CN212610103U - Duplex oxidation ditch method integrated sewage treatment device - Google Patents
Duplex oxidation ditch method integrated sewage treatment device Download PDFInfo
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- CN212610103U CN212610103U CN202020388695.6U CN202020388695U CN212610103U CN 212610103 U CN212610103 U CN 212610103U CN 202020388695 U CN202020388695 U CN 202020388695U CN 212610103 U CN212610103 U CN 212610103U
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Abstract
The patent provides a duplex oxidation ditch method integration sewage treatment ware, it includes process units such as anaerobism pond, duplex oxidation ditch, two heavy ponds. The reaction tank of the duplex oxidation ditch is divided into an upper layer reaction tank and a lower layer reaction tank, each layer reaction tank is connected end to end through a pipeline, and the circulating pump supplies sewage of the bottom layer reaction tank to the top layer reaction tank through a circulating pipeline, so that the closed endless circulation canal-shaped arrangement taking the reaction tank as a main body is formed, and oxygenation and plug flow are realized. Sludge at the bottom of the secondary sedimentation tank flows automatically in a siphon manner and flows back to the anaerobic tank without power; the circulating pump is automatically started and stopped according to the water level of the anaerobic tank. And the filter tank is siphoned for automatic backwashing, and backwashing water is discharged into the anaerobic tank or the low-level reaction tank, so that the zero-emission zero-power filter tank is formed. According to this patent, can greatly reduced the reaction tank length of traditional oxidation ditch technology, can develop the production and take zero power, zero release filtering ponds, can take out fertile automatically, can highly integrate in a barrel with whole equipment and process unit.
Description
The technical field is as follows:
a duplex oxidation ditch method integrated sewage processor belongs to the field of water treatment.
Background art:
according to the definition of the national environmental protection standard HJ-578-2010, the oxidation ditch activated sludge method is an activated sludge method sewage treatment method, called oxidation ditch method or OD method for short, in which a reaction tank is arranged in a closed endless circulating flow channel shape and oxygenation and plug flow are completed in the reaction tank. Different from the AAO method which clearly distinguishes an anoxic zone and an aerobic zone, the oxidation ditch method concentrates the aerobic and anoxic (even anaerobic and sedimentation) in the reaction tank to finish the process. There are also many variations of the oxidation ditch method.
The oxidation ditch methods which are put into production at present are basically large and medium sewage treatment projects, and the large and medium sewage treatment projects are mainly characterized in that ditches connected end to end are poured by concrete; an integrated sewage treatment device without an oxidation ditch method. The general oxidation ditch and the secondary sedimentation tank can reach the second-level B standard of urban domestic sewage discharge; if the requirement reaches the effluent first grade A, advanced treatment processes such as MBR (membrane bioreactor) membrane and the like are required to be added.
The oxidation ditch method has many advantages, such as good effluent quality, high nitrogen and phosphorus removal efficiency, simple structure, equipment and control, stable effluent, strong impact resistance and the like. These advantages make it very suitable for household and small domestic sewage, and the water quantity and quality of the sewage change greatly, and the equipment and control are simple. However, the reaction tanks of the traditional oxidation ditch method are all arranged on a plane elevation, and have the defects of large floor area, long total hydraulic retention time, fear of sewage with large oil content and the like. In particular, in order to prevent sedimentation, it is required that the flow velocity of the wastewater in the reaction tank reaches 0.3 m/s, and it is also required that aerobic and anoxic sections should be present in the entire reaction tank. Since the time for reducing the dissolved oxygen from the aerobic section of > 2mg/L to the oxygen-deficient section of 0.2-0.5 mg/L is at least several minutes to more than ten minutes, the reaction tank of the oxidation ditch is required to be very long. If the time for one circulation of the reaction cells of the oxidation ditch is 10 minutes, the required length of the reaction cells should be at least 10 x 60 x 0.3 ═ 180 m! These significantly limit the range of use of the oxidation ditch, making it very difficult to implement and to miniaturize.
