CN116282683B - sMBR garbage leachate treatment system and process reflux method thereof - Google Patents
sMBR garbage leachate treatment system and process reflux method thereof Download PDFInfo
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- 238000010992 reflux Methods 0.000 title claims abstract description 90
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims description 73
- 239000010802 sludge Substances 0.000 claims description 42
- 230000001546 nitrifying effect Effects 0.000 claims description 24
- 239000000149 chemical water pollutant Substances 0.000 claims description 10
- 238000000108 ultra-filtration Methods 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 8
- 239000012528 membrane Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- 239000000243 solution Substances 0.000 description 42
- 239000012141 concentrate Substances 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 230000002349 favourable effect Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000010276 construction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 206010017472 Fumbling Diseases 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F3/302—Nitrification and denitrification treatment
- C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
-
- 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
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
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- Environmental & Geological Engineering (AREA)
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- Organic Chemistry (AREA)
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Abstract
The application relates to an sMBR garbage leachate treatment system and a process reflux method thereof, and relates to the technical field of garbage leachate treatment.
Description
Technical Field
The application relates to the field of landfill leachate treatment, in particular to a sMBR landfill leachate treatment system and a process reflux method thereof.
Background
The landfill leachate is high-concentration organic wastewater which is obtained by infiltration due to substance fermentation, rain wash and groundwater soaking in the process of stacking and landfill of the garbage, and has complex water quality and great environmental hazard.
At present, sMBR (two-stage AO+external ultrafiltration UF) +NF (nanofiltration)/RO (reverse osmosis) technology is adopted for garbage leachate treatment, sMBR comprises an AO unit and a UF device, the AO unit comprises a primary A pool, a primary O pool, a secondary A pool and a secondary O pool which are sequentially communicated, the UF device is provided with an inlet end and an outlet end, the other end of the secondary O pool is communicated with the UF inlet end, and the UF device is adopted to realize total backflow of sludge, so that the biochemical pool can be designed to adopt very high sludge concentration, and has the advantages of large biomass, long sludge age, small sludge load, good treatment effect, small sludge yield and great advantages.
However, besides the conventional internal and external reflux, the reflux quantity of the AO unit in the process flow is 7-10 times of the water inlet treatment capacity according to the characteristics of the external UF device, and the stable operation of a biochemical system is influenced by the reflux of the high flow, so that the water quality of the effluent is always out of standard.
The sMBR stably operates, the concentration of suspended solid MLSS in the mixed solution is ensured, the mixed solution is influenced by the dilution of inlet water, and the first-stage A pool needs to be supplemented with sludge with a concentration higher than the designed concentration to ensure the concentration of MLSS in the first-stage A pool. Therefore, in theory, the traditional sMBR process needs to reflux all UF device concentrated solution to the first-stage A pool to meet the requirements, however, the UF device concentrated solution is completely refluxed to the first-stage A pool to meet the MLSS concentration, but the energy consumption for removing nitrogen-containing denitrification in the inflow water is greatly increased due to the greatly increased flow rate of the inflow water, and a large amount of residual dissolved oxygen carried by the concentrated solution can enter the first-stage A pool along with the concentrated solution, so that the normal operation of the first-stage A pool mainly bearing denitrification is severely disturbed.
In actual operation, a great deal of concentrated solution of the UF device is returned to the primary O pool, and a reflux pump is arranged in the primary O pool to return the solution to the primary A pool, so that under the condition, the concentration of nitrate nitrogen in the primary O pool is greatly diluted, and the denitrification efficiency can not reach ideal data at the cost of high reflux ratio and high energy consumption.
The UF concentrate with several times of water inflow flows back into the first-stage A pool or the first-stage O pool, so that the hydraulic load of the UF concentrate entering the second-stage AO system is increased by several times, and the total nitrogen load is far larger under ideal conditions, which can lead to Chi Rongzeng of the second-stage AO system to be large, and the construction investment is increased.
Disclosure of Invention
The application aims to provide a sMBR garbage leachate treatment system and a sMBR process reflux method which have high denitrification efficiency and low manufacturing cost.
