CN102351371B - Reactor for deep purification of drinking water and method for deep purification of drinking water - Google Patents

Abstract

The invention relates to a reactor for deep purification of drinking water and a method for deep purification of drinking water. The reactor includes a main ozone oxidation unit, a biological oxidation unit and an ultrafiltration membrane filtration unit; the biological oxidation unit is located in the main ozone oxidation unit Between the ultrafiltration membrane filtration unit, the biological oxidation unit and the ultrafiltration membrane filtration unit are placed in the same reaction pool. Ozone oxidation destroys refractory pollutants and converts large molecular weight organics into small and medium molecular weight organics. After the ozone reaction, the effluent enters the reaction pool in which the biological filler and the ultrafiltration membrane module are fixed. When the water source is seriously polluted, powdered activated carbon can also be added. Use activated carbon to adsorb medium molecular weight or volatile organic compounds; use microorganisms on the surface of biological fillers and powder activated carbon to remove ammonia nitrogen and small molecular weight organic compounds; use ultrafiltration to ensure microbial safety. The invention can be used for the deep purification of polluted water sources, and can also be applied to the deep treatment of urban sewage plants and regenerated water.

Description

Reactor for deep purification of drinking water and method for deep purification of drinking water

technical field

The invention belongs to the field of drinking water purification, in particular to a reactor for deep purification of drinking water capable of realizing separation of ozone oxidation, microbial degradation and ultrafiltration, and the depth of drinking water filtered by ozone oxidation, microbial degradation and ultrafiltration membrane method of purification.

Background technique

my country will implement the "Drinking Water Sanitation Standard (GB5749-2006)" in 2012. Compared with the "Drinking Water Sanitation Standard (GB5749-1985)", the new drinking water standard has greatly increased the indicators of synthetic organic substances such as pesticide chemicals and disinfection by-products, and set the limit of ammonia nitrogen concentration in water to 0.5mg/ Below L. In addition, some urban drinking water sources are polluted by natural organic matter, and the oxygen consumption is difficult to meet the standard; some urban drinking water sources have pollution problems such as algae and their metabolites, resulting in high smell and taste of the factory water, which affects the taste of drinking water .

Ozone/activated carbon and ozone/biologically activated carbon, as products used in typical drinking water advanced treatment processes, are widely used in water plant upgrades. The basic principle of ozone/activated carbon and ozone/biological activated carbon in the advanced treatment process of drinking water is to use ozone oxidation to destroy small molecular organic substances such as pesticides, and to convert organic substances with large molecular weight and difficult to be used by microorganisms into small molecular weight organic substances that are easily destroyed. Small organic molecules used by microorganisms. In the activated carbon (or biological activated carbon) unit, the adsorption of activated carbon (or biological activated carbon) and the degradation of microorganisms grown on the surface of activated carbon (or biological activated carbon) are used to remove organic matter and improve the taste of drinking water. The synergistic effect of ozone and activated carbon (or biological activated carbon) enables ozone/activated carbon and ozone/biological activated carbon to maintain good purification effects for a long time. However, the investment and operating costs of advanced treatment of drinking water using ozone/activated carbon and ozone/biologically activated carbon are high, which is unaffordable for small and medium-sized water plants in many underdeveloped areas. In addition, many water plants often have very limited available space when upgrading drinking water advanced treatment, and there is not enough land for a new ozone/activated carbon advanced treatment process structure.

Microfiltration and ultrafiltration technologies are essentially not advanced treatment technologies for drinking water; nanofiltration or reverse osmosis can greatly improve the removal capacity of organic matter, but there are problems such as high cost, complicated operation and management, and low water production rate. There are very few applications in drinking water plants. Therefore, the development of a deep purification method for drinking water with low investment and operating costs and simple operation and management is of great significance for solving the problem of water quality compliance in some economically backward areas of our country.

In recent years, ultrafiltration technology has been gradually developed and pushed to engineering applications, and with the large-scale application of ultrafiltration, investment and operating costs have been effectively reduced. However, ultrafiltration has a high ability to intercept and remove particulate pollutants such as bacteria, viruses, algae, and colloids in water, but has almost no ability to remove dissolved natural organic matter, artificially synthesized organic matter, and ammonia nitrogen. Many researchers have developed combined processes and technologies based on ultrafiltration. For example, the combination of coagulation and ultrafiltration, and the use of coagulation adsorption and sweeping to convert dissolved organic matter into particulate organic matter can effectively improve the removal capacity of ultrafiltration for dissolved macromolecular organic matter. However, this method has limited ability to improve the removal of medium or small molecular weight organic matter, especially for ammonia nitrogen. As another example, combining powdered activated carbon with ultrafiltration, and ensuring the residence time of powdered activated carbon in the reactor, using powdered activated carbon to adsorb pollutants and biodegradation of the microbial film formed on the surface of powdered activated carbon under long-term operating conditions , Effectively improve the removal capacity of organic matter, ammonia nitrogen and other pollutants in water. However, powdered activated carbon particles are easy to gather on the surface of the membrane, and may cause physical damage to the membrane surface under the condition of membrane negative pressure suction, affecting the life of the membrane filament; once the membrane filament in the membrane module is broken, the powdered activated carbon with microorganisms on the surface is easy to Penetrating the ultrafiltration barrier and may cause water supply accidents; in addition, how to ensure the sludge age of powdered activated carbon during the sludge discharge process is also difficult to effectively control in operation management. It has also been proposed to place UF after the ozone/BAC unit to avoid loss or penetration of activated carbon debris and microorganisms into the pipe network. However, this scheme further increases the process complexity and head loss, and the operation and management of the water plant are more complicated. Therefore, how to develop an advanced treatment process that is efficient, economical, stable and easy to operate is a key problem that needs to be solved urgently for my country to achieve water plant compliance.

Contents of the invention

One of the objectives of the present invention is to provide a reactor for advanced purification of drinking water capable of realizing ozone oxidation, microbial degradation and ultrafiltration separation.

The second object of the present invention is to provide a method for advanced purification of drinking water with high performance, economical feasibility, stable operation, simple maintenance and easy implementation.

The present invention aims at the problems existing in the above prior art, and proposes that after the main ozone oxidation unit, a biological oxidation unit and an ultrafiltration membrane filtration unit using biological fillers to form membranes are arranged. The basic principle is that in the main ozone oxidation unit, ozone contact oxidation is used to oxidize and destroy trace organic pollutants and odorous substances that are difficult to degrade in water, and degrade large molecular weight (generally, the range of number average molecular weight is > 30KDa) organic matter in water Converted into small molecular organic matter that is easily utilized by microorganisms; in the biological oxidation unit, use biological fillers to fix the microbial hanging film on the surface of the biological fillers to form a microbial film, increase the amount of microorganisms in the reactor, and use microbial degradation to convert medium molecular weight (generally The number average molecular weight range is 3KDa ~ 30KDa), small molecular weight (generally the number average molecular weight range is <3KDa) organic matter is assimilated and removed, and ammonia nitrogen is removed through microbial nitrification; in the ultrafiltration membrane filtration unit, the interception of the ultrafiltration membrane is used Filtration intercepts pollutants such as microorganisms, shed microbial films, and colloidal particles in the water. In addition, for raw water with serious pollution, powdered activated carbon can also be added to the front of the biological oxidation unit, and the sufficient residence time of powdered activated carbon can be ensured, so as to further increase the biomass and microbial degradation ability, and improve the removal effect of pollutants in water. In addition, most of the powdered activated carbon is intercepted and intercepted in the biological filler area, which greatly reduces the amount of powdered activated carbon accumulated on the surface of the ultrafiltration membrane and avoids physical damage to the surface of the ultrafiltration membrane. The invention can be used for deep purification of drinking water from polluted water sources, and can also be applied to deep treatment of urban sewage plants and deep purification of regenerated water.

The reactor for deep purification of drinking water of the present invention comprises a main ozone oxidation unit, a biological oxidation unit and an ultrafiltration membrane filtration unit; wherein, the biological oxidation unit is located between the main ozone oxidation unit and the ultrafiltration Between the membrane filtration units; the biological oxidation unit and the ultrafiltration membrane filtration unit are arranged in the same reaction pool. As shown in Figure 1.

The main ozone oxidation unit includes two parts: an ozone contact pool and an ozone reaction pool.

A partition divides a container into the ozone contact tank and the ozone reaction tank, and there is a gap between the partition and the bottom of the container; at the top of the ozone contact tank A water inlet is provided, and an ozone aeration head is installed on the lower part, and the ozone aeration head is connected to the ozone generator through a pipeline; the upper part of the ozone reaction tank is connected to the biological oxidation unit through a pipeline .

The biological oxidation unit includes biological filler, aeration device and sludge tank.

A perforated plate is installed in the reaction tank of the described biological oxidation unit and ultrafiltration membrane filtration unit, and the top of the space formed between one side of the perforated plate and the wall of the reaction tank is set as an opening (available powdered activated carbon), and a pipeline connected to the upper part of the ozone reaction tank is installed at the opening; a support filled with the biological filler is installed on the other side of the perforated plate, An aeration device and a sludge tank are installed below the biological filler; the aeration device is connected with an air compressor through a pipeline.

The ultrafiltration membrane filtration unit includes an aeration device, a sludge tank and an ultrafiltration membrane module.

The ultrafiltration membrane assembly is installed in the reaction tank, and an aeration device and a sludge tank are installed below the ultrafiltration membrane assembly; the aeration device is connected with air through a pipeline. The compressors are connected; a water outlet pipe is installed above the ultrafiltration membrane module, and the water outlet pipe is connected with a suction pump.

A vacuum gauge and a water outlet valve are installed on the outlet pipe.

The outlet pipe is connected to a backwash pipe, and preferably, the place where the outlet pipe is connected to the backwash pipe is located on the outlet pipe above the valve of the outlet pipe.

A backwashing pipe valve is installed on the pipeline of the backwashing pipe.

A sludge discharge pipe is installed in the sludge tank.

The space formed between one side of the perforated plate and the pool wall of the reaction pool where the biological oxidation unit and the ultrafiltration membrane filtration unit are arranged constitutes a steady flow area.

The area where biological fillers and ultrafiltration membrane modules are installed in the reaction pool is the reaction area.

The pool type design of the ozone contact pool and the ozone reaction pool is the same as the common ozone contact pool and ozone reaction pool. The purpose of the ozone contact tank is to fully dissolve the ozone gas in the water, and the purpose of the ozone reaction tank is to exert the ozone oxidation effect to degrade pollutants or oxidize large molecular weight organic matter into small molecular weight organic matter that is easily utilized by microorganisms. The water to be treated first enters the ozone contact tank, and then enters the ozone reaction tank. The hydraulic retention time of the ozone contact tank is 2 to 4 minutes, and the hydraulic retention time of the ozone reaction tank is 10 to 20 minutes.

The biological filler in the biological oxidation unit is fixed in the reaction tank, and the degradation and removal of pollutants can be realized through the biological oxidation of the microorganisms fixed on the surface of the biological filler by hanging film. The biological filler can be soft fiber filler made of aldehyde chemical fiber, semi-soft filler made of aldehyde chemical fiber, semi-soft filler made of polypropylene or polyethylene, combined filler made of aldehyde chemical fiber or activated carbon fiber ( It has the advantages of both soft and semi-soft fillers), fiber bundle fillers made of fiber materials, etc. The hydraulic retention time of the effluent from the main ozone oxidation unit in the biological reaction zone filled with biological filler is preferably 20-120 minutes.

Powdered activated carbon can also be added to the biological oxidation unit, and the pollutant removal effect can be further improved through the adsorption of powdered activated carbon and microbial degradation on the surface of powdered activated carbon. The dosage of powdered activated carbon ranges from 2 to 20 mg/L. Powdered activated carbon is added before the water intake of the biological oxidation unit, and is mixed and fully contacted with pollutants through the aeration of the biological oxidation unit. Afterwards, the effluent from the main ozone oxidation unit evenly enters the biological oxidation unit filled with biological fillers. Medium-molecular-weight organics and small-molecular-weight volatile organics in the effluent of the main ozonation unit are removed by the adsorption of powdered activated carbon; ammonia nitrogen in the effluent of the main ozonation unit is transformed under the nitrification of microorganisms on the surface of the biological filler and the surface of the powdered activated carbon for nitrate.

The ultrafiltration membrane module is a submerged membrane module, the ultrafiltration membrane may be a hollow fiber membrane or a flat membrane, and the material of the ultrafiltration membrane may be polyvinyl chloride or polyvinylidene fluoride. The pore diameter of the ultrafiltration membrane ranges from 0.01 to 0.20 μm, and the membrane flux of the ultrafiltration membrane is 10 to 60 L/m ² ·h. The hydraulic retention time of water in the area of the ultrafiltration membrane filtration unit equipped with the ultrafiltration membrane module is 4 to 10 minutes. The effluent from the biological oxidation unit passes through the ultrafiltration membrane filtration unit, and the impurity particles such as colloids, bacteria, viruses, and exfoliated microbial films in the water are removed under the action of membrane separation.

The flow of the effluent from the biological oxidation unit through the ultrafiltration membrane filtration unit is accomplished by the suction of the suction pump. A water outlet pipe is installed above the ultrafiltration membrane module, and the water outlet pipe is connected with a suction pump. The water in the reactor enters from the outside of the membrane to the inside under the negative pressure formed by the suction pump, and finally flows out through the outlet pipe. The suction negative pressure formed by the suction pump on the ultrafiltration membrane module is controlled between 10kPa and 80kPa.

In order to ensure the membrane flux, during the operation of deep purification of drinking water, it is necessary to periodically backwash the ultrafiltration membrane components in the ultrafiltration membrane filtration unit. The backwash water is the effluent filtered by the ultrafiltration membrane module. Under the action of the backwash pump, the backwash water flows out from the inside of the ultrafiltration membrane to the outside, and the pollutants attached to the membrane surface can be detached from the membrane surface. The backwash cycle of the ultrafiltration membrane module is 2 to 20 minutes. When the backwash pump is turned on, the backwash inlet valve is opened, the suction pump stops and the outlet pipe valve is closed; after the backwash stops, the backwash inlet valve is closed, and the suction pump starts to run and the outlet valve is opened.

An aeration device is arranged under the bracket filled with the biological filler and the ultrafiltration membrane module, and the compressed air is pumped into the water through the air compressor respectively, thereby providing dissolved oxygen in the water and providing hydraulic effect Mix and stir and shear and scrub the attachments on the surface of the membrane filaments. Compressed air can be pumped into the reactor continuously or intermittently. The air-water ratio range in the biological oxidation unit area is 10:1-150:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 5:1-50:1. The compressed air in the biooxidation unit area and the ultrafiltration membrane filtration unit area can be provided by the same air compressor, or by different air compressors. The aeration device may be a perforated aeration tube or an aeration head and the like.

A sludge tank is arranged under the support filled with the biological filler and the ultrafiltration membrane module. Impurities such as dense particles, exfoliated microbial film, and powdered activated carbon in the water enter the sludge tank under the action of gravity, and the sludge in the sludge tank is discharged through the sludge discharge pipe. The sludge discharge period can be 12-72 hours; when powdered activated carbon is added, the residence time of powdered activated carbon in the reactor should be guaranteed to be 4-20 days.

The deep purification method of drinking water of the present invention: the water to be treated enters the ozone contact pool from the water inlet, the ozone generated by the ozone generator is dispersed by the ozone aeration head, fully contacts and dissolves with the water to be treated to form dissolved ozone, and then enters together The ozone oxidation reaction occurs in the ozone reaction tank; the effluent from the ozone reaction tank enters the steady flow area in the reaction tank where the biological oxidation unit and the ultrafiltration membrane filtration unit are installed, and flows through the filling area of the biological oxidation unit area after the water is evenly distributed through the perforated plate. The bioreaction area with biological filler and the ultrafiltration membrane filtration unit area with ultrafiltration membrane modules installed, when water flows through the bioreaction area filled with biological fillers and the ultrafiltration membrane filtration unit area with ultrafiltration membrane modules installed, at the same time Compressed air is provided to the water by the aeration device for aeration, and the treated water flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The space formed between one side of the perforated plate and the pool wall of the reaction pool where the biological oxidation unit and the ultrafiltration membrane filtration unit are arranged constitutes a steady flow area.

The hydraulic retention time of the water to be treated in the ozone contact tank is 2 to 4 minutes, and the hydraulic retention time in the ozone reaction tank is 10 to 20 minutes.

The hydraulic retention time of the effluent of the main ozonation unit in the biological reaction zone filled with biological fillers is preferably 20 to 120 minutes (the volume occupied by the biological fillers can be designed to realize the hydraulic retention time).

The hydraulic retention time of the water in the ultrafiltration membrane filtration unit area equipped with the ultrafiltration membrane assembly is 4 to 10 minutes (the volume occupied by the ultrafiltration membrane assembly can be designed to realize the hydraulic retention time).

The suction negative pressure formed by the suction pump on the ultrafiltration membrane module is controlled between 10kPa and 80kPa.

The air-water ratio range in the biological oxidation unit area is 10:1-150:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 5:1-50:1.

When the ultrafiltration membrane module is backwashed, the backwashing time is 2 to 20 minutes.

The function of the steady flow zone is to eliminate the residual pressure brought by the water inlet, ensure that the water flow can evenly enter the reaction zone 8, and avoid short-circuit flow and dead zone. The function of the reaction zone 8 is to realize functions such as microbial oxidation and ultrafiltration separation. If necessary, powdered activated carbon can be added to opening 6 (powdered activated carbon dosing point). The dosage range of the powdered activated carbon is 2-20 mg/L.

The present invention has the following advantages:

1. Combining the main ozone oxidation with microbial degradation, ultrafiltration membrane filtration, etc., through the synergy between different processes, the removal of ammonia nitrogen, organic matter and other pollutants in drinking water is achieved, and the ultrafiltration membrane is used to fully ensure the microbial safety.

2. In the case of serious water pollution, the adsorption of powdered activated carbon and the degradation of surface microorganisms can be used to further improve the removal capacity of organic matter and ammonia nitrogen, and the dosage of powdered activated carbon can be adjusted according to the pollution of water sources, which is very convenient for application.

3. Small footprint, small head loss, easy to apply to the renovation of old water plants and the construction of new water plants.

4. Low operating cost and convenient operation and management.

Description of drawings

Figure 1. Schematic diagram of a reactor for drinking water purification according to the present invention.

reference sign

1. Water inlet 2. Ozone aeration head 3. Ozone generator

4. Ozone contact pool 5. Ozone reaction pool 6. Opening

7. Steady flow zone 8. Reaction zone 9. Perforated plate

10. Biological filler 11. Aeration device 12. Sludge tank

13. Ultrafiltration membrane module 14. Suction pump 15. Air compressor

16. Outlet pipe 17. Backwash pipe 18. Vacuum gauge

19. Backwash pipe valve 20. Outlet pipe valve 21. Mud discharge pipe

Detailed ways

Example 1

Design and set up the reactor for the deep purification of drinking water as shown in Figure 1; Wherein, a biological oxidation unit is positioned between a main ozone oxidation unit and an ultrafiltration membrane filtration unit; Described biological oxidation unit and described The ultrafiltration membrane filtration unit is set in the same reaction pool.

The main ozone oxidation unit includes two parts: an ozone contact tank 4 and an ozone reaction tank 5 .

A separator separates a container into the ozone contact tank 4 and the ozone reaction tank 5, and there is a gap between the separator and the bottom of the container; in the ozone contact tank The top of 4 is provided with water inlet 1, and the bottom is equipped with ozone aeration head 2, and described ozone aeration head is connected with ozone generator 3 by pipeline; The biological oxidation unit mentioned above is connected.

The biological oxidation unit includes biological filler 10 , aeration device 11 (perforated aeration pipe or aeration head, etc.) and sludge tank 12 .

A perforated plate 9 is installed in the reaction tank of the described biological oxidation unit and ultrafiltration membrane filtration unit, and the top of the space formed between one side of the perforated plate 9 and the pool wall of the reaction tank is arranged as available In the opening 6 where the powdered activated carbon is added, the space below the opening forms a steady flow zone 7, and a pipeline communicating with the upper part of the ozone reaction tank 5 is installed at the opening; The other side of the plate 9 is installed with a support filled with the biological filler 10, an aeration device 11 and a sludge tank 12 are installed below the biological filler 10, and a row is installed in the sludge tank 11. Mud pipe 21; the aeration device 11 is connected with an air compressor 15 through a pipeline.

The ultrafiltration membrane filtration unit includes an aeration device 11 , a sludge tank 12 and an ultrafiltration membrane module 13 .

The ultrafiltration membrane assembly 13 is installed in the reaction tank, the aeration device 11 and the sludge tank 12 are installed below the ultrafiltration membrane assembly 13, and the sludge tank 12 is installed There is a mud discharge pipe 21; the aeration device 11 is connected with an air compressor 15 through a pipeline; an outlet pipe with a vacuum gauge 18 and an outlet pipe valve 20 is installed above the ultrafiltration membrane module 13 16. The outlet pipe 16 is connected to the suction pump 14; and the outlet pipe is also connected to a backwash pipe 17 with a backwash pipe valve 19, and the place where the outlet pipe communicates with the backwash pipe 17 is located at the On the outlet pipe above the outlet pipe valve 20 above.

The area where the biological filler 10 and the ultrafiltration membrane module 13 are installed in the reaction pool is the reaction area 8 .

The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, the hydraulic retention time of water in the ozone contact tank is 2 minutes, and then enters the ozone reaction tank 5 together to generate ozone oxidation reaction, and makes the hydraulic retention time of water in the ozone reaction tank be 10 minutes; The soft filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow zone 7 of the reaction tank, and the water is evenly distributed through the perforated plate 9, and then flows through the soft material filled with aldehyde fiber in the area of the biological oxidation unit. The bioreaction area of permanent filler and the ultrafiltration membrane filtration area installed with hollow fiber membranes, at the same time, the air compressor 15 provides compressed air to the water through the aeration head for aeration; When the bioreaction zone of permanent filler is used, the hydraulic retention time of water in the described biological oxidation unit area is 20 minutes, and the hydraulic retention time of water in the ultrafiltration membrane filtration area equipped with the described hollow fiber membrane is 4 minutes. minutes; the treated water flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The hollow fiber membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinyl chloride; the pore size range of the ultrafiltration membrane is 0.20 μm, and the membrane flux of the ultrafiltration membrane is 60 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 80KPa. The backwash cycle of the ultrafiltration membrane module is 2 minutes. Compressed air is pumped into the water through an air compressor, the air-water ratio in the biological oxidation unit area is 10:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 5:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge period is 72 hours.

The concentration of oxygen consumption in the water to be treated is 5 mg/L, and the concentration of ammonia nitrogen is 0.8 mg/L. Using the above method for treatment, the concentration of oxygen consumption in the effluent is 1.5 mg/L, and the concentration of ammonia nitrogen is 0.1 mg/L, meeting the requirements of the National Sanitary Standard for Drinking Water (GB5749-2006).

Example 2

Design and establish the reactor for the deep purification of drinking water as in Example 1. The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, the hydraulic retention time of water in the ozone contact tank is 4 minutes, and then enters the ozone reaction tank 5 together to generate ozone oxidation reaction, and makes the hydraulic retention time of water in the ozone reaction tank be 20 minutes; The semi-soft filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow area 7 of the reaction tank, and the water is uniformly distributed through the perforated plate 9 and then flows through the carbon fiber filled with aldehyde fiber in the area of the biological oxidation unit. The biological reaction area of the semi-soft filler and the ultrafiltration membrane filtration area installed with flat membranes are simultaneously provided with compressed air by the air compressor 15 and through the aeration head to the water for aeration; During the bioreaction zone of semi-soft packing, make the hydraulic retention time of water in the described biological oxidation unit area be 120 minutes, the hydraulic retention time of water in the ultrafiltration membrane filtration area that described flat membrane is housed is 10 minutes; the treated water flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The flat membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinylidene fluoride; the pore size range of the ultrafiltration membrane is 0.01 μm, and the membrane flux of the ultrafiltration membrane is 10 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 10kPa. The backwash cycle of the ultrafiltration membrane module is 20 minutes. Compressed air is pumped into the water through an air compressor, the air-water ratio in the biological oxidation unit area is 150:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 50:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge period is 48 hours.

The concentration of oxygen consumption in the water to be treated is 6mg/L, and the concentration of ammonia nitrogen is 1.5mg/L. Using the above method for treatment, the concentration of oxygen consumption in the effluent is 2.5 mg/L, and the concentration of ammonia nitrogen is 0.2 mg/L, meeting the requirements of the National Sanitary Standard for Drinking Water (GB5749-2006).

Example 3

Design and establish the reactor for the deep purification of drinking water as in Example 1. Design and establish the reactor for the deep purification of drinking water as in Example 1. The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, water has a hydraulic retention time of 3 minutes in the ozone contact tank, and then enters the ozone reaction tank 5 to generate an ozone oxidation reaction, and makes the water hydraulic retention time in the ozone reaction tank 15 minutes; the combination of activated carbon fiber material The filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow zone 7 of the reaction tank, and after being evenly distributed through the perforated plate 9, it flows through the biological oxidation unit filled with the combined filler made of activated carbon fiber material. The reaction area and the ultrafiltration membrane filtration area installed with flat membranes are simultaneously provided with compressed air by the air compressor 15 and through the perforated aeration pipe to the water for aeration; , the hydraulic retention time of water in the bio-oxidation unit area is 60 minutes, and the hydraulic retention time of water in the ultrafiltration membrane filtration area of the flat membrane is 6 minutes; the treated water The suction flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The flat membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinylidene fluoride; the pore size range of the ultrafiltration membrane is 0.10 μm, and the membrane flux of the ultrafiltration membrane is 30 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 40kPa. The backwash cycle of the ultrafiltration membrane module is 10 minutes. Compressed air is pumped into the water through an air compressor, the air-water ratio in the biological oxidation unit area is 80:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 30:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge period is 36 hours.

The concentration of oxygen consumption in the water to be treated is 3mg/L, and the concentration of ammonia nitrogen is 2mg/L. Using the above method for treatment, the concentration of oxygen consumption in the effluent is 1.5mg/L, and the concentration of ammonia nitrogen is 0.4mg/L, meeting the requirements of the "National Hygienic Standard for Drinking Water (GB5749-2006)".

Example 4

Design and establish the reactor for the deep purification of drinking water as in Example 1. The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, the water's hydraulic retention time in the ozone contact tank is 4 minutes, and then enters the ozone reaction tank 5 together to generate an ozone oxidation reaction, and makes the water's hydraulic retention time in the ozone reaction tank be 20 minutes; the fiber bundle of fiber material The filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow zone 7 of the reaction tank, and the water is uniformly distributed through the perforated plate 9, and then flows through the biological material filled with fiber bundle filler in the biological oxidation unit area. The reaction area and the ultrafiltration membrane filtration area installed with flat membranes are simultaneously provided with compressed air by the air compressor 15 and through the perforated aeration pipe to the water for aeration; when water flows through the biological reaction area filled with fiber bundle fillers When, the hydraulic retention time of water in the described biological oxidation unit area is 100 minutes, the hydraulic retention time of water in the ultrafiltration membrane filtration area of described flat membrane is housed is 8 minutes; The suction flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The flat membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinylidene fluoride; the pore size range of the ultrafiltration membrane is 0.15 μm, and the membrane flux of the ultrafiltration membrane is 20 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 60kPa. The backwash cycle of the ultrafiltration membrane module is 10 minutes. Compressed air is pumped into the water through an air compressor, the air-water ratio in the biological oxidation unit area is 20:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 15:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge period is 24 hours.

The concentration of oxygen consumption in the water to be treated was 3mg/L, and the concentration of ammonia nitrogen was 0.5mg/L, and the detection of water found that there were pesticide pollution such as DDT and alachlor. Using the above method for treatment, the effluent oxygen consumption concentration is 2mg/L, the ammonia nitrogen concentration is 0.2mg/L, and the DDT and alachlor concentrations are all below the detection limit, reaching the "National Drinking Water Sanitation Standard (GB5749-2006) "Require.

Example 5

Design and establish the reactor for the deep purification of drinking water as in Example 1. The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, the hydraulic retention time of water in the ozone contact tank is 4 minutes, and then enters the ozone reaction tank 5 together to generate ozone oxidation reaction, and makes the hydraulic retention time of water in the ozone reaction tank be 20 minutes; The soft filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow zone 7 of the reaction tank, and the water is uniformly distributed through the perforated plate 9 and then flows through the semi-soft plastic filled with polypropylene material in the biological oxidation unit area. The bioreaction area with permanent packing and the ultrafiltration membrane filtration area with flat membrane are installed. At the same time, the air compressor 15 provides compressed air to the water through the perforated aeration pipe for aeration; when the water flows through the semi-soft filter filled with polypropylene material When the bioreaction zone of permanent filler is used, the hydraulic retention time of water in the described biological oxidation unit area is 100 minutes, and the hydraulic retention time of water in the ultrafiltration membrane filtration area equipped with the flat membrane is 10 minutes ; The treated water flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The flat membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinylidene fluoride; the pore size range of the ultrafiltration membrane is 0.15 μm, and the membrane flux of the ultrafiltration membrane is 30 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter. In addition, powdered activated carbon is added before the water intake of the biological oxidation unit. The dosage range of powdered activated carbon is 2mg/L, and the aeration of the biological oxidation unit realizes mixing and full contact with pollutants. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 20kPa. The backwash cycle of the ultrafiltration membrane module is 5 minutes. Compressed air is pumped into the water through an air compressor, the air-water ratio in the biological oxidation unit area is 100:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 40:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge period is 72 hours. The sludge discharge time is controlled so that the residence time of the powdered activated carbon in the reactor is 4 days.

The concentration of oxygen consumption in the water to be treated is 8mg/L, and the concentration of ammonia nitrogen is 3mg/L. Using the above method for treatment, the concentration of oxygen consumption in the effluent is 2 mg/L, and the concentration of ammonia nitrogen is 0.2 mg/L, meeting the requirements of the National Hygienic Standard for Drinking Water (GB5749-2006).

Example 6

Design and establish the reactor for the deep purification of drinking water as in Example 1. The method of deep purification of drinking water using the above reactor is as follows: the water to be treated enters the ozone contact tank 4 from the water inlet 1, and the ozone generated by the ozone generator 3 is dispersed by the ozone aeration head 2 and then fully contacted with the water to be treated and dissolved to form Dissolved ozone, the hydraulic retention time of water in the ozone contact tank is 4 minutes, and then enters the ozone reaction tank 5 together to generate ozone oxidation reaction, and makes the hydraulic retention time of water in the ozone reaction tank be 20 minutes; The combined filler is fixed in the biological oxidation unit, and the effluent from the ozone reaction tank 5 enters the steady flow area 7 of the reaction tank, and the water is uniformly distributed through the perforated plate 9, and then flows through the combined filler filled with aldehyde fiber in the area of the biological oxidation unit. The biological reaction area and the ultrafiltration membrane filtration area installed with flat membranes are simultaneously provided with compressed air by the air compressor 15 and through the perforated aeration tube aeration device to the water for aeration; When combining the biological reaction zone of filler, make the hydraulic retention time of water in the described biological oxidation unit zone be 100 minutes, the hydraulic retention time of water in the ultrafiltration membrane filtration zone that described flat membrane is housed is 10 minutes ; The treated water flows out of the reactor through the suction of the suction pump connected to the outlet pipe installed above the ultrafiltration membrane module.

The flat membrane used is a submerged membrane module, and the material of the ultrafiltration membrane is polyvinylidene fluoride; the pore size range of the ultrafiltration membrane is 0.15 μm, and the membrane flux of the ultrafiltration membrane is 30 L/m ² ·h.

The above deep purification method for drinking water is to use the main ozone oxidation unit to convert the organic matter with large molecular weight (general number average molecular weight range > 30KDa) in the water into medium molecular weight (general number average molecular weight range is 3KDa ~ 30KDa) which is easily utilized by microorganisms and Small molecular weight (generally the number average molecular weight range is <3KDa) organic matter, and partially degrades and destroys pesticide pollutants in water. In addition, powdered activated carbon is added before the water intake of the biological oxidation unit. The dosage range of powdered activated carbon is 5mg/L, and the mixing and full contact with pollutants are realized through the aeration of the biological oxidation unit. Through the suction of the suction pump, the effluent of the biological oxidation unit enters from the outside of the membrane to the inside, and finally flows through the ultrafiltration membrane filtration unit. The suction pump is formed on the ultrafiltration membrane module. Suction negative pressure is controlled at 60kPa. The backwash cycle of the ultrafiltration membrane module is 5 minutes. Compressed air is pumped into the water by an air compressor, the air-water ratio in the biological oxidation unit area is 100:1, and the air-water ratio range in the ultrafiltration membrane filtration unit area is 50:1. The sludge settled in the sludge tank is discharged through the sludge discharge pipe, and the sludge discharge cycle is 36 hours. The sludge discharge time is controlled so that the residence time of the powdered activated carbon in the reactor is 20 days.

The concentration of oxygen consumption in the water to be treated was 4mg/L, and the concentration of ammonia nitrogen was 1.5mg/L, and the detection of water found that there were pesticide pollution such as DDT and alachlor. Using the above method for treatment, the effluent oxygen consumption concentration is 2mg/L, the ammonia nitrogen concentration is 0.2mg/L, and the DDT and alachlor concentrations are all below the detection limit, reaching the "National Drinking Water Sanitation Standard (GB5749-2006) "Require.

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.

Images