CN102351371B - Reactor for deep purification of drinking water and deep purification method of drinking water - Google Patents
Reactor for deep purification of drinking water and deep purification method of drinking water Download PDFInfo
- Publication number
- CN102351371B CN102351371B CN 201110185360 CN201110185360A CN102351371B CN 102351371 B CN102351371 B CN 102351371B CN 201110185360 CN201110185360 CN 201110185360 CN 201110185360 A CN201110185360 A CN 201110185360A CN 102351371 B CN102351371 B CN 102351371B
- Authority
- CN
- China
- Prior art keywords
- water
- ozone
- bio
- oxidation unit
- membrance filter
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a reactor for deep purification of drinking water and a deep purification method of drinking water. The reactor comprises a main ozone oxidation unit, a biological oxidation unit and an ultrafilter membrane filtration unit, wherein the biological oxidation unit is positioned between the main ozone oxidation unit and the ultrafilter membrane filtration unit; and the biological oxidation unit and the ultrafilter membrane filtration unit are disposed in a same reaction tank. Ozone oxidizes and destroys hardly degraded pollutants and converts high molecular weight organic matters into intermediate and low molecular weight organic matters. After ozonization, an effluent respectively enters into the reaction tank fixed with a biological filling material and an ultrafilter membrane assembly. When the pollution of the water source is severe, powdered active carbon can be also added. The active carbon is used to absorb intermediate molecular weight or volatile organic compounds; microorganisms on the surface of the biological filling material and on the surface of the powdered active carbon are used to remove ammonia nitrogen and low molecular weight organic matters; and the security of the microorganisms is guaranteed by ultrafiltration. The reactor provided by the invention can be used for deep purification of polluted water sources, and also can be applied for deep processing of urban sewage treatment plants and reclaimed water.
Description
Technical field
The invention belongs to the drink water purifying field, be particularly related to a kind of reactor that is used for drinking water deep purification that can realize ozone oxidation, microbiological deterioration and ultra-filtration and separation, and the method for utilizing the drinking water deep purification of ozone oxidation, microbiological deterioration and ultrafiltration membrance filter.
Background technology
China will carry out in 2012 " drinking water sanitary standard (GB5749-2006) ".Compare with " drinking water sanitary standard (GB5749-1985) ", new drinking water standard has significantly increased the index of the artificial synthetic organic materials such as chemistry of pesticide product and disinfection byproduct (DBP), and the ammonia nitrogen concentration limit value is set to below the 0.5mg/L in the water.In addition, some urban drinking water source are polluted by natural organic matter, and oxygen-consumption is difficult to up to standard; There are the pollution problems such as algae and metabolite thereof in some urban drinking water source, cause output water to smell flavor intensity higher, affect the mouthfeel of tap water.
Ozone and active carbon, ozone/biological activated carbon are widely used in water factory's upgrading as employed product in the typical drinking water deep treatment process.Ozone and active carbon, the ultimate principle of ozone/biological activated carbon in the drinking water deep treatment process are, utilize ozone oxidation to destroy the small organic molecules such as agricultural chemicals, and the small organic molecule that molecular weight organism larger, that microorganism is difficult to utilize is converted into molecular weight, is easily utilized by microorganism.In gac (or biological activated carbon) unit, then utilize the adsorption of gac (or biological activated carbon) and the Degradation of the epontic microorganism of gac (or biological activated carbon) to remove organism, and improve the mouthfeel of tap water.The synergy of ozone and gac (or biological activated carbon) is so that ozone and active carbon, ozone/biological activated carbon can keep good decontamination effect improving for a long time.But, utilize ozone and active carbon, ozone/biological activated carbon to carry out investment and running cost that drinking water deep processes all higher, the middle-size and small-size water factory of many low developed areas is difficult to bear.In addition, many water factories are when carrying out drinking water deep processing upgrading, and often available space is very limited, do not have enough soils to be used for newly-built cover ozone and active carbon advanced treatment process structures.
Micro-filtration and ultra-filtration technique do not belong to Advanced Treatment of Drinking Water in essence; Nanofiltration or reverse osmosis can significantly improve the organic matter removal ability, but have the problems such as cost is higher, operational management is complicated, producing water ratio is low, use considerably less in China municipal drinking water factory.Therefore, development investment and running cost are lower, the simple drinking water deeply purifying method of operational management, and comparatively the water quality reaching standard problem of backward areas is significant for solving some economy of China.
Ultra-filtration technique is developed and push engineering to and use gradually in recent years, and along with the large-scale application of ultrafiltration, investment and running cost are all effectively reduced.But ultrafiltration is higher to the removal ability of holding back of the particulate pollutants such as bacterium, virus, algae, colloid in the water, and solvability natural organic matter, artificial synthetic organic materials, ammonia nitrogen etc. are not almost removed ability.Many investigators have been developed combination process and technology based on this take ultrafiltration as core.For example, with coagulation and combining ultrafiltration, utilize the absorption of coagulation, the volume effect such as sweep that dissolved organic matter is converted into particulate organic matter, this can the Effective Raise ultrafiltration technology to the removal ability of solvability larger molecular organics.But this method is limited in one's ability to the organic matter removal that improves medium or small molecular weight, and is helpless especially to ammonia nitrogen.And for example, with Powdered Activated Carbon and combining ultrafiltration, and the assurance residence time of Powdered Activated Carbon in reactor, utilize Powdered Activated Carbon to the biological degradation of the adsorption of pollutent and the microbial film that under the long-time running condition, forms at the powder activity carbon surface, the contaminant removal capacity such as organism, ammonia nitrogen in the Effective Raise water.But the Powdered Activated Carbon particle is easily at the film surface aggregation, and may cause the physical damnification on film surface under film negative pressure-pumping condition, affects the film silk life-span; Film silk in the membrane module is fracture in a single day, and the Powdered Activated Carbon that the surface has microorganism is easy to penetrate the ultrafiltration barrier and may causes the water supply accident; In addition, how to guarantee the Powdered Activated Carbon sludge age in the spoil disposal process, this also is difficult to effective control in operational management.Somebody's proposition is placed on ultrafiltration after ozone/biological activated carbon unit, thereby avoids gac fragment and microorganism loss or penetrate into pipe network.But this scheme has further increased process complexity and head loss, and water factory's operational management is more complicated.Therefore, how to develop efficient, economical, stable and move simple advanced treatment process, this realizes that for China water factory is up to standard, and this is the key issue of needing solution in the engineering badly.
Summary of the invention
One of purpose of the present invention provides a kind of reactor that is used for drinking water deep purification that can realize ozone oxidation, microbiological deterioration and ultra-filtration and separation.
Two of purpose of the present invention provides that a kind of performance is efficient, economically feasible, stable, the method for safeguarding drinking water deep purification simple and easy to implement.
The present invention is directed to the problem that above-mentioned prior art exists, propose after main ozone oxidation unit, the bio-oxidation unit and the ultrafiltration membrance filter unit that utilize the biologic packing material biofilm to be set.Its ultimate principle is, in main ozone oxidation unit, utilize the O3 contacted oxidation effect with micro quantity organic pollutant and the stink substance Oxidative demage of difficult degradation in the water, and with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organic matter degradation is converted into and is easy to the small organic molecule that utilized by microorganism; In the bio-oxidation unit, utilize biologic packing material that microorganism colonization is fixed on the biologic packing material surface and form microbial film, improve the amount of microorganism in the reactor, utilize microbiological deterioration with intermediate molecular weight (general number-average molecular weight scope be 3KDa～30KDa), small molecular weight (general number-average molecular weight scope is removed for＜3KDa) organism assimilation, and by the microorganism nitrification with ammonia nitrogen removal; In the ultrafiltration membrance filter unit, utilize the filteration of holding back of ultra-filtration membrane that the pollutents such as microorganism, the microbial film that comes off, colloidal solid in the water are held back.In addition, for polluting comparatively serious former water, can also add Powdered Activated Carbon at bio-oxidation unit front end, and guarantee the sufficient residence time of Powdered Activated Carbon, thereby further improve biomass and microbiological deterioration ability, improve the removal effect to water pollutant.In addition, most Powdered Activated Carbons are held back in the biologic packing material district, significantly reduce the amount of the Powdered Activated Carbon that is gathered in the ultra-filtration membrane surface, avoid physical damnification is caused on the ultra-filtration membrane surface.The present invention can be used for the drinking water deep purification at contaminated water source, also can be applicable to municipal wastewater treatment plant advanced treatment and reuse water deep purifying.
Reactor for drinking water deep purification of the present invention comprises main ozone oxidation unit, bio-oxidation unit and ultrafiltration membrance filter unit; Wherein, described bio-oxidation unit is between described main ozone oxidation unit and described ultrafiltration membrance filter unit; Described bio-oxidation unit and described ultrafiltration membrance filter unit are arranged in the same reaction tank.As shown in Figure 1.
Described main ozone oxidation unit comprises ozone contact tank and ozone reaction pond two portions.
One dividing plate is separated into described ozone contact tank and described ozone reaction pond with a container, and leaves the space between the bottom of described dividing plate and described container; Top at described ozone contact tank is provided with water-in, and the bottom is equipped with ozonation aerated head, and described ozonation aerated head is connected by pipeline with ozonizer; The top in described ozone reaction pond is connected with described bio-oxidation unit by pipeline.
Described bio-oxidation unit comprises biologic packing material, aerating apparatus and sludge sump.
One perforation plate is installed in the described reaction tank that bio-oxidation unit and ultrafiltration membrance filter unit be set, the top in the space that forms between one side of described perforation plate and the pool wall of this reaction tank is set to opening (can be used for Powdered Activated Carbon adds), and at this opening part the pipeline that is connected with the top in described ozone reaction pond is installed; Be filled with the support of described biologic packing material at the opposite side of described perforation plate, aerating apparatus be installed below described biologic packing material and be provided with sludge sump; Described aerating apparatus is connected with air compressor by pipeline.
Described ultrafiltration membrance filter unit comprises aerating apparatus, sludge sump and hyperfiltration membrane assembly.
Described hyperfiltration membrane assembly is installed in described reaction tank, aerating apparatus is installed below described hyperfiltration membrane assembly and is provided with sludge sump; Described aerating apparatus is connected with air compressor by pipeline; Rising pipe is installed above described hyperfiltration membrane assembly, and described rising pipe is connected with suction pump.
Vacuum meter and rising pipe valve are installed on the described rising pipe.
Described rising pipe is connected with a backwash tube, and on the rising pipe above optimizing water pipe and the backwash tube place of being connected being positioned at described rising pipe valve.
The backwash tube valve is installed on the pipeline of described backwash tube.
In the described sludge sump shore pipe is installed.
One side of described perforation plate and the bio-oxidation unit is set and the pool wall of the reaction tank of ultrafiltration membrance filter unit between the space that forms consisted of a current stabilization district.
The zone that biologic packing material and hyperfiltration membrane assembly are installed in the described reaction tank is reaction zone.
The pond type design in described ozone contact tank and described ozone reaction pond is identical with the ozone reaction pond with common ozone contact tank.The purpose of ozone contact tank is ozone gas fully is dissolved in the water, and the purpose in ozone reaction pond is to bring into play ozonidation with contaminant degradation or with the small molecular weight organism of macromolecule oxidation operation for easily being utilized by microorganism.Pending water at first enters ozone contact tank, enters afterwards the ozone reaction pond.The hydraulic detention time of ozone contact tank is 2～4 minutes, and the hydraulic detention time in ozone reaction pond is 10～20 minutes.
Biologic packing material in the described bio-oxidation unit is to be fixed in the reaction tank, and the biological oxidation that is fixed on the microorganism on biologic packing material surface by biofilm is achieved degraded and the removal of pollutent.Described biologic packing material can be the fibrous bundle filler of the fine synthetic fibre of semi soft packing, hydroformylation of semi soft packing, polypropylene or polyethylene material of soft cellulose filler, the fine synthetic fibre material of hydroformylation of the fine synthetic fibre material of hydroformylation or activated carbon fiber Texture composition of materials filler (it has soft and advantage semi soft packing concurrently), Fiber Materials etc.The hydraulic detention time of the water outlet of described main ozone oxidation unit in the described biological respinse zone that is filled with biologic packing material is preferably 20～120 minutes.
Described bio-oxidation can also add Powdered Activated Carbon in the unit, and the adsorption by Powdered Activated Carbon, the epontic microbiological deterioration of Powdered Activated Carbon etc. are with further raising pollutant removal.The throwing weight range of Powdered Activated Carbon is 2～20mg/L.Powdered Activated Carbon adds to the water inlet of bio-oxidation unit, and realizes mixing and fully contacting with pollutent by the aeration effect of bio-oxidation unit.Afterwards, main ozone oxidation unit water outlet enters the bio-oxidation unit that is filled with biologic packing material equably.Intermediate molecular weight organism in the unit water outlet of main ozone oxidation, small molecular weight volatile organic matter etc. are removed under the adsorption of Powdered Activated Carbon; Ammonia nitrogen in the unit water outlet of main ozone oxidation is converted into nitrate under the nitrification of the microorganism of biologic packing material surface and powder activity carbon surface.
Described hyperfiltration membrane assembly is immersion type membrane component, and described ultra-filtration membrane can be hollow-fibre membrane or flat sheet membrane etc., and the material of described ultra-filtration membrane can be polyvinyl chloride or polyvinylidene difluoride (PVDF) etc.The pore diameter range of described ultra-filtration membrane is between 0.01～0.20 μ m, and the membrane flux of ultra-filtration membrane is 10～60L/m
2H.The hydraulic detention time of water in the ultrafiltration membrance filter unit area that described hyperfiltration membrane assembly is housed is 4～10 minutes.Bio-oxidation unit water outlet is through described ultrafiltration membrance filter unit, the impurity particles such as microbial film that go down to dewater middle colloid, bacterium, virus, come off in the membrane sepn effect.
The water outlet of the described bio-oxidation unit described ultrafiltration membrance filter unit of flowing through is that suction function by suction pump is accomplished.Rising pipe is installed above described hyperfiltration membrane assembly, and described rising pipe is connected with suction pump.Water in the described reactor enters the inboard from the film outside under the suction function that suction pump forms, and is finally flowed out by rising pipe.The suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is between 10kPa～80kPa.
In order to guarantee membrane flux, in the operational process that carries out drinking water deep purification, need regularly the hyperfiltration membrane assembly in the described ultrafiltration membrance filter unit to be carried out back flushing.Backwashing water adopts the water outlet after hyperfiltration membrane assembly filters.Under the effect of backwashing pump, backwashing water is flowed out laterally by the ultra-filtration membrane inboard, and the pollutent that is attached to the film surface is able to break away from from the film surface.Described hyperfiltration membrane assembly backwashing period is 2～20 minutes.When backwashing pump is opened, back flushing water inlet pipe valve opening, and suction pump is out of service and the rising pipe valve closes; After back flushing stops, back flushing water inlet pipe valve closes, and suction pump brings into operation and the rising pipe valve opening.
Below the support that is filled with described biologic packing material and described hyperfiltration membrane assembly, be provided with aerating apparatus, and in water, pump into pressurized air by air compressor respectively, thereby for dissolved oxygen is provided in the water, and provides hydraulic action to carry out mix and blend and shear the dirt settling of cleaning film silk surface.Pressurized air can be to pump into constantly in the reactor, also can be to pump in the reactor off and on.Gas-water ratio scope in the described bio-oxidation unit area is 10: 1～150: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 5: 1～50: 1.Pressurized air in the described bio-oxidation unit area and the described ultrafiltration membrance filter unit area can be provided by same air compressor, also can be provided by different air compressor.Described aerating apparatus can be that boring aeration pipe or aeration are first-class.
Below the support that is filled with described biologic packing material and described hyperfiltration membrane assembly, be provided with sludge sump.The impurity such as the particulate matter that density is larger in the water, the microbial film that comes off, Powdered Activated Carbon enter in the sludge sump under action of gravity, and by shore pipe the mud in the sludge sump are discharged.Sludge discharging period can be 12～72 hours; When adding Powdered Activated Carbon, should guarantee that the residence time of Powdered Activated Carbon in described reactor is 4～20 days.
The deep-purifying method of tap water of the present invention: pending water enters ozone contact tank by water-in, the ozone that ozonizer produces fully contacts with pending water after ozonation aerated head disperses and dissolves formation solubilised state ozone, enters together afterwards ozone reaction pond ozone oxidizing reaction; The water outlet in ozone reaction pond enters the current stabilization district in the reaction tank that bio-oxidation unit and ultrafiltration membrance filter unit are set, and the bio-reaction zone that is filled with biologic packing material in the bio-oxidation unit area of behind the perforation plate water distribution uniformity, flowing through and the ultrafiltration membrance filter unit area that hyperfiltration membrane assembly has been installed, at the bio-reaction zone of current through being filled with biologic packing material with when the ultrafiltration membrance filter unit area of hyperfiltration membrane assembly has been installed, simultaneously provide pressurized air to carry out aeration by aerating apparatus in water, water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in the hyperfiltration membrane assembly top.
One side of described perforation plate and the bio-oxidation unit is set and the pool wall of the reaction tank of ultrafiltration membrance filter unit between the space that forms consisted of a current stabilization district.
Described pending water is 2～4 minutes at the hydraulic detention time of ozone contact tank, and the hydraulic detention time in the ozone reaction pond is 10～20 minutes.
The hydraulic detention time of the water outlet of described main ozone oxidation unit in the described biological respinse zone that is filled with biologic packing material is preferably 20～120 minutes (design the shared volume of described biologic packing material, can realize described hydraulic detention time).
The hydraulic detention time of described water in the ultrafiltration membrance filter unit area of described hyperfiltration membrane assembly is housed is 4～10 minutes (design the shared volume of described hyperfiltration membrane assembly, can realize described hydraulic detention time).
The suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is between 10kPa～80kPa.
Gas-water ratio scope in the described bio-oxidation unit area is 10: 1～150: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 5: 1～50: 1.
Described hyperfiltration membrane assembly is when carrying out back flushing, and the time of back flushing is 2～20 minutes.
The function in described current stabilization district is to eliminate the surplus pressure that water inlet brings, and guarantees that current can enter reaction zone 8 equably, avoid short-circuit flow and dead angle area.The function of reaction zone 8 is to realize the effects such as microbiological oxidation and ultra-filtration and separation.Such as needs, can locate to add Powdered Activated Carbon opening 6 (Powdered Activated Carbon adds a little).The throwing weight range of described Powdered Activated Carbon is 2～20mg/L.
The present invention has following advantage:
1. with main ozone oxidation and the combinations such as microbiological deterioration, ultrafiltration membrance filter, realize the pollutant removals such as ammonia nitrogen, organism in the tap water by the synergy between different process, and utilize ultra-filtration membrane fully to guarantee microbial safety.
2. for the more serious situation of pollution of waterhead, can utilize the adsorption of Powdered Activated Carbon and the Degradation of surface microorganism further to improve organism and ammonia nitrogen removal ability, and can adjust Powdered Activated Carbon throwing amount according to the pollution of waterhead situation, use very convenient.
3. floor space is little, and head loss is little, is easy to be applied to old water factory and transforms and new waterworks construction.
4, running cost is cheap, and operational management is convenient.
Description of drawings
Fig. 1. the reactor schematic diagram for drink water purifying of the present invention.
Reference numeral
1. 2. ozonation aerated 3. ozonizers of water-in
4. ozone contact tank 5. ozone reaction ponds 6. openings
7. current stabilization district 8. reaction zones 9. perforation plates
10. biologic packing material 11. aerating apparatuss 12. sludge sumps
13. hyperfiltration membrane assembly 14. suction pumps 15. air compressor
16. rising pipe 17. backwash tubes 18. vacuum meters
19. backwash tube valve 20. rising pipe valves 21. shore pipes
Embodiment
Embodiment 1
The reactor that is used for drinking water deep purification is as shown in Figure 1 set up in design; Wherein, a biological oxidation unit is between a main ozone oxidation unit and a ultrafiltration membrance filter unit; Described bio-oxidation unit and described ultrafiltration membrance filter unit are arranged in the same reaction tank.
Described main ozone oxidation unit comprises ozone contact tank 4 and ozone reaction pond 5 two portions.
One dividing plate is separated into described ozone contact tank 4 and described ozone reaction pond 5 with a container, and leaves the space between the bottom of described dividing plate and described container; Be provided with water-in 1 at the top of described ozone contact tank 4, the bottom is equipped with ozonation aerated 2, and described ozonation aerated head and ozonizer 3 are connected by pipeline; The top in described ozone reaction pond 5 is connected with described bio-oxidation unit by pipeline.
Described bio-oxidation unit comprises biologic packing material 10, aerating apparatus 11 (boring aeration pipe or aeration are first-class) and sludge sump 12.
One perforation plate 9 is installed in the described reaction tank that bio-oxidation unit and ultrafiltration membrance filter unit be set, the top in the space that forms between one side of described perforation plate 9 and the pool wall of this reaction tank is set to can be used for the opening 6 that Powdered Activated Carbon adds, the space of this opening below has consisted of a current stabilization district 7, and at this opening part the pipeline that is connected with the top in described ozone reaction pond 5 is installed; Be filled with the support of described biologic packing material 10 at the opposite side of described perforation plate 9, aerating apparatus 11 be installed below described biologic packing material 10 and be provided with sludge sump 12, and in the sludge sump 11 shore pipe 21 is installed; Described aerating apparatus 11 is connected with an air compressor 15 by pipeline.
Described ultrafiltration membrance filter unit comprises aerating apparatus 11, sludge sump 12 and hyperfiltration membrane assembly 13.
