CN212450817U - Moving bed biofilm reaction system and application thereof - Google Patents
Moving bed biofilm reaction system and application thereof Download PDFInfo
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- CN212450817U CN212450817U CN202020893785.0U CN202020893785U CN212450817U CN 212450817 U CN212450817 U CN 212450817U CN 202020893785 U CN202020893785 U CN 202020893785U CN 212450817 U CN212450817 U CN 212450817U
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/26—Activated sludge processes using pure oxygen or oxygen-rich gas
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Biological Treatment Of Waste Water (AREA)
- Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
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Abstract
The utility model discloses a remove bed biofilm reaction system, it includes: a housing; the inner shell is arranged in the outer shell, and suspended fillers are arranged in the inner shell; the water inlet pipe penetrates through the outer shell and is communicated with the inner shell; a water outlet pipe communicated with the housing; a pure oxygen aeration device communicated with the inner shell; an ozone supply device in communication with the inner housing. The utility model solves the problems that the oxygen content generated by air aeration is low and the sewage treatment is not facilitated in the prior moving bed biomembrane reactor technology.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, especially relate to a remove bed biofilm reaction system and application thereof.
Background
With the rapid development of the industry in China, more and more industries can generate a large amount of high-concentration organic wastewater, such as the industries of petrifaction, printing and dyeing, papermaking, pharmacy, leather, cosmetics and the like. The high-concentration organic wastewater is large in quantity and dispersed, a large amount of organic pollutants, nitrogen elements and the like contained in the sewage are discharged into surface water body to carry out oxidative decomposition reaction, a large amount of dissolved oxygen in the water body needs to be consumed in the decomposition process, finally, the water body is anoxic, so that aquatic animals such as fish and the like in the water body can not breathe and die, the dead aquatic animals carry out anaerobic decomposition in the water body and generate malodorous gases such as hydrogen sulfide, methane and the like, and the water body is smelly and blackened, so that the water quality condition of the watershed of the water body is deteriorated, and meanwhile, the water body, soil and even the whole ecological environment are seriously damaged.
Moving Bed Biofilm Reactors (MBBR) are a novel biofilm reactor, and the main principle is that after sewage continuously flows through a reactor filler carrier, a biofilm is formed on the carrier, and microorganisms propagate and grow on the biofilm in large quantities and degrade organic pollutants in the sewage, so that the sewage is purified. In the aerobic reactor, carriers need to be driven to move by aeration, in the prior art, the aeration gas is usually air, but because the oxygen content in the air is limited, and the oxygen concentration directly influences the sewage treatment capacity of the moving bed biofilm reactor, the increase of the oxygen concentration of aeration is an important direction for improving the sewage treatment capacity.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a remove bed biofilm reaction system and application thereof has solved the produced oxygen content of air aeration low among the current removal bed biofilm reactor technique, is unfavorable for sewage treatment's problem.
In order to solve the technical problem, the utility model discloses a realize through following technical scheme:
the utility model provides a remove bed biofilm reaction system, it includes:
a housing;
the inner shell is arranged in the outer shell, and suspended fillers are arranged in the inner shell;
the water inlet pipe penetrates through the outer shell and is communicated with the inner shell;
a water outlet pipe communicated with the housing;
a pure oxygen aeration device communicated with the inner shell;
an ozone supply device in communication with the inner housing.
In one embodiment of the present invention, the pure oxygen aeration device comprises a pure oxygen supply device, and the pure oxygen supply device is one of a cryogenic air separation oxygen generation device or a pressure swing adsorption oxygen generation device.
In an embodiment of the present invention, the reaction system further includes a water distribution pipe, and the water distribution pipe is disposed between the inner shell and the outer shell.
In an embodiment of the present invention, the water distribution pipe is provided with a plurality of water distribution ports passing through the inner shell.
In an embodiment of the present invention, the pure oxygen aeration apparatus further comprises an aeration pipe, one end of the aeration pipe is communicated with the pure oxygen aeration apparatus, and the other end of the aeration pipe passes through the inner shell and is disposed in the inner shell.
In one embodiment of the present invention, the ozone supply device is in communication with the aeration pipe.
In an embodiment of the present invention, the pure oxygen aeration apparatus further comprises a plurality of aeration heads, and the plurality of aeration heads are disposed on the aeration pipe.
In an embodiment of the present invention, the aeration pipe is disposed on a side of the inner shell near the bottom wall.
In one embodiment of the present invention, the aerator pipe is movable.
The utility model also provides a sewage treatment system, it includes:
a sewage tank;
a grid well in communication with the lagoon;
a conditioning tank in communication with the grid well;
a moving bed biofilm reaction system in communication with the conditioning tank, the moving bed biofilm reaction system comprising:
a housing;
the inner shell is arranged in the inner shell, and suspended fillers are arranged in the inner shell;
the water inlet pipe penetrates through the outer shell and is communicated with the inner shell;
a water outlet pipe communicated with the housing;
a pure oxygen aeration device communicated with the inner shell;
an ozone supply device in communication with the inner housing.
The utility model discloses a remove bed biofilm reactor adopts pure oxygen aeration equipment to aerate, and pure oxygen aeration equipment dissolved oxygen concentration is high, and the oxygen content is annotated to unit volume height, can supply oxygen volume according to the quality of water condition automatically regulated of intaking to can ensure stable treatment effeciency and play water quality of water. The pure oxygen aeration device saves land occupation and civil engineering investment, has less equipment investment, the aeration tank in the pure oxygen aeration device has no odor, the sludge yield is less, the foam generated by the reactor is less, the treatment capacity of the reactor or the effluent quality can be improved under the condition of not increasing the volume of the reactor when the reactor is modified, the volume load of the reactor is high, and the volume required by the reactor is small. The pure oxygen aeration device has short construction period and simple installation. In addition, the dissolved oxygen driving force in the pure oxygen aeration device is 4.7 times higher than that of an air aeration system, the shearing force of the biological flocculating constituents caused by the fact that pure oxygen is aerated into the reactor is smaller, and oxygen can stretch into the zoogloea, so that the zoogloea is more compact, the biological flocculating constituents are larger, the settling performance is better, sludge is easier to dewater, and the proportion among microbial populations is more reasonable. By adopting the pure oxygen aeration device of the utility model, the dissolved oxygen efficiency can reach more than 85 percent. The utility model discloses a pure oxygen aeration equipment can communicate with ozone recovery unit, because the concentration of oxygen is greater than 80% in the ozone, so can let in the ozone that obtains through ozone recovery unit the utility model discloses an among the pure oxygen aeration system, realize waste gas utilization.
Of course, it is not necessary for any particular product to achieve all of the above-described advantages at the same time.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural view of a sewage treatment system of the present invention;
FIG. 2 is a schematic structural diagram of a moving bed biofilm reactor of the present invention;
FIG. 3 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 4 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 5 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 6 is a schematic structural view of another embodiment of a moving bed biofilm reactor according to the present invention;
FIG. 7 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 8 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 9 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 10 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 11 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 12 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 13 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 14 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 15 is a schematic structural view of another embodiment of a moving bed biofilm reactor of the present invention;
FIG. 16 is a schematic structural view of another application of the pure oxygen aeration apparatus of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative efforts belong to the protection scope of the present invention.