The utility model has the following contents:
the patent of the utility model provides a leap layer formula oxidation ditch method integration sewage treatment ware, it includes the anaerobism pond, leap layer formula oxidation ditch, two heavy pond process units, characterized by: the reaction tank of the skip-layer oxidation ditch is divided into an upper layer reaction tank and a lower layer reaction tank with more than 2 layers, the reaction tanks of all layers are connected end to end through pipelines, and the circulating pump supplies water at the tail end of the reaction tank of the bottom layer to the head end of the reaction tank of the top layer through a circulating pipeline, so that closed endless annular flow arrangement taking channels as main bodies is formed, and oxygenation and plug flow are realized; the water level of the secondary sedimentation tank is lower than that of the top layer reaction tank but higher than that of the anaerobic tank, and sludge at the bottom of the secondary sedimentation tank flows back to the anaerobic tank by siphon gravity flow; the process units, the main equipment and the pipelines of all the jump-layer oxidation ditches are integrated in a barrel body.
The reaction tanks of the traditional oxidation ditch process are basically arranged on the same elevation, and the head end and the tail end of the whole reaction tank form a closed endless loop channel-shaped arrangement and an annular channel arranged in an oxygenation and plug flow device; the anaerobic tank, the reaction tank and the secondary sedimentation tank are all basically arranged on the same elevation, and the water level of the sewage flows from the anaerobic tank, the reaction tank and the secondary sedimentation tank from high to low; the sludge reflux of the device needs a reflux pump, and the whole arrangement occupies a very large area. It is difficult to miniaturize and equip.
The reaction tank of the spring-layer oxidation ditch method provided by the patent is divided into an upper layer and a lower layer (2 layers and above), each reaction tank is in a ditch shape, and the length-width ratio is very large; the upper layer reaction tank and the lower layer reaction tank are connected through the head end and the tail end of a pipeline, and the connection mode can be an overflow pipeline or a siphon pipe assembly; the circulating pump supplies the water from the bottom layer reaction tank to the top end of the top layer reaction tank through the circulating pipeline to form a closed endless loop flow mode which takes the reaction tank as a main body, and oxygen is filled and aerated in the closed endless loop flow mode, and the water flow of the circulating pump forms plug flow in the reaction tank.
The aeration mode can adopt the traditional oxygenation aeration mode of the oxidation ditch, such as aeration at the bottom of a fan, and can also adopt the power of a circulating pump to carry out water jet aeration. Because the lift of a common sewage pump is larger and higher than the water depth of a plurality of reaction tanks, the energy can be better saved by utilizing the high lift to carry out water jet aeration. On the other hand, the oxidation ditch generally requires that aeration and plug flow are carried out synchronously, and the characteristic is just realized by utilizing the power of a circulating pump to carry out water jet aeration. The water jet aeration is also available in two types, one is that a water jet is arranged on a circulating pipeline for air suction aeration, and the other is that a water jet aeration device is arranged on the bottom of the pool for aeration.
The water level of the secondary sedimentation tank is lower than that of the top layer reaction tank and higher than that of the anaerobic tank. After long-term stable operation, the circulation ratio of the duplex oxidation ditch is very high, sewage in the duplex oxidation ditch is circulated for many times, part of sewage automatically flows into a secondary sedimentation tank from a top layer reaction tank for sedimentation, and the sewage after sedimentation is discharged or enters the next process. The sludge sediment is collected at the bottom of the secondary sedimentation tank. Because the water level of the secondary sedimentation tank is higher than that of the anaerobic tank, as long as the water level ensures enough fall, the aged sludge at the bottom of the secondary sedimentation tank can automatically flow back to the anaerobic tank by adopting a siphon method to form sludge backflow. Sludge siphoning can be generated by either own overflow guidance or other powered suction guidance. After the siphon is generated, the water level of the secondary sedimentation tank can be quickly reduced, and when the water level is reduced to a set destruction port, the siphon can be automatically destroyed. The sludge reflux quantity can be determined jointly according to the siphon diameter and the siphon duration of the sludge, and the sludge reflux quantity can be adjusted by adjusting the elevation of the destroying pipe orifice or the siphon reflux pipe diameter (through a valve).