The sMBR garbage leachate treatment system provided by the application adopts the following technical scheme:
the utility model provides a sMBR landfill leachate treatment system, includes AO unit and UF device, the UF device is equipped with UF entrance point and UF exit end, the AO unit is including the one-level A pond, one-level O pond, second grade A pond and the second grade O pond of intercommunication in proper order, sMBR landfill leachate treatment system still includes disk separator and backward flow storage tank, the second grade O pond with be provided with first pipeline between the UF entrance point, the both ends of first pipeline respectively with second grade O pond with UF entrance point intercommunication, be provided with feed pump and circulating pump on the first pipeline, the feed pump sets up first pipeline is close to the one end of second grade O pond, the circulating pump sets up first pipeline is kept away from the one end of second grade O pond, the disk separator respectively with one-level A pond with backward flow storage tank intercommunication, backward flow storage tank with UF exit end intercommunication.
In order to avoid interference caused by residual dissolved oxygen, in actual operation, the concentrated solution of the UF device is often partially refluxed to the first-stage A pool, so that the running sludge concentration of the first-stage AO system cannot meet the design requirement, the suspended solid MLSS concentration is reduced under the condition that the volume of the biochemical reaction pool is unchanged, the sludge load is improved, the treatment efficiency is reduced, the pollution load of the second-stage AO system is increased, and a larger pool capacity is needed to meet the removal requirement.
Through adopting above-mentioned technical scheme, the disk separator can carry out centrifugal separation to the concentrate that forms after UF device ultrafiltration, and the concentrate after centrifugal separation forms clear solution and dewatered sludge, and dewatered sludge discharges into one-level A pond in order to satisfy one-level A pond's MLSS concentration requirement, and the concentrate also no longer is favorable to improving denitrification efficiency through a large amount of backward flows to one-level O pond and pump again and carry one-level A pond.
The nitrifying liquid in the second-stage O pool enters the UF device from the inlet end through the feed pump, the circulating pump provides power to meet the cross flow speed requirement of the mixed liquid in the UF device, the nitrifying liquid is ultrafiltered by the UF device to form clear liquid and concentrated liquid, the clear liquid enters the next-stage treatment process unit, part of concentrated liquid flows out from the outlet end and enters the reflux storage tank, and the residual concentrated liquid enters the UF device from the inlet end to continue ultrafiltering treatment.
Optionally, the reflux storage tank is communicated with the secondary A tank.
In the traditional sMBR reflux pipeline design, a concentrated solution reflux pipeline is respectively arranged in a primary A tank, a primary O tank, a secondary A tank and a secondary O tank, and a reflux pump is arranged to provide power for the reflux of concentrated solution;
in the design of multiple return pipelines, the reflux quantity of the concentrated solution returned by the UF device to each pool cannot be accurately determined, and the design flow quantity value of each return branch pipe adopts the total reflux of the concentrated solution of the UF device as the pipeline flow design, namely 7-10 times of the water inlet flow;
in addition, in the design of multiple return pipelines, the return flow of the UF device to different AO pools can be controlled by operation and maintenance personnel to be less than or equal to 1 time of the inflow flow. Under the running condition, the flow speed of the reflux branch is only 1/(7-10) of the designed value, and the extremely low flow speed can cause the pollution and blockage in the pipeline.
Through adopting above-mentioned technical scheme, the backward flow storage tank only communicates with second grade A pond and video disc separating centrifuge, and connecting tube quantity reduces for the pipe diameter design of backward flow pipeline has also reduced the dirty stifled possibility of pipeline in more reasonable, and no longer is equipped with the backwash pump with the backward flow pipeline of second grade A pond intercommunication, and the reduction of connecting tube quantity and backwash pump has reduced the construction cost and the operation energy consumption of sMBR equipment.
Optionally, a second pipeline is arranged between the backflow storage tank and the disc separator, two ends of the second pipeline are respectively communicated with the backflow storage tank and the disc separator, a stop valve, a sludge backflow feed pump and an electromagnetic flowmeter are arranged on the second pipeline, the sludge backflow feed pump is arranged at one end, far away from the disc separator, of the second pipeline, the stop valve is arranged behind the sludge backflow feed pump, the electromagnetic flowmeter is arranged behind the stop valve, and the length of a front straight pipe section of the electromagnetic flowmeter is at least 5 times of the diameter of the pipeline.