Referring to fig. 1, the present invention provides a sewage treatment system comprising: the device comprises a sewage tank 100, a grid well 200, a regulating reservoir 300 and a moving bed biofilm reaction system 400, wherein the grid well 200 is communicated with the sewage tank 100, the regulating reservoir 300 is communicated with the grid well 200, and the moving bed biofilm reaction system 400 is communicated with the regulating reservoir 300. The grid well has a grid width of, for example, 0.3m and a grid gap of, for example, 2-40 mm. The sewage automatically flows into the regulating tank, the regulating tank plays a role in regulating the quality and the quantity of water, impact on subsequent treatment procedures is avoided, the regulating tank has certain water storage capacity, the water outlet pipeline is provided with the flowmeter, the flow is controlled by the pipeline valve, the instantaneous water inflow quantity can be visually displayed, and the operation and the running are convenient. In actual work, sewage flowing through the sewage tank 100 flows into the regulating tank 300 after passing through the grid well 200, the grid well 200 is used for intercepting large-particle solid dirt, the solid dirt can be manually removed after being intercepted, the sewage can be lifted into the moving bed biomembrane reaction system 400 through the submersible sewage pump, the moving bed biomembrane reaction system 400 is filled with suspended fillers, microbial membranes grow on the fillers, the microbial membranes grow and propagate by utilizing carbon, nitrogen, phosphorus and the like in the sewage, water pollutants and water eutrophic substances are digested and absorbed and removed, and the purified water can further enter the clarifying/disinfecting tank to further remove suspended matters and bacterial viruses, so that the purified water can be discharged to a receiving water body or subjected to deep treatment to be used as landscape water, irrigation water and the like.
Referring to fig. 2 to 9, the present invention further provides a moving bed biofilm reaction system 400 comprising: a water inlet pipe 401, an outer shell 402, an inner shell 403, a water outlet pipe 404, a suspended filler 405 and a pure oxygen aeration device.
Referring to fig. 2 to 9, one end of a water inlet pipe 401 passes through an outer shell 402 to be communicated with an inner shell 403, the other end of the water inlet pipe 401 is connected with a power pump, a water outlet pipe 404 is communicated with the outer shell 402, a filter screen may be arranged at the water outlet pipe 404, a suspended filler 405 is arranged in the inner shell 403, the filler 405 is sponge particles with a diameter of 5-10mm, the reactor further includes a water distribution pipe 410 arranged between the inner shell 403 and the outer shell 402, a plurality of water distribution ports 411 passing through the inner shell 403 are arranged on the water distribution pipe 410, the pure oxygen aeration device may be a micro-pore aerator or a nano aerator, in this embodiment, the pure oxygen aeration device includes a pure oxygen supply device 407, an aeration pipe 408 and an aeration head 409, the arrangement of the aeration pipe 408 in the inner shell may be in various forms, for example, the pure oxygen aeration pipe 408 may be arranged on the bottom and the side wall, as long as the arrangement mode can realize and is beneficial to the mutual mixing and collision of the sewage, the oxygen and the filler 405 in the inner shell 403, the aeration heads may also be arranged on the aeration pipe 408 as required, in some embodiments, the aeration pipe 408 is, for example, an "inverted t" shape, the aeration heads 409 are all arranged around the aeration pipe 408, the aeration head 409 at the lowest side may be directed downward, and the orientations of the other aeration heads 409 are different, in this embodiment, the opening of the aeration head 409 is upward, for example, forms an inclination angle of 45 degrees with the vertical direction. In other embodiments, the aeration pipe 408 may also be a "one" type, the aeration pipe 408 is provided with a plurality of aeration heads 409, the orientations of the plurality of aeration heads 409 are different, and in some embodiments, the arrangement form of the aeration pipe 408 may be combined in various ways as long as the arrangement form is capable of realizing and facilitating the mixing and collision of the sewage, the oxygen, and the filler 405 in the inner shell 403. The pure oxygen aeration device releases pure oxygen into the inner shell 403, when the pure oxygen aeration device operates, sewage enters from the water inlet pipe 401 through the first power pump, is distributed in the water distribution pipes 410, enters the inner shell 403 of the reactor from the water distribution ports 411, the pure oxygen is sprayed out from the aeration heads 409 of the aeration pipes 408, the sewage, the oxygen and the filler 405 inside the inner shell 403 are mixed and collided with each other, the activated sludge attached to the filler 405 degrades pollutants, the treated water enters the outer shell 402 from the inner shell 403, the sludge is precipitated at the bottom of the outer shell 402, is pumped by the second power pump and flows back to the inner shell 403, and the sewage can pass through a filter screen and is discharged from the water outlet pipe 404. The utility model discloses well pure oxygen aeration utilizes pure oxygen (oxygen boosting) to carry out aeration biological treatment process, specifically utilizes the pure oxygen of oxygen volume fraction more than 90% to carry out the aeration. Pure oxygen supply apparatus 407 can adopt techniques such as cryrogenic air separation system oxygen, pressure swing adsorption system oxygen to prepare high-purity oxygen, in some embodiments, the gas that also can adopt the oxygen boosting replaces the pure oxygen, for example, can adopt ozone to replace the pure oxygen, aeration pipe 408 and ozone supply apparatus 417 intercommunication in this embodiment, ozone supply apparatus 417 can communicate with ozone recovery unit, the negative pressure effect through the aeration pump inhales the ozone that ozone recovery unit retrieved, because the concentration of oxygen is greater than 80% in the ozone, so can aerate through ozone replacement pure oxygen, let in the ozone that ozone recovery unit obtained simultaneously the utility model discloses an among the pure oxygen aeration equipment, realize waste gas utilization. The pure oxygen aeration sewage treatment mechanism is that aerobic microorganisms carry out biochemical reaction on organic matters in sewage to purify the sewage, and the decomposition of the organic matters in the sewage is completed by uniformly dispersing the activated sludge, namely the aerobic microorganisms, and fully contacting the sewage. The treatment efficiency of pure oxygen aeration is significantly higher than that of air aeration, and the aeration time required for treating the same sewage to the same level is, for example, only about 1/3 of the air aeration, because the oxygen concentration in the air is, for example, only 21%, and the oxygen concentration of pure oxygen is, for example, 90% to 95% which is, for example, 4.7 times higher than that of the air, so that the partial pressure of oxygen in the pure oxygen aeration system, i.e., the driving force of dissolved oxygen, is also, for example, 4.4 to 4.7 times higher than that of the air aeration, the saturation value of dissolved oxygen in water is also increased, for example, 4.4 to 4.7 times, the oxygenation rate is also increased, for example, 4.4 to 4.7 times, and the transfer rate of oxygen is significantly increased, thereby increasing both the concentration and the activity of aerobic microorganisms. In some embodiments, the pure oxygen aeration oxygen utilization rate is 80% -90%, the general air aeration oxygen utilization rate is only 12%, in addition, the pure oxygen aeration impact load resistance is strong, and the effluent quality is stable. In pure oxygen conditions, the organisms are in a highly endogenous metabolic, i.e. autoxidative, state, which results in a large reduction in sludge production, which may reduce excess sludge by, for example, 25% compared to air-aerated activated sludge processes. The pure oxygen aeration oxygenation capacity is improved, the power input into the aeration tank and the shearing force on active biological flocs are reduced, meanwhile, the growth of filamentous bacteria causing sludge bulking can be inhibited by high dissolved oxygen concentration, the sludge bulking phenomenon is less, and the sludge index of the pure oxygen aeration method is 30-50 for example. The high dissolved oxygen concentration of pure oxygen aeration can realize the complete nitrification of NH3-N in the sewage, because the pure oxygen aeration greatly improves the treatment effect on ammonia nitrogen, in the biological filter tank, heterotrophic bacteria and autotrophic nitrifying bacteria compete with each other to compete for the dissolved oxygen, the growth space on the surface of the filler 405 and other environmental factors, because the growth and propagation rate of the heterotrophic bacteria is greater than that of the nitrifying bacteria, when the oxygen supply amount in the aeration tank is insufficient, the heterotrophic bacteria firstly utilize the dissolved oxygen to remove organic matters, the nitrifying bacteria are inhibited, the effect of removing ammonia nitrogen is poor, and when the pure oxygen aeration is adopted, the dissolved oxygen does not become the limiting factor of the growth of the nitrifying bacteria, thereby having better nitrification effect on the sewage. The volume load of the pure oxygen aeration is 3-5 times of that of air aeration due to the high sludge concentration and the high sludge load, the volume of the reactor can be greatly reduced, and the energy consumption is reduced by about 25%. In addition, because pure oxygen aeration is adopted, the volatile organic compounds are decomposed quickly and react completely, so that no peculiar smell is emitted in the reactor. According to the pure oxygen aeration process, the pure oxygen is used, the air is used in the air aeration process, namely the oxygen concentration of the air source is different, the high oxygen dissolution rate and the high oxygen concentration of the pure oxygen aeration process accelerate the metabolism of microorganisms, so that the number of the microorganisms, namely the concentration of sludge, is increased, the reaction rate is accelerated, and the sewage treatment efficiency is greatly improved. The aerator used for pure oxygen aeration and the air aerator can be universal and can be properly adjusted according to different air volumes. In addition, pure oxygen (or oxygen-enriched oxygen) is adopted to replace air aeration, and the concentration of dissolved oxygen can be flexibly adjusted according to the process requirement, so that the aeration process has good performance. The driving force of oxygen in water and the transfer rate of oxygen are obviously improved, and the penetrating power to activated sludge particles is strong. Because the concentration of the mixed liquid sludge in the pure oxygen aeration reactor is higher than that of the mixed liquid sludge in the air aeration reactor, the hydraulic retention time and the volume of the pure oxygen aeration reactor are far lower than those of the air aeration reactor under the condition of the same sewage treatment capacity. The pure oxygen aeration system has much lower noise than the blast aeration system, and basically has no gas escape of volatile organic compounds, thereby reducing the adverse effect of the sewage treatment plant on the ambient environment.
Referring to fig. 2 to 9, in other embodiments, the aeration pipe 408 may be mechanically moved, and the aeration head 409 is disposed on the aeration pipe 408 and is communicated with the aeration pipe 408. Specifically, the aerator pipe 408 may be connected to an output end of a rotational driving motor, so that the aerator pipe 408 performs a rotational motion around a geometric center line of a shape formed by the aerator pipe 408. In other embodiments, the aeration pipe 408 may be connected to an output end of a hydraulic driving motor, and the aeration pipe 408 is moved by the hydraulic driving motor, specifically, the aeration pipe 408 may be moved in a vertical direction in the inner casing, or may be moved in a horizontal direction in the inner casing. In other embodiments, when the aeration tube 408 can be connected to the output end of the rotation driving motor, the pure oxygen supply device 407 can be connected to the aeration tube 408 by a shaft, and specifically, for example, an output pipeline can be connected to the output end of the pure oxygen supply device 407, and one end of the output pipeline can be connected to the aeration tube 408 by a shaft, so that when the aeration tube 408 is rotated by the rotation driving motor, the output pipeline does not rotate, and thus the normal operation of the pure oxygen supply device 407 is not affected. In other embodiments, when the aeration tube 408 is connected to the output end of the hydraulic driving motor, an elastic tube may be used between the pure oxygen supply device 407 and the aeration tube 408, so that when the aeration tube 408 moves, the elastic tube stretches or contracts, thereby not affecting the normal operation of the pure oxygen supply device 407.
Referring to fig. 2 to 9, in another embodiment, the pure oxygen supply device 407 may further communicate with the dissolved oxygen tank 413, introduce pure oxygen or ozone into the dissolved oxygen tank 413 to obtain an oxygen-containing liquid, and then introduce the oxygen-containing liquid into the aeration pipe 408, for example, a plurality of nozzles 421 may be disposed on the aeration pipe 408, for example, the nozzles 421 with adjustable flow rate may be adopted to spray the oxygen-containing liquid into the inner shell 403, so that the sewage, the oxygen and the filler 405 are fully mixed and collided, and the oxygen content is further increased due to the oxygen pre-dissolving process. In the aerobic moving bed biofilm reaction system 400, the dissolved oxygen concentration is an important control parameter, the level of the dissolved oxygen concentration in the reactor directly influences the removal efficiency of organic matters and the growth of activated sludge, and the effective operation control of the aeration process is a very important aspect. The dissolved oxygen supply of the system is insufficient, the metabolism of the microorganism is influenced, the removal efficiency of the pollutants is reduced, the dissolved oxygen of the system is too high, the microorganism carries out consumption endogenous respiration, the amount of the activated sludge is reduced, the flocculent structure of the activated sludge is damaged, and meanwhile, the energy is wasted. In the embodiment, the oxygen concentration at the water outlet end of the reactor can be controlled to be 2 mg/L. In other embodiments, for the removal of organic pollutants which are difficult to be biodegraded, higher oxygen concentration can be adopted, the microbial activity can be improved, and the pollutant removal effect can be improved, for example, the dissolved oxygen concentration in the reactor can be controlled to be 6mg/L when petrochemical wastewater is treated. In addition, because the low oxygen concentration is always considered to be one of the main factors causing filamentous bacterium sludge bulking, filamentous bacteria have a larger specific surface area and a lower oxygen saturation constant and proliferate faster than flocculent bacteria under the low oxygen concentration, so that the filamentous bacterium sludge bulking is caused, and the pure oxygen aeration can maintain the higher oxygen concentration in the reactor, so that the filamentous bacterium sludge bulking can be effectively avoided. The main principle of aerobic biological treatment of waste water is to convert organic matters in the waste water into carbon dioxide, water and energy by utilizing the metabolic activity of microorganisms, and simultaneously, the microorganisms are proliferated. The number of microorganisms in the reactor determines the capacity of the reactor. Under certain conditions, the higher the sludge concentration in the reactor, the greater the pollutant degradation amount, i.e., the higher the feed load that the reactor can bear. The sludge concentration has great relation with the treatment process, the water inlet characteristic and the operation mode. The pure oxygen aeration mode enables high sludge concentration to enable high-load feeding, and the high load brings benefits of reducing occupied area and the like. Meanwhile, the higher the sludge concentration of the mixed liquid in the reactor is, the lower the total nitrogen of the effluent is, and the more obvious the synchronous nitrification-denitrification is. Since pure oxygen aeration can maintain higher sludge concentration and higher dissolved oxygen concentration can enhance the activity of microorganisms, namely the number of the microorganisms in the reactor is increased and the activity is enhanced, the same reactor can treat more wastewater, and the reactor has higher feeding load and removal load. Under the same sludge load condition, along with the increase of the dissolved oxygen concentration in the reactor, the sludge yield shows a trend of reduction, and the control of higher dissolved oxygen concentration can reduce the residual sludge amount and save the sludge treatment cost. At the same dissolved oxygen concentration level, the sludge yield of the system increases with increasing sludge load. The reactor contains a relatively large number of microorganisms, and the available substrate is low, i.e., the initial energy level is low, the growth of the microorganisms is mainly reflected in the accumulation of molecular aggregates in cells and the individual growth, and no or only few cells will proliferate, and when the sludge concentration is low and the feed load is high, relatively more substrate is provided for the small number of microorganisms, the initial energy level is high, so that it is possible to provide enough energy to complete various reactions in the cell division and proliferation process, such as the reactions for synthesizing ferment, protein and nucleic acid, etc., and the number of cells is increased. That is, the amount of the substrate consumed for producing biomass per unit mass at a higher sludge load is relatively large, and the amount of the excess sludge is large, so that the discharge of the excess sludge can be reduced by controlling a higher sludge concentration and a lower sludge load in the reactor, and in this embodiment, the amount of the excess sludge can be reduced by 30%, for example, so that the sludge disposal cost is saved. Pure oxygen aeration can remove various volatile organic compounds, for example, aromatic hydrocarbons (benzene, toluene, xylene, etc.), aliphatic hydrocarbons (butane, gasoline, etc.), halogenated hydrocarbons (carbon tetrachloride, chloroform, vinyl chloride, freon, etc.), alcohols (methanol, butanol, etc.), aldehydes (formaldehyde, acetaldehyde, etc.), ketones (acetone, etc.), ethers (diethyl ether, etc.), esters (ethyl acetate, butyl acetate, etc.), and the like. When the wastewater containing volatile organic compounds is treated, the air aeration causes a large amount of volatile organic compounds in the wastewater to volatilize into the air, which causes great influence on the surrounding environment, while the pure oxygen aeration is adopted to treat the wastewater, the amount of waste gas generated in the process is very small, which is only 1% -2% of that of the traditional air aeration method, most of volatile organic compounds are adsorbed by sludge and finally degraded into harmless substances, and the influence of the volatile organic compounds on the environment is avoided. Pure oxygen aeration can solve the problem of foam, almost all sewage treatment plants have the problem of foam, and the generated foam has great proportion to the water quality of inlet water. When the foam is serious, a large amount of sludge can be brought out, so that the aerobic biological treatment system is paralyzed. In addition, environmental problems associated with foam are also important and can cause significant inconvenience to the operation. Evidence suggests that increasing the sludge concentration in the reactor may alleviate the foaming problem to some extent. Meanwhile, the aeration quantity also has important influence on the generation of foam, and pure oxygen aeration can adopt small aeration quantity, so that the problem of foam is avoided. The comparison of pure oxygen aeration and air aeration shows that the pure oxygen aeration can reduce the influence of volatile organic compounds in the wastewater on the environment, can avoid the adverse effect of foam on the operation, can ensure that the concentration of dissolved oxygen in the reaction tank reaches a higher level, has higher feeding load and strong impact resistance, can reduce the output of residual sludge, can ensure that high-load feeding becomes possible, can greatly reduce the floor area of the reaction tank, and has the water quality of the pure oxygen aeration which is obviously higher than that of the outlet water of the air aeration.
Referring to fig. 2 to 9, in other embodiments, the moving bed biofilm reaction system 400 of the present invention may further include a control system, and the control system is connected to the aeration pipe 408 and the aeration head 409. The aerator pipe is mechanically moved under the action of the control system. In other embodiments, the control system is connected to the driving motor 412, the driving motor 412 enables the aeration tube 408 to perform mechanical motion, the aeration tube 408 can be set in a rotating manner, for example, can be set in a lifting manner, can be set in a swinging manner, or can perform mechanical motion in all forms such as regular motion setting in XYZ directions, specifically, in this embodiment, the aeration tube 408 can perform rotational motion, specifically, for example, a rotating motor is installed on the housing 402, an output shaft of the rotating motor is connected to the aeration tube 408, and can drive the aeration tube 408 to rotate, for example, the rotating motor is installed on the top of the housing 402 and connected to one end of the vertical rod of the "t" shaped aeration tube 408, and the "t" shaped aeration tube 408 is driven to rotate by the rotating motor, so that the aeration tube 408 can perform mechanical stirring function while the aeration head 409 releases pure oxygen, thereby enabling the sewage, oxygen, and the filler 405 to be more sufficiently, And (3) collision further promotes the activated sludge attached to the filler 405 to degrade pollutants, and the treated water passes through the filter screen and is discharged from the water outlet pipe 404. In other embodiments, also can set up mechanical stirring device alone in the reactor, the agitating unit shape can be confirmed according to the reactor shape, it is wear-resisting durable to pack, agitating unit adopts the stirring vane of banana type, appearance profile lines is soft, do not damage the filler, whole stirring and aeration system maintain the management very easily, because the filler improves oxygen transfer efficiency to the cutting effect of bubble, can use perforation aeration to improve aeration system security, the extension overhauls the cycle, through agitating unit sewage in to the reactor, oxygen, the filler 405 three stirs, make its more abundant mixture, the collision. In other embodiments, part of the aeration heads 409 may be distributed on the sidewall of the inner shell 403, and the outlet direction is tangential to the sidewall of the inner shell 403, and pure oxygen released by the aeration heads 409 may form a circular flow around the circumferential direction of the sidewall of the inner shell 403, so as to further promote the flow of the filler 405, so that the sewage, the oxygen and the filler 405 are more fully mixed and collided, further promoting the degradation of the pollutants by the activated sludge attached to the filler 405, and avoiding the generation of dead corners. In other embodiments, a plurality of baffles may be further disposed on the inner wall of the inner shell 403, and the baffles may form any angle with the side wall, so that when pure oxygen is sprayed out from each aeration head 409 of the aeration pipe 408 or oxygen-containing liquid is sprayed out from each spray head 421, the pure oxygen or the oxygen-containing liquid may be further dispersed under the blocking effect of the baffles, thereby further promoting the mixing of the sewage, the oxygen, and the filler 405.
Referring to fig. 10, in other embodiments, the moving bed biofilm reaction system 400 of the present invention may further include: a first aeration pipe 4081, a plurality of spray heads 421, a second aeration pipe 4082 and a plurality of aeration heads 409. The first aeration pipe 4081 is disposed in the inner casing 403 and is communicated with the dissolved oxygen tank 413, the plurality of nozzles 421 are disposed on the first aeration pipe 4081 and are communicated with the first aeration pipe 4081, the direction of the nozzles 421 is different, and the flow rate of the dissolved oxygen liquid of the nozzles 421 is adjustable. Specifically, shower nozzle 421 can include shower nozzle 421 outer shell and shower nozzle 421 inner shell, be equipped with first liquid hole and second on shower nozzle 421 outer shell and the shower nozzle 421 inner shell respectively and go out the liquid hole, first liquid hole and second go out the liquid hole and align control system's effect allows shower nozzle 421 inner shell is relative shower nozzle 421 outer shell rotates, makes first liquid hole and the second changes of going out the coincidence area in liquid hole, and then changes the dissolved oxygen liquid play liquid measure of shower nozzle 421. A second aeration pipe 4082 is provided in the inner case 403 and communicates with the pure oxygen supply device 407, and a plurality of aeration heads 409 are provided on the second aeration pipe 4082 and communicate with the second aeration pipe 4082. In some embodiments, the second aeration pipe 4082 may be disposed on the side of the first aeration pipe 4081 close to the side wall of the inner housing 403, the plurality of aeration heads 409 may face the direction of the first aeration pipe 4081, and the plurality of aeration heads 409 may face different directions. The first and second aeration pipes 4081 and 4082 may move mechanically under the action of the control system, for example, in this embodiment, the second aeration pipes 4082 are disposed in a staggered manner, for example, in an "t" shape, the first aeration pipe 4081 is disposed in a "U" shape, and the first aeration pipe 4081 surrounds the outside of the second aeration pipe 4082, in this embodiment, the second aeration pipe 4082 may move in a rotating manner, for example, and the first aeration pipe 4081 may move in a swinging manner, for example, specific embodiments have been described in detail in other embodiments, which are not described herein again, and it is understood that in other embodiments, other arrangement forms and movement forms may also be adopted, and all technical features in the foregoing embodiments may be combined arbitrarily, which is not limited herein. In some other embodiments, the moving bed biofilm reaction system 400 of the present invention may further include a flow controller, the flow controller is disposed at the liquid outlet end of the dissolved oxygen tank 413, and controls the liquid outlet amount of the dissolved oxygen liquid of the spray head 421, so as to achieve the purpose of adjusting the oxygen content in the system. The utility model discloses an in the moving bed biomembrane reaction system 400 through with pure oxygen supply arrangement 407 and dissolved oxygen pond 413 intercommunication, let in pure oxygen or ozone in dissolving oxygen pond 413, carry out the process of dissolving in advance of oxygen, obtain oxygen-containing liquid, for example, let in a plurality of shower nozzles 421 that are equipped with on the first aeration pipe 4081 with this oxygen-containing liquid again, spray oxygen-containing liquid in the inner shell, thereby make sewage, oxygen, the abundant mixture of filler 405 three, the collision, owing to passed through the process of dissolving in advance of oxygen, make the oxygen content further improve, thereby the decontamination efficiency of effectual improvement organic matter to sewage. The utility model discloses can also let in pure oxygen and oxygen-containing liquid simultaneously in the system to can detect and control the various oxygen content of system, thereby can make the system have suitable oxygen content, further improve the decontamination efficiency of organic matter to sewage.
Referring to fig. 11, in other embodiments, one end of the aeration tube 408 may be fixed on one side wall of the inner shell 403, the other end of the aeration tube 408 extends to the other side wall of the inner shell 403 along the diameter direction of the inner shell 403, and is fixed with the other side wall of the inner shell 403, the aeration pipe 408 has at least one bending part, specifically, the aeration pipe 408 is, for example, arranged in a "U" shape or in an "M" shape or in a "V" shape, a second driving motor 4122 is respectively fixed on two side walls of the inner shell close to two ends of the aeration pipe 408, the second driving motor 4122 is rotatably connected with two ends of the aeration pipe 408, the second driving motor 4122 is started, the U-shaped aeration pipe 408 can swing around the two ends in the inner shell 403, thereby enabling the sewage, the oxygen and the filler 405 to be more fully mixed and collided, and further promoting the activated sludge attached to the filler 405 to degrade pollutants. In other embodiments, the aeration head 409 may further include an outer shell of the aeration head 409 and an inner shell of the aeration head 409, the outer shell of the aeration head 409 and the inner shell of the aeration head 409 are respectively provided with a first aeration hole and a second aeration hole, and the first aeration hole and the second aeration hole are aligned. In other embodiments, the control system allows the inner shell of the aeration head 409 to rotate relative to the outer shell of the aeration head 409, so that the overlapping area of the first aeration hole and the second aeration hole is changed, thereby changing the aeration flow rate, and the aeration amount is adjusted according to the sewage treatment amount by the aeration head 409 capable of adjusting the aeration flow rate, thereby achieving the purpose of saving energy on the premise of ensuring the sewage treatment quality.
Referring to fig. 12 and 13, in some embodiments, the moving bed biofilm reaction system 400 may further include a sealed outer shell 402 and an inner shell 403, a plurality of chambers connected in series are disposed in the inner shell 403, each chamber is disposed with a suspension packing 405, one side of each chamber connected in series is communicated with the water inlet pipe 401, the other side is communicated with the water outlet pipe 404, a water distribution pipe 410 is further disposed in the outer shell 402, the water distribution pipe 410 is disposed on one side of the top wall or the bottom wall of the inner shell 403, the water distribution pipe 410 is communicated with the water inlet pipe 401, the water distribution pipe 410 is disposed with a plurality of water distribution ports 411, the moving bed biofilm reaction system 400 further includes an aeration pipe 408, the aeration pipe 408 is communicated with the pure oxygen supply device 407, one side of each chamber connected in series passes through the plurality of chambers connected in series, the aeration pipe 408 is disposed on the opposite side of the water distribution pipe 410 in the inner shell 403, the aeration pipe 408 is further disposed with a plurality, during operation, sewage enters from the water inlet pipe 401 through the first power pump, is distributed in the water distribution pipes 410, enters the inner shell 403 of the reactor from the water distribution ports 411, pure oxygen is sprayed out from the aeration heads 409 of the aeration pipes 408, the sewage, the oxygen and the filler 405 are mixed and collided with each other in the inner shell 403, activated sludge attached to the filler 405 degrades pollutants, and the treated water passes through the filter screen and is discharged from the water outlet pipe 404.