Because the aeration effect is positively correlated with the depth of the aeration water, a deep aeration tank should be adopted as far as possible. The structure of the upper and lower multi-layer reaction tanks enables the depth of each reaction tank to be reduced, and an aeration tank can be additionally arranged before the top reaction tank. The depth of the aeration tank is not limited by the depth of the single-layer reaction tank, for example, the upper and lower multi-layer reaction tanks can be divided into a section and then communicated up and down to form a vertical separation bin as the aeration tank, and the depth of the vertical separation bin is the sum of the depths of the multi-layer reaction tanks. The water level of the aeration tank is higher than that of the top layer reaction tank, and the effluent of the circulating pump firstly enters the top layer reaction tank after being aerated in the aeration tank. In order to prevent a large amount of sediment from silting up in the aeration tank, the aeration tank can adopt a bottom aeration mode.
After the separate aeration tank is added, water can be supplied to the top layer reaction tank at the middle upper part of the aeration tank, a long-time aeration air floatation oil removal tank is left near the top of the aeration tank, and an oil removal device is additionally arranged for removing oil.
The effluent after the oxidation ditch-secondary sedimentation tank can only reach the first grade B generally. In order to improve the quality of the effluent, advanced treatment such as MBR biological membrane, flocculation and precipitation by adding a flocculating agent, and filtration can be added after the secondary sedimentation tank. The jump-layer oxidation ditch method can also add a filter tank and a backwashing water reservoir behind the secondary sedimentation tank. The backwashing water reservoir is generally arranged above the filter tank, and the water level of the backwashing water reservoir is lower than the secondary sedimentation tank and higher than the anaerobic tank and part of the low-level reaction tank. And the effluent of the secondary sedimentation tank automatically flows into the filter tank to be filtered and then is stored in the backwashing water storage tank, and the water level of the backwashing water storage tank rises to a certain height and then is discharged. The filter tank adopts siphon automatic backwashing, backwashing drainage is directly discharged into the anaerobic tank or the low-level reaction tank, and zero power and zero emission are formed.
The filter tank can also be designed into a double-filter integrated filter tank (also called a double-filter integrated filter) with a slow filter tank (the filtering speed is lower than 0.3 m/h). According to the research (biological slow water filtration treatment technology for guaranteeing the safety of drinking water in rural areas, subject number ring 0120012007, first-class award applied by national department of science and technology in 2010) of the research institute of water conservancy and hydropower science in China, the research results show that: the biological slow filtration has good removal effect on bacteria, viruses, organic pollutants, smelly pollutants, chromaticity and other pollutants. Firstly, the removal rate of escherichia coli reaches 100 percent; the total bacteria removal rate is more than 97%. ② the removal rate of ammonia nitrogen is as high as 98.5 percent. Removing turbidity more than 99%. Fourthly, the effect of removing heavy metals is also good, the removal rate of copper, cadmium and iron is more than 95 percent, and the removal rate of manganese, lead and zinc is between 60 and 88 percent. Fifthly, removing the organic substances CODMn and TOC is stabilized at 28.1-37.1% and 31-36% respectively. The biological slow filtration can treat 30-50 NTU into 1NTU, and has obvious effect of removing organic pollution. In combination with the technology of 'a rapid and slow filtration integrated water purifier capable of carrying out cyclic layered backwashing on filter materials of a slow filter' (patent number ZL 20140489268.1) of the company, a siphon backwashing device can be adopted to carry out siphon backwashing on a coaxial rapid filtration and slow filtration two-stage filter; therefore, the quality of the discharged water can be greatly improved by only adopting a double-filter integrated filter with slow filtration; as long as the effluent of the AAO-secondary sedimentation tank is good enough (slightly higher than the standard of the first-level B), the effluent can reach the standard of the first-level A after passing through the double-filtration integrated filter. After the jump-layer AAO method is adopted, backwash water can be discharged into an anaerobic tank or a low-layer reaction tank, zero emission is realized, and a zero-emission and zero-power technical path is provided for lifting the effluent of the first-level B to the effluent of the first-level A.
