CN103253836A - Deep purification and treatment device and method of landfill leachate - Google Patents
Deep purification and treatment device and method of landfill leachate Download PDFInfo
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- CN103253836A CN103253836A CN2013102265375A CN201310226537A CN103253836A CN 103253836 A CN103253836 A CN 103253836A CN 2013102265375 A CN2013102265375 A CN 2013102265375A CN 201310226537 A CN201310226537 A CN 201310226537A CN 103253836 A CN103253836 A CN 103253836A
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Abstract
The invention relates to deep purification and treatment device and method of landfill leachate. The method comprises the steps of (1) processing the landfill leachate by a membrane bioreactor so as to remove organic matters and solid particles out of the landfill leachate; (2) carrying out physical and chemical coagulation on water discharged by the membrane bioreactor in the step (1), so as to form settlement and colloid; (3) separating the material of the discharged water in the step (2) to remove the settlement and the colloid, so as to reduce the hardness and the turbidity of the discharged water; and (4) carrying out reverse osmosis treatment on the discharged water in the step (3), so as to remove ions out of the discharged water. The deep purification and treatment device and method have the beneficial effects that the nanofiltration process in the traditional membrane depth treatment technology is replaced by physical and chemical coagulation and membrane separation technologies; concentrate produced at the nanofiltration process stage is avoided; the output of fresh water in the entire system is improved; the water production rate of the system is improved; the recycling amount of the fresh water is increased; the operation cost of a power plant is reduced; and the phenomena of equipment corrosion, scale formation and the like in the power plant are avoided when nanofiltration concentrate is reused in the power plant.
Description
Technical field
The present invention relates to sewage treatment area, the present invention relates to a kind of percolate deep purifying treatment unit and method particularly, relate in particular to a kind of technology that is applied in the high concentrated organic wastewater advanced treatment process, be applicable to and burn power plant's percolate treatment industry, also can be applicable to landfill percolate and other high concentrated organic wastewater industries.
Background technology
Along with constant development of economy, the protection of ecotope and resource are utilized the focus that becomes people's growing interest rationally and effectively.Serious in China's environmental pollution at present, the discharging of trade effluent and urban domestic wastewater has caused the pollution of environment, and especially consumer waste infiltration liquid is more serious to environmental hazard, and overexploitation and the use of water resources make China face serious water crisis simultaneously.
It has been undisputable fact that the present mankind face the water crisis; though country has increased the input to urban infrastructure construction and environment protection; strengthen comprehensive environmental improvement; thereby gross contamination emission is effectively controlled; some areas and city environmental quality make moderate progress, but according to the environmental monitoring results statistical study, it is still very severe that China's water pollutes situation; every gross contamination emission is very big, and pollution level still is in quite high level.
Simultaneously, along with the urbanization degree is accelerated, water consumption increases, and water displacement increases simultaneously, and the sewage disposal demand also strengthens thereupon, and with sewage disposal regeneration, the utilization of reuse water also becomes the effective way of alleviating water resources pressure.
In various sewage, percolate Organic pollutants concentration height, ammonia nitrogen concentration are high and contain a large amount of soluble solids and heavy metal ion, as not dealing carefully with, can cause severe contamination to water body and soil on every side, to the peripheral people's healthy generation serious threat.
At present percolate is handled the more and more strictness of requirement of back effluent quality, the special percolate that produces for waste incineration power plant, some ring areas, major river valley require the percolate water outlet to reach one-level A emission standard in " urban wastewater treatment firm pollutant emission standard " or reach recirculated cooling water moisturizing standard in " the urban sewage reutilization process water water quality " standard (GB/T 19923-2005).Therefore the advanced treatment of percolate is a technology that presses for.
The advanced treatment technology of existing domestic garbage burning electricity generation factory percolate is as shown in Figure 1: its technical matters flow process is that filter and reverse osmosis process are directly admitted in the MBR water outlet, wherein pollution-resistant membrane is generally adopted in nanofiltration, the fresh water productive rate of nanofiltration technique is about 75%～85%, pass through reverse osmosis process again through the percolate after the nanofiltration processing, reverse osmosis process adopts brackish water or sea water desaltination film more, the fresh water productive rate of reverse osmosis is about 70%～75% of flooding quantity, and then entire depth treatment system fresh water productive rate is about 50%～60%.
Select nanofiltration+reverse osmosis process of the prior art for use, water outlet can be satisfied the recirculated cooling water moisturizing standard in one-level A standard or the reuse water, but after nanofiltration and reverse osmosis, can produce a large amount of dense water, wherein the dense water of nanofiltration contains a large amount of divalent-metal ions and the organic pollutant of difficult degradation, and its dense water generates rate is about 15%～25%; Reverse osmosis concentrated water contains higher salinity, and dense water generates amount is about 25%～30%; Then the total dense water generates rate of system is about 50%～60%.And dense water treatment does not have economically viable way temporarily at percolate in the industry, in the face of so many dense water, burns power plant's reuse and has difficulties.
Though art methods can realize one-level A emission standard or GB/T 19923-2005 standard, nanofiltration concentrated solution productive rate is about 15%～25% of flooding quantity, and the reverse osmosis concentrated liquid productive rate is about 25%～30% of feed water by reverse osmosis amount; Because nanofiltration concentrated solution and reverse osmosis concentrated liquid water quality difference are big, adopt the mode of reuse respectively to dispose, but no matter adopt which kind of disposal options, so many concentrated solution all is a difficult problem concerning power plant.
At the predicament that faces in the industry, the advanced treatment technical scheme of developing a kind of economical rationality, technical feasibility is imperative, to reduce dense water generates amount, guarantees that the dense water yield satisfies power plant's reuse requirement.
Summary of the invention
Introduced the concept of a series of reduced forms in the summary of the invention part, this will further describe in the embodiment part.Summary of the invention part of the present invention does not also mean that key feature and the essential features that will attempt to limit technical scheme required for protection, does not more mean that the protection domain of attempting to determine technical scheme required for protection.
One aspect of the present invention provides a kind of percolate deep purifying treatment process, comprising:
(1) select for use membrane bioreactor that percolate is handled, to remove organism and the solid particulate in the described percolate;
(2) the materialization coagulation is carried out in the water outlet of membrane bioreactor in the step (1), to form precipitation and colloid;
(3) feed separation is carried out in the water outlet of step (2), remove described precipitation and colloid, go out water hardness and turbidity to reduce this;
(4) reverse-osmosis treated is carried out in the water outlet of step (3), to remove the ion in this water outlet.
As preferably, the materialization coagulation in the step (2) comprises following substep:
(2-1) pH regulator is carried out in the water outlet of membrane bioreactor in the step (1), pH regulator is extremely alkaline;
(2-2) sterilization is carried out in the water outlet of step (2-1);
(2-3) flocculation treatment is carried out in the water outlet of step (2-2), in described water outlet, to form precipitation or colloid.
As preferably, in described step (2-1) with pH regulator to 11.5～12.5 of described water outlet.
As preferably, in described step (2-3), add flocculation agent flocculation treatment is carried out in the water outlet of described step (2-2).
As preferably, in described step (2-3), add coagulant aids flocculation treatment is carried out in the water outlet of described step (2-2).
As preferably, between described step (3) and described step (4), also comprise the extremely near neutral step of pH regulator with the water outlet of step (3).
As preferably, in the described step (1) with the CODcr control of the water outlet after Membrane Bioreactor for Wastewater Treatment at 800～1200mg/L.
As preferably, the control of the concentrated solution producing water ratio of reverse osmosis is between 25～30% in the described step (4).
The present invention also provides a kind of percolate deep purifying treatment unit, comprising:
Membrane bioreactor is for the organism of removing percolate;
The materialization coagulation system is used for percolate is carried out flocculation treatment;
The feed separation system is used for realizing solid-liquid separation, reduces hardness and the turbidity of percolate;
And reverse osmosis system, with removing the percolate intermediate ion.
As preferably, described membrane bioreactor is immersion curtain type membrane or external placed type tubular membrane.
As preferably, described materialization coagulation system comprises pH regulator pond, sterilization pond, the coagulation reaction tank that is communicated with successively, to realize pH regulator, sterilization and the flocculation treatment to percolate.
As preferably, select for use the feed separation film to carry out solid-liquid separation in the described feed separation system.
As preferably, select brackish water film or sea water desaltination film in the described reverse osmosis system for use.
Beneficial effect of the present invention is:
(1) employing materialization coagulation and membrane separation process replace the nanofiltration technique in the existing film advanced treatment technology, have avoided the dense water of nanofiltration technique stage generation, improve total system fresh water generation;
(2) system's producing water ratio improves, and fresh water reuse amount increases, and saves power plant's running cost;
(3) it is big to the invention solves dense water generates amount, the predicament that power plant can't dissolve;
(4) the present invention has avoided the generation of nanofiltration stage concentrated solution, has reduced the laying of dense water reuse pipeline, saves one-time investment;
(5) avoided nanofiltration concentrated solution reuse power plant, phenomenon such as the equipment corrosion that power plant is caused, fouling.
Description of drawings
Following accompanying drawing of the present invention is used for understanding the present invention at this as a part of the present invention.Embodiments of the invention and description thereof have been shown in the accompanying drawing, have been used for explaining principle of the present invention.In the accompanying drawings,
Fig. 1 is the advanced treatment process schema of domestic garbage burning electricity generation factory percolate in the prior art;
Fig. 2 is the advanced treatment process schema of domestic garbage burning electricity generation of the present invention factory percolate.
Embodiment
In the following description, a large amount of concrete details have been provided in order to more thorough understanding of the invention is provided.Yet, it will be apparent to one skilled in the art that the present invention can need not one or more these details and implemented.In other example, for fear of obscuring with the present invention, be not described for technical characterictics more well known in the art.
The present invention reclaims too much in order to solve the dense water that exists in the prior art, the problem of complex process, a kind of new percolate deep purifying treatment process is provided, and described method adopts materialization coagulation+feed separation+reverse osmosis process as the advanced treatment process of percolate.
Wherein, employing materialization coagulation and membrane separation process replace the nanofiltration technique in the existing film advanced treatment technology, have avoided the dense water of nanofiltration technique stage generation, improve total system fresh water generation.
Mainly be made up of pH regulator pond, sterilization pond, coagulation reaction tank at the materialization coagulation process, main purpose is that suspended substance and the colloid in the percolate that will handle through life flocculates, and forms flco.
Wherein, feed separation is a kind of membrane separation process, uses the feed separation film, and the passage of this film is big, flux is big, can bear bigger working pressure.
Wherein, reverse osmosis membrane mainly adopts brackish water or sea water desaltination film, and whether to water outlet chlorion have requirement, as water outlet the chlorion requirement is arranged if looking, then adopt the sea water desaltination film, as direct discharging, then adopts the brackish water film.
Embodiment 1
Below in conjunction with accompanying drawing a kind of preferred implementation of the present invention is further described, as shown in Figure 2, the technical program technical process is: MBR water outlet+materialization coagulation+feed separation membrane sepn+reverse osmosis process.
(1) MBR technology
The film of MBR technology both can be that the immersion curtain type membrane also can be the external placed type tubular membrane, and the CODcr control of its effluent quality is at 800～1200mg/L;
Described MBR technology has not only improved the effluent quality of system and the stability of operation, has also prolonged the hydraulic detention time of macromolecular substance in bio-reactor, makes it to be degraded to greatest extent, and has strengthened the removal effect of system to hard-degraded substance.
The step that comprises nitrification and denitrification in this embodiment in the described MBR reactor:
Denitrification: at first the water outlet of anaerobic technique enters the denitrification pond, under anaerobic environment, microorganism will intake and return digestion liquid in nitric nitrogen and nitrite nitrogen be reduced into nitrogen and discharge, reach the purpose of biological denitrificaion; Influence denitrifying factor and mainly contain 2 points, the one, the concentration of control dissolved oxygen between 0～0.5mg/L, the 2nd, guarantee denitrifying carbon source, carbon source concentration is generally between 4～6 times of water total nitrogen concentration into.
Nitrated: the percolate behind the denitrification pond enters nitrification tank and carries out nitration reaction, and the effect of nitrification tank mainly contains 2 points, and the one, the remaining organic pollutant of degrading, the 2nd, under ammonification, convert ammonia nitrogen to nitric nitrogen and nitrite nitrogen.
As preferably, can also be according to organic removal ratio in the percolate after denitrification step, selectivity increases the strengthened denitrification step, particularly, the waste water after nitrated enters strengthened denitrification system, i.e. rear-mounted denitrification, in rear-mounted denitrification, add additional carbon to obtain higher TN clearance, nitric nitrogen can more be broken down into nitrogen and remove, and the TN clearance further improves, and has saved running cost simultaneously.
As further preferred, the water outlet after the process biochemical treatment is again through ultrafiltration membrance filter.The effect of described ultra-filtration membrane mainly contains 2 points, and the first is kept the sludge concentration in the biochemistry pool, and its sludge loading is improved; It two is that water outlet is filtered, and tackles more macromolecular organic pollutant.Ultra-filtration membrane both can be that the immersion curtain type membrane also can be the external placed type tubular membrane, and the CODcr control of its effluent quality is at 800～1200mg/L.
(2) materialization coagulation process
The materialization coagulation process is made up of steps such as the adjusting of pH, sterilization and disinfection, coagulatings, and pH regulator is carried out in the water outlet of handling through MBR, and pH value is transferred to 11.5～12.5, selects for use the method for adding alkali lye to regulate usually.PH regulator arranges pH meter in the pond, and pH meter and alkali lye throwing device are chain, and the realization pH regulator is controlled automatically.
Water outlet behind pH regulator enters the sterilization pond and carries out sterilization, it mainly is by adding the strong oxidizing property material percolate to be carried out germicidal treatment, on the one hand can sterilization algae removal in this step, the living organism amount that reduction is held back by ultra-filtration membrane, thereby operation steady in a long-term is guaranteed in the pollution that the material separator of using in the assurance subsequent disposal and reverse osmosis membrane are not grown by the bacterium algae.
In this embodiment, can add DBNPA(2,2-dibromo-3-nitrilo-proprionamide, the two bromos of 2,2--3-nitrilo-propionic acid amide), sterilant such as clorox or hydrogen peroxide carry out sterilization.Wherein DBNPA is non-oxide sterilant, and with the mould material compatibility, it adds does not have influence to film.Hydrogen peroxide and clorox are the strong oxidizing property sterilant, when adding it are added concentration and dosage has requirement, and the concentration of hydrogen peroxide is not higher than 0.2%, and clorox concentration is no more than 10%, to prevent described sterilant mould material is caused damage.The concrete dosage of sterilant will be decided according to actual water quality situation.
Add flocculation agent in the water outlet after sterilisation step, make percolate generation flocculation reaction, owing to contain a large amount of HCO in the percolate
3-, when adding alkali lye transfers to 12 with the pH value of solution value, can generate a large amount of CO
3 2+, and with water in Ca
2+, Mg
2+Reaction forms CaCO
3, MgCO
3Precipitation, iron ion and OH in the solution
-Ionic reaction forms Fe (HO)
3Colloid, and with described precipitation and colloid removal, to reduce hardness and the turbidity in the water.
For better with described CaCO
3, MgCO
3Precipitation and Fe (HO)
3Colloid is removed, in percolate, add flocculation agent, make the precipitation or the colloid that form in the percolate more stable by adding flocculation agent, and make these particles concentrate by its aggregation property, obtain more closely knit precipitation, thereby be more prone to separate.Wherein flocculation agent can aluminium salt or molysite, and as preferably, described flocculation agent selects for use its dosage of molysite (massfraction is 5% iron salt solutions) of 5% for being less than or equal to 150ppm.
As preferably, can also further add coagulant aids in order to improve flocculating effect, described coagulant aids also can improve the structure of flocs unit, utilize the strong adsorption bridging action of polymer coagulant aids, make tiny loose flocs unit become thick and tight, commonly used is that its dosage of anionic polyacrylamide is decided on the water quality situation, and as preferably, its dosage is that the solution dosage of 0.1 ‰～0.15 ‰ concentration is for being less than or equal to 3ppm.
(3) feed separation
Described feed separation step also is a kind of membrane separation process, by this step precipitation, colloid and the percolate that forms in the materialization coagulation step separated, realize solid-liquid separation, remove the most of solid particulate in the water, reduce hardness and the turbidity of percolate.
Select for use the feed separation film to carry out solid-liquid separation in this step, this feed separation film has porous, high strength, erosion resistance, chemical stability, but advantage such as flux is big, easy cleaning working pressure scope is wide.The working pressure of this film is between 0.05～0.1MPa, and flux can reach 100～200L/m
2H.
Not only removed the solid particulate in the water in the coagulation process of materialization described in the present invention and the feed separation technology, hardness and the turbidity of percolate have been reduced, also can not produce dense water simultaneously, thereby reduced dense water generates rate in the whole processing step, improved the fresh water generation of total system, avoided selecting for use diverse ways that the dense water that produces in the different step is handled respectively, made whole technological process simple more, efficient, the technology cost reduces.
The precipitation of removing in this step, colloid and mud can be discharged in the mud storage pond, reclaim and utilize.
After feed separation, removed the Ca in most percolates
2+, Mg
2+And Fe
2+/ Fe
3+, its removal effect is as shown in table 1, and this step also has certain effect to the removal of COD.
Feed separation film service data of the present invention is as shown in table 1:
| ? | The MBR water outlet | Feed separation membrane filtration clear liquid | Clearance % |
| Ca(mg/L) | 185 | 22 | 88.11% |
| Mg(mg/L) | 287 | 14.5 | 94.95% |
| COD(mg/L) | 653 | 457 | 30.02% |
(4) reverse osmosis process
In this step, under action of pressure, remove impurity such as salt in the percolate, heavy metal by reverse osmosis membrane, to the further separation and purification of percolate, to reach emission standard.
Reverse osmosis membrane mainly adopts brackish water or sea water desaltination film in this step, and whether look has requirement to the water outlet chlorion, as water outlet the chlorion requirement is arranged, then adopt the sea water desaltination film, as direct discharging, then adopt the brackish water film, the reverse osmosis concentrated water producing water ratio is controlled between 25～30%.
As preferably, before carrying out reverse-osmosis treated, can also comprise the step of described percolate being carried out pH regulator, particularly, by in percolate, adding acid, in and the excessive alkali that in the pH regulator pond, adds, make last water outlet as far as possible for neutral, in order to water outlet is directly used, wherein the kind of the acid of Jia Ruing can be selected this area pH regulator agent commonly used for use, is not limited to a certainly, does not repeat them here.
Water quality (the brackish water film is adopted in reverse osmosis) through the percolate after the present invention's processing is as shown in table 2, finds out in CODcr described in this step and all greatly reductions of amplitude of TDS to have good effect from this table, has reached emission standard.
The water quality of the percolate of brackish water film is adopted in table 2 reverse osmosis
| The water quality classification | CODcrmg/L） | TDSmg/L） |
| The water outlet of feed separation film | 439 | 11758 |
| Reverse osmosis 70% producing water ratio water quality | 21 | 875 |
| Reverse osmosis 75% producing water ratio water quality | 37 | 1401 |
In order to solve the too high problem of dense aquatic products rate in the prior art, sewage treatment process is improved among the present invention, and the order that arranges of each processing step is improved, to improve the treatment effect to percolate.At first adopt MBR technology that the organic pollutant in the percolate and big solid particulate are removed in the present invention, adopt coagulation-settlement process afterwards, feed water by reverse osmosis is softened, avoid reverse osmosis inorganic salt structure, improve the producing water ratio of reverse osmosis and the cleaning frequency of reduction reverse osmosis, when reaching emission standard, reduce dense aquatic products rate, solved the drawback that exists in the prior art.
Embodiment 2
The present invention also provides a kind of percolate deep purifying treatment unit, described device comprises membrane bioreactor, materialization coagulation system, feed separation system and the reverse osmosis system that connects successively, wherein, described materialization coagulation system comprises pH regulator pond, sterilization pond, the coagulation reaction tank that is communicated with successively, be used for regulating percolate pH and forming flocculation sediment, to reduce hardness and the turbidity of percolate, in this process, do not produce dense water simultaneously.
Wherein, the feed separation system comprises the feed separation film at least, to realize solid-liquid separation.
Particularly, membrane bioreactor can be selected this area reactor commonly used for use in this embodiment, described reactor is made up of membrane module and bio-reactor two portions usually, the membrane module of described MBR technology both can be that the immersion curtain type membrane also can be the external placed type tubular membrane, its principle of work is that a large amount of microorganisms (active sludge) fully contacts with matrix (labile organic compound in the waste water etc.) in membrane bioreactor, carry out metabolism by oxygenolysis and grow, breed to keep self, make organic pollutant degradation simultaneously; Membrane module carries out solid-liquid separation by mechanical grading, effect such as hold back to waste water and mud mixed liquid then, and the CODcr control of its effluent quality is at 800～1200mg/L.Described MBR technology has not only improved the effluent quality of system and the stability of operation, has also prolonged the hydraulic detention time of macromolecular substance in bio-reactor, makes it to be degraded to greatest extent, and has strengthened the removal effect of system to hard-degraded substance.
Described membrane bioreactor can be selected aerobic MBR, anaerobism MBR for use or with the reactor of both combinations.Wherein, aerobic MBR effluent quality height is controlled described aerobic MBR rate of load condensate at 1.2～4.2kg COD/ (m
3D) between, anaerobism MBR rate of load condensate is at 2.9～50kg COD/ (m
3D) between; Anaerobism MBR can select as the case may be, when organic content is high especially in percolate or the sewage, select for use anaerobism MBR to can be used as the pre-treatment process of waste water or used water difficult to degradate, again according to the type of water quality, handle in conjunction with aerobic MBR, make the water outlet qualified discharge.
Wherein, the materialization coagulation system mainly is made up of pH regulator pond, sterilization pond, coagulation reaction tank, water outlet process pH regulator pond through the MBR processing, by adding alkali lye the pH value is transferred to 11.5～12.5, enter the sterilization pond afterwards, the sterilization pond mainly is to add clorox, and coagulation reaction tank mainly is to add flocculation agent and coagulant aids.Contain a large amount of HCO in the percolate
3-, when adding alkali lye transfers to 12 with the pH value of solution value, can generate a large amount of CO
3 2+, and with water in Ca
2+, Mg
2+Reaction forms CaCO
3, MgCO
3Precipitation, iron ion and OH in the solution
-Ionic reaction forms Fe (HO)
3Colloid.By above reaction, most calcium, magnesium, iron form in the solution throw out and colloid, and the silicate that carries all will precipitate flocculation.
Arranging of feed separation film in the described feed separation system can be with reference to the setting of membrane module among the MBR, by the feed separation film with the precipitation, colloid and the percolate that form in the materialization coagulation step separately, realizes solid-liquid separation.
Utilizing the aperture in the reverse osmosis unit is the reverse osmosis membrane (RO film) of 1/10000 μ m, make the water of higher concentration become low concentration of water, the impurity that industrial pollutants, heavy metal, bacterium, virus etc. are sneaked in the water is in a large number all isolated simultaneously, thereby reach physical and chemical index and the hygienic standard of drinking regulation, output is to clear extremely pure water.
In this embodiment, described reverse osmosis system can comprise: pretreatment unit, reverse osmosis units, post-processing unit, cleaning unit and electric control unit etc.
Wherein reverse osmosis units mainly comprises compositions such as multistage high-pressure pump, reverse-osmosis membrane element, putamina (pressurized vessel), support.It mainly acts on is the impurity of removing in the water, make water outlet satisfy service requirements, select brackish water or sea water desaltination film in the described reverse-osmosis membrane element for use, whether look has requirement to the water outlet chlorion, as water outlet the chlorion requirement is arranged, then adopt the sea water desaltination film, as direct discharging, then adopt the brackish water film, the reverse osmosis concentrated water producing water ratio is controlled between 25～30%.
Certain described reverse osmosis system is not limited to above-mentioned configuration, can arrange according to concrete needs.
By apparatus and method of the present invention, after percolate is handled through this advanced treatment process, the control of dense water generates amount is in 30%, and water outlet reaches one-level A emission standard in " urban wastewater treatment firm pollutant emission standard " or reaches recirculated cooling water moisturizing standard in " urban sewage reutilization process water water quality " standard (GB/T19923-2005).
The invention has the advantages that:
(1) employing materialization coagulation and membrane separation process replace the nanofiltration technique in the existing film advanced treatment technology, have avoided the dense water of nanofiltration technique stage generation, improve total system fresh water generation;
(2) system's producing water ratio improves, and fresh water reuse amount increases, and saves power plant's running cost;
(3) it is big to the invention solves dense water generates amount, the predicament that power plant can't dissolve;
(4) the present invention has avoided the generation of nanofiltration stage concentrated solution, has reduced the laying of dense water reuse pipeline, saves one-time investment;
(5) avoided nanofiltration concentrated solution reuse power plant, phenomenon such as the equipment corrosion that power plant is caused, fouling.