Referring to fig. 12 and 13, in other embodiments, the moving bed biofilm reaction system 400 of the present invention comprises: a plurality of chambers connected in series, a pure oxygen supply 407, a plurality of screws 420, a plurality of first aeration tubes 4081, and a first driving motor 4121. In this embodiment, the moving bed biofilm reaction system 400 may further include an oxygen dissolving tank 413, one end of the oxygen dissolving tank 413 is communicated with the pure oxygen supply device 407, the other end of the oxygen dissolving tank 413 passes through the housing 402 and is communicated with the plurality of chambers connected in series, meanwhile, the moving bed biofilm reaction system 400 further includes a plurality of first aeration pipes 4081, and the first aeration pipes 4081 are disposed in the plurality of chambers connected in series and are communicated with the oxygen dissolving tank 413. In this embodiment, a plurality of screws are further provided, each screw 420 is vertically arranged in each chamber, each first aeration pipe 4081 is vertically sleeved on the screw 420, and is in threaded connection with each screw rod 420, allows the first aeration pipe 4081 to move along the extending direction of the screw rods 420, and the first driving motor 4121 is connected with one end of each screw rod 420, allows the first driving motor 4121 to drive the screw rods 420 to rotate, enables the first aeration pipe 4081 sleeved on the screw rods 420 to move along the extending direction of the screw rods 420, enables the first aeration pipe 4081 to play a role of mechanical stirring in the chamber, the sewage, the oxygen and the filler 405 are stirred to be more fully mixed and collided, a plurality of nozzles 421 are arranged on the first aeration pipe 4081, the plurality of spray heads 421 are obliquely arranged, and the adjacent spray heads 421 are arranged at an included angle of 45 degrees, so that the coverage range can be maximized when all the spray heads 421 spray oxygen-containing liquid at the same time. The embodiment further comprises a second aeration pipe 4082, wherein the second aeration pipe 4082 is further provided with a plurality of aeration heads 409, and the plurality of aeration heads 409 can be obliquely arranged. The second aeration pipe 4082 is arranged on the side, close to the bottom of the inner shell 403, of the first aeration pipe 4081, the spray head 421 is arranged on the first aeration pipe 4081, the spray head 421 is communicated with the first aeration pipe 4081, the flow rate of the spray head 421 can be adjusted, and the oxygen-containing liquid in the spray head 421 is sprayed and then mixed with oxygen exposed by the second aeration pipe 4082 instantaneously, which is beneficial to improving the concentration of dissolved oxygen in the system. The moving bed biofilm reaction system 400 can further comprise a flow controller, wherein the flow controller is arranged at the communication position of the first aeration pipe 4081 and the dissolved oxygen tank 413, and the flow controller is used for controlling the amount of the oxygen-containing liquid in the aeration system, so that the oxygen content in the system is controlled. In some embodiments, the moving bed biofilm reaction system 400 can further include an ozone supply device 417, and the ozone supply device 417 is in communication with the second aeration pipe 4082, the function of which is described in detail above and will not be described herein again. In some embodiments, the moving bed biofilm reaction system 400 may further include a second driving motor 4122, the second driving motor 4122 is connected to the second aeration pipe 4082, and allows the second driving motor 4122 to drive the second aeration pipe 4082 to make a mechanical motion, for example, in this embodiment, the second aeration pipe 4082 is U-shaped, two ends of the U-shaped are rotatably installed on two sidewalls of the chamber, and the second driving motor 4122 may drive the second aeration pipe 4082 to swing around two ends thereof.
Referring to fig. 14 and 15, in another embodiment, the moving bed biofilm reaction system 400 can also adopt a structure form that an anaerobic reactor 414 is combined with an aerobic reactor 415, and specifically, the moving bed biofilm reaction system 400 can include a water inlet pipe 401, an anaerobic reactor 414, an aerobic reactor 415, and a water outlet pipe 404. Wherein the anaerobic reactor 414 is communicated with the water inlet pipe 401, the aerobic reactor 415 is communicated with the anaerobic reactor 414, and the water outlet pipe 404 is communicated with the aerobic reactor 415. The aerobic reactor 415 can include an outer shell 402, an inner shell 403, suspended packing 405, and a pure oxygen supply 407. The inner shell 403 is filled with suspended filler 405, the filler 405 is sponge particles with a diameter of 5-10mm, for example, the aerobic reactor 415 further comprises a water distribution pipe 410 arranged between the inner shell 403 and the outer shell 402, the water distribution pipe 410 is provided with a plurality of water distribution ports 411 penetrating through the inner shell 403, the pure oxygen supply device 407 comprises a pure oxygen supply device 407, an aeration pipe 408 and aeration heads 409, in some embodiments, the aeration pipe 408 is arranged on the inner shell 403, the aeration pipe 408 is in an inverted T shape, the aeration heads 409 are arranged around the aeration pipe 408, and the direction of the aeration heads 409 at the lowest side is downward and the directions of the other aeration heads 409 are different. In other embodiments, the aeration pipe 408 may be a "one" type, and a plurality of aeration heads 409 are disposed on the aeration pipe 408, and the pure oxygen supply device 407 releases pure oxygen into the inner shell 403. The anaerobic reactor 414 is internally provided with a mechanical stirring device, the mechanical stirring device and a driving motor 412 are continuously stirred in the anaerobic reactor 414 under the driving of the driving motor 412, so that the sewage and the filler 405 are mixed more uniformly, when in operation, the sewage enters the anaerobic reactor 414 from the water inlet pipe 401 through a first power pump, primary treatment is carried out under the action of anaerobic bacteria, the treated sewage enters the aerobic reactor 415 again and is distributed in the water distribution pipes 410, the sewage enters the inner shell 403 of the aerobic reactor 415 from each water distribution port 411, pure oxygen is sprayed out from each aeration head 409 of the aeration pipe 408, the sewage, the oxygen and the filler 405 are mixed and collided with each other in the inner shell 403, the active sludge attached to the filler 405 degrades the pollutants, and the treated water passes through a filter screen and is discharged from the water outlet pipe 404.
Referring to fig. 14 and 15, in other embodiments, the moving bed biofilm reaction system 400 can also be configured by combining an anoxic reactor 416, an anaerobic reactor 414 and an aerobic reactor 415, wherein the anoxic reactor 416 is communicated with the water inlet pipe 401, the anaerobic reactor 414 is communicated with the anoxic reactor 416, the aerobic reactor 415 is communicated with the anaerobic reactor 414, the aerobic reactor 415 is communicated with the water outlet pipe 404, the pure oxygen supply device 407 is communicated with the aerobic reactor 415, the water outlet pipe 404 of the aerobic reactor 415 is also communicated with the water inlet pipe 401 of the anoxic reactor 416, a plurality of series-connected chambers can be arranged in the aerobic reactor 415, the pure oxygen aeration adopts the staged gradual reduction aeration in the plurality of series-connected chambers, so that the discharged water is refluxed to the anoxic reactor 416 after the oxygen content is reduced, therefore, the denitrification effect is better, and the cyclic utilization can be realized, which is beneficial to improving the energy utilization rate. In other embodiments, the moving bed biofilm reaction system 400 can further comprise a primary sedimentation tank 418 disposed at the front end of the anoxic reactor 416 and a secondary sedimentation tank 419 disposed at the rear end of the aerobic reactor 415 to facilitate better sewage treatment. The sewage containing sludge from the outlet pipe 404 of the aerobic reactor 415 can enter a secondary sedimentation tank 419 for further sedimentation, wherein part of the sludge flows back to the anoxic reactor 416 and the anaerobic reactor 414 for recycling, and part of the residual sludge enters a sludge collecting well 420 for discharge. Specifically, the sewage after passing through the primary sedimentation tank 418 enters the anoxic reactor 416 and the anaerobic reactor 414 to be merged with the return water of the return sludge and the secondary sedimentation tank 419, the sewage enters the aerobic reactor 415 after being denitrified and dephosphorized in the anoxic reactor 416 and the anaerobic reactor 414 to be aerated by pure oxygen, the oxygen supply device 407 supplies oxygen to the aerobic reactor 415 for aeration, the discharged water is disinfected after being removed of the sludge in the secondary sedimentation tank 419, part of the discharged water returns to the anoxic reactor 416 and the anaerobic reactor 414, and the residual sludge is discharged from the sludge collecting well 420.
Referring to fig. 14 and 15, in other embodiments, the moving bed biofilm reaction system 400 of the present invention comprises: the system comprises a water inlet pipe 401, an anoxic reactor 416, an anaerobic reactor 414, an aerobic reactor 415, a dissolved oxygen tank 413, a water quality detection device, a first water outlet pipe 4041, a first control valve, a second water outlet pipe 4042, a pure oxygen supply device 407 and a control system. Wherein, the anoxic reactor 416 is communicated with the water inlet pipe 401, the anoxic reactor 416 is communicated with the anaerobic reactor 414, the aerobic reactor 415 is communicated with the anaerobic reactor 414, and the aerobic reactor 415 comprises an outer shell 402, an inner shell 403 and a filler 405 arranged in the inner shell 403. The water quality detection device is arranged in the aerobic reactor 415, a first water outlet pipe 4041 is communicated with the aerobic reactor 415, a first control valve is arranged at the position where the first water outlet pipe 4041 is communicated with the aerobic reactor 415, and the first control valve is communicated with the water quality detection device. The water quality to be discharged is detected by the water quality detection device, when the water quality reaches the discharge standard, the first control valve is opened, and the purified water is discharged through the first water outlet pipe 4041. One end of the second water outlet pipe 4042 is communicated with the anoxic reactor 416, and the other end thereof is communicated with the aerobic reactor 415, so as to allow water in the second water outlet pipe 4042 to flow from the aerobic reactor 415 to the anoxic reactor 416, and a water quality detection device is used for detecting the water quality to be drained, when the water quality does not reach the discharge standard, the first control valve is closed, and sewage in the aerobic reactor 415 flows to the anoxic reactor 416 through the second water outlet pipe 4042, so as to form a closed loop system for sewage treatment, so as to achieve a more efficient and high-quality sewage treatment effect. The pure oxygen supply device 407 is communicated with the aerobic reactor 415, and exposes pure oxygen into the reaction system to ensure the oxygen content in the aerobic reactor 415, so as to effectively improve the sewage treatment effect in the aerobic reactor 415, in the sewage treatment closed loop system, the oxygen content in the aerobic reactor 415 is higher, when sewage which does not reach the discharge standard enters the anoxic reactor 416, the oxygen content is reduced to reach the standard of stain removal reaction in the anoxic reactor, after the sewage is treated by the anoxic reactor 416, the sewage enters the anaerobic reactor 414, at this time, the oxygen content is further reduced, so that the standard of stain removal reaction in the anaerobic reactor 414 can be ensured. The control system is connected with the pure oxygen supply device 407, the water quality detection device and the first control valve. In some embodiments, the moving bed biofilm reaction system 400 of the present invention may further include a dissolved oxygen tank 413, one end of the dissolved oxygen tank 413 is communicated with the pure oxygen supply device 407, and the other end of the dissolved oxygen tank 413 passes through the outer shell of the aerobic reactor 415 and is communicated with the inner shell of the aerobic reactor 415. In some embodiments, a first aeration pipe 4081 is disposed in the aerobic reactor 415, the first aeration pipe 4081 is communicated with the dissolved oxygen tank 413, a spray head 421 is disposed on the first aeration pipe 4081, and the spray head 421 is communicated with the first aeration pipe 4081. In some embodiments, a second aeration pipe 4082 may be further disposed in the aerobic reactor 415, the second aeration pipe 4082 is communicated with the pure oxygen supply device 407, an aeration head 409 is disposed on the second aeration pipe 4082, and the aeration head 409 is communicated with the second aeration pipe 4082. The aerobic reactor 415 may further be provided with an oxygen content detecting device for detecting the oxygen content in the aerobic reactor 415, a second control valve is provided at a communication position of the second aeration pipe 4082 and the aerobic reactor 415, the second control valve is connected to the control system, the control system controls opening and closing of the second control valve, so as to control the amount of pure oxygen to be aerated into the reaction system, when the oxygen content in the aerobic reactor 415 exceeds a threshold value, the second control valve is closed, the second aeration pipe 4082 stops aeration of the pure oxygen into the reaction system, when the oxygen content in the aerobic reactor 415 is lower than the threshold value, the second control valve is opened, and the second aeration pipe 4082 starts aeration of the pure oxygen into the reaction system, so as to ensure that the oxygen content in the aerobic reactor 415 is constant, which can ensure a decontamination effect of aerobic bacteria, and can avoid waste of energy. In this embodiment, the first aeration pipe 4081 and the second aeration pipe 4082 may also be connected to the control system, and the control system controls the first aeration pipe 4081 and the second aeration pipe 4082 to make mechanical movement.
Referring to fig. 16, the pure oxygen supply device 407 of the present invention can also be applied to a biological filter structure, wherein the biological filter structure comprises a housing, a supporting layer 500, a filtering material layer 600, a water distribution system and a pure oxygen supply device 407. The supporting layer 500 is located on one side of the shell close to the bottom wall, the filter material layer 600 is located on the supporting layer 500, the water distribution pipe 410 of the water distribution system can be arranged between the bottom wall of the shell and the supporting layer 500, and the water distribution port 411 of the water distribution system can penetrate through the supporting layer 500 to be communicated with the filter material layer 600. An aeration pipe 408 of the pure oxygen supply device 407 passes through the shell to be communicated with the filter material layer 600, and oxygen is aerated into the biological filter through an aeration head 409.
The above embodiments are not divided into independent embodiments, and the components and features of the embodiments can be combined and replaced with each other without departing from the basic principle, for example, the pure oxygen supply device 407 and the ozone supply device 417 in the above embodiments can be replaced with each other as required.
The selected embodiments of the present invention disclosed above are merely provided to help illustrate the present invention. The preferred embodiments are not intended to be exhaustive or to limit the invention to the precise embodiments disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and its practical applications, to thereby enable others skilled in the art to best understand the invention for and utilize the invention. The present invention is limited only by the claims and their full scope and equivalents.
Claims (10)
1. A moving bed biofilm reaction system, comprising:
a housing;
the inner shell is arranged in the outer shell, and suspended fillers are arranged in the inner shell;
the water inlet pipe penetrates through the outer shell and is communicated with the inner shell;
a water outlet pipe communicated with the housing;
a pure oxygen aeration device communicated with the inner shell;
an ozone supply device in communication with the inner housing.
