the biochemical unit utilizes biochemical organic matters, alkalinity, ammonia nitrogen, nitrate and the like in water to generate a series of biochemical reactions and converts the biochemical reactions into N2、CO2In the process, the ammonia nitrogen removal rate generally reaches more than 99.5 percent, and the total nitrogen removal rate is 85-90 percent.
And thirdly, filtering the penetrating fluid.
In at least one embodiment, the ultrafiltration membrane device is adopted for filtration, and the cut-off molecular weight is 1000-50000 Da.
The biochemical treatment in the previous step carries certain biochemical sludge, so the sludge and water are required to be separated by a physical membrane filtration mode.
And fourthly, further degrading organic matters in the penetrating fluid through the first advanced oxidation treatment (AOP).
Advanced Oxidation (AOP) means that organic matters are decomposed and degraded by using strong oxidizing radicals, such as Fenton (Fenton) oxidation, ozone/hydrogen peroxide oxidation, electrocatalytic oxidation, wet oxidation, supercritical oxidation, electron beams, etc., so that organic matters with high molecular weight and difficult degradation in sewage can be converted into degradable organic matters with small molecular weight, or the organic matters can be directly removed.
In at least one embodiment, the first advanced oxidation treatment includes one or more combinations of fenton oxidation, ozone/hydrogen peroxide oxidation, and electron beam.
As the effluent water in the third step contains some macromolecular refractory organic matters, mainly including charged organic acid substances such as humic acid, fulvic acid and the like, the problems of organic pollution and the like of a subsequent membrane system can be caused. The AOP technologies (Fenton oxidation, ozone/hydrogen peroxide oxidation and electron beams) can realize the fracture of C-C pi bonds of benzene rings of macromolecular degradation-resistant organic compounds (aromatic compounds) in the leachate, and the C-C pi bonds of the benzene rings react with active hydroxyl radicals to realize the full degradation of the organic compounds, and the removal rate of COD reaches 40-80%. In the process of realizing the degradation of most organic matters, the organic matters which cannot be removed are decomposed into small molecular organic matters, the molecular size is reduced, and the blockage and pollution to the overflowing pore channel of a subsequent membrane system are not easy to cause.
And fifthly, obtaining first fresh water and first concentrated water by treating (EDR) penetrating fluid through reversed electrodialysis.
Electrodialysis (ED) refers to the phenomenon in which charged solute particles (e.g., ions) in a solution migrate through a membrane when dialysis is performed under the influence of an electric field. The technique of purifying and separating substances by electrodialysis is called electrodialysis.
Electrodialysis reversal (EDR) is an operation of automatically switching the electrical properties of electrodes and simultaneously changing the flow direction of concentrated and dilute water, based on electrodialysis. The operation can prevent the membrane pollution caused by precipitation and scaling due to concentration polarization on the membrane surface, reduce the adhesion and accumulation of charged colloid or zoogloea in water on the membrane surface, provide the operation stability of electrodialysis treatment sewage, avoid or reduce the addition of chemical medicines such as acid or scale inhibitor and the like, and reduce the operation cost.
Under the action of direct current, anion and cation migration in the wastewater is realized by utilizing the ion membrane, and organic matters are intercepted by the ion membrane, so that the effective separation of inorganic salt and the organic matters is realized.
In at least one embodiment, the reverse electrodialysis treatment adopts a homogeneous ion membrane and adopts a continuous reverse electrode operation mode, and the reverse electrode period is 20-180 min.
And sixthly, evaporating and crystallizing the first concentrated water to obtain inorganic salt.
The first concentrated water enters an evaporation unit for further concentration and reduction treatment, evaporation utilizes the air humidification-dehumidification principle to realize evaporation and desalination of wastewater, and hot water can be used as an evaporation heat source due to low evaporation temperature and wide heat source requirements.
The evaporation unit can reduce the first concentrated water, finally produce water near saturated salt solution, then enter the crystallization unit to crystallize, and the combined technology of thermal crystallization and centrifugal dehydration can be adopted to realize the continuous crystallization of the system to produce salt according to the inorganic salt component condition in the leachate. The obtained inorganic salt has good chromaticity and low impurity content, and can be used as a snow-melting agent and the like to realize resource utilization.