The operation control of the circulating pump can be various, if the water inflow amount is stable and uniform, the circulating pump can operate for 24 hours; the flow switch can also be used for collecting the incoming water to automatically control the on and off of the circulating pump. If the anaerobic tank has a certain regulation volume, the opening and the closing of the circulating pump can be controlled according to the water level of the anaerobic tank; when the water level of the anaerobic tank is at a high level, the circulating pump is started; and when the water level of the anaerobic pool is at a low level, the circulating pump stops running to prevent the circulating pump from running without water, and the control is very simple.
The minimum sewage pump is 180W at present, and the flow is about 10 tons/hour at 1.5 m lift; if the fan is adopted for aeration, the continuous circulating water amount in one day is 240 tons/day; considering the cycle number of 30 times, the daily treatment capacity is about 8 tons/day. The water jet aeration is adopted, the flow rate can be reduced to about 2 tons/hour, and the gas-water ratio of natural air suction is about 0.4-0.5 liter/liter. If the aeration gas-water ratio is 10 liters/liter, the water flow circulation times are 10/(0.4-0.5) 20-25 times, namely the average water inflow rate of the oxidation ditch is about 2 × 1000/(20-25) 80-100 liters/hour, which is equivalent to the treatment capacity of more than 2 tons/day.
The oxidation ditch process generally requires that sewage circulates for one circle and passes through an aerobic section and an anoxic section, and the time ratio of the anoxic section to the aerobic section is kept in a certain proportion range (generally, 40-60% is considered to be the most suitable); on the other hand, the sewage in the reaction tank is required to keep a certain flow rate (not less than 0.3 m/s in domestic specifications, and mostly 0.25-0.35 m/s abroad) to prevent sludge precipitation. Both require very long cell lengths for the oxidation ditch process.
The total length of the reaction tank is set as L, and the length of the aerobic section is set as L when the circulating pump runs stablyOThe length of the anoxic zone is LA，L＝L0+LA. If the circulating pump operates in an intermittent mode, the operation period is T, and the T is operatedOpening deviceStop after a certain timeTStopTime, T ═ TOpening device+TStop(ii) a Delta T (< T) after the operation of the circulating pump is stoppedStop) In time, all aerobic sections are converted into anoxic sections at uniform speed, and then:
in the continuous operation period of the circulating pump, the oxygen deficiency ratio muOpening device＝LA/L
In delta T period after the circulation pump stops running, the oxygen deficiency ratio muΔ＝(LA+L0/2)/L＝ (1+μOpening device)/2
When the circulation pump stops operating for delta T period, the anoxic ratio muStop＝1
The hypoxia percentage after comprehensive weighting is as follows:
μ＝Topening device/T*μOpening device+ΔT/T*μΔ+(TStop-ΔT)/T*1
＝μOpening device+(TStop/T+ΔT/2T)(1-μOpening device)
If the total length of the reaction tank is short, the whole oxidation ditch becomes an aerobic section L during the continuous operation of the circulating pumpA＝0，μOpening deviceWhen the ratio is 0, the weighted hypoxia percentage is:
μ＝Tstop/T-ΔT/2T
Assuming that T is 60 minutes, TStopWhen Δ T is 12 minutes and 25 minutes, μ is 33.3%, which corresponds to a deficiency/oxygen ratio of 50%. For one plant configuration, Δ T is substantially fixed, and if T is also fixed, then only the on-time ton of the circulation pump needs to be adjusted to obtain the corresponding oxygen/oxygen ratio. T isOpening deviceThe longer the length, the smaller the oxygen/oxygen ratio.
For the 180W water pump with water jet aeration scheme, if an intermittent operation mode is further adopted, the adaptive treated water quantity can be further reduced. The method can be used for designing the integrated sewage treatment device for the production user.
For the duplex oxidation ditch method, the normal operation flow velocity can be separated from the scouring and silting flow velocity, the normal operation flow velocity can be lower, and certain precipitation is allowed in the reaction tank during operation; but the reaction tank is flushed by adopting the flushing silt flow rate at intervals, and the flushing silt flow rate is required to meet the requirement of the design specification. This allows the length of the reaction cell to be reduced. For the oxidation ditch adopting water jet aeration, as the water jet has great resistance, the resistance is larger when the flow rate is larger; the greater the resistance the smaller the flow. Experiments prove that the normal flow of the 180W submersible pump can reach about 130 liters/minute under the lift of 1.5 meters, and the flow is reduced to about 25 liters/minute after the submersible pump is provided with a water ejector. If a pipeline without a water ejector is connected with a bypass flow on the circulating pipeline in front of the water ejector, namely a silt flushing pipeline, an outlet of the silt flushing pipeline is directly connected to the head end of the top layer reaction tank, and a valve is arranged on the silt flushing pipeline to control the opening and closing of the silt flushing pipeline. When the sewage water is normally operated, the sewage water is oxygenated and aerated by the water injector, but the valve on the silt flushing pipeline is opened at regular intervals to flush silt. By adopting the method, the normal running flow rate can be greatly reduced, and conditions are created for shortening the length of the reaction tank.
In a word, the circulating pump adopts the method of intermittent operation and intermittent sludging, and the total length of the reaction tank can be greatly reduced. In fact, when the water jet aeration mode is adopted, the air-water ratio in a period of time is in direct proportion to the running time of the circulating pump because the air adding amount is in direct proportion to the flow rate of the circulating pump, and the running time T of the circulating pump is adjustedOpening deviceThe gas-water ratio is also adjusted. In combination, it can be designed to let the user adjust T by himselfOpening deviceThe device is suitable for different incoming water qualities, so that the saltus oxidation ditch has better raw water universality.
Compared with the traditional oxidation ditch method, the duplex oxidation ditch method has the following obvious advantages:
(1) the pump-free automatic sludge backflow is adopted, only 1 pump is needed, and if water jet aeration is adopted, a fan is not needed. The investment and the operation cost are both lower, and the overall reliability is higher.
(2) The filter tank can carry zero power and zero emission: the spring layer formula circulation AAO method of this patent can join in marriage the filtering ponds behind two heavy ponds, as long as filtering ponds and backwash cistern minimum water level still are higher than the anaerobism pond water level, then during the filtering ponds just can adopt automatic siphon backwash and discharge the backwash drainage into the anaerobism pond, form zero release, zero dynamic filtration! The filter tank is added, so that the drainage quality is higher and more reliable.
(3) The integrated filter tank can be provided with double filters (fast filter and slow filter), and the drainage is lifted from the first level B to the first level A with zero power and zero emission.
(4) The circulating pump can be automatically started and stopped according to the actual water volume of a user: therefore, not only can a complex control device be omitted, but also the ton water power consumption is not changed along with the quantity of the water, and the method is better suitable for the actual situation that the quantity of the water coming from rural families is variable.
(5) The volume is adjusted from the area, can better adapt to the volume of changing water.
(6) The circulating pump can adopt an intermittent operation mode, and a user can adapt to different incoming water quality changes by adjusting the operation time (such as a time relay) of the circulating pump so as to meet different water outlet standards, select the optimal operation time and reduce the operation cost.
(7) The bypass flow silt flushing pipeline mode can be adopted, the normal running flow speed is reduced, and the length of the reaction tank is shortened.
(8) Can be provided with an aeration tank and an air-flotation oil removal tank, and further develops the universality of the sewage, so that the oily sewage can be treated by the duplex oxidation ditch method.
(9) The control is simpler and more reliable: the whole integrated sewage treatment device only needs one water pump and one fan, so that the quantity of equipment and the control difficulty are greatly reduced.
In a word, through the improvement, the length of the reaction tank can be greatly reduced, the equipment and the control are simplified, and a new way is opened up for developing a household and small micro integrated sewage treatment device by the skip-layer oxidation method. After the water ejector is adopted for aeration, the equipment is further simplified, and even all the equipment and the treatment units can be arranged in a barrel, so that the user can install the equipment by himself.
Of course, the skip-layer oxidation ditch method also brings new problems, mainly including (1) the stacking of the reaction tanks up and down, requiring high bearing strength of each layer, and increasing the structural difficulty. (2) In order to prevent sludge precipitation, the flow rate is required to be high, the sectional area of the reaction tank is small and long, great challenges are brought to the production process, and the welding production workload is very large. In response to the above problems, we have developed a layered injection molding, multilayer hot melt process, and have applied for additional patent. Solving these structural problems can be accomplished using this process.
Description of the drawings:
FIGS. 1, 2, 3, 4 and 5 are schematic structural views of an embodiment of an integrated sewage treatment device designed according to a duplex oxidation ditch method with a filter tank.
Fig. 1 is a top view of an embodiment.
Fig. 2 is a front view of the embodiment.
Fig. 3 is a front view in section a-a.
FIG. 4 is a schematic view of a circulation pipeline and a fertilizer extraction pipeline.
FIG. 5 is a schematic view of a sludge siphon return pipe.
The specific implementation mode is as follows:
the embodiment shown in the attached figures 1, 2, 3, 4 and 5 is a duplex oxidation ditch method integrated sewage treatment device with a filter tank. The device comprises a grating tank 4, an anaerobic tank 48, an upper multi-layer reaction tank 15, a lower multi-layer reaction tank 15, a secondary sedimentation tank 2, a filter tank 24, a reverse water selecting reservoir 34, an ultraviolet sterilizer 9 and other main water treatment process units; the upper and lower multi-layer reaction tanks 15 include a top reaction tank 29, a bottom reaction tank 23 and a middle reaction tank (4 layers in this embodiment), each reaction tank is formed by connecting a plurality of semicircular reaction tanks end to end, and the height-to-width ratio of each reaction tank is large, so that a channel form is formed. The tail end of the top layer reaction tank 29 is connected with the head end of the second-time reaction tank 2 through the communicating pipe 20, and the like until the head end of the bottom layer reaction tank 23; the water at the tail end of the bottom reaction tank 23 returns to the head end of the top reaction tank 29 through the circulating pump 10, the circulating pipeline 40 and the aeration tank 12 to form a closed non-terminal jump-layer type oxidation ditch taking the reaction tank as a main body.
The whole device is arranged in a circular barrel body 1 to form a highly integrated sewage treatment device. Wherein, the center of the barrel body 1 is provided with an inner barrel 18, the filter tank 24 is arranged at the center middle part of the inner barrel 18, the backwashing water reservoir 34 is arranged at the upper part of the filter tank 24, and the anaerobic tank 48 is arranged at the lower layer of the filter tank 24; the reaction tank of the skip-layer oxidation ditch is divided into an upper layer and a lower layer by 3 horizontal clapboards, and each layer of reaction tank is divided into a plurality of semicircular annular ditches surrounding the inner barrel body 18; 5 vertical partition plates 49 are radially arranged between the tub body 1 and the inner tub body 18 to vertically partition the secondary sedimentation tank 2, the grid tank 4, the equipment room 11 and the aeration tank 12, all of which are as high as the tub body 1 (the vertical partition plate between the grid tank 4 and the equipment room 11 is slightly short to leave more space for installation of the equipment).
The sewage enters the grating tank 4 from the water inlet 5, and the grating net 6 prevents large impurities in the sewage from influencing the operation of the circulating pump 10 and the water ejector 42; the sewage filtered by the grid net 6 is mixed with the sludge in the sludge siphon return pipe 3 and enters the annular groove 19 in the anaerobic tank 48 from the bottom hole 50 between the grid tank 4 and the inner barrel body 18; on the other hand, the sewage passing through the bottom reaction tank 23 for multiple cycles also enters the annular groove 19 from the bottom hole 53 between the end of the inner ring of the bottom reaction tank 23 and the inner barrel body 18; the two sewage flows are mixed in the annular groove 19 and then enter the equipment room 11 from the bottom hole 52 between the inner barrel body 18 and the equipment room 11. Because the sludge siphon backflow time is short and the flow rate is large, the sludge siphon backflow device can form certain back flushing on the grid mesh 6 and is also beneficial to preventing the annular groove 19 from precipitating.
The circulation pump 10 is a submersible sewage pump, and is disposed at the bottom of the equipment room 11. The circulation pump 10 supplies the mixed sewage to the bottom of the aeration tank 12 through the circulation line 40 by turning over the vertical partition plate 49. The circulating pipeline 40 is provided with a water ejector 42 and a water distribution head 41, and the water distribution head 41 is arranged at the bottom of the aeration tank 12; the water ejector 42 is provided with an air inlet pipe 43, a fertilizer pumping pipeline 44 is communicated in front of the water ejector 42, and a fertilizer pumping valve 45 is arranged on the fertilizer pumping pipeline 44. During normal operation, the fertilizer pumping valve 45 is closed, and the water discharged from the circulating pump 10 is sucked by the water ejector 42 (through the air inlet pipe 43) and sprayed out from the water distribution head 41 to form oxygenation and plug flow. When a user needs to pump the fertilizer, the fertilizer pumping valve 45 can be opened, and a large amount of sewage is discharged from the fertilizer pumping pipeline 40 due to the large water resistance of the water ejector 42, so that the fertilizer pumping is realized.
The water ejector 42 can well mix with the sewage after sucking air; the depth of the aeration tank 12 is equivalent to that of the 4-layer reaction tank, so that the oxidation conversion rate is improved. The sewage after aeration in the aeration tank 12 enters the head end of the top layer reaction tank 29 through the water inlet hole 14 near the top thereof, the main sewage at the tail end of the top layer reaction tank 29 reaches a certain water level and then enters the next layer reaction tank through the communicating pipes 20 (2 in the embodiment), and so on, the sewage returns to the tail end of the bottom layer reaction tank 23 layer by layer, and then enters the plant room after being mixed with the sewage in the anaerobic tank 48 through the bottom hole 53 between the sewage and the inner barrel body 18, closed circulation is realized under the drive of the circulating pump 10, and oxygenation and plug flow are realized through the water ejector 42 in the circulation process.
On the other hand, the other part of the sewage at the tail end of the top layer reaction tank 29 enters the secondary sedimentation tank 2 through the secondary sedimentation tank water inlet pipe 21 for sedimentation; the water after precipitation enters the filter tank 24 through the filter water inlet pipe 17 and the siphon ascending pipe 31 for filtration, and the water after downward flow filtration is converted into upward flow through the holes 37 at the bottom of the filter tank 24 and stored in the backwashing water reservoir 34; when the water level of the backwashing water reservoir 34 rises to a certain level, the water is sterilized by the ultraviolet sterilizer 9 and then discharged through the drain valve 8 and the water outlet 7.
Although the bottom of the secondary sedimentation tank 2 has the same elevation as the bottom of the anaerobic tank 48 and the grid tank 4, the water level of the secondary sedimentation tank 2 is much higher than the water levels of the anaerobic tank 48 and the grid tank 4, so that when the water level in the secondary sedimentation tank 2 reaches a certain elevation, the sludge siphon pipe 3 forms automatic siphon, and the sludge siphon pipe can extract the aged sludge at the bottom of the secondary sedimentation tank 2 and discharge the aged sludge into the water inlet (in the grid tank 4) of the anaerobic tank 48 to form aged sludge backflow. After the sludge siphon is formed, the siphon drainage flow can be greater than the inflow flow of the water inlet pipe 21 of the secondary sedimentation tank, and the water level of the secondary sedimentation tank 2 can gradually drop. When the water level is lower than the breaking bucket 46, the breaking pipe 47 can immediately suck the water in the breaking bucket 46 to be dry and then suck air, so that the sludge is broken by siphoning. As long as the pipe diameter of sludge siphon and the elevation of the damage bucket are designed, the amount and time of sludge backflow can be controlled, so that the sludge backflow amount is controlled, and pump-free automatic sludge backflow is realized.
After the filtering tank 24 filters for a period of time, the quartz sand filter material in the filtering tank 24 is gradually blocked, so that the water level in the siphon ascending pipe 31 is raised; when the water level rises to the level of the horizontal drainage tube 32 (which is slightly lower than the water inlet level of the siphon down pipe 33), the horizontal drainage tube 32 supplies water to the siphon auxiliary pipe 18, and pushes the water ejector 27 arranged on the siphon auxiliary pipe 18 to suck air through the air suction pipe 30, so that negative pressure is formed in the siphon up pipe 31 to guide backwashing siphon production. After the backwashing siphon is generated, water in the backwashing water reservoir 34 is discharged into the anaerobic tank 48 through the hole 37, the filter tank 24, the siphon ascending pipe 31 and the siphon descending pipe 33 in sequence, and the siphon backwashing on the quartz sand filter material of the filter tank 24 is formed. When the water level in the backwash water reservoir 34 drops to the level of the siphon break tank 26, the siphon break pipe 28 will immediately draw the water from the break tank 26 dry and then draw in air, causing the backwash siphon to break and the filtration tank 24 to resume normal filtration operation. The filtration backwash does not require any power and the backwash drain drains into the anaerobic tank 48, thus being a zero-power, zero-emission backwash.
The operation of the circulation pump 10 and the uv sterilizer 9 is controlled by the control box 13. Considering that the water is stable and uniform when the processor runs, the circulating pump 10 adopts a fixed-period intermittent start-stop control mode; the uv sterilizer 9 is designed to operate continuously.
In the embodiment, a skip-layer circulation AAO method is adopted, a zero-emission and zero-power filter is adopted, nitrogen and phosphorus can be simultaneously removed by only using 1 water pump, only a first-stage filter tank is arranged, and the effluent is stable and reliable and can reach a first-stage B. Compared with the traditional integrated sewage treatment device, the device only needs 1 pump, and is simple and reliable in structure and control. All equipment is integrated in a barrel, packaging and transportation are simple, operation can be achieved through water and electricity, and users can install the equipment by themselves.
Claims (6)
1. The utility model provides a spring layer formula oxidation ditch method integration sewage treatment ware, it includes anaerobism pond, spring layer formula oxidation ditch, two heavy pond process units, characterized by: the reaction tank of the skip-layer oxidation ditch is divided into an upper layer reaction tank and a lower layer reaction tank with more than 2 layers, the reaction tanks of all layers are connected end to end through pipelines, and the circulating pump supplies water at the tail end of the reaction tank of the bottom layer to the head end of the reaction tank of the top layer through a circulating pipeline, so that closed endless annular flow arrangement taking channels as main bodies is formed, and oxygenation and plug flow are realized; the water level of the secondary sedimentation tank is lower than that of the top layer reaction tank but higher than that of the anaerobic tank, and sludge at the bottom of the secondary sedimentation tank flows back to the anaerobic tank by siphon gravity flow; the process units, the main equipment and the pipelines of all the jump-layer oxidation ditches are integrated in a barrel body.
2. The integrated sewage treatment device of claim 1, wherein: and a filtering tank and a backwashing water reservoir are arranged behind the secondary sedimentation tank, the water level of the backwashing water reservoir is lower than that of the secondary sedimentation tank and higher than that of the anaerobic tank, the filtering tank adopts siphon automatic backwashing, and backwashing water is discharged into the anaerobic tank or a low-level reaction tank.
3. The integrated sewage treatment device of claim 2, wherein: the filter tank adopts a double-filter integrated filter.
4. The integrated sewage treatment device of claim 1, 2 or 3, wherein: an aeration tank with deeper water depth is additionally arranged in front of the top layer reaction tank, the water level of the aeration tank is higher than that of the top layer reaction tank, and the effluent of the circulating pump firstly enters the top layer reaction tank after being aerated in the aeration tank.
5. The integrated sewage treatment device of claim 4, wherein: the top of the aeration tank is additionally provided with an oil removal tank.
6. The integrated sewage treatment device of claim 1, 2, 3 or 5, wherein: the jump-layer oxidation ditch carries out water jet aeration by the power of a circulating pump.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020388695.6U CN212610103U (en) | 2020-03-13 | 2020-03-13 | Duplex oxidation ditch method integrated sewage treatment device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020388695.6U CN212610103U (en) | 2020-03-13 | 2020-03-13 | Duplex oxidation ditch method integrated sewage treatment device |
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| CN212610103U true CN212610103U (en) | 2021-02-26 |
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|---|---|---|---|
| CN202020388695.6U Expired - Fee Related CN212610103U (en) | 2020-03-13 | 2020-03-13 | Duplex oxidation ditch method integrated sewage treatment device |
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| Country | Link |
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| CN (1) | CN212610103U (en) |
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- 2020-03-13 CN CN202020388695.6U patent/CN212610103U/en not_active Expired - Fee Related
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