CN214936359U - Multistage circulating flow moving bed biofilm reactor - Google Patents
Multistage circulating flow moving bed biofilm reactor Download PDFInfo
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- CN214936359U CN214936359U CN202121125134.8U CN202121125134U CN214936359U CN 214936359 U CN214936359 U CN 214936359U CN 202121125134 U CN202121125134 U CN 202121125134U CN 214936359 U CN214936359 U CN 214936359U
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Abstract
The utility model belongs to the technical field of sewage treatment, and particularly discloses a multistage circulating flow moving bed biofilm reactor, which comprises a first reaction tank and a second reaction tank, wherein the first reaction tank is an anoxic reaction tank or an anaerobic reaction tank, and the second reaction tank is an aerobic reaction tank; the water outlets of the first reaction tank and the second reaction tank are respectively provided with a perforated sieve pipe, the perforated sieve pipes are of cylindrical structures with one ends closed and the other ends open, and a plurality of water holes are uniformly distributed on the surfaces of the perforated sieve pipes. The reactor is provided with a multi-stage reaction tank and an internal reflux device, so that circulation is formed in the reactor, and a perforated sieve pipe is arranged at a water outlet, so that the problems of filler accumulation and loss are effectively avoided.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, more specifically relates to a multistage circulating flow removes bed biofilm reactor.
Background
The Moving Bed Biofilm Reactor (MBBR) has the principle that a certain amount of suspension carriers are added into the reactor to ensure that microorganisms are attached to and grow, the types of the microorganisms are increased, and the biomass is improved, so that the treatment effect and the effluent quality are improved. The density of the filler after film formation is close to that of the activated sludge mixed liquid, and the filler is in a fluidized state under the action of aeration and water flow, so that the mixing and mass transfer efficiency is improved. The MBBR has the advantages of short construction period, more biomass, stable process operation, strong impact load resistance and the like, saves investment, has low operation cost, is simple and convenient to manage, is suitable for centralized and decentralized treatment, is an economical and efficient sewage treatment process, and is particularly suitable for centralized and decentralized treatment and upgrading and reconstruction of the existing sewage plant. MBBR has been widely used in domestic and foreign fields for treatment of domestic sewage, industrial wastewater and landfill leachate and modification of traditional activated sludge process.
Most of the conventional MBBR reactors maintain the fluidization state of a filler carrier by virtue of the actions of aeration, water flow and a propeller (stirrer), but in practical engineering application, the problem of filler accumulation usually occurs, particularly in a water outlet area, so that the filler fluidization is insufficient, the treatment efficiency is low, and the quality of outlet water is reduced. Therefore, it is necessary to provide a moving bed biofilm reactor capable of improving the flow regime of the packing.
SUMMERY OF THE UTILITY MODEL
To the defect of prior art, the utility model aims to provide a multistage circulating flow removes bed biofilm reactor aims at solving and leads to the problem that the filler fluidization is not enough, sewage treatment efficiency is low, play water quality of water descends because the filler piles up in the current MBBR is used.
In order to realize the aim, the utility model provides a multistage circulating flow moving bed biofilm reactor, which comprises a first reaction tank and a second reaction tank which are communicated, wherein the first reaction tank is an anoxic reaction tank or an anaerobic reaction tank, and the second reaction tank is an aerobic reaction tank; suspended biological fillers are arranged in the first reaction tank and/or the second reaction tank;
one or more perforated sieve pipes are respectively arranged in the first reaction tank and the second reaction tank, one end of each perforated sieve pipe is closed, the other end of each perforated sieve pipe is open, and the pipe wall of each perforated sieve pipe is provided with a plurality of water through holes; the water through holes are used for enabling sewage to enter the perforated sieve pipe to be collected, and the suspended biological filler is blocked outside the perforated sieve pipe; the open end of the perforated sieve tube arranged in the first reaction tank is communicated with a first water outlet pipe, and the first water outlet pipe is used for conveying the sewage in the first reaction tank to the second reaction tank; the open end of the perforated sieve tube arranged in the second reaction tank is communicated with a second water outlet pipe, and the second water outlet pipe is used for discharging sewage in the second reaction tank; the size of the suspended biological filler is larger than that of the water through holes;
and a backflow module is arranged in the second reaction tank and used for enabling the sewage part in the second reaction tank to flow back into the first reaction tank.