In the traditional sMBR backflow pipeline design, a stop valve is arranged on a backflow pipeline instead of a flow measuring instrument, so that actual operation cannot control backflow quantity of each pool accurately in real time, and the system is easy to collapse when the treated water quantity changes due to long-term fumbling adjustment control of operation and maintenance personnel;
through adopting above-mentioned technical scheme, electromagnetic flowmeter can measure the concentrate reflux volume that gets into the second pipeline, and operation and maintenance personnel can calculate according to mud concentration and inflow and obtain suitable concentrate reflux volume, and the size that the concentrate reflux volume that shows according to electromagnetic flowmeter adjusts the stop valve and control the entering into the second pipeline reaches the calculated value at last, is favorable to accurate regulation and control.
Optionally, a first stirrer is arranged in the first-stage pool A.
Through adopting above-mentioned technical scheme, the dehydrated sludge that forms through disc separating centrifuge centrifugal separation can more abundant mixing with the solution in the first class A pond under the stirring effect of first mixer after entering first class A pond, is favorable to improving denitrification efficiency.
Optionally, a third pipeline is arranged between the first-stage O pool and the first-stage A pool, two ends of the third pipeline are respectively communicated with the first-stage O pool and the first-stage A pool, and a reflux pump for pumping the first-stage O pool solution back to the first-stage A pool is arranged on the third pipeline.
By adopting the technical scheme, the nitrified liquid formed after the primary O pool treatment is refluxed to the primary A pool for denitrification under the action of the reflux pump.
Optionally, a second stirrer is arranged in the reflux storage tank.
Through adopting above-mentioned technical scheme, the concentrate that enters into the backward flow storage tank is through the intensive mixing of second mixer, is favorable to guaranteeing the material even, prevents the deposit.
The application also discloses an sMBR process reflux method adopting the sMBR landfill leachate treatment system, which comprises the following steps:
s1, primary denitrification: the garbage leachate enters a primary A pool and then flows into a primary O pool, nitrifying liquid is formed after the effect of the primary A pool and the primary O pool, and part of primary nitrifying liquid flows back to the primary A pool through a nitrifying liquid reflux pump;
s2, secondary denitrification: the nitrifying liquid in the primary O pool enters the secondary A pool for denitrification and then enters the secondary O pool;
s3, ultrafiltration: the nitrifying liquid in the second-stage O pool enters the UF device through a first pipeline under the action of a feed pump, the circulating pump provides power to meet the requirement of cross flow velocity of the nitrifying liquid in the membrane pipe, clear liquid and concentrated liquid are formed after the nitrifying liquid is subjected to ultrafiltration, and the clear liquid enters the next treatment unit;
s4, splitting concentrated solution: part of concentrated solution flows back to the UF device from the first pipeline under the action of the circulating pump, the rest enters a backflow storage tank, part of concentrated solution in the backflow storage tank enters the disc separator from the second pipeline under the action of the sludge backflow feed pump, and the rest overflows into a secondary A tank;
s5, centrifugal separation: the concentrated solution entering the disc separator forms clear liquid and dehydrated sludge under the action of the disc separator, the clear liquid enters a secondary A pool, and the dehydrated sludge enters a primary A pool.
Through adopting above-mentioned technical scheme, the partial concentrate in the backward flow storage tank enters into disc separating centrifuge after, forms dewatered sludge and clear liquid, and dewatered sludge compares in the sludge concentration of concentrate and improves greatly, is favorable to reducing the adverse effect of the hydraulic load and dissolved oxygen to the denitrification that get into first level A pond, and the surplus concentrate in the backward flow storage tank gets into second grade A pond, and the clear liquid after disc separating centrifuge centrifugation also gets into second grade A pond, is favorable to further improving the system denitrification volume.
Optionally, the reflux ratio of the nitrifying liquid in the S1 from the primary O pool to the primary A pool is N, and the value range of N is 2-4.
By adopting the technical scheme, the denitrification efficiency of the first-stage A pool can reach N/(N+1) by 100%, and when the value of N exceeds 4, the reflux pump can improve the denitrification efficiency less and less under the condition of increasing the same energy consumption, so that the value of N is not too high.
Optionally, if the feed flow from the secondary O-tank to the UF device is M times the system throughput, the feed flow from the reflux storage tank to the disc separator in S4 is controlled to be (M-1)/M times the system throughput.
By adopting the technical scheme, the concentration of the concentrated solution entering the reflux storage tank is M/(M-1) times of the concentration of the sludge in the secondary O pool, and after the feeding flow entering the disc separator is controlled to be (M-1)/M times of the system throughput, the concentration of the sludge in the primary A pool solution can be kept relatively stable after the dehydrated sludge centrifugally separated by the disc separator enters the primary A pool and is fully mixed with the solution.
In summary, the present application includes at least one of the following beneficial technical effects:
1. through setting up the disc separating centrifuge, carry out centrifugal separation with the partial concentrate that flows in of backward flow storage tank, form the clear solution of the dehydration mud and the liquid phase of solid phase after centrifuging, the MLSS concentration in one-level A pond has been ensured to dehydration mud discharge one-level A pond, and the clear solution flows into second grade A pond and carries out denitrification, has avoided remaining dissolved oxygen to mainly playing denitrification function pond one-level A pond's denitrification interference.
2. The reflux liquid does not enter into the first-stage A pool, the first-stage O pool, the second-stage A pool and the second-stage O pool respectively, the reflux storage tank is only communicated with the second-stage A pool and the disc separator, the number of connecting pipelines is reduced, the possibility of blocking the pipelines under the condition that the pipe diameter is large and the flow speed is too low is reduced, a reflux pump is not arranged on the pipeline communicated with the second-stage A pool any more, and the manufacturing cost of the sMBR device is reduced while the nitrogen element removal rate is further increased.
3. The concentrated solution is not returned to the first-stage 0 pool and is pumped back to the first-stage A pool, the MLSS concentration of the first-stage A pool is maintained, the nitrified solution concentration of the first-stage O pool is not diluted greatly, the nitrified solution can be pumped to the first-stage A pool at an internal reflux ratio which is 2-4 times smaller, the greater denitrification and denitrification efficiency is realized with lower energy consumption, the pool capacity requirement on the first-stage O pool is reduced while the denitrification efficiency is improved, and the manufacturing cost of the sMBR device is further reduced.
4. The electromagnetic flowmeter can measure the reflux amount of the concentrated solution entering the second pipeline, operation and maintenance personnel can calculate according to the sludge concentration and the inflow amount to obtain the appropriate reflux amount of the concentrated solution, and the stop valve is regulated according to the reflux amount shown by the electromagnetic flowmeter to control the reflux amount of the concentrated solution entering the second pipeline and finally reach the calculated value range, so that the accurate regulation and control are facilitated.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present application.
In the figure, 1, AO unit; 11. a first-level pool A; 111. a first mixer; 12. a primary O pool; 13. a secondary A pool; 14. a secondary O pool; 2. a disc separator; 3. a UF device; 31. a UF inlet end; 32. a UF outlet end; 4. a reflux storage tank; 41. a second stirrer; 5. a first pipe; 51. a feed pump; 52. a circulation pump; 6. a second pipe; 61. a sludge reflux feed pump; 62. a stop valve; 63. an electromagnetic flowmeter; 7. a third conduit; 71. and a reflux pump.
Detailed Description
The present application will be described in further detail with reference to fig. 1.
A sMBR garbage leachate treatment system, referring to FIG. 1, comprises an AO unit 1, a disc separator 2, a UF device 3 and a reflux storage tank 4, wherein the disc separator 2 is communicated with the AO unit 1 and the reflux storage tank 4, the reflux storage tank 4 is respectively communicated with the AO unit 1, the disc separator 2 and the UF device 3, and the AO unit 1 is communicated with the UF device 3.
Referring to fig. 1, the ao unit 1 includes a first-stage a tank 11, a first-stage O tank 12, a second-stage a tank 13, and a second-stage O tank 14, where the second-stage O tank 14 is respectively connected to the second-stage a tank 13 and the UF device 3, one end of the second-stage O tank 14 is connected to the second-stage a tank 13, the other end of the second-stage O tank 14 is connected to the UF device 3, a third pipeline 7 is additionally provided between the first-stage a tank 11 and the first-stage O tank 12, one end of the third pipeline 7 is connected to the first-stage a tank 11, the other end is connected to the first-stage O tank 12, a reflux pump 71 is provided on the third pipeline 7, and the reflux pump 71 lifts the nitrified liquid after being processed by the first-stage O tank 12 to the first-stage a tank 11.
Referring to fig. 1, the UF device 3 includes a UF inlet port 31 and a UF outlet port 32, the UF outlet port 32 is communicated with the reflux storage tank 4, a first pipeline 5 is arranged between the UF inlet port 31 and the secondary O tank 14, two ends of the first pipeline 5 are respectively communicated with the UF inlet port 31 and the secondary O tank 14, a feed pump 51 and a circulating pump 52 are arranged on the first pipeline 5, the feed pump 51 is arranged at one end of the first pipeline 5 close to the secondary O tank 14, the circulating pump 52 is arranged at one end of the first pipeline 5 far away from the secondary O tank 14, the reflux storage tank 4 is communicated with the first pipeline 5 and is positioned between the feed pump 51 and the circulating pump 52, the nitrified liquid treated by the AO unit 1 is powered by the feed pump 51 to enable the nitrified liquid to enter the UF device 3 from the first pipeline 5, the circulating pump 52 is powered to meet the requirement of the cross flow rate of the nitrified liquid in the UF device 3, the concentrated liquid and water are formed after ultrafiltration by the UF device 3, the water enters the next unit for treatment, a part of the concentrated liquid flows from the UF outlet port 32 into the reflux storage tank 4, and the remaining part of the nitrified liquid returns to the UF device 3 under the effect of the circulating pump 52 from the first pipeline 5.
Referring to fig. 1, a second stirrer 41 is arranged on a reflux storage tank 4, when concentrated solution enters the reflux storage tank 4, the second stirrer 41 rotates to stir the concentrated solution, so that concentrated solution deposition is prevented, the reflux storage tank 4 is communicated with a secondary A tank 13, one end of a disc separator 2 is communicated with the secondary A tank 13, the bottom end of the disc separator 2 is communicated with a primary A tank 11, a second pipeline 6 is arranged between the top end of the disc separator 2 and the reflux storage tank 4, two ends of the second pipeline 6 are respectively communicated with the top end of the disc separator 2 and the reflux storage tank 4, an electromagnetic flowmeter 63, a stop valve 62 and a sludge reflux feed pump 61 are arranged on the second pipeline 6, the sludge reflux feed pump 61 is arranged at one end of the second pipeline 6 far away from the disc separator 2, the stop valve 62 is arranged behind the sludge reflux feed pump 61, and the electromagnetic flowmeter 63 is arranged behind the stop valve 62.
Referring to fig. 1, a part of the concentrated solution in the reflux storage tank 4 is refluxed to the secondary a tank 13, the rest enters the disc separator 2 through the sludge reflux feed pump 61, a liquid phase clear solution and a solid phase dehydrated sludge are formed through the centrifugal action of the disc separator 2, the clear solution flows into the secondary a tank 13, the removal amount of nitrogen element is improved, the dehydrated sludge is discharged into the primary a tank 11, a first stirrer 111 is arranged in the primary a tank 11 and is arranged at one side of the primary a tank 11 close to the disc separator 2, and after the dehydrated sludge enters the primary a tank 11, the first stirrer 111 rotates, so that the dehydrated sludge and the mixed solution in the primary a tank 11 are fully mixed.
The implementation principle of the embodiment of the application is as follows: the garbage leachate enters a first-stage tank A11 and then enters a first-stage tank O12, a nitrified liquid part nitrified by the first-stage tank O12 flows back to the first-stage tank A11 from a third pipeline 7 through a reflux pump 71, the reflux ratio is controlled between 2 and 4, nitrified liquid of the first-stage tank O12 flows into a UF device 3 through a first pipeline 5 after the subsequent reaction of the second-stage tank A13 and the second-stage tank O14, a circulating pump 52 supplies power for the garbage leachate to meet the cross flow speed requirement of mixed liquid in the UF device 3, the nitrified liquid is ultrafiltered by the UF device 3 to form clear liquid and concentrated liquid, the clear liquid enters a next-stage treatment process unit, part of concentrated liquid flows out from a UF outlet end 32 to enter a reflux storage tank 4, the residual concentrated liquid enters the UF device 3 from a UF inlet end 31 to continue to be ultrafiltered, the concentrated liquid reflux quantity of the reflux storage tank 4 entering the disc separator 2 is accurately determined through an electromagnetic flowmeter 63 and a stop valve 62, the residual concentrated liquid overflows into the second-stage tank A13 to be nitrified and denitrified, the concentrated liquid entering the disc 2 is centrifugally separated to form clear liquid and dehydrated sludge, and the clear liquid enters the second-stage tank A13 to be denitrified to enter the MLA 11 to keep the concentration stable relatively, and the concentration of the SS 11 is stable.
The embodiment also discloses an sMBR process reflux method adopting the sMBR landfill leachate treatment system, which comprises the following steps:
s1, primary denitrification: the garbage leachate enters a first-stage A pool 11 and then flows into a first-stage O pool 12, nitrifying liquid is formed after the garbage leachate acts on the first-stage O pool 12, and part of the first-stage nitrifying liquid flows back to the first-stage A pool 11 through a nitrifying liquid reflux pump 71;
s11, setting a reflux ratio: the reflux ratio of the nitrifying liquid from the primary O pool 12 to the primary A pool 11 is N, and the value of N is 2-4;
s2, secondary denitrification: the nitrified liquid in the primary O pool 12 enters the secondary A pool 13 for denitrification and then enters the secondary O pool 14;
s3, ultrafiltration: the nitrifying liquid in the secondary O pool 14 enters the UF device 3 through the first pipeline 5 under the action of the feed pump 51, the circulating pump 52 provides power to meet the cross flow speed requirement of the nitrifying liquid in the membrane pipe, the nitrifying liquid forms clear liquid and concentrated liquid after ultrafiltration, and the clear liquid enters the next treatment unit;
s4, splitting concentrated solution: part of the concentrated solution flows back to the UF device 3 from the first pipeline 5 under the action of the circulating pump 52, the rest enters the reflux storage tank 4, part of the concentrated solution in the reflux storage tank 4 enters the disc separator 2 from the second pipeline 6 under the action of the sludge reflux feed pump 61, and the rest enters the secondary A tank 13;
s41, controlling the feeding flow: if the feeding flow from the secondary O pool 14 to the UF device 3 is M times of the system throughput, controlling the feeding flow of the reflux storage tank 4 entering the disc separator 2 in the S4 to be (M-1)/M times of the system throughput;
s5, centrifugal separation: the concentrated solution entering the disc separator 2 forms clear liquid and dehydrated sludge under the action of the disc separator 2, the clear liquid enters the secondary A tank 13, and the dehydrated sludge enters the primary A tank 11.
The reflux ratio of the nitrified liquid from the first-stage O pool 12 to the first-stage A pool 11 is N, so that the denitrification efficiency can reach N/(n+1) 100%, and the value of N is between 2 and 4.
If the feeding flow from the secondary O pool to the UF device 3 is M times of the system throughput, the concentration of the concentrated solution entering the reflux storage tank 4 is M/(M-1) times of the concentration of the secondary O pool, and the feeding flow entering the disc separator 2 is controlled to be (M-1)/M times of the system throughput through the electromagnetic flowmeter 63 and the stop valve 62, so that the dewatered sludge formed by centrifugal separation of the disc separator 2 enters the primary A pool 11 and is fully mixed with the solution, and the concentration of the sludge in the solution of the primary A pool 11 can be kept relatively stable.
The embodiments of the present application are all preferred embodiments of the present application, and are not intended to limit the scope of the present application, wherein like reference numerals are used to refer to like elements throughout. Therefore: all equivalent changes in structure, shape and principle of the application should be covered in the scope of protection of the application.
Claims (7)
1. The sMBR garbage leachate treatment system comprises an AO unit (1) and an UF device (3), wherein the UF device (3) is provided with an UF inlet end (31) and an UF outlet end (32), the AO unit (1) comprises a primary A tank (11), a primary O tank (12), a secondary A tank (13) and a secondary O tank (14) which are sequentially communicated, and the sMBR garbage leachate treatment system is characterized by further comprising a disc separator (2) and a reflux storage tank (4), a first pipeline (5) is arranged between the secondary O tank (14) and the UF inlet end (31), two ends of the first pipeline (5) are respectively communicated with the secondary O tank (14) and the UF inlet end (31), a feed pump (51) and a circulating pump (52) are arranged on the first pipeline (5), one end, close to the secondary O tank (14), of the first pipeline (5) is arranged at one end, far away from the disc separator (14), of the second pipeline (5) is respectively communicated with the reflux storage tank (14), and one end, far from the second pipeline (14), and the reflux storage tank (4) are respectively communicated with the UF inlet end (31);
the utility model discloses a disc separator, including disc separator (2), disc separator, back flow storage tank (4), second pipeline (6) are provided with between back flow storage tank (4) with second level A pond (13) intercommunication, back flow storage tank (4) with be provided with stop valve (62), mud backward flow feed pump (61) and electric-magnetic flow meter (63) on second pipeline (6) respectively between back flow storage tank (4) with disc separator (2), mud backward flow feed pump (61) set up second pipeline (6) keep away from the one end of disc separator (2), stop valve (62) set up behind mud backward flow feed pump (61), electric-magnetic flow meter (63) set up behind stop valve (62), electric-magnetic flow meter (63) front tube section length is more than 5 times pipeline diameter at least.
2. A sMBR landfill leachate treatment system according to claim 1, wherein a first stirrer (111) is arranged in the primary a-tank (11).
3. The sMBR garbage leachate treatment system according to claim 1, wherein a third pipeline (7) is arranged between the primary O tank (12) and the primary A tank (11), two ends of the third pipeline (7) are respectively communicated with the primary O tank (12) and the primary A tank (11), and a reflux pump (71) for pumping the primary O tank (12) solution back to the primary A tank (11) is arranged on the third pipeline (7).
4. A sMBR landfill leachate treatment system according to claim 1, wherein a second stirrer (41) is arranged in the reflux storage tank (4).
5. A method of srbr process reflux for a landfill leachate treatment system according to any of claims 1 to 4, comprising the steps of:
s1, primary denitrification: the garbage leachate enters a primary A pool (11) and then flows into a primary O pool (12), nitrifying liquid is formed after the garbage leachate acts on the primary A pool (11) and the primary O pool (12), and part of the primary nitrifying liquid flows back to the primary A pool (11) through a nitrifying liquid reflux pump (71);
s2, secondary denitrification: the nitrifying liquid in the first-stage O pool (12) enters the second-stage A pool (13) for denitrification and then enters the second-stage O pool (14);
s3, ultrafiltration: nitrifying liquid in the secondary O pool (14) enters the UF device (3) through the first pipeline (5) under the action of the feed pump (51), the circulating pump (52) provides power to meet the cross flow speed requirement of the nitrifying liquid in the membrane tube, the nitrifying liquid forms clear liquid and concentrated liquid after ultrafiltration, and the clear liquid enters the next treatment unit;
s4, splitting concentrated solution: part of concentrated solution flows back to the UF device (3) from the first pipeline (5) under the action of the circulating pump (52), the rest part of concentrated solution enters the reflux storage tank (4), part of concentrated solution in the reflux storage tank (4) enters the disc separator (2) from the second pipeline (6) under the action of the sludge reflux feed pump (61), and the rest part of concentrated solution enters the secondary A tank (13);
s5, centrifugal separation: the concentrated solution entering the disc separator (2) forms clear liquid and dehydrated sludge under the action of the disc separator (2), the clear liquid enters the secondary A tank (13), and the dehydrated sludge enters the primary A tank (11).
6. The sMBR process reflux method according to claim 5, wherein the reflux ratio of the nitrified liquid in S1 from the primary O pool (12) to the primary A pool (11) is N, and the value of N is in the range of 2-4.
7. The sMBR process reflux method according to claim 5, wherein the feed flow from the secondary O tank (14) to the UF device (3) is M times the system throughput, and the feed flow from the reflux storage tank (4) to the disc separator (2) in S4 is controlled to be (M-1)/M times the system throughput.
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