CN102674622A - Integral processing device for garbage leachate - Google Patents
Integral processing device for garbage leachate Download PDFInfo
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- CN102674622A CN102674622A CN2011100667774A CN201110066777A CN102674622A CN 102674622 A CN102674622 A CN 102674622A CN 2011100667774 A CN2011100667774 A CN 2011100667774A CN 201110066777 A CN201110066777 A CN 201110066777A CN 102674622 A CN102674622 A CN 102674622A
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Abstract
The invention discloses an integral processing device for garbage leachate, and the integral processing device mainly consists of a contact oxidation pond (1), a low-oxygen aeration pond (2), a nitrosation reaction pond (3), an anaerobic ammonia oxidation reaction pond (4), a microwave processor (5), a separator (6) and an automatic feeding device (16) for activated carbon which are integral. The integral processing device for garbage leachate is an energy-saving, efficient and low-consumption garbage leachate processing device; pollutants, such as organic pollutants (COD (chemical oxygen demand)), nitrogen (N), nitrogen (P) and the like in the garbage leachate can be simultaneously removed to realize the standard processing and discharging of the garbage leachate; mobility and flexibility on processing the leachate can be realized; the processing cost is greatly saved; the integration degree and reusable property of the garbage leachate processing device are improved; and the processing operation cost of the garbage leachate is lowered.
Description
Technical field
The present invention relates to a kind of wastewater treatment equipment, particularly a kind of percolate integrated treatment unit.
Background technology
The processing of percolated liquid in city refuse landfill is a unusual stubborn problem in landfill yard design, operation and the management always.The high concentrated organic wastewater of this complicated component of percolate is handled and is not directly entered environment if do not add, and can cause serious water pollution accident and endangers ecotope.
Rubbish leachate treatment method comprises physico-chemical processes and biological process.Physico-chemical processes mainly contains charcoal absorption, chemical precipitation, density separation, chemical oxidation, chemical reduction, IX, film dialysis, gas and mentions several different methods such as wet oxidation process.The physical chemistry method processing cost is higher, pollutes to be difficult to thorough removal.Though the ammonia blow-off method like domestic frequent employing at present has higher ammonia nitrogen removal efficient, there is the shortcoming that investment running cost is high, deamination tail gas is difficult to administer.Shenzhen Xia Ping refuse landfill to adopt stripping tower is an example, and the construction investment of ammonia stripping part accounts for about 30% of gross investment, and running cost accounts for more than 70% of total processing cost.In addition, blow-off method receives the weather restriction very big.Therefore percolate processing at present mainly is to adopt biological process.Biological process is divided into aerobe processing, anaerobic biological treatment and the combination of the two.Aerobic treatment comprises activated sludge process, biomembrance process, oxidation ditch, aerobic stabilization pond, blodisc and trickling filter etc.Anaerobic treatment comprises up-flow anaerobic sludge blanket, anaerobic immobilized bio-reactor, mixing reactor, anaerobism stabilization pond and air supporting method, soil facture, reverse osmosis system or the like.Existing these treatment scheme complex process, treatment step is many, and equipment is various, complicated, and facility, investment of devices are bigger, cause depreciation, upkeep cost higher, and investment, the running cost of processing are higher, and the mobility and flexibility of treatment facility is relatively poor.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of percolate integrated treatment unit, realizes efficient, energy-conservation, the low consumption of percolate are handled, and had mobility and flexibility preferably.
For solving the problems of the technologies described above technical scheme of the present invention: a kind of percolate integrated treatment unit.This device mainly is made up of the contact-oxidation pool that connects as one, low-oxygen aeration pond, nitrosation reaction pond, Anammox reaction tank, microwave treater, separator and the automatic throwing device of gac; The water outlet of contact-oxidation pool directly is communicated with the low-oxygen aeration pond, and the water outlet in low-oxygen aeration pond directly is communicated with the nitrosation reaction pond, and the water outlet in nitrosation reaction pond directly is communicated with the Anammox reaction tank; To microwave treater, the automatic throwing device of gac is contained on the pipeline section between Anammox reaction tank and the microwave treater water outlet of Anammox reaction tank through pipe connection; The water outlet of microwave treater passes through pipe connection to separator.
In the above-mentioned percolate integrated treatment unit, on the pipeline of the water outlet of described connection Anammox reaction tank and microwave treater, and connect on the pipeline of water outlet and separator of microwave treater valve all is housed.
In the aforesaid percolate integrated treatment unit, the stirring pump all is housed in the bottom of described low-oxygen aeration pond, nitrosation reaction pond and Anammox reaction tank.
In the aforesaid percolate integrated treatment unit, in described nitrosation reaction pond and Anammox reaction tank, the thermostatically heating rod is housed, to keep nitrosation reaction pond and Anammox reaction tank homo(io)thermism.
In the aforesaid percolate integrated treatment unit, at described contact-oxidation pool and bottom, nitrosation reaction pond aeration head is housed, aeration head connects aerator.
Beneficial effect of the present invention: compared with prior art, this device utilizes the microbial film of contact-oxidation pool domestication that the biodegradable COD in the percolate is removed, and removes a certain amount of NH3-N, P and BOD simultaneously; Utilize in the low-oxygen aeration pond and tamed active sludge (containing aerobic bacteria and aerobic-anaerobic microbe) difficult degradation COD is degraded, transforms, improve the biodegradable of percolate; Utilize the nitrosation reaction pond, realize stable nitrosification through control reaction tank envrionment conditions, the accumulation nitrite, and guarantee that water outlet NH3-H/NO2-N maintains 1.1～1.3, for the Anammox reaction tank provides suitable water inlet condition; The Anammox reaction tank utilizes the water outlet of nitrosation reaction pond as water inlet, under the Degradation of anaerobic ammonia oxidizing bacteria, removes most NH3-H; Microwave treater utilizes residual COD, NH3-N in the water outlet of microwave catalysis oxidation removal anaerobic ammonia oxidation reactor, guarantees that system's effluent quality is up to standard; The main effect of separator is the gac that contains through precipitating and isolating in the water outlet, makes effluent quality satisfy " consumer waste filling and embedding pollution control criterion " (GB16889-1997) primary standard.
The present invention is a kind of garbage filter liquid processing device of energy-conservation, efficient, low consumption; Can remove organic pollutant (COD), nitrogen (N), phosphorus pollutents such as (P) in the percolate simultaneously; Realize the processing discharging up to standard of percolate; And this device is the integrated percolate treatment facility that can drag, and can realize mobility and flexibility that percolate is handled, and realize that large-scale production, the batch production of percolate treatment facility are prefabricated; Can after landfill yard closes, this percolate treatment facility be dragged new processing place and handle operation once more; Can greatly practice thrift processing cost, but improve the integrated degree and reuse of garbage filter liquid processing device, reduce the treatment operating costs of percolate.
For verifying effect of the present invention, the applicant has carried out lot of test and research, below is the pollutant removal changing conditions that adopts the present invention's (hereinafter to be referred as this device) treating refuse percolate:
One, COD removes situation
Water inlet, effluent COD concentration changing conditions are seen Fig. 2 during the steady running of this device, and COD clearance changing conditions is seen Fig. 3.
Can know by Fig. 2: when this device water inlet COD concentration is between 978.6mg/L～1054.1mg/L; Effluent COD concentration reduces along with the increase of working time gradually; Show that this device constantly strengthens the flexibility of percolate; When steady running in the time of 2 months, COD water outlet mean concns has only 43.5mg/L, explains that this device stability is better.In the preceding 20d of this device steady running, effluent COD concentration changes greatly, explains that the biological activity in the device is improving constantly, and the device water outlet is reduced to the 51.6mg/L of 19d from initial 179.8mg/L.Since 21d, device water outlet COD mean concns is 45.3mg/L, and fluctuation range is less.
Can know by Fig. 3; This device improves along with the prolongation of working time the removal efficient of COD; At initial 20d, the clearance rangeability is bigger, explains that this stage this device biological community structure renewal rate is very fast; Dominant bacteria status in each reactor drum is tending towards consolidating, and reactor drum has also adapted to the variation of influent quality gradually.It is that the load impact that causes more greatly of change of water quality is to bioactive influence that this device initial operating stage COD removes the efficient reason of lower.Through operation after a while, the dominant bacteria in each reactor drum has adapted to new hydraulic load and organic loading gradually, shows improving constantly of clearance.From 21d, this device changes comparatively the clearance of COD and relaxes, and the removal effect of COD is reached best effect, and this moment, average removal rate was 95.3%.
Two, NH3-N removes situation
Water inlet, water outlet NH3-N concentration change situation are seen Fig. 4 during the steady running of this device, and NH3-N clearance changing conditions is seen Fig. 5.
Can know that by Fig. 4 this device water inlet NH3-N concentration change is less, between 995～1017mg/L; Water outlet NH3-N concentration reduces along with the prolongation of working time gradually; This device water outlet NH3-N concentration reduction amplitude is bigger in preceding 20d, but water outlet NH3-N is higher, and treatment effect is not satisfactory.Its reason is that influent quality changes to the shock action of Anammox reaction greatly, causes denitrification effect bad.Prolongation along with working time; Water outlet NH3-N concentration still presents reduction trend; But rangeability is less, and on average going out water concentration is 11.5mg/L, and this moment, this device was better to the NH3-N removal effect; Explain that nitrosation reaction pond and Anammox reaction tank recover normal, bringing into play important effect aspect the removal ammonia nitrogen.
Can be known that by Fig. 5 this device is bigger to removal efficient rangeability in preceding 20d of NH3-N, mainly be that the mikrobe volume of holding is higher because each reactor drum has adapted to the water inlet condition that changes gradually, and the quantity of the dominant bacteria that this device is held is in continuous increase.The rising of NH3-N clearance reflects that the biological activity in nitrosation reaction pond and the Anammox reaction tank is higher, and the usefulness of performance is increasing aspect removal NH3-N.The later NH3-N clearance of 20d tends to be steady basically, and the highest clearance of NH3-N is 99%, and this device is good to the removal effect of NH3-N.
Three, TN removes situation
Water inlet, water outlet TN concentration change situation are seen Fig. 6 during the steady running of this device, and TN clearance changing conditions is seen Fig. 7.
Can be known that by Fig. 6 water inlet TN variation range is 1287～1318mg/L during the operation of this device, initial operating stage water outlet TN concentration is higher, but presents downward trend gradually.The water outlet TN concentration MV at initial stage is about 180mg/L.Behind this device operation 30d, water outlet TN obviously reduces, and the water outlet TN concentration of this moment has been reduced to below the 50mg/L, and effluent quality is better.The later water outlet TN concentration MV of this device operation 40d is 15mg/L.
Can be known that by Fig. 7 the TN clearance of this device initial operating stage is below 80%, along with the prolongation of working time, the TN clearance increases very fast, fluctuates to some extent at the initial operating stage clearance, but totally presents increase.Behind this device operation 30d, the TN clearance has reached 97%, and TN clearance rangeability is less in the time subsequently, and the TN clearance increases to about 99% from 97%, and overall removal effect is good.
Four, other pollutant removal situation
In this device operational process, water inlet, water outlet BOD5 (five-day BOD) and SS (suspended substance) are measured in not timing.Test result shows, during the steady running of this device, water outlet BOD5, SS can stablize and reach " consumer waste filling and embedding pollution control criterion " (GB16889-1997) primary standard limit value.
To sum up analyze; Water outlet COD, NH3-N, SS, BOD5 concentration can satisfy " consumer waste filling and embedding pollution control criterion " (GB16889-1997) primary standard limit value during the steady running of this device, and percolate is through can directly entering near the surface water body landfill yard after this apparatus processes.
Brief summary: (1) is because the active sludge in the Anammox reaction tank is the key that influences the denitrogenation of this device; For making this device obtain good removal effect; Through the adjustment of water inlet, water-out manners being satisfied its operation control condition; Through the 30d debugging, this device makes moderate progress to the removal effect of pollutent.
(2) during the steady running of this device, water outlet average COD concentration is 45.3mg/L, is 95.3% to the average removal rate of COD; The equal NH3-N concentration of level is 11.5mg/L, is 99% to the highest clearance of NH3-N; The equal TN concentration of level is 15mg/L, is 99% to the clearance of TN.
(3) during the steady running of this device, water outlet COD, NH3-N, SS, BOD5 concentration can satisfy " consumer waste filling and embedding pollution control criterion " (GB16889-1997) primary standard limit value.
" water and the effluent monitoring analytical procedure " that water monitoring method of the present invention is all worked out according to NEPA.COD adopts potassium dichromate process; BOD5 adopts the dilution inoculation method; NH3-N adopts Na Shi reagent spectrophotometer method; NO2--N adopts N-1 naphthodiamide spectrophotometry; NO3--N adopts the Pbenoldisulfonic Acid spectrophotometry, and TN adopts alkaline alkaline potassium per-sulfate digestion ultraviolet spectrophotometer method, and SS adopts weighting method.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Water inlet, effluent COD concentration changing conditions graphic representation when Fig. 2 is the steady running of this device, curve A is water inlet COD concentration among the figure, curve B is an effluent COD concentration;
COD clearance changing conditions graphic representation when Fig. 3 is the steady running of this device;
Water inlet, water outlet NH3-N concentration change situation graphic representation when Fig. 4 is the steady running of this device, curve C is water inlet NH3-N concentration among the figure, curve D is a water outlet NH3-N concentration;
NH3-N clearance changing conditions graphic representation when Fig. 5 is the steady running of this device;
Water inlet, water outlet TN concentration change situation graphic representation when Fig. 6 is the steady running of this device, curve E is water inlet TN concentration among the figure, curve F is a water outlet TN concentration;
TN clearance changing conditions graphic representation when Fig. 7 is the steady running of this device.
Below in conjunction with accompanying drawing and embodiment the present invention is further described.
Embodiment
Embodiment 1.As shown in Figure 1; This device mainly is made up of the automatic throwing device 16 of the contact-oxidation pool that is assembled into one 1, low-oxygen aeration pond 2, nitrosation reaction pond 3, Anammox reaction tank 4, microwave treater 5, separator 6 and gac; In low-oxygen aeration pond 2, the bottom of nitrosation reaction pond 3 and Anammox reaction tank 4 all is equipped with and stirs pump 8; Thermostatically heating rod 9 is housed in nitrosation reaction pond 3 and Anammox reaction tank 4; In contact- oxidation pool 1 and 3 bottoms, nitrosation reaction pond aeration head 17 is housed, aeration head 17 is connected to aerator 7.The water outlet 10 of contact-oxidation pool 1 directly is communicated with low-oxygen aeration pond 2, and the water outlet 11 in low-oxygen aeration pond 2 directly is communicated with nitrosation reaction pond 3, and the water outlet 12 in nitrosation reaction pond 3 directly is communicated with Anammox reaction tank 4; The water outlet 13 of Anammox reaction tank 4 is through pipe connection to microwave treater 5; Pipeline section between Anammox reaction tank 4 and microwave treater 5 is provided with the automatic throwing device 16 of gac; The water outlet 14 of microwave treater 5 is through pipe connection to separator 6; On the pipeline of water outlet that connects Anammox reaction tank 4 13 and microwave treater 5, valve 15 is housed; On the pipeline of water outlet that connects microwave treater 5 14 and separator 6, valve 15 is housed also, valve 15 is used to control draining, realizes intermittent drainage.
In the present embodiment: the pond type of contact-oxidation pool 1 is a rectangular parallelepiped, L * B * H=350 * 350 * 600mm, and useful volume is 50L, superelevation is 192mm.Pond body material is an ABS sheet material.Contact-oxidation pool 1 is a single flow; Fill medium-soft property suspension type Vilaterm filler in the pond; The filler filling ratio is 30%; Aeration head 17 is evenly arranged in the bottom, and the dissolved oxygen concentration of contact-oxidation pool 1 is regulated through the control aeration rate, and the HRT (hydraulic detention time) of percolate in contact-oxidation pool 1 is 1d.Hang during the film, contact-oxidation pool 1 operation scheme adopts intermittent water inflow, intermittent drainage, and the cycle of operation is 12h, and wherein flooding time is 0.5h, and the aeration phase time length is 10h, and the time of staticly settling is 1h, and water discharge time is 0.5h.Each, flooding quantity was 1/2 of a reactor drum useful volume reaction time.The pond type in low-oxygen aeration pond 2 is a rectangular parallelepiped, and material is an ABS sheet material, is of a size of L * B * H=500 * 350 * 750mm, and superelevation is 179mm, and useful volume is 100L.The bottom central position in low-oxygen aeration pond 2 is provided with one and stirs pump 8, utilizes the DO and the pH value of portable dissolved oxygen meter and pH meter continuous monitoring reactor drum.The seed sludge in low-oxygen aeration pond 2 is an aerobic activated sludge, and the seed sludge amount accounts for 20% of low-oxygen aeration pond useful volume, and percolate is 2d in the optimal HRT (hydraulic detention time) in low-oxygen aeration pond 2.The operation scheme in low-oxygen aeration pond 2 adopts intermittent water inflow, intermittent drainage between the active sludge during cultivation, and the cycle of operation is 12h, and wherein flooding time is 0.5h, and the aeration phase time length is 10h, and the time of staticly settling is 1h, and water discharge time is 0.5h.Each, flooding quantity was 1/2 of a reactor drum useful volume reaction time.The material in nitrosation reaction pond 3 is an ABS sheet material, is of a size of L * B * H=500 * 350 * 750mm, and useful volume is 100L.Thermostatically heating rod 9 is housed in nitrosation reaction pond 3, is used for keeping the homo(io)thermism in the pond, dissolved oxygen concentration is regulated through the control aeration rate.Nitrosation reaction pond 3 with 80% aerobic nitrification mud, 20% garden soil extract as seed sludge; The sludge seeding amount accounts for 20% of reactor drum useful volume; The optimal HRT (hydraulic detention time) of percolate in nitrosation reaction pond 3 is 2d, and SRT (mud mud age) is 3d.Intermittent water inflow, intermittent drainage are adopted in nitrosation reaction pond 3.Be 12h each reaction time, and wherein flooding time is 11.5h, and aeration time is 11.5h, leaves standstill 25min, and water discharge time is 5min; Be one-period (12h) idle mixing time.Each cycle water inlet in nitrosation reaction pond 3, water displacement are 1/4 of nitrosation reaction pond useful volume.Anammox reaction tank 4 be shaped as rectangular parallelepiped, L * B * H=350 * 350 * 600mm, useful volume is 50L, superelevation is 192mm, material is an ABS sheet material.ABS has opacifying property, can avoid the restraining effect of light to anaerobic ammonia oxidizing bacteria.One cover thermostatically heating rod 9 is housed in Anammox reaction tank 4, and temperature is controlled by thermostatically heating rod 9, and 8 one of stirring pumps are housed in Anammox reaction tank 4.The water-in in oxygen oxidative ammonolysis pond 4 is positioned at Anammox reaction tank 4 middle and upper parts, and water port is positioned at the mid-way of Anammox reaction tank useful volume, at the top of Anammox reaction tank 4 venting port is set, and protects with water seal.Anammox reaction tank 4 is a seed sludge with 50% aerobic nitrification mud, 25% anaerobic sludge, 25% garden soil transudate.The optimal water power standing time of percolate in Anammox reaction tank 4 is 1d, and this moment, denitrification effect was better.The operation scheme of Anammox reaction tank 4 adopts intermittent water inflow, intermittent drainage, and be 12h each reaction time, and wherein flooding time is 0.5h, and be 10h working time, leaves standstill 1h, and water discharge time is 0.5h; Be one-period (12h) idle mixing time.Microwave treater 5 frequencies are 2450MHz, and power is 1200W, and model is EM-202MS1.Select for use gac as sensitizing agent, the best dosage of sensitizing agent is 20g/L, and the microwave treatment Best Times of percolate in microwave treater 5 is 30min.Separator 6 is used for the sensitizing agent that microwave processing process is used and from the percolate water outlet, separates.
During the operation of this device; The water outlet of contact-oxidation pool 1 is just as the water inlet in low-oxygen aeration pond 2; The water outlet in low-oxygen aeration pond 2 is as the water inlet in nitrosation reaction pond 3; The water outlet in nitrosation reaction pond 3 is that Anammox reaction tank 4 provides nutritive substance, and 5 pairs of anaerobic ammonia oxidation reactor 4 water outlets of microwave treater are carried out further mineralising and decomposed, and passes through separator 6 at last and sensitizing agent (gac) is separated from water outlet gets final product qualified discharge.The water inlet of this integrated apparatus is percolate, and operation scheme adopts intermittent water inflow, intermittent drainage.In this device, contact-oxidation pool 1, low-oxygen aeration pond 2, nitrosation reaction pond 3, anaerobic ammonia oxidation reactor 4 all are provided with two covers, and another group then is in idle state during one group of operation.
Embodiment of the present invention is not limited to the foregoing description, and the various variations of under the prerequisite that does not break away from aim of the present invention, making all belong within protection scope of the present invention.
Claims (5)
1. a percolate integrated treatment unit is characterized in that: mainly be made up of the contact-oxidation pool that is assembled into one (1), low-oxygen aeration pond (2), nitrosation reaction pond (3), Anammox reaction tank (4), microwave treater (5), separator (6) and the automatic throwing device of gac (16); The water outlet (10) of contact-oxidation pool (1) directly is communicated with low-oxygen aeration pond (2), and the water outlet (11) of low-oxygen aeration pond (2) directly is communicated with nitrosation reaction pond (3), and the water outlet (12) of nitrosation reaction pond (3) directly is communicated with Anammox reaction tank (4); The water outlet (13) of Anammox reaction tank (4) is through pipe connection to microwave treater (5), and the automatic throwing device of gac (16) is contained on this pipeline section; The water outlet (14) of microwave treater (5) is through pipe connection to separator (6).
2. percolate integrated treatment unit according to claim 1; It is characterized in that: on the pipeline of the water outlet (13) of described connection Anammox reaction tank (4) and microwave treater (5), and on the pipeline of the water outlet (14) that connects microwave treater (5) and separator (6) valve (15) is housed all.
3. percolate integrated treatment unit according to claim 1 is characterized in that: in described low-oxygen aeration pond (2), the bottom of nitrosation reaction pond (3) and Anammox reaction tank (4) is equipped with and stirs pump (8).
4. percolate integrated treatment unit according to claim 1 is characterized in that: in described nitrosation reaction pond (3) and Anammox reaction tank (4), thermostatically heating rod (9) is housed.
5. percolate integrated treatment unit according to claim 1 is characterized in that: at described contact-oxidation pool (1) and nitrosation reaction pond (3) bottom aeration head (17) is housed, aeration head (17) connects aerator (7).
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| CN2011100667774A CN102674622A (en) | 2011-03-18 | 2011-03-18 | Integral processing device for garbage leachate |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103539319A (en) * | 2013-10-31 | 2014-01-29 | 华北电力大学 | Garbage leachate treating device |
| CN109354169A (en) * | 2018-12-05 | 2019-02-19 | 青岛思普润水处理股份有限公司 | A kind of efficient autotrophic denitrification system and quick start method based on MBBR |
| CN110127955A (en) * | 2019-06-12 | 2019-08-16 | 成都工业学院 | A kind of double pond manual controlled infusions and method for low C/N than wastewater efficient denitrogenation |
| CN110655289A (en) * | 2019-11-20 | 2020-01-07 | 上海贤晋质安环保科技有限公司 | Purification device is handled in landfill leachate integration |
| CN112390364A (en) * | 2020-11-06 | 2021-02-23 | 陕西麦可罗生物科技有限公司 | Environment-friendly process for improving treatment capacity of EMBR (enhanced fluidized bed reactor) system by utilizing homogenization tank volume synergism and inflow and return water diversion design |
| CN112479491A (en) * | 2020-11-18 | 2021-03-12 | 三桶油环保科技(宜兴)有限公司 | Advanced treatment and discharge method for fracturing flow-back fluid |
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2011
- 2011-03-18 CN CN2011100667774A patent/CN102674622A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103539319A (en) * | 2013-10-31 | 2014-01-29 | 华北电力大学 | Garbage leachate treating device |
| CN109354169A (en) * | 2018-12-05 | 2019-02-19 | 青岛思普润水处理股份有限公司 | A kind of efficient autotrophic denitrification system and quick start method based on MBBR |
| CN109354169B (en) * | 2018-12-05 | 2021-08-17 | 青岛思普润水处理股份有限公司 | MBBR-based efficient autotrophic nitrogen removal system and rapid starting method |
| CN110127955A (en) * | 2019-06-12 | 2019-08-16 | 成都工业学院 | A kind of double pond manual controlled infusions and method for low C/N than wastewater efficient denitrogenation |
| CN110127955B (en) * | 2019-06-12 | 2024-04-30 | 成都工业学院 | Double-pond artificial rapid infiltration system and method for high-efficiency denitrification of low-C/N ratio sewage |
| CN110655289A (en) * | 2019-11-20 | 2020-01-07 | 上海贤晋质安环保科技有限公司 | Purification device is handled in landfill leachate integration |
| CN112390364A (en) * | 2020-11-06 | 2021-02-23 | 陕西麦可罗生物科技有限公司 | Environment-friendly process for improving treatment capacity of EMBR (enhanced fluidized bed reactor) system by utilizing homogenization tank volume synergism and inflow and return water diversion design |
| CN112390364B (en) * | 2020-11-06 | 2023-03-24 | 陕西麦可罗生物科技有限公司 | Environment-friendly process for improving treatment capacity of EMBR (enhanced fluidized bed reactor) system by utilizing homogenization tank volume synergism and inflow and return water diversion design |
| CN112479491A (en) * | 2020-11-18 | 2021-03-12 | 三桶油环保科技(宜兴)有限公司 | Advanced treatment and discharge method for fracturing flow-back fluid |
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Application publication date: 20120919 |