2. A moving bed biofilm reaction system according to claim 1, wherein said pure oxygen aeration device comprises a pure oxygen supply device, said pure oxygen supply device being one of a cryogenic air separation oxygen generation device or a pressure swing adsorption oxygen generation device.
3. A moving bed biofilm reaction system according to claim 1, wherein the reaction system further comprises a water distribution pipe, and the water distribution pipe is arranged between the inner shell and the outer shell.
4. A moving bed biofilm reaction system according to claim 3, wherein a plurality of water distribution ports are formed on the water distribution pipe and penetrate through the inner shell.
5. A moving bed biofilm reaction system according to claim 1, wherein said pure oxygen aeration device further comprises an aeration pipe, one end of said aeration pipe is communicated with said pure oxygen aeration device, and the other end of said aeration pipe passes through said inner shell and is arranged in said inner shell.
6. A moving bed biofilm reaction system according to claim 5, wherein said ozone supply means is in communication with said aeration tubes.
7. A moving bed biofilm reaction system according to claim 5, wherein said pure oxygen aeration device further comprises a plurality of aeration heads, said plurality of aeration heads being disposed on said aeration tubes.
8. A moving bed biofilm reaction system according to claim 5, wherein said aeration pipe is arranged on the side of said inner shell close to the bottom wall.
9. A moving bed biofilm reaction system according to claim 5, wherein said aeration tubes are movable.
10. A wastewater treatment system, comprising:
a sewage tank;
a grid well in communication with the lagoon;
a conditioning tank in communication with the grid well;
a moving bed biofilm reaction system in communication with the conditioning tank, the moving bed biofilm reaction system comprising:
a housing;
the inner shell is arranged in the inner shell, and suspended fillers are arranged in the inner shell;
the water inlet pipe penetrates through the outer shell and is communicated with the inner shell;
a water outlet pipe communicated with the housing;
a pure oxygen aeration device communicated with the inner shell;
an ozone supply device in communication with the inner housing.
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112390365A (en) * | 2020-11-12 | 2021-02-23 | 广州创领水产科技有限公司 | Tri-oxygen microorganism nitrogen and phosphorus removal filter and method thereof |
| CN112678957A (en) * | 2020-12-24 | 2021-04-20 | 华北水利水电大学 | Electrically driven rotary aeration inversion A with multi-point water inlet2O + MBBR device |
| CN112678956A (en) * | 2020-12-24 | 2021-04-20 | 华北水利水电大学 | Oxygen deficiency-good oxygen MBBR integrated device based on electric drive rotary aeration |
| CN113197133A (en) * | 2021-05-13 | 2021-08-03 | 珠江水利委员会珠江水利科学研究院 | A integration culture apparatus for zooplankton hatching breeds |
| CN113800715A (en) * | 2021-09-15 | 2021-12-17 | 北京清河北苑水务有限公司 | Sewage treatment system and method |
| CN113788532A (en) * | 2021-09-27 | 2021-12-14 | 肇庆市鹏凯环保装备有限公司 | Water treatment circulating equipment and treatment method |
| CN116462282B (en) * | 2023-05-31 | 2023-09-26 | 广州市科翔环保有限公司 | Equipment for removing ultrahigh-concentration ammonia nitrogen wastewater by electrochemical method and treatment process thereof |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2850119C2 (en) * | 1978-11-18 | 1984-10-04 | Wilhelm Roediger GmbH + Co Haustechnik, 6450 Hanau | Device for lifting an aeration unit for liquids |
| ATE112754T1 (en) * | 1990-01-23 | 1994-10-15 | Kaldnes Miljoteknologi As | METHOD AND REACTOR FOR PURIFICATION OF WATER. |
| CN2737787Y (en) * | 2004-05-24 | 2005-11-02 | 北京科技大学 | Sewage treatment apparatus with swinging aeration head |
| US20090008311A1 (en) * | 2006-02-02 | 2009-01-08 | Jai-Hun Lee | Pure Oxygen Aeration System for Wastewater Treatment |
| CN202594841U (en) * | 2012-04-24 | 2012-12-12 | 广西益江环保科技有限责任公司 | Solar nanometer packing moving bed biofilm reactor |
| CN202576071U (en) * | 2012-05-10 | 2012-12-05 | 武汉市政工程设计研究院有限责任公司 | Rotary micropore aeration round ring coil system for sewage treatment |
| RU2015136629A (en) * | 2013-02-18 | 2017-03-23 | Мейпел Грин Энерджи Лтд | AEROUSED LAYER BIOFILM REACTOR |
| KR101617426B1 (en) * | 2015-07-24 | 2016-05-03 | 주식회사 송림 | Advanced water-treating apparatus |
| CN206298435U (en) * | 2016-12-30 | 2017-07-04 | 重庆博之鸣畜产品有限公司 | Aeration tank |
| CN206544952U (en) * | 2017-01-21 | 2017-10-10 | 深圳市宏利电镀制品有限公司 | Sewage disposal system |
| CN207726811U (en) * | 2017-12-06 | 2018-08-14 | 广西南宁科环环保科技有限公司 | A kind of moving bed biofilm reactor |
| CN209923032U (en) * | 2018-10-31 | 2020-01-10 | 苏州绿蓝环保服务有限公司 | Aeration equipment for waste water treatment |
| CN109553196A (en) * | 2019-01-11 | 2019-04-02 | 王涛 | A kind of anaerobic-aerobic multiple-hearth biofilm reactor and its technique |
| CN209471379U (en) * | 2019-02-26 | 2019-10-08 | 邢台天宏祥燃气有限公司 | A kind of gas discharge Intellectualized controller |
-
2020
- 2020-05-25 CN CN202010450038.4A patent/CN111675315A/en not_active Withdrawn
- 2020-05-25 CN CN202010451238.1A patent/CN111592102A/en not_active Withdrawn
- 2020-05-25 CN CN202010450035.0A patent/CN111675314A/en not_active Withdrawn
- 2020-05-25 CN CN202020895476.7U patent/CN212799819U/en active Active
- 2020-05-25 CN CN202020893796.9U patent/CN212799816U/en active Active
- 2020-05-25 CN CN202020893817.7U patent/CN213171657U/en active Active
- 2020-05-25 CN CN202020893841.0U patent/CN212799817U/en active Active
- 2020-05-25 CN CN202020895428.8U patent/CN212799818U/en active Active
- 2020-05-25 CN CN202010450034.6A patent/CN112939214B/en active Active
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|---|---|
| CN111675314A (en) | 2020-09-18 |
| CN111592102A (en) | 2020-08-28 |
| CN212799819U (en) | 2021-03-26 |
| CN112939214A (en) | 2021-06-11 |
| CN111675315A (en) | 2020-09-18 |
| CN213171657U (en) | 2021-05-11 |
| CN212799818U (en) | 2021-03-26 |
| CN112939214B (en) | 2022-11-11 |
| CN212799816U (en) | 2021-03-26 |
| CN212799817U (en) | 2021-03-26 |
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