Described hyperfiltration membrane assembly 13 is installed in described reaction tank, aerating apparatus 11 is installed below described hyperfiltration membrane assembly 13 and is provided with sludge sump 12, and in the sludge sump 12 shore pipe 21 is installed; Described aerating apparatus 11 is connected with an air compressor 15 by pipeline; Rising pipe 16 with vacuum meter 18 and rising pipe valve 20 is installed above described hyperfiltration membrane assembly 13, and described rising pipe 16 is connected with suction pump 14; And this rising pipe also is connected with a backwash tube 17 with backwash tube valve 19, and rising pipe is positioned on the rising pipe of described rising pipe valve 20 tops with backwash tube 17 places of being connected.
The zone that biologic packing material 10 and hyperfiltration membrane assembly 13 are installed in the described reaction tank is reaction zone 8.
The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 2 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 10 minutes; The soft-filler of the fine synthetic fibre material of hydroformylation is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone of the soft-filler that is filled with the fine synthetic fibre material of hydroformylation in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that hollow-fibre membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by aeration head simultaneously; When the bio-reaction zone of the soft-filler of current through being filled with the fine synthetic fibre material of hydroformylation, making the hydraulic detention time of water in described bio-oxidation unit area is 20 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described hollow-fibre membrane is housed is 4 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The hollow-fibre membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinyl chloride; The pore diameter range of ultra-filtration membrane is 0.20 μ m, and the membrane flux of ultra-filtration membrane is 60L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 80KPa.The hyperfiltration membrane assembly backwashing period is 2 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 10: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 5: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 72 hours.
Oxygen-consumption concentration is 5mg/L in the pending water, and ammonia nitrogen concentration is 0.8mg/L.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 1.5mg/L, and ammonia nitrogen concentration is 0.1mg/L, reaches " national drinking water sanitary standard (GB5749-2006) " requirement.
Embodiment 2
The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 4 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 20 minutes; The semi soft packing of the fine synthetic fibre material of hydroformylation is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone of the semi soft packing that is filled with the fine synthetic fibre material of hydroformylation in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that flat sheet membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by aeration head simultaneously; When the bio-reaction zone of the semi soft packing of current through being filled with the fine synthetic fibre material of hydroformylation, making the hydraulic detention time of water in described bio-oxidation unit area is 120 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described flat sheet membrane is housed is 10 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The flat sheet membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinylidene difluoride (PVDF); The pore diameter range of ultra-filtration membrane is 0.01 μ m, and the membrane flux of ultra-filtration membrane is 10L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 10kPa.The hyperfiltration membrane assembly backwashing period is 20 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 150: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 50: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 48 hours.
Oxygen-consumption concentration is 6mg/L in the pending water, and ammonia nitrogen concentration is 1.5mg/L.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 2.5mg/L, and ammonia nitrogen concentration is 0.2mg/L, reaches " national drinking water sanitary standard (GB5749-2006) " requirement.
Embodiment 3
The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 3 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 15 minutes; Activated carbon fiber Texture composition of materials filler is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone that is filled with activated carbon fiber Texture composition of materials filler in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that flat sheet membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by boring aeration pipe simultaneously; At current when being filled with the bio-reaction zone of activated carbon fiber Texture composition of materials filler, making the hydraulic detention time of water in described bio-oxidation unit area is 60 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described flat sheet membrane is housed is 6 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The flat sheet membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinylidene difluoride (PVDF); The pore diameter range of ultra-filtration membrane is 0.10 μ m, and the membrane flux of ultra-filtration membrane is 30L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 40kPa.The hyperfiltration membrane assembly backwashing period is 10 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 80: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 30: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 36 hours.
Oxygen-consumption concentration is 3mg/L in the pending water, and ammonia nitrogen concentration is 2mg/L.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 1.5mg/L, and ammonia nitrogen concentration is 0.4mg/L, reaches " national drinking water sanitary standard (GB5749-2006) " requirement.
Embodiment 4
The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 4 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 20 minutes; The fibrous bundle filler of Fiber Materials is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone of the fibrous bundle filler that is filled with Fiber Materials in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that flat sheet membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by boring aeration pipe simultaneously; When the bio-reaction zone of the fibrous bundle filler of current through being filled with Fiber Materials, making the hydraulic detention time of water in described bio-oxidation unit area is 100 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described flat sheet membrane is housed is 8 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The flat sheet membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinylidene difluoride (PVDF); The pore diameter range of ultra-filtration membrane is 0.15 μ m, and the membrane flux of ultra-filtration membrane is 20L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 60kPa.The hyperfiltration membrane assembly backwashing period is 10 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 20: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 15: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 24 hours.
Oxygen-consumption concentration is 3mg/L in the pending water, and ammonia nitrogen concentration is 0.5mg/L, and detects in the water and find to exist the pesticidal contamination such as DDT, alachlor.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 2mg/L, and ammonia nitrogen concentration is 0.2mg/L, and DDT and alachlor concentration all below detection limit, reach " national drinking water sanitary standard (GB5749-2006) " requirement.
The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 4 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 20 minutes; The semi soft packing of polypropylene material is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone of the semi soft packing that is filled with the polypropylene material in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that flat sheet membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by boring aeration pipe simultaneously; When the bio-reaction zone of the semi soft packing of current through being filled with the polypropylene material, making the hydraulic detention time of water in described bio-oxidation unit area is 100 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described flat sheet membrane is housed is 10 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The flat sheet membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinylidene difluoride (PVDF); The pore diameter range of ultra-filtration membrane is 0.15 μ m, and the membrane flux of ultra-filtration membrane is 30L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism.In addition, add Powdered Activated Carbon before the water inlet of bio-oxidation unit, the throwing weight range of Powdered Activated Carbon is 2mg/L, and realizes mixing and fully contacting with pollutent by the aeration effect of bio-oxidation unit.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 20kPa.The hyperfiltration membrane assembly backwashing period is 5 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 100: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 40: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 72 hours, controls the spoil disposal time so that the residence time of Powdered Activated Carbon in reactor is 4 days.
Oxygen-consumption concentration is 8mg/L in the pending water, and ammonia nitrogen concentration is 3mg/L.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 2mg/L, and ammonia nitrogen concentration is 0.2mg/L, reaches " national drinking water sanitary standard (GB5749-2006) " requirement.
Embodiment 6
The reactor that is used for drinking water deep purification such as embodiment 1 is set up in design.The deep-purifying method that utilizes above-mentioned reactor to carry out tap water is: pending water enters ozone contact tank 4 by water-in 1, the ozone that ozonizer 3 produces fully contacts and dissolves with pending water after disperseing through ozonation aerated 2 and forms solubilised state ozone, water is 4 minutes at the hydraulic detention time of ozone contact tank, enter together afterwards ozone reaction pond 5 ozone oxidizing reactions, and to make the hydraulic detention time of water in the ozone reaction pond be 20 minutes; The fine synthetic fibre Texture composition of materials of hydroformylation filler is fixed in the bio-oxidation unit, the water outlet in ozone reaction pond 5 enters the current stabilization district 7 of reaction tank, and the bio-reaction zone that is filled with the fine synthetic fibre Texture composition of materials of hydroformylation filler in the bio-oxidation unit area of behind perforation plate 9 water distribution uniformities, flowing through and the ultrafiltration membrance filter zone that flat sheet membrane has been installed, in water, provide pressurized air to carry out aeration by air compressor 15 and by the boring aeration tube aeration device simultaneously; At current when being filled with the bio-reaction zone of the fine synthetic fibre Texture composition of materials of hydroformylation filler, making the hydraulic detention time of water in described bio-oxidation unit area is 100 minutes, and the hydraulic detention time of water in the ultrafiltration membrance filter zone of described flat sheet membrane is housed is 10 minutes; Water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in hyperfiltration membrane assembly top.
The flat sheet membrane that adopts is immersion type membrane component, and the ultra-filtration membrane material is polyvinylidene difluoride (PVDF); The pore diameter range of ultra-filtration membrane is 0.15 μ m, and the membrane flux of ultra-filtration membrane is 30L/m
2H.
The deep-purifying method of above-mentioned tap water, be utilize main ozone oxidation unit with macromolecule in the water (general number-average molecular weight scope for＞30KDa) organism be converted into the intermediate molecular weight easily utilized by microorganism (general number-average molecular weight scope be 3KDa～30KDa) and small molecular weight (general number-average molecular weight scope is＜3KDa) organism, and water Pesticides pollutant Partial digestion destroyed.In addition, add Powdered Activated Carbon before the water inlet of bio-oxidation unit, the throwing weight range of Powdered Activated Carbon is 5mg/L, and realizes mixing and fully contacting with pollutent by the aeration effect of bio-oxidation unit.Suction function by suction pump is so that the water outlet of bio-oxidation unit enters the inboard from the film outside, and the described ultrafiltration membrance filter unit of finally flowing through, and the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is built in 60kPa.The hyperfiltration membrane assembly backwashing period is 5 minutes.Pump into pressurized air by air compressor in water, the gas-water ratio in the bio-oxidation unit area is 100: 1, and the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 50: 1.The mud of sedimentation is discharged by shore pipe in the sludge sump, and sludge discharging period is 36 hours, controls the spoil disposal time so that the residence time of Powdered Activated Carbon in reactor is 20 days.
Oxygen-consumption concentration is 4mg/L in the pending water, and ammonia nitrogen concentration is 1.5mg/L, and detects in the water and find to exist the pesticidal contamination such as DDT, alachlor.Adopt aforesaid method to process, water outlet oxygen-consumption concentration is 2mg/L, and ammonia nitrogen concentration is 0.2mg/L, and DDT and alachlor concentration all below detection limit, reach " national drinking water sanitary standard (GB5749-2006) " requirement.
Claims (10)
1. reactor that is used for drinking water deep purification, it comprises main ozone oxidation unit, bio-oxidation unit and ultrafiltration membrance filter unit; It is characterized in that: described bio-oxidation unit is between described main ozone oxidation unit and described ultrafiltration membrance filter unit; Described bio-oxidation unit and described ultrafiltration membrance filter unit are arranged in the same reaction tank;
The hyperfiltration membrane assembly that comprises in the described ultrafiltration membrance filter unit is immersion type membrane component; Described bio-oxidation includes biologic packing material in the unit.
2. the reactor for drinking water deep purification according to claim 1, it is characterized in that: described main ozone oxidation unit comprises ozone contact tank and ozone reaction pond two portions;
One dividing plate is separated into described ozone contact tank and described ozone reaction pond with a container, and leaves the space between the bottom of described dividing plate and described container; Top at described ozone contact tank is provided with water-in, and the bottom is equipped with ozonation aerated head, and described ozonation aerated head is connected by pipeline with ozonizer; The top in described ozone reaction pond is connected with described bio-oxidation unit by pipeline;
Described bio-oxidation unit comprises biologic packing material, aerating apparatus and sludge sump;
One perforation plate is installed in the described reaction tank that bio-oxidation unit and ultrafiltration membrance filter unit be set, the top in the space that forms between one side of described perforation plate and the pool wall of this reaction tank is set to opening, and at this opening part the pipeline that is connected with the top in described ozone reaction pond is installed; Be filled with the support of described biologic packing material at the opposite side of described perforation plate, aerating apparatus be installed below described biologic packing material and be provided with sludge sump; Described aerating apparatus is connected with air compressor by pipeline;
Described ultrafiltration membrance filter unit comprises aerating apparatus, sludge sump and hyperfiltration membrane assembly;
Described hyperfiltration membrane assembly is installed in described reaction tank, aerating apparatus is installed below described hyperfiltration membrane assembly and is provided with sludge sump; Described aerating apparatus is connected with air compressor by pipeline; Rising pipe is installed above described hyperfiltration membrane assembly, and described rising pipe is connected with suction pump.
3. the reactor for drinking water deep purification according to claim 2 is characterized in that: vacuum meter and rising pipe valve are installed on the described rising pipe;
Described rising pipe is connected with a backwash tube, and rising pipe is positioned on the rising pipe of described rising pipe valve top with the backwash tube place of being connected; The backwash tube valve is installed on the pipeline of described backwash tube.
4. one kind is utilized the described method of carrying out drinking water deep purification for the reactor of drinking water deep purification of claim 1～3 any one, it is characterized in that: pending water enters ozone contact tank by water-in, the ozone that ozonizer produces fully contacts with pending water after ozonation aerated head disperses and dissolves formation solubilised state ozone, enters together afterwards ozone reaction pond ozone oxidizing reaction; The water outlet in ozone reaction pond enters the current stabilization district in the reaction tank that bio-oxidation unit and ultrafiltration membrance filter unit are set, and the bio-reaction zone that is filled with biologic packing material in the bio-oxidation unit area of behind the perforation plate water distribution uniformity, flowing through and the ultrafiltration membrance filter unit area that hyperfiltration membrane assembly has been installed, at the bio-reaction zone of current through being filled with biologic packing material with when the ultrafiltration membrance filter unit area of hyperfiltration membrane assembly has been installed, simultaneously provide pressurized air to carry out aeration by aerating apparatus in water, water after treatment is by the suction outflow reactor of the suction pump that is connected with the rising pipe that is installed in the hyperfiltration membrane assembly top;
The space that forms between the pool wall of the reaction tank of one side of described perforation plate and placement bio-oxidation unit and ultrafiltration membrance filter unit has consisted of a current stabilization district.
5. root method claimed in claim 4, it is characterized in that: described pending water is 2～4 minutes at the hydraulic detention time of ozone contact tank, and the hydraulic detention time in the ozone reaction pond is 10～20 minutes.
6. root method claimed in claim 4 is characterized in that: the hydraulic detention time of the water outlet of described main ozone oxidation unit in the described biological respinse zone that is filled with biologic packing material is 20～120 minutes; The hydraulic detention time of described water in the ultrafiltration membrance filter unit area of described hyperfiltration membrane assembly is housed is 4～10 minutes.
7. root method claimed in claim 4 is characterized in that: the suction negative pressure control that described suction pump forms at described hyperfiltration membrane assembly is between 10kPa～80kPa.
8. root method claimed in claim 4, it is characterized in that: the gas-water ratio scope in the described bio-oxidation unit area is 10:1～150:1, the gas-water ratio scope in the described ultrafiltration membrance filter unit area is 5:1～50:1.
9. root method claimed in claim 4, it is characterized in that: described current stabilization has added Powdered Activated Carbon in the district, and the throwing weight range of described Powdered Activated Carbon is 2～20mg/L.
10. root claim 4 or 6 described methods is characterized in that: described biologic packing material is selected from a kind of in the fibrous bundle filler of the fine synthetic fibre of semi soft packing, hydroformylation of semi soft packing, polypropylene or polyethylene material of soft cellulose filler, the fine synthetic fibre material of hydroformylation of the fine synthetic fibre material of hydroformylation or activated carbon fiber Texture composition of materials filler, Fiber Materials;
Described hyperfiltration membrane assembly is immersion type membrane component, and the material of described ultra-filtration membrane is polyvinyl chloride or polyvinylidene difluoride (PVDF); The pore diameter range of described ultra-filtration membrane is between 0.01～0.20 μ m, and the membrane flux of ultra-filtration membrane is 10～60L/m
2H.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110185360 CN102351371B (en) | 2011-07-01 | 2011-07-01 | Reactor for deep purification of drinking water and deep purification method of drinking water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110185360 CN102351371B (en) | 2011-07-01 | 2011-07-01 | Reactor for deep purification of drinking water and deep purification method of drinking water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102351371A CN102351371A (en) | 2012-02-15 |
| CN102351371B true CN102351371B (en) | 2013-01-30 |
Family
ID=45575053
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110185360 Active CN102351371B (en) | 2011-07-01 | 2011-07-01 | Reactor for deep purification of drinking water and deep purification method of drinking water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102351371B (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102795745A (en) * | 2012-08-18 | 2012-11-28 | 江苏凌志市政工程设计研究院有限公司 | Integrated multi-cycle biological multiplication sewage treatment system |
| CN106587499A (en) * | 2016-12-09 | 2017-04-26 | 深圳市康源环境纳米科技有限公司 | System and method for treating black-odor water |
| CN107117742A (en) * | 2017-07-05 | 2017-09-01 | 合肥市片叶装饰工程有限公司 | River water treatment and purification device and purification method thereof |
| CN107673504A (en) * | 2017-09-25 | 2018-02-09 | 广东粤港供水有限公司 | A kind of method of ozone ceramic membrane activated carbon combination purification drinking water |
| CN107935161A (en) * | 2017-12-16 | 2018-04-20 | 傲自然成都生物科技有限公司 | A kind of bioelectrochemical system and purification method for purifying drinking water |
| CN108002660B (en) * | 2017-12-29 | 2024-03-19 | 清华大学 | Advanced wastewater treatment system and wastewater treatment method |
| CN107915311A (en) * | 2017-12-29 | 2018-04-17 | 清华大学 | A kind of efficient mass transfer catalytic ozonation fluidizes bed waste water treatment system |
| CN112723679B (en) * | 2020-12-30 | 2022-12-02 | 南京市给排水工程设计院有限公司 | System and method for synchronously removing odor substances and organic matters in water |
| CN113180171A (en) * | 2021-06-10 | 2021-07-30 | 黑龙江省科学院自然与生态研究所 | Preparation method of cranberry plant near-water beverage based on natural weak-alkaline water |
| CN113754197B (en) * | 2021-09-29 | 2022-11-11 | 哈尔滨工业大学 | Near-zero maintenance village and town drinking water integrated purification device and method for treating source water by applying same |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1396128A (en) * | 2002-08-30 | 2003-02-12 | 天津开发区建硕实业发展有限公司 | System and process for preparing superpur drinking water |
| CN1796314A (en) * | 2004-12-24 | 2006-07-05 | 中国科学院生态环境研究中心 | Method for processing urban sewage deeply |
| CN101289249A (en) * | 2008-06-06 | 2008-10-22 | 东华大学 | Combination treatment method for combined HMBR and device |
| CN101475287A (en) * | 2009-01-06 | 2009-07-08 | 环境保护部华南环境科学研究所 | Novel membrane-biological membrane reactor system and use thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10314554A (en) * | 1997-05-16 | 1998-12-02 | Hitachi Metals Ltd | Membrane separation activated sludge process |
-
2011
- 2011-07-01 CN CN 201110185360 patent/CN102351371B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1396128A (en) * | 2002-08-30 | 2003-02-12 | 天津开发区建硕实业发展有限公司 | System and process for preparing superpur drinking water |
| CN1796314A (en) * | 2004-12-24 | 2006-07-05 | 中国科学院生态环境研究中心 | Method for processing urban sewage deeply |
| CN101289249A (en) * | 2008-06-06 | 2008-10-22 | 东华大学 | Combination treatment method for combined HMBR and device |
| CN101475287A (en) * | 2009-01-06 | 2009-07-08 | 环境保护部华南环境科学研究所 | Novel membrane-biological membrane reactor system and use thereof |
Non-Patent Citations (1)
| Title |
|---|
| JP特开平10-314554A 1998.12.02 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102351371A (en) | 2012-02-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102351371B (en) | Reactor for deep purification of drinking water and deep purification method of drinking water | |
| CN102336493B (en) | Reaction device for deep treatment of drinking water and method for deep treatment of drinking water by water factory | |
| CN101891336B (en) | System and method for leachate treatment in sanitary landfill | |
| CN100562500C (en) | A kind of drinking water deeply purifying method and device | |
| CN101219846B (en) | Ultrafiltration membrane coagulation /adsorption/bioreactor integrating advanced water treatment method and device | |
| CN102417273B (en) | Dynamic membrane purifying reactor and method for removing ammonia nitrogen and organic matters from reclaimed water | |
| CN202322568U (en) | Deep treatment system of high-concentration percolate of integrated garbage treatment site | |
| CN103359894B (en) | Groundwater microbial denitrification system | |
| CN102503046A (en) | Advanced treatment system and method for high-concentration percolate in comprehensive garbage disposal plant | |
| CN101219842A (en) | Technique and equipment for recycling leachate of garbage | |
| CN102515432A (en) | Method for removing microcystin and odor substances in high-algae source water | |
| BR112020017168A2 (en) | SYSTEMS AND METHODS FOR TREATING LITTLE ENVIRONMENTAL IMPACT OF CONTAMINATED FLUID | |
| CN202152309U (en) | Complete set of modularized small-scale device for treatment of high-concentration organic wastewater | |
| KR20050012875A (en) | A water reclamation and reuse system with an equipment for removing TDS | |
| CN102351370B (en) | Integrated reactor and method for removing ammonia nitrogen and organic matter from drinking water | |
| CN101955301B (en) | Method and equipment for treating micropollution raw water based on biological bamboo charcoal contact oxidation method | |
| CN1524810A (en) | Method for cyclically utilizing middle water of public toilet sewage and specialized equipment therefor | |
| CN1931750B (en) | Petrochemical effluent treating and reusing process | |
| CN205061810U (en) | Garbage leachate treatment system | |
| CN210150897U (en) | Reclaimed water recycling device | |
| KR20050049437A (en) | A high pollution waste water disposal plant | |
| CN103588327B (en) | The method of heterogeneous catalytic ozonation-nanofiltration combination unit and water purifying and disinfection thereof | |
| JP4889269B2 (en) | Water purification equipment using microorganism-immobilized carrier | |
| CN102267782B (en) | Integrated reactor and method for removing ammonia nitrogen from drinking water | |
| CN104045206A (en) | UV (ultraviolet)/O3+BAF (biological aerated filter) advanced oxidation sewage treatment facility |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |