CN104402170A - Landfill leachate treatment method and system thereof - Google Patents
Landfill leachate treatment method and system thereof Download PDFInfo
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- CN104402170A CN104402170A CN201410616983.1A CN201410616983A CN104402170A CN 104402170 A CN104402170 A CN 104402170A CN 201410616983 A CN201410616983 A CN 201410616983A CN 104402170 A CN104402170 A CN 104402170A
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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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
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Abstract
The invention relates to a landfill leachate treatment method and a system thereof, and belongs to the technical field of sewage biological treatment. The method comprises the following steps: a landfill leachate containing high concentration organic pollutants and ammonia nitrogen enters an anaerobic treatment unit to remove most organic pollutants and reduce the C/N ratio to below 2:1; the obtained landfill leachate enters an anaerobic ammoxidation unit to realize the ammonia nitrogen removal rate of 85% and the total nitrogen removal rate of 80% without adding an external carbon source; and the obtained landfill leachate enters a biochemical treatment unit, the aerobic segment of the biochemical treatment unit is a membrane bioreactor generally, and a carbon oxidation reaction and a nitrification and denitrification reaction are carried out to further remove the remaining organic pollutants, ammonia nitrogen and total nitrogen. The method has the advantages of no need of the external carbon source, high nitrogen removal efficiency, stable system running, and low output of residual sludge. The anaerobic treatment unit can greatly reduce the organic matters in water, regenerates biogas and uses the biogas, and the tank body of the anaerobic ammoxidation unit is heated and insulated, so recycling of the organic matters in the leachate is realized, and the treatment cost is further reduced.
Description
Technical field
The present invention relates to a kind of method for treating garbage percolation liquid and system thereof, particularly the landfill leachate treatment of high ammonia nitrogen, high COD, belongs to technical field of biological sewage treatment.
Background technology
Percolate has pollutant component complexity, Pollutant levels are high, pollutant kind is many, C/N than features such as imbalances, its COD concentration is generally 2000mg/L ~ 50000mg/L, and ammonia nitrogen concentration is 2000mg/L ~ 8000mg/L; The percolate that the facility such as incineration plant, Refuse bin produces due to fermentation time short, document shows that its chemical oxygen demand (COD) (hereinafter referred to as COD), ammonia nitrogen concentration can up to 80000mg/L, 10000mg/L, and Pollutant levels are too high, C/N proposes huge technological challenge to process up to standard than features such as numerous imbalances.
Garbage leachate treatment process conventional is at present " anaerobic reactor+membrane bioreactor (hereinafter referred to as MBR) ", wherein the object of anaerobic reactor significantly removes organic pollutant, its water outlet COD value can reach 4000mg/L ~ 6000mg/L, and organonitrogen is converted into ammonia nitrogen; Membrane bioreactor (MBR) is made up of anoxic pond, Aerobic Pond and ultra-filtration membrane, reacts further organics removal pollutent COD by oxidation of coal, and removes total nitrogen by nitration denitrification reaction.
Theoretical according to biological denitrificaion, in membrane bioreactor during denitrogenation, C/N should be kept to be between 6 ~ 9, to ensure normally carrying out of nitrated, anti-nitration reaction.Therefore, in above-mentioned garbage leachate treatment process, water enters membrane bioreactor after anaerobic reactor, and its ammonia nitrogen is generally 2000mg/L ~ 3000mg/L, occurs following problem:
Needed for a, denitrogenation, COD should be between 12000mg/L ~ 18000mg/L, and after anaerobic reactor, COD concentration is 4000mg/L ~ 6000mg/L, cannot meet the demands, and needs additionally to add carbon source, creates higher processing cost;
After b, anaerobic reactor, the COD of remaining 4000mg/L ~ 6000mg/L removes with aerobic form, compares anaerobic treatment cost higher;
C, anoxic, aerobic nitrogen removal technique need higher reflux ratio, further increase running cost; Be subject to the restriction of technique itself, when reflux ratio is 400%, nitrogen removal rate is only 80% simultaneously, cannot reach Effluent criteria when total nitrogen of intaking is too high;
The principle of anaerobic ammonia oxidation process be anaerobic ammonia oxidizing bacteria under anaerobic, be that ammonia nitrogen is direct oxidation into nitrogen by electron acceptor(EA) with nitrite, compared with, denitrification denitrogenation technique nitrated with traditional, its principal feature does not need to add additional carbon, running cost is cheap, reduces the ammonia nitrogen loading of subsequent treatment process.Adopt anaerobic ammonia oxidation process, the clearance of ammonia nitrogen can reach 85%, and nitrogen removal rate can reach 80%.Sewage after anaerobism and Anammox process, organic pollutant still containing higher concentration and ammonia nitrogen, membrane bioreactor (MBR) is set, utilize oxidation of coal and nitrated, anti-nitration reaction, organic pollutant, ammonia nitrogen and total nitrogen in further removal sewage, then utilize membrane module to carry out solid-liquid separation.
In sum, percolate effectively removes ammonia nitrogen, total nitrogen before entering membrane bioreactor, and remove organic pollutant accordingly, be the key factor affecting garbage leachate treatment process, discharge significant to reduction running cost, raising processing efficiency, stably reaching standard.
Summary of the invention
The object of the invention is to propose a kind of method for treating garbage percolation liquid and system thereof, utilize the combination process of the technical unit such as multistage anaerobic, Anammox, solve conventional processing technique exist operation energy consumption high, need additionally to add the shortcomings such as carbon source, outlet effect be unstable, to be applied to the process of the percolate of the facility such as refuse landfill, garbage burning factory.
The method for treating garbage percolation liquid that the present invention proposes, comprises the following steps:
(1) percolate is made to enter one-level anaerobic treatment reactor, percolate stops 8 ~ 12 days in one-level anaerobic treatment reactor, the sludge concentration produced when percolate is stopped is reached for 8 ~ 13g/L, make sludge retention time in one-level anaerobic treatment reactor be 25 ~ 40 days, make the dissolved oxygen in one-level anaerobic treatment reactor be 0.1 ~ 0.5mg/L;
(2) above-mentioned coagulation liquid is made to enter secondary anaerobic treatment reactor, stop 4 ~ 10 days in secondary anaerobic treatment reactor at coagulation liquid, the sludge concentration produced when coagulation liquid is stopped is reached for 6 ~ 12g/L, sludge retention time in two anaerobic treatment reactors is made to be 18 ~ 35 days, make the dissolved oxygen in secondary anaerobic treatment reactor be 0.1 ~ 0.5mg/L, obtain anaerobic treatment liquid;
(3) above-mentioned anaerobic treatment liquid is made to enter in anaerobic ammonia oxidation reactor, the sludge concentration that anaerobic treatment liquid is produced in anaerobic ammonia oxidation reactor is reached for 3 ~ 10g/L, sludge retention time in anaerobic ammonia oxidation reactor (SRT) is made to be 10 ~ 35 days, oxygen is blasted to anaerobic ammonia oxidation reactor, dissolved oxygen (DO) value in anaerobic ammonia oxidation reactor is made to be 0.1 ~ 0.5mg/L, control at-200mV ~ 50mV with reference to redox potential (ORP), obtain the Anammox treatment solution after removing nitrogen;
(4) Anammox treatment solution is made to enter settling tank, Anammox treatment solution is made to stop 1.5-2.5 hour in settling tank, Anammox treatment solution is made to carry out solid-liquid separation, obtain supernatant liquor and anaerobic ammonium oxidation sludge, and make anaerobic ammonium oxidation sludge wherein be back in anaerobic ammonia oxidation reactor;
(5) supernatant liquor of step (4) is made, and in step (6) phegma mixing after enter anoxic pond, mixed solution is made to stop 0.5-1 hour in anoxic pond, dissolved oxygen (DO) value in anoxic pond is made to be 0.2 ~ 1.0mg/L, sludge concentration is 3 ~ 4.5g/L, obtains anaerobic treatment liquid;
(6) the anoxic pond treatment solution of step (5) is made to enter Aerobic Pond, anaerobic treatment liquid residence time in Aerobic Pond is 1.5-4 hour, oxygen is blasted in Aerobic Pond, dissolved oxygen (DO) value in Aerobic Pond is made to be 2.5 ~ 4.0mg/L, sludge concentration is 3 ~ 4.5g/L, Aerobic Pond end-o f-pipe-control liquid is made to be back to anoxic pond, reflux ratio is 200-400%, at Aerobic Pond end or rear portion, ultra-filtration membrane is set, make Aerobic Pond end-o f-pipe-control liquid obtain solid-liquid separation, the aerobic treatment liquid after solid-liquid separation is treatment system water outlet.
The garbage percolation liquid treating system that the present invention proposes, comprising: one-level anaerobic reactor, secondary anaerobic reactor, anaerobic ammonia oxidation reactor, settling tank, anoxic pond, Aerobic Pond, membrane module and gas blower, the entrance end of described one-level anaerobic reactor is connected with water, the exit end of one-level anaerobic reactor is connected with described secondary anaerobic reactor, the exit end of secondary anaerobic reaction is connected with the entrance end of described anaerobic ammonia oxidation reactor, the water outlet of anaerobic ammonia oxidation reactor enters settling tank, the exit end of settling tank is connected with the entrance end of described anoxic pond, the water outlet of anoxic pond enters described Aerobic Pond, the entrance end of anoxic pond is delivered in the part water outlet of Aerobic Pond by reflux pump, the water outlet of Aerobic Pond enters membrane module and carries out solid-liquid separation, air is sent into anaerobic ammonia oxidation reactor and Aerobic Pond by described gas blower, to meet anaerobic ammonia oxidation reactor and Aerobic Pond to the demand of oxygen.
The method for treating garbage percolation liquid that the present invention proposes and system thereof, have the following advantages:
1, method for treating garbage percolation liquid of the present invention, fully in conjunction with the advantage that anaerobic reactor removes COD, Anammox technology removes total nitrogen, membrane bioreactor high efficiency separation, multistage anaerobic reactor, Anammox technology, membrane Bio-reactor Technology are combined, the inventive method is had does not need the advantages such as additional carbon, nitric efficiency are high, system run all right, excess sludge production are low.
2, garbage percolation liquid treating system of the present invention, by arranging multistage anaerobic reactor, can effectively reduce the COD concentration in percolate, reduces processed in units cost, for follow-up Anammox unit creates favourable flow condition; The recycling of organic pollutant can also be realized simultaneously, the biogas utilizing anaerobic reactor to produce is Anammox unit heating and thermal insulation, Anammox unit significantly can remove ammonia nitrogen, the total nitrogen of system, the load of subsequent film bio-reactor is reduced to normal level, can fully play out that Membrane Bioreactor for Wastewater Treatment efficiency is high, the advantage of good effect of separating solid from liquid, denitrogenation stability and high efficiency, make its stable water outlet up to standard; Utilize anaerobic reactor to remove COD, utilize Anammox technology to carry out denitrogenation, compare aerobic removal COD, nitration denitrification denitrogenation in traditional technology, greatly reduce the cost such as blast aeration, pumping backflow, overall power consumption reduces by 50 ~ 60%; Not needing additionally to add carbon source, is a kind of continuable biologic treating technique.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of garbage leachate treatment process of the present invention
In Fig. 1,1 is one-level anaerobic reactor, and 2 is secondary anaerobic reactors, and 3 is anaerobic ammonia oxidation reactors, and 4 is settling tanks, and 5 is anoxic pond, and 6 is Aerobic Ponds, and 7 is membrane modules, and 8 is reflux pumps, and 9 is gas blowers.
Embodiment
The method for treating garbage percolation liquid that the present invention proposes, comprises the following steps:
(1) percolate is made to enter one-level anaerobic treatment reactor, percolate stops 8 ~ 12 days in one-level anaerobic treatment reactor, the sludge concentration produced when percolate is stopped is reached for 8 ~ 13g/L, sludge retention time (SRT) in one-level anaerobic treatment reactor is made to be 25 ~ 40 days, the dissolved oxygen (DO) in one-level anaerobic treatment reactor is made to be 0.1 ~ 0.5mg/L, the object of this step removes the organism of percolate, namely realize, to the clearance of chemical oxygen demand (COD) (COD) 70 ~ 85%, obtaining coagulation liquid;
(2) above-mentioned coagulation liquid is made to enter secondary anaerobic treatment reactor, stop 4 ~ 10 days in secondary anaerobic treatment reactor at coagulation liquid, the sludge concentration produced when coagulation liquid is stopped is reached for 6 ~ 12g/L, make sludge retention time (SRT) in two anaerobic treatment reactors be 18 ~ 35 days, make the dissolved oxygen (DO) in secondary anaerobic treatment reactor be 0.1 ~ 0.5mg/L; The object of this step removes the organism in coagulation liquid further, namely realizes, to the clearance of chemical oxygen demand (COD) (COD) 60 ~ 75%, obtaining anaerobic treatment liquid;
(3) above-mentioned anaerobic treatment liquid is made to enter in anaerobic ammonia oxidation reactor, the sludge concentration that anaerobic treatment liquid is produced in anaerobic ammonia oxidation reactor is reached for 3 ~ 10g/L, sludge retention time in anaerobic ammonia oxidation reactor (SRT) is made to be 10 ~ 35 days, oxygen is blasted to anaerobic ammonia oxidation reactor, dissolved oxygen (DO) value in anaerobic ammonia oxidation reactor is made to be 0.1 ~ 0.5mg/L, control at-200mV ~ 50mV with reference to redox potential (ORP), obtain the Anammox treatment solution after removing nitrogen; The object of this step makes the ammonia nitrogen in anaerobic treatment liquid be obtained by reacting removal by Anammox, and realize ammonia nitrogen removal frank and be greater than 85%, nitrogen removal rate is greater than 80%;
(4) Anammox treatment solution is made to enter settling tank, Anammox treatment solution is made to stop 1.5-2.5 hour in settling tank, Anammox treatment solution is made to carry out solid-liquid separation, obtain supernatant liquor and anaerobic ammonium oxidation sludge, and make anaerobic ammonium oxidation sludge wherein be back in anaerobic ammonia oxidation reactor;
(5) supernatant liquor of step (4) is made, and in step (6) phegma mixing after enter anoxic pond, mixed solution is made to stop 0.5-1 hour in anoxic pond, dissolved oxygen (DO) value in anoxic pond is made to be 0.2 ~ 1.0mg/L, sludge concentration is 3 ~ 4.5g/L, obtains anaerobic treatment liquid; The object of this step is that remaining nitrate nitrogen in supernatant liquor, by anti-nitration reaction, is removed from system with nitrogen form.
(6) the anoxic pond treatment solution of step (5) is made to enter Aerobic Pond, anaerobic treatment liquid residence time in Aerobic Pond is 1.5-4 hour, oxygen is blasted in Aerobic Pond, dissolved oxygen (DO) value in Aerobic Pond is made to be 2.5 ~ 4.0mg/L, sludge concentration is 3 ~ 4.5g/L, in Aerobic Pond, reflux pump is set, Aerobic Pond end-o f-pipe-control liquid is made to be back to anoxic pond, reflux ratio is 200-400%, at Aerobic Pond end or rear portion, ultra-filtration membrane is set, make Aerobic Pond end-o f-pipe-control liquid obtain solid-liquid separation, the aerobic treatment liquid after solid-liquid separation is treatment system water outlet.The object of this step makes remaining organism in anoxic pond treatment solution be oxidized and remove, and the ammonia nitrogen in anoxic pond treatment solution is oxidized to nitrate nitrogen, is removed after being back to anoxic pond with phegma.
The garbage percolation liquid treating system that the present invention proposes, its structure as shown in Figure 1, comprising: one-level anaerobic reactor 1, secondary anaerobic reactor 2, anaerobic ammonia oxidation reactor 3, settling tank 4, anoxic pond 5, Aerobic Pond 6, membrane module 7 and gas blower 8, the entrance end of one-level anaerobic reactor 1 is connected with water, the exit end of one-level anaerobic reactor 1 is connected with secondary anaerobic reactor 2, the exit end of secondary anaerobic reaction 2 is connected with the entrance end of anaerobic ammonia oxidation reactor 3, the water outlet of anaerobic ammonia oxidation reactor 3 enters settling tank 4, the exit end of settling tank 4 is connected with the entrance end of described anoxic pond 5, the water outlet of anoxic pond 5 enters described Aerobic Pond 6, the entrance end of anoxic pond 5 is delivered in the part water outlet of Aerobic Pond 6 by reflux pump 8, the water outlet of Aerobic Pond 6 enters membrane module 7 and carries out solid-liquid separation, air is sent into anaerobic ammonia oxidation reactor 3 and Aerobic Pond 6 by described gas blower 9, to meet anaerobic ammonia oxidation reactor and Aerobic Pond to the demand of oxygen.
By reference to the accompanying drawings technology involved in the present invention is described further.
In the garbage percolation liquid treating system that the present invention proposes, anaerobic treatment adopts multistage anaerobic reactor (2 grades and more than), realizes higher Ammoniation efficiency and COD clearance.One-level anaerobic reactor maintains higher sludge concentration, runs under high-load condition, and the COD in water inlet is reduced by 70 ~ 85%; Secondary anaerobic reactor sludge concentration, load are lower slightly compared with one-level anaerobic reactor, reduce COD further, realize clearance 60% ~ 75%, make it meet the favourable operational conditions of subsequent film bio-reactor.When inlet COD concentration is too high, when two-stage anaerobic reactor can not meet COD processing requirements, the mode of three grades of anaerobic reactor series connection can be adopted.In the practical application of this technology, usually select the anaerobic reactor such as anaerobic biofilter, UASB, IC, EGSB, also can select other anaerobic reactors;
Anaerobic ammonia oxidation reactor 3 in treatment system of the present invention, rely on the removal of effect realization to nitrogen of microorganism, its concrete form of implementation can be implemented with active sludge state, biofilm states, its pond type can be rectangular plug-flow configuration, also can be channel-type structure, also can adopt the water decanter form of Inlet and outlet water simultaneously.Anaerobic ammonium oxidation tank adopts major control dissolved oxygen, with reference to the operation scheme of controlled oxidization reduction potential (ORP), restriction gas blower is to the keeping of Chi Tizhong, create the dominant growth condition of Anammox flora, make nitrite bacteria can be nitrite nitrogen by part ammonium oxidation, nitrite nitrogen is converted into nitrogen with other ammonia nitrogens again under the effect of anaerobic ammonium oxidizing bacteria, realizes the removal of total nitrogen.
Anoxic pond in present treatment system and Aerobic Pond constitute A/O denitrification system jointly, after the process of two-stage anaerobic reactor and anaerobic ammonia oxidation reactor, during A/O system is intake, C/N ratio reaches proper ratio, be beneficial to A/O denitrification system and remove remaining COD, ammonia nitrogen etc. in water simultaneously, stablize and reach Chinese effluent standard.
Anaerobic ammonia oxidation reactor in treatment system of the present invention, rely on the removal of effect realization to nitrogen of microorganism, comprise Anammox reaction, short-cut denitrification reaction etc., its microorganism mainly comprises anaerobic ammonia oxidizing bacteria, autotrophic type denitrifying bacteria and heterotroph denitrifying bacteria etc.; Under the condition not needing additional carbon, realize ammonia nitrogen removal frank and be greater than 85%, nitrogen removal rate is greater than 80%.Anaerobic ammonia oxidation reactor provides oxygen by gas blower, for the carrying out of nitrosation reaction, as being nitrite nitrogen etc. by ammonium oxidation.
Membrane module in treatment system of the present invention, adopts built-in ultra-filtration membrane.
Below introduce one embodiment of the present of invention:
The percolate concentration that destructor plant produces is higher, and COD reaches 75000mg/L, and TKN reaches 3000mg/L.Owing to adopting common process intractability large, cost is higher, uses the inventive method and system to process, water inlet is introduced into anaerobic treatment unit, and select two stage UASB reactor, COD removal efficiency reaches 80%, 70% respectively, water outlet COD is reduced to 4500mg/L, makes C/N ratio reach 1.5:1.Follow-up Anammox unit selects flow lifting type anaerobic ammonia oxidation reactor, its influent COD 4500mg/L, ammonia nitrogen 3000mg/L, and by blast aeration for reactor provides oxygen, carry out Anammox reaction, water outlet ammonia reaches nitrogen 450mg/L.Follow-uply enter biochemical reaction unit, this unit is A/O technique, and O section selects membrane bioreactor, adopts micro-pore aeration mode, uses built-in ultra-filtration membrane to carry out solid-liquid separation.After membrane bioreactor, realize water outlet ammonia nitrogen and be less than 10mg/L, TN and be less than 40mg/L, meet " household refuse landfill sites Environmental capacity standard (GB16889-2008 " table 2 requirement.Entire system is stable, and outlet effect is good, compares traditional nitration denitrification denitrogenation process, and overall power consumption reduces by 58%.
The chemical oxygen demand COD (Chemical Oxygen Demand) related in the inventive method chemically measures in water sample the amount needing oxidized reducing substances, refer in waste water, wastewater treatment plant effluent and contaminated water, the oxygen equivalent of the material (being generally organism) that can be oxidized by strong oxidizer.In the operational management of trade effluent Quality Research and waste water treatment plant, it is important and can comparatively fast measure an Organic pollutants parameter, often represents with symbol COD.
The sludge retention time SRT (Sludge Retention Time) related in the inventive method, refers to the mean residence time of pond microorganism cells in reaction tank, namely mud mud age.The dissolved oxygen DO (Dissolved Oxygen) related to, refers to that the molecular oxygen in air is dissolved in water, is called dissolved oxygen.Redox potential ORP (Oxidation-ReductionPotential) is the relative extent characterizing medium oxidizing property or reductibility.Redox potential is higher, and oxidisability is stronger, and current potential is lower, and oxidisability is more weak.Current potential is just representing that solution demonstrates certain oxidisability, then illustrates that solution demonstrates reductibility for negative.
Claims (2)
1. a method for treating garbage percolation liquid, is characterized in that the method comprises the following steps:
(1) percolate is made to enter one-level anaerobic treatment reactor, percolate stops 8 ~ 12 days in one-level anaerobic treatment reactor, the sludge concentration produced when percolate is stopped is reached for 8 ~ 13g/L, make sludge retention time in one-level anaerobic treatment reactor be 25 ~ 40 days, make the dissolved oxygen in one-level anaerobic treatment reactor be 0.1 ~ 0.5mg/L;
(2) above-mentioned coagulation liquid is made to enter secondary anaerobic treatment reactor, stop 4 ~ 10 days in secondary anaerobic treatment reactor at coagulation liquid, the sludge concentration produced when coagulation liquid is stopped is reached for 6 ~ 12g/L, sludge retention time in two anaerobic treatment reactors is made to be 18 ~ 35 days, make the dissolved oxygen in secondary anaerobic treatment reactor be 0.1 ~ 0.5mg/L, obtain anaerobic treatment liquid;
(3) above-mentioned anaerobic treatment liquid is made to enter in anaerobic ammonia oxidation reactor, the sludge concentration that anaerobic treatment liquid is produced in anaerobic ammonia oxidation reactor is reached for 3 ~ 10g/L, sludge retention time in anaerobic ammonia oxidation reactor (SRT) is made to be 10 ~ 35 days, oxygen is blasted to anaerobic ammonia oxidation reactor, dissolved oxygen (DO) value in anaerobic ammonia oxidation reactor is made to be 0.1 ~ 0.5mg/L, control at-200mV ~ 50mV with reference to redox potential (ORP), obtain the Anammox treatment solution after removing nitrogen;
(4) Anammox treatment solution is made to enter settling tank, Anammox treatment solution is made to stop 1.5-2.5 hour in settling tank, Anammox treatment solution is made to carry out solid-liquid separation, obtain supernatant liquor and anaerobic ammonium oxidation sludge, and make anaerobic ammonium oxidation sludge wherein be back in anaerobic ammonia oxidation reactor;
(5) supernatant liquor of step (4) is made, and in step (6) phegma mixing after enter anoxic pond, mixed solution is made to stop 0.5-1 hour in anoxic pond, dissolved oxygen (DO) value in anoxic pond is made to be 0.2 ~ 1.0mg/L, sludge concentration is 3 ~ 4.5g/L, obtains anaerobic treatment liquid;
(6) the anoxic pond treatment solution of step (5) is made to enter Aerobic Pond, anaerobic treatment liquid residence time in Aerobic Pond is 1.5-4 hour, oxygen is blasted in Aerobic Pond, dissolved oxygen (DO) value in Aerobic Pond is made to be 2.5 ~ 4.0mg/L, sludge concentration is 3 ~ 4.5g/L, Aerobic Pond end-o f-pipe-control liquid is made to be back to anoxic pond, reflux ratio is 200-400%, at Aerobic Pond end or rear portion, ultra-filtration membrane is set, make Aerobic Pond end-o f-pipe-control liquid obtain solid-liquid separation, the aerobic treatment liquid after solid-liquid separation is treatment system water outlet.
2. a garbage percolation liquid treating system, is characterized in that this system comprises: one-level anaerobic reactor, secondary anaerobic reactor, anaerobic ammonia oxidation reactor, settling tank, anoxic pond, Aerobic Pond, membrane module and gas blower, the entrance end of described one-level anaerobic reactor is connected with water, the exit end of one-level anaerobic reactor is connected with described secondary anaerobic reactor, the exit end of secondary anaerobic reaction is connected with the entrance end of described anaerobic ammonia oxidation reactor, the water outlet of anaerobic ammonia oxidation reactor enters settling tank, the exit end of settling tank is connected with the entrance end of described anoxic pond, the water outlet of anoxic pond enters described Aerobic Pond, the entrance end of anoxic pond is delivered in the part water outlet of Aerobic Pond by reflux pump, the water outlet of Aerobic Pond enters membrane module and carries out solid-liquid separation, air is sent into anaerobic ammonia oxidation reactor and Aerobic Pond by described gas blower, to meet anaerobic ammonia oxidation reactor and Aerobic Pond to the demand of oxygen.
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| CN105384242A (en) * | 2015-12-28 | 2016-03-09 | 郑州轻工业学院 | Starting method of process for synchronously removing carbon, nitrogen and suspended matter in low carbon source wastewater through membrane bioreactor |
| CN108191161A (en) * | 2018-01-25 | 2018-06-22 | 轻工业环境保护研究所 | It is a kind of to handle biogas slurry technique using sulfate reducing bacteria |
| CN109607786A (en) * | 2018-12-21 | 2019-04-12 | 济南尚方环保科技有限公司 | A kind of combined anaerobic ammoxidation-anaerobism-membrane bioreactor sewage-treatment plant and method |
| CN110204045A (en) * | 2018-12-31 | 2019-09-06 | 上海康恒环境股份有限公司 | A kind of method of municipal solid waste incinerator percolate treating process drop total nitrogen |
| JP2020075233A (en) * | 2018-11-01 | 2020-05-21 | 株式会社クボタ | Organic wastewater treatment device and operation method of the same |
| WO2020119217A1 (en) * | 2018-12-10 | 2020-06-18 | 北京城市排水集团有限责任公司 | Anaerobic ammoxidation synergistic nitrogen removal process device of municipal sewage main and side streams and application method thereof |
| CN111499133A (en) * | 2020-04-17 | 2020-08-07 | 宁波财经学院 | Device for simultaneously treating excess sludge and leachate |
| CN112062398A (en) * | 2020-09-04 | 2020-12-11 | 浙江埃克钛环境科技有限公司 | Method for treating landfill leachate |
| CN114275976A (en) * | 2021-12-31 | 2022-04-05 | 珠海力新环保有限公司 | Full-quantitative treatment process for landfill leachate |
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