The present invention is illustrated by above-described embodiment, but should be understood that, above-described embodiment just is used for for example and illustrative purposes, but not is intended to the present invention is limited in the described scope of embodiments.It will be appreciated by persons skilled in the art that in addition the present invention is not limited to above-described embodiment, can also make more kinds of variants and modifications according to instruction of the present invention, these variants and modifications all drop in the present invention's scope required for protection.Protection scope of the present invention is defined by the appended claims and equivalent scope thereof.
Claims (14)
1. percolate deep purifying treatment process comprises:
(1) select for use membrane bioreactor that percolate is handled, to remove organism and the solid particulate in the described percolate;
(2) the materialization coagulation is carried out in the water outlet of membrane bioreactor in the step (1), to form precipitation and colloid;
(3) feed separation is carried out in the water outlet of step (2), remove described precipitation and colloid, go out water hardness and turbidity to reduce this;
(4) reverse-osmosis treated is carried out in the water outlet of step (3), to remove the ion in this water outlet.
2. method according to claim 1 is characterized in that, the materialization coagulation in the step (2) comprises following substep:
(2-1) pH regulator is carried out in the water outlet of membrane bioreactor in the step (1), pH regulator is extremely alkaline;
(2-2) sterilization is carried out in the water outlet of step (2-1);
(2-3) flocculation treatment is carried out in the water outlet of step (2-2), in described water outlet, to form precipitation or colloid.
3. method according to claim 2 is characterized in that, in described step (2-1) with pH regulator to 11.5～12.5 of described water outlet.
4. method according to claim 2 is characterized in that, adds flocculation agent in described step (2-3) flocculation treatment is carried out in the water outlet of described step (2-2).
5. method according to claim 4 is characterized in that, adds coagulant aids in described step (2-3) flocculation treatment is carried out in the water outlet of described step (2-2).
6. method according to claim 1 is characterized in that, also comprises the extremely near neutral step of pH regulator with the water outlet of step (3) between described step (3) and described step (4).
7. method according to claim 1 is characterized in that, the CODcr with the water outlet after Membrane Bioreactor for Wastewater Treatment in the described step (1) controls at 800～1200mg/L.
8. method according to claim 1 is characterized in that, the control of the concentrated solution producing water ratio of reverse osmosis is between 25～30% in the described step (4).
9. percolate deep purifying treatment unit comprises:
Membrane bioreactor is for the organism of removing percolate;
The materialization coagulation system is used for percolate is carried out flocculation treatment;
The feed separation system is used for realizing solid-liquid separation, reduces hardness and the turbidity of percolate;
And reverse osmosis system, with removing the percolate intermediate ion.
10. device according to claim 9 is characterized in that, described membrane bioreactor is immersion curtain type membrane or external placed type tubular membrane.
11. device according to claim 9 is characterized in that, described materialization coagulation system comprises pH regulator pond, sterilization pond, the coagulation reaction tank that is communicated with successively, to realize pH regulator, sterilization and the flocculation treatment to percolate.
12. device according to claim 9 is characterized in that, selects for use the feed separation film to carry out solid-liquid separation in the described feed separation system.
13. device according to claim 12 is characterized in that, the working pressure of described feed separation film is between 0.05-0.1MPa, and described membrane flux is 100～200L/m
2H.
14. device according to claim 9 is characterized in that, selects brackish water film or sea water desaltination film in the described reverse osmosis system for use.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310226537.5A CN103253836B (en) | 2013-06-07 | 2013-06-07 | A kind of percolate deep purifying treatment unit and method |
Applications Claiming Priority (1)
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| CN104418465A (en) * | 2013-09-03 | 2015-03-18 | 上海御隆膜分离设备有限公司 | Landfill leachate treatment method and equipment |
| CN111718025A (en) * | 2020-06-16 | 2020-09-29 | 重庆杰润科技有限公司 | Coagulant aid for advanced wastewater treatment, preparation method thereof and advanced wastewater treatment method by membrane treatment |
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| CN103253836B (en) | 2016-01-06 |
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