In at least one embodiment, the biogas generated by the anaerobic unit is desulfurized and dehydrated by a biogas purification device and then enters a biogas hot water boiler, and the purified biogas is combusted in the boiler to generate hot water at 80 ℃ and then enters the heat source inlet end of the evaporation system heater. The hot water of the boiler is cooled by the contact of EDR concentrated water in the heater and then returns to the biogas boiler for reheating, thereby realizing the continuous operation and heat balance of the system.
And seventhly, filtering the first fresh water to obtain second fresh water and second concentrated water, wherein the second fresh water is discharged as produced water.
The first fresh water enters a Nanofiltration (NF) membrane unit, the produced water can be directly discharged or recycled after being treated by the NF membrane, and the second concentrated water returns to enter a second advanced oxidation treatment unit. In at least one embodiment, the filtration is performed by using a nanofiltration membrane, and the molecular weight cut-off range is 100-400 Da. In at least one embodiment, a reverse osmosis membrane unit is adopted to replace a nanofiltration membrane, and the quality of the final effluent can reach the standard. But the reverse osmosis membrane has higher operating pressure than the nanofiltration membrane unit and slightly higher overall operating cost.
And step eight, further degrading organic matters in the second concentrated water through second advanced oxidation treatment.
The second concentrated water mainly contains organic matters and part of inorganic salt, wherein the organic matters are enriched to a certain extent. The second advanced oxidation treatment is different from the first advanced oxidation treatment, so that the enriched organic matters which are not degraded by the first advanced oxidation treatment can be further treated, and the removal rate of the organic matters can reach more than 80 percent through the advanced treatment of the second advanced oxidation treatment. The second advanced oxidation treatment comprises one or more combined processes of electrocatalytic oxidation, supercritical oxidation and wet oxidation. It should be noted that these processes (electrocatalytic oxidation, supercritical oxidation, wet oxidation) can realize the non-selective conversion of the organic substances difficult to remove in the leachate into H through chemical reaction2O、CO2And the COD removal rate reaches over 90 percent, so that the full conversion of organic matters in the percolate is realized, and the accumulation of the organic matters in a system is avoided.
And ninthly, repeatedly executing the third step to the eighth step on the second concentrated water treated in the eighth step.
The effluent from the second advanced oxidation treatment directly returns to the front end to be mixed with the effluent from the third step and then enters the first advanced oxidation treatment.
The invention is described below in some specific examples:
example 1:
the process of the invention is adopted to treat the percolate of a certain refuse incineration plant, and the water quality conditions are as follows: COD is 30000-50000 mg/L, TDS is 10000-12000 mg/L, NH3N is 1000 to 2000 mg/L.
The anaerobic unit is in a UASB form, the COD of the effluent after the leachate is treated by the anaerobic unit is 5000-7000 mg/L, wherein the marsh gas generated by the anaerobic unit is purified by the marsh gas and then is sent to a marsh gas boiler to generate hot water at 90 ℃, and the hot water is sent to the marsh gas boilerThe evaporation unit is used as a heat source for the evaporation unit; anaerobic effluent enters a biochemical unit which adopts an A/O form, the cutoff molecular weight of an ultrafiltration membrane is 1000 Da, after the anaerobic effluent is treated by the biochemical unit and filtered by the ultrafiltration membrane, the COD (chemical oxygen demand) of the ultrafiltration effluent is 500 mg/L, and NH (hydrogen peroxide) is generated3N is 10-30 mg/L; the ultrafiltration effluent is sent into a first advanced oxidation treatment unit, the first advanced oxidation treatment unit adopts a Fenton oxidation device, H2O2With Fe2+The addition amount ratio of (A) is 3-5, H2O2The adding amount is 0.1-0.3 mol/L, the COD of the effluent is 200 mg/L, and then the effluent enters an EDR electrodialysis device; the EDR device adopts a homogeneous ion membrane, the continuous electrode-reversing operation period is 180min, the EDR fresh water COD after treatment is 280 mg/L, TDS to be 800 mg/L, and the EDR concentrated water COD is 200 mg/L, TDS to be 80000 mg/L; EDR fresh water is sent into a nanofiltration membrane unit, the molecular weight cut-off of the nanofiltration membrane is 100Da, the COD of nanofiltration product water is 20 mg/L, TDS to 400 mg/L, the EDR fresh water reaches the water supplement standard of circulating cooling water (GB/T19923-2005) and is recycled in a factory, nanofiltration concentrated water is sent into a second advanced oxidation treatment unit, the second advanced oxidation treatment unit uses an electrocatalytic oxidation device, the reaction retention time is 30-60 min, the COD of treated effluent water is 100 mg/L, and effluent water of the electrocatalytic oxidation device directly returns to be mixed with ultrafiltration effluent water and then enters a subsequent unit for continuous treatment.
The EDR concentrated water sequentially enters an evaporation unit and a crystallization unit, the evaporator adopts a humidification-dehumidification type evaporator, the maximum evaporation temperature of the evaporator based on the air humidification-dehumidification principle is 80 ℃, a heat source is 90 ℃ hot water of water produced by an anaerobic biogas boiler, and other heat sources do not need to be supplemented. And concentrating the EDR concentrated water to a saturated solution by an evaporator, and then sending the saturated solution into a crystallization unit for further treatment. Finally forming a solid inorganic crystal mixed salt product through a thickener, a plate-and-frame filter press, a dryer and an automatic packaging machine. The quality of the crystallized mixed salt meets the standard of snow-melting agent (GB 23851-2017), so the crystallized mixed salt can be used as the snow-melting agent. The process system does not produce evaporation mother liquor, and realizes full treatment, full reuse and zero discharge of leachate wastewater.
After the combined process is adopted, the whole treatment capacity of the EDR system is reduced within 10% after the EDR system continuously and stably operates for 3 months, and the treatment capacity of the EDR system can be recovered by cleaning with conventional chemical acid and alkali liquor.
Comparative example 1:
the ultrafiltration effluent from example 1 was directly fed to an EDR electrodialysis unit. The EDR device adopts a homogeneous ion membrane, the continuous electrode-reversing operation period is 180min, the treatment capacity of the EDR device is rapidly reduced within 1 month, the maximum treatment capacity is reduced by more than 30%, and only part of the treatment capacity can be recovered by fully cleaning with chemical acid and alkali liquor.
Example 2:
the process of the invention is adopted to treat the percolate of a certain refuse incineration plant, and the water quality conditions are as follows: COD is 30000-50000 mg/L, TDS is 10000-12000 mg/L, NH3N is 1000 to 2000 mg/L.
The anaerobic unit is in an IC form, the COD of the effluent after the leachate is treated by the anaerobic unit is 4000-6000 mg/L, wherein the biogas generated by the anaerobic unit is purified by the biogas and then is sent to a biogas boiler to generate hot water at 75 ℃, and the hot water is sent to the evaporation unit to be used as a heat source for the evaporation unit; anaerobic effluent enters a biochemical unit, the biochemical unit adopts a short-cut nitrification and denitrification process, the cutoff molecular weight of an ultrafiltration membrane is 20000 Da, after the treatment of the biochemical unit and the filtration of the ultrafiltration membrane, the COD (chemical oxygen demand) of the ultrafiltration effluent is 800 mg/L, and NH (hydrogen peroxide) is generated3-N is 20-30 mg/L; the ultrafiltration effluent is sent into a first advanced oxidation treatment unit, the first advanced oxidation treatment unit adopts an ozone/hydrogen peroxide oxidation device, H2O2And O3The adding amount ratio of the ozone is 0.3-0.5, the adding amount of the ozone is 0.02-0.1%, COD of treated effluent is 500 mg/L, and then the treated effluent enters an EDR electrodialysis device; the EDR device adopts a homogeneous ion membrane, the continuous electrode-reversing operation period is 90min, the EDR fresh water COD after treatment is 400 mg/L, TDS to 800 mg/L, and the EDR concentrated water COD is 200 mg/L, TDS to 80000 mg/L; EDR fresh water is sent into a nanofiltration membrane unit, the molecular weight cut-off of the nanofiltration membrane is 200Da, the COD of nanofiltration produced water is 35 mg/L, TDS to 500 mg/L, the EDR fresh water reaches the water supplement standard of circulating cooling water (GB/T19923-2005) for recycling in a factory, the nanofiltration concentrated water is sent into a second advanced oxidation treatment unit, the second advanced oxidation treatment unit uses a supercritical oxidation device, the reaction pressure is 22-30 MPa, the reaction temperature is 400-450 ℃, the retention time is 10-30 min, the COD of treated effluent is 100 mg/L, the effluent of the supercritical oxidation device directly returns to be mixed with the ultrafiltration effluent and then enters the supercritical oxidation deviceThe continuation unit continues processing.
The EDR concentrated water sequentially enters an evaporation unit and a crystallization unit, the evaporator adopts a humidification-dehumidification type evaporator, the maximum evaporation temperature of the evaporator based on the air humidification-dehumidification principle is 65 ℃, a heat source is 75 ℃ hot water produced by an anaerobic biogas boiler, and other heat sources are not required to be supplemented. Concentrating the EDR concentrated water to a saturated solution by an evaporator, and then sending the saturated solution into a crystallization unit for further treatment to finally form solid inorganic crystal mixed salt. The quality of the crystallized mixed salt meets the standard of snow-melting agent (GB 23851-2017), so the crystallized mixed salt can be used as the snow-melting agent. The process system does not produce evaporation mother liquor, and realizes full treatment, full reuse and zero discharge of leachate wastewater.
Example 3:
the process of the invention is adopted to treat the percolate of a certain refuse incineration plant, and the water quality conditions are as follows: COD is 30000-50000 mg/L, TDS is 10000-12000 mg/L, NH3N is 1000 to 2000 mg/L.
The anaerobic unit is in an IOC form, the COD of the effluent after the leachate is treated by the anaerobic unit is 3000-5000 mg/L, wherein the biogas generated by the anaerobic unit is purified by biogas and then is sent to a biogas boiler to generate hot water at 50 ℃, and the hot water is sent to the evaporation unit to be used as a heat source for the evaporation unit; anaerobic effluent enters a biochemical unit which adopts an anaerobic ammonia oxidation form, the cutoff molecular weight of an ultrafiltration membrane is 50000 Da, after the anaerobic effluent is treated by the biochemical unit and filtered by the ultrafiltration membrane, the COD (chemical oxygen demand) of the ultrafiltration effluent is 1000 mg/L, and NH (ammonia) is generated3-N is 20-40 mg/L; feeding the ultrafiltration effluent into a first advanced oxidation treatment unit, wherein the first advanced oxidation treatment unit adopts an electron beam device, the irradiation dose rate is 10-20 kGy, the COD of the treated effluent is 400 mg/L, and then the treated effluent enters an EDR electrodialysis device; the EDR device adopts a homogeneous ion membrane, the continuous electrode-reversing operation period is 20min, the EDR fresh water COD is 350 mg/L, TDS to be 800 mg/L after treatment, and the EDR concentrated water COD is 200 mg/L, TDS to be 80000 mg/L; EDR fresh water is sent into a nanofiltration membrane unit, the molecular weight cut-off of the nanofiltration membrane is 400Da, the COD of nanofiltration produced water is 50 mg/L, TDS to 500 mg/L, the EDR fresh water reaches the water supplement standard of circulating cooling water (GB/T19923-2005) for recycling in a factory, the nanofiltration concentrated water is sent into a second advanced oxidation treatment unit, a wet oxidation device is used in the second advanced oxidation treatment unit, the reaction temperature isThe reaction pressure is 1-5 MPa at 200-300 ℃, the COD of the treated effluent is 100 mg/L, and the effluent of the wet oxidation device directly returns to be mixed with the ultrafiltration effluent and then enters a subsequent unit for continuous treatment.
The EDR concentrated water sequentially enters an evaporation unit and a crystallization unit, the evaporator adopts a humidification-dehumidification type evaporator, the maximum evaporation temperature of the evaporator based on the air humidification-dehumidification principle is 45 ℃, a heat source is 50 ℃ hot water of water produced by an anaerobic biogas boiler, and other heat sources are not required to be supplemented. Concentrating the EDR concentrated water to a saturated solution by an evaporator, and then sending the saturated solution into a crystallization unit for further treatment to finally form solid inorganic crystal mixed salt. The quality of the crystallized mixed salt meets the standard of snow-melting agent (GB 23851-2017), so the crystallized mixed salt can be used as the snow-melting agent. The process system does not produce evaporation mother liquor, and realizes full treatment, full reuse and zero discharge of leachate wastewater.
Example 4:
the process of the invention is adopted to treat the percolate of a certain refuse incineration plant, and the water quality conditions are as follows: COD is 30000-50000 mg/L, TDS is 10000-12000 mg/L, NH3N is 1000 to 2000 mg/L.
The anaerobic unit is in a UBF form, the COD of the effluent after the leachate is treated by the anaerobic unit is 6000-8000 mg/L, wherein the biogas generated by the anaerobic unit is purified by biogas and then is sent to a biogas boiler to generate hot water at 90 ℃, and the hot water is sent to the evaporation unit to be used as a heat source for the evaporation unit; anaerobic effluent enters a biochemical unit which adopts a combination form of A/O and anaerobic ammonia oxidation, the cutoff molecular weight of an ultrafiltration membrane is 20000 Da, after the treatment of the biochemical unit and the filtration of the ultrafiltration membrane, the COD of the ultrafiltration effluent is 1000 mg/L, NH3N is 10-20 mg/L; feeding the ultrafiltration effluent into a first advanced oxidation treatment unit, wherein the first advanced oxidation treatment unit adopts a combination unit of an electron beam device and an ozone/hydrogen peroxide oxidation device, the irradiation dose rate of the electron beam device is 10-15 kGy, and H2O2And O3The adding amount ratio of the ozone is 0.3-0.4, the adding amount of the ozone is 0.02-0.08%, the COD of treated effluent is 200 mg/L, and then the effluent enters an EDR electrodialysis device; the EDR device adopts a homogeneous ion membrane, the continuous electrode-reversing operation period is 20min, the EDR fresh water COD is 200 mg/L, TDS to 800 mg/L after treatment, and the EDR concentrated water COD is 100 mg/L, TDS to 80000 mg/L; EDR fresh water is sent into a nanofiltration membrane unit, the molecular weight cut-off of the nanofiltration membrane is 400Da, the COD of nanofiltration product water is 30 mg/L, TDS to be 500 mg/L, the EDR fresh water reaches the reuse water standard for reuse in a factory, nanofiltration concentrated water is sent into a second advanced oxidation treatment unit, the second advanced oxidation treatment unit uses a supercritical oxidation device, the reaction pressure is 22-25 MPa, the reaction temperature is 400-420 ℃, the retention time is 15-30 min, the COD of treated outlet water is 80 mg/L, and the outlet water of a wet oxidation device directly returns to be mixed with ultrafiltration outlet water and then enters a subsequent unit for continuous treatment.
The EDR concentrated water sequentially enters an evaporation unit and a crystallization unit, the evaporator adopts a humidification-dehumidification type evaporator, the maximum evaporation temperature of the evaporator based on the air humidification-dehumidification principle is 80 ℃, a heat source is 90 ℃ hot water of water produced by an anaerobic biogas boiler, and other heat sources do not need to be supplemented. Concentrating the EDR concentrated water to a saturated solution by an evaporator, and then sending the saturated solution into a crystallization unit for further treatment to finally form solid inorganic crystal mixed salt. The quality of the crystallized mixed salt meets the standard of snow-melting agent (GB 23851-2017), so the crystallized mixed salt can be used as the snow-melting agent. The process system does not produce evaporation mother liquor, and realizes full treatment, full reuse and zero discharge of leachate wastewater.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A leachate treatment method, comprising:
firstly, performing biodegradation reaction on penetrating fluid through anaerobic microorganisms to remove partial organic matters in the penetrating fluid;
secondly, biologically denitrifying the penetrating fluid through anaerobic microorganisms to remove part of nitrogen in the penetrating fluid;
thirdly, filtering the penetrating fluid;
fourthly, further degrading organic matters in the penetrating fluid through the first advanced oxidation treatment;
fifthly, treating the penetrating fluid through reversed electrodialysis to obtain first fresh water and first concentrated water;
sixthly, evaporating and crystallizing the first concentrated water to obtain inorganic salt;
seventhly, filtering the first fresh water to obtain second fresh water and second concentrated water, wherein the second fresh water is discharged as produced water;
eighthly, further degrading organic matters in the second concentrated water through second advanced oxidation treatment;
and ninthly, repeatedly executing the third step to the eighth step on the second concentrated water treated in the eighth step.
2. The leachate treatment method according to claim 1, wherein the gas produced by the biodegradation reaction in the first step is collected, desulfurized and dehydrated and then enters a biogas hot water boiler to be combusted to produce hot water, the hot water is used to evaporate and crystallize the first concentrated water in the fifth step, and the hot water is cooled by contacting with the first concentrated water and then returns to the biogas boiler to be heated again.
3. The leachate treatment process of claim 1, wherein the first advanced oxidation treatment comprises one or more combinations of Fenton oxidation, ozone/hydrogen peroxide oxidation, and electron beam oxidation, and the second advanced oxidation treatment comprises one or more combinations of electro-catalytic oxidation, supercritical oxidation, and wet oxidation.
4. The leachate treatment process of claim 1 wherein in the first step, the leachate is subjected to biodegradation reaction using one or more of the combination of an upflow anaerobic sludge blanket reactor, an internal circulation anaerobic reactor, an upflow anaerobic sludge blanket filter, and an internal and external circulation anaerobic reactor.
5. The leachate treatment process of claim 1 wherein in the second step, the permeate is biologically denitrified using one or more of anoxic-aerobic process, partial nitrification-denitrification, and anaerobic ammonia oxidation.
6. The leachate treatment method according to claim 1, wherein in the third step, the leachate is filtered by using an ultrafiltration membrane device, and the cut-off molecular weight is 1000-50000 Da; in the seventh step, a nanofiltration membrane is adopted for filtering, and the range of the molecular weight cut-off is 100-400 Da.
7. The leachate treatment method according to claim 1, wherein in the fifth step, a homogeneous ionic membrane is adopted, and a continuous pole-reversing operation mode is adopted, wherein the pole-reversing period is 20-180 min.
8. A leachate treatment system is characterized by comprising an anaerobic unit, a biochemical unit, an ultrafiltration unit, a first advanced oxidation unit, a reverse electrode electrodialysis unit, a nanofiltration unit, a second advanced oxidation unit, an evaporation unit and a crystallization unit; the anaerobic unit, the biochemical unit, the ultrafiltration unit, the first advanced oxidation unit, the reverse electrode electrodialysis unit and the nanofiltration unit are sequentially connected through pipelines; the second advanced oxidation unit is connected with the nanofiltration unit through a pipeline, and is also connected with a pipeline between the ultrafiltration unit and the first advanced oxidation unit through a pipeline; the evaporation unit is connected to the electrodialysis reversal unit, and the crystallization unit is connected to the evaporation unit.
9. The leachate treatment system of claim 8, further comprising a biogas purification apparatus connected to the anaerobic unit to purify biogas generated by the anaerobic unit, and a biogas boiler for generating hot water by burning the biogas for use by the evaporation unit, wherein the evaporation unit employs a humidification-dehumidification type evaporator.
10. The leachate treatment system of claim 8, wherein said crystallization unit comprises a thickener, a plate and frame filter press, a dryer, and an automatic packing machine.
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