Preferably, a first guide plate and a second guide plate are arranged in the first reaction tank and the second reaction tank respectively; the first guide plate is vertically arranged in the center of the first reaction tank and/or the second reaction tank along the length direction of the first reaction tank and the second reaction tank, and divides the first reaction tank and the second reaction tank into two galleries respectively; the second guide plate is arc-shaped and is arranged at two ends of the first reaction tank and the second reaction tank, and the arc-shaped opening of the second guide plate faces the first guide plate.
Preferably, the suspended biological filler is a flexible suspended filler, which is a spongy porous cube made of hydrophilic material.
Preferably, the reactor further comprises a primary reaction tank, the primary reaction tank is communicated with the first reaction tank through a water inlet pipe, the primary reaction tank is an anaerobic reaction tank, and the first reaction tank is an anoxic reaction tank.
Preferably, the backflow module comprises a backflow pipe and an internal backflow device, and a water outlet of the internal backflow device is communicated with the backflow pipe; the return pipe is used for returning the sewage part of the second reaction tank to the first reaction tank; the internal reflux device is a gas stripping reflux device or a reflux pump.
Preferably, the gas stripping reflux device is of a U-shaped structure and comprises a water collecting pipe, two 90-degree elbows, a lifting pipe and a gas pipe, the top ends of the water collecting pipe and the lifting pipe are provided with openings, the bottom end of the water collecting pipe is communicated with the bottom end of the lifting pipe through the two 90-degree elbows, and the gas pipe penetrates through the side wall of the lifting pipe and extends into the bottom in the lifting pipe;
a water inlet is formed in the side surface of the water collecting pipe and communicated with the open end of the other perforated sieve pipe arranged in the second reaction tank; a water outlet is arranged on the side surface of the lifting pipe and is communicated with the return pipe; the height of the water outlet is higher than that of the water inlet, and the height of the opening of the gas pipe in the lifting pipe is lower than that of the water outlet.
Preferably, the multistage circulating flow moving bed biofilm reactor further comprises an aeration system, wherein the aeration system comprises a blower, an aeration pipeline and an aeration head, and the aeration pipeline and the aeration head are arranged at the bottom of the second reaction tank.
Preferably, the multistage circulating flow moving bed biofilm reactor further comprises a plurality of submersible propellers, and the submersible propellers are arranged at the middle lower parts of the first reaction tank and the second reaction tank.
Preferably, the submersible is positioned upstream of the perforated screen.
Preferably, the multistage circulating flow moving bed biofilm reactor further comprises a water distributor, the bottom of the water distributor is perforated, the water distributors are arranged in the first reaction tank and the second reaction tank, and one end of the first water outlet pipe, which is far away from the first reaction tank, is communicated with the water distributor arranged in the second reaction tank; one end of the return pipe, which is far away from the second reaction tank, is communicated with a water distributor arranged in the first reaction tank.
Preferably, the flow rate of the mixed liquid in the first reaction tank and the second reaction tank is 0.25-0.5 m/s, and the flow rate of the mixed liquid at the water hole of the perforated sieve pipe is not higher than 0.2 m/s.
Generally, through the utility model discloses above technical scheme who conceives compares with prior art, has following beneficial effect:
(1) the utility model provides a multistage circulating flow removes bed biofilm reactor sets up two biochemical ponds of AO at least, throws suspended solid filler as required in A pond (oxygen deficiency or anaerobic reaction pond) and O pond (aerobic reaction pond), separates the filler of difference in two ponds and circulates separately, has improved the microorganism growing environment, improves the microorganism volume to improve sewage treatment efficiency.
(2) The utility model discloses the reactor goes out water department at each reaction tank and sets up the perforated sieve pipe, through the length of control perforated sieve pipe, cross water hole quantity and area size, the velocity of flow of control rivers through the perforated sieve pipe is equal or is less than the velocity of flow of rivers in the corridor with the corridor velocity of flow, when guaranteeing higher water efficiency, has avoided the biological filler of suspension in the reaction tank to pile up in perforated sieve pipe department, has avoided the loss of filler simultaneously.
(3) The utility model discloses the reactor sets up the guide plate, separate into two galleries with reaction tank at different levels, and set up underwater propeller in the suitable position of gallery, under underwater propeller's impetus, suspended biofilm carrier can be along with mixed liquid along gallery circulation flow in the reaction tank, has improved the flow state of packing, has avoided the one-way current of conventional reactor one side inflow one side play water to lead to packing and locate accumulational problem in a water, has prolonged the dwell time of suspended biofilm carrier in the reaction tank simultaneously, improves the treatment effect of sewage.
(4) The suspended biological filler added in the reactor of the utility model has larger specific surface area, can enrich more organisms and increase the volume load of the reactor; and the density of the suspended biological filler is close to that of water, the suspended biological filler can circularly flow in the reactor along with sewage, and organic matters, nitrogen, phosphorus and other substances in the sewage are efficiently degraded and converted through a biological film on the surface of the filler.
(5) The utility model discloses produce easily to the filler and pile up, the problem that the flow state is not good, multistage circulation flow has been proposed and has been removed bed biofilm reactor, the advantage of removing bed biofilm reactor has both been remain, can further improve treatment efficiency and play water quality of water, adopt multistage series connection can satisfy different treatment process's requirement, take different types of sewage treatment process such as "oxygen deficiency + good oxygen", "anaerobism + good oxygen" and "anaerobism + oxygen deficiency + good oxygen" according to different processing requirements, the range of application is wide, the improvement that is applicable to the MBBR technology and the upgrading transformation of the conventional activated sludge process of current sewage plant.
(6) The reactor of the utility model adopts an internal reflux device, and a reflux area is not required to be specially arranged, thereby reducing the occupied area; and a gas stripping reflux mode is adopted, so that the energy consumption is saved, and the operation cost is reduced.
(7) The utility model provides a multistage circulating flow removes bed biofilm reactor can be through carrying out the upgrading transformation and realize on the conventional activated sludge treatment equipment of current sewage plant, need not to produce again and change brand-new equipment, and the multistage circulating removes bed biofilm reactor filler that obtains is reformed transform and has overcome the accumulational technical defect of traditional removal bed biofilm reactor filler, is assisted with the high strength and the flexibility of multistage sewage treatment technology simultaneously, can show treatment effect such as improvement sewage nitrogen and phosphorus removal.
Drawings
FIG. 1 is a plan view of a multistage circulating flow moving bed biofilm reactor of the present invention;
FIG. 2 is a sectional view taken along line A-A of a multistage circulating flow moving bed biofilm reactor according to the present invention;
FIG. 3 is a B-B sectional view of the multistage circulating flow moving bed biofilm reactor of the present invention;
FIG. 4 is a schematic diagram of a stripping reflux unit in a multistage circulating flow moving bed biofilm reactor according to the present invention;
FIG. 5 is a schematic diagram of a perforated sieve tube in a multistage circulating flow moving bed biofilm reactor according to the present invention;
the same reference numbers will be used throughout the drawings to refer to the same or like elements or structures, wherein:
1-1 is a first reaction tank; 1-2 is a second reaction tank; 2-1 is a first guide plate; 2-2 is a second guide plate; 3 is a perforated sieve tube; 3-1 is a water collecting part; 3-2 is an interface part; 4 is a water inlet pipe; 5 is a first water outlet pipe; 6 is a second water outlet pipe; 7 is a return pipe; 8 is an internal reflux device; 8-1 is a water collecting pipe; 8-2 is a 90-degree elbow; 8-3 is a riser; 8-4 is a gas conveying pipe; 9-1 is an aeration pipe; 9-2 is an aeration head; 10 is a diving propeller; and 11 is a water distributor.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
A multi-stage circulating flow moving bed biofilm reactor is shown in a figure 1, a figure 2 and a figure 3 and comprises a first reaction tank 1-1, a second reaction tank 1-2, a first guide plate 2-1, a second guide plate 2-2, a perforated sieve pipe 3, a water inlet pipe 4, a first water outlet pipe 5 and a second water outlet pipe 6, wherein the first reaction tank 1-1 is an anoxic reaction tank or an anaerobic reaction tank, and the first reaction tank 1-2 is an aerobic reaction tank.
The first guide plate 2-1 is vertically arranged in the center of the first reaction tank 1-1 and/or the second reaction tank 1-2 along the length direction of the first reaction tank 1-1 and the second reaction tank 1-2, and divides the first reaction tank 1-1 and the second reaction tank 1-2 into two galleries; the second guide plates 2-2 are arc-shaped, the number of the second guide plates in each reaction tank is two, the second guide plates are arranged at two ends of the first reaction tank 1-1 and the second reaction tank 1-2, and arc-shaped openings of the second guide plates 2-2 face the first guide plates 2-1; therefore, the suspended biological filler can circularly flow along with the mixed liquid in the reaction tank, the flow state of the filler is improved, and the problem that the filler is accumulated at the water outlet position due to the unidirectional flow of the water at the water inlet side and the water outlet side of the conventional reactor is solved. The ratio of the corridor width to the effective water depth is preferably 1 to 2.
The perforated sieve tube 3 is of a cylindrical structure with one closed end and the other open end, and a plurality of water through holes are distributed on the surface of the perforated sieve tube; the water holes are used for enabling sewage to enter the perforated screen pipe 3 to be collected, and the suspended biological filler is blocked outside the perforated screen pipe 3. The open end of the perforated sieve tube 3 arranged in the first reaction tank 1-1 is communicated with the first water outlet pipe 5; and the open end of the perforated sieve tube 3 arranged in the second reaction tank 1-2 is communicated with the second water outlet pipe 6.
One side of the first reaction tank 1-1 is connected with a water inlet pipe 4, the other side of the first reaction tank is connected with a first water outlet pipe 5, one side of the second reaction tank 1-2 is connected with the first water outlet pipe 5, the other side of the second reaction tank is connected with a second water outlet pipe 6, and the first water outlet pipe 5 is used for introducing sewage in the first reaction tank 1-1 into the second reaction tank 1-2; suspended biological fillers are arranged in the first reaction tank 1-1 and/or the second reaction tank 1-2; the size of the suspended biological filler is larger than that of the water through holes.
A backflow module is arranged in the second reaction tank and comprises a backflow pipe 7 and an internal backflow device 8, and a water outlet of the internal backflow device 8 is communicated with the backflow pipe 7; the return pipe 7 and the internal reflux device 8 are used for returning the sewage of the second reaction tank 1-2 to the first reaction tank 1-1.
When the reactor works, sewage flows into the first reaction tank 1-1 through the water inlet pipe 4 and then flows into the second reaction tank 1-2 through the perforated sieve pipe 3 and the first water outlet pipe 5 in sequence, one part of mixed liquid in the second reaction tank 1-2 flows out through the second water outlet pipe 6, and the other part of mixed liquid flows back into the first reaction tank 1-1 through the internal reflux device 8 and the reflux pipe 7 in sequence; by controlling the total area of the water passing holes on the surface of the perforated sieve pipe, the flow speed of water passing through the water passing holes is lower than that of the water in the gallery, so that the suspended biological filler is prevented from being accumulated.
In order to meet the requirements of different process conditions, the multistage circulating flow moving bed bio-membrane reactor can be formed by connecting different reaction tanks such as two stages or three stages in series in sequence. The reactor can be formed by connecting two or more than two anoxic/anaerobic reaction tanks and aerobic reaction tanks which are separated and communicated through pipelines in series, so that the microorganisms in each reaction tank can improve the activity of the microorganisms and keep enough biomass under the optimal condition to achieve good biological treatment effect. For example, when the reactor is formed by connecting two reaction tanks in series, the reactor comprises a first reaction tank 1-1 and a second reaction tank 1-2, wherein the first reaction tank 1-1 is an anoxic reaction tank or an anaerobic reaction tank, and the second reaction tank 1-2 is an aerobic reaction tank.
When the denitrification effect of treating domestic sewage by a conventional activated sludge process is mainly considered, the first reaction tank 1-1 is set as an anoxic tank for denitrification, the second reaction tank 1-2 is set as an aerobic tank for nitrification, and fillers are added into the two reaction tanks.
When considering the shortcut nitrification-anaerobic ammonia oxidation treatment of wastewater (such as landfill leachate) with higher ammonia nitrogen concentration, the first reaction tank 1-1 is set as an anoxic tank for anaerobic ammonia oxidation denitrification, the second reaction tank 1-2 is set as an aerobic reaction tank for shortcut nitrification, and fillers are added into both reaction tanks.
If biological phosphorus removal is considered on the basis, an anaerobic tank can be arranged in front of the first-stage reaction tank, so that the returned sludge in the secondary sedimentation tank carries out anaerobic phosphorus release, and no filler is added into the anaerobic tank. Therefore, in some embodiments, a primary reaction tank is further disposed in front of the first reaction tank 1-1, the primary reaction tank is communicated with the first reaction tank 1-1 through a water inlet pipe 4, the primary reaction tank is an anaerobic reaction tank, and the first reaction tank 1-1 is an anoxic reaction tank.
The parameters of load, hydraulic retention time, length, width, height, size and the like of each stage of reaction tank can be determined by referring to the outdoor drainage design specification (GB 50014-2006) and combining the water quality of inlet and outlet water.
The utility model discloses set up the guide plate in multistage reaction tank, the guide plate can make mixed liquid form the corridor that the circulation flows, just so can improve non-endless one-way flow to a certain extent and lead to packing near the accumulational problem of play water. When the treatment scale is small, the material can be stainless steel, and when the treatment scale is large or when the treatment scale is used for modification of the existing sewage plant, the material can be reinforced concrete.
In some embodiments, the corners of the first reaction tank 1-1 and the second reaction tank 1-2 are rounded to avoid the formation of hydraulic dead zones at the corners of the reactor, which may result in packing accumulation. The radius of the chamfer should be determined according to the reactor size and the gallery width.
The suspended biological filler is a flexible suspended filler, and is a spongy porous cube made of hydrophilic materials. In some embodiments, the filler is a flexible suspension filler, and is a spongy porous cube made of polyurethane foam (PUF) with extremely hydrophilic properties, and the cube has an edge length of about 2 cm. The density of the filler after film formation is close to that of water, the porosity is about 98 percent, and the specific surface area is about 3000m2/m3The wear resistance is strong, and the service life reaches 15 years. The adding rate of the filler is 15-70%, and the optimal adding rate is 20-40%.
The internal reflux device 8 is arranged in the second reaction tank 1-2, and can adopt gas stripping reflux or a reflux pump.
The water collector of the water outlet and the internal reflux of the multi-stage reaction tank of the utility model adopts a perforated sieve tube. The perforated sieve tube is a cylindrical water collector with round-hole-shaped water outlets densely distributed on the surface, the surface of the upstream surface is smooth, burrs cannot be generated, and abrasion of fillers and adhesion of impurities such as hairs are reduced; the back water surface is required to be provided with a reinforcing rib to ensure that the perforated sieve tube has no obvious deformation under the hydraulic action. The water passing ports of the perforated screen are less susceptible to plugging by packing than conventional plate and tubular grids. The size of the water passing hole is smaller than that of the filler, for example, for the filler with the side length of 2cm, the diameter of the round hole is preferably 8-10 mm, the filler loss can be avoided, and the water passing efficiency is high.
The utility model discloses a control the total area in water hole is crossed on perforation screen pipe surface, makes rivers pass the velocity of flow in water hole is less than the velocity of flow in the corridor, in order to avoid the piling up of suspension biofilm carrier. To the delivery port of any reaction tank that is provided with suspended biological filler, for example the utility model discloses the perforation screen pipe that is linked together with first outlet pipe that sets up in the first reaction tank is used for sending into the sewage in the first reaction tank into the second reaction tank and handles in the preferred embodiment, the perforation screen pipe that is linked together with the second outlet pipe that sets up in the second reaction tank is used for discharging the sewage in the second reaction tank, the perforation screen pipe that is linked together with reflux unit that sets up in the second reaction tank communicates with the back flow, be used for handling in refluxing partial sewage to the first reaction tank, the velocity of flow of water hole department on these perforation screen pipe surfaces is if be greater than the velocity of flow of rivers in the corridor, all probably lead to suspended biological filler to gathering at the surface of water hole of crossing. The utility model discloses some embodiments, according to handling capacity and backward flow volume in the reaction tank, confirm the water capacity of crossing of each perforation screen pipe to confirm its velocity of flow of crossing water hole department's rivers of each perforation screen pipe according to the velocity of flow of corridor, confirm the total area in the water hole of crossing that perforation screen pipe surface set up according to excessive flow and target velocity of flow, and then the preparation has the perforation screen pipe that suitable size and hole distribute. For example, in some embodiments, raw sewage enters the first reaction tank 1-1 through the water inlet pipe 4, and is fully mixed with the mixed liquor to perform an anoxic denitrification reaction or an anaerobic ammoxidation denitrification reaction, the mixed liquor is made to circularly flow along the gallery at a plug flow speed of 0.25-0.5 m/s by the propeller 10, the flow rate of the water passing opening of the perforated sieve pipe is controlled to be not more than 0.2m/s, for this purpose, the length of the perforated sieve pipe can be increased, or a plurality of groups of perforated sieve pipes are arranged, meanwhile, in a preferred embodiment, the submersible propeller is arranged at the upstream of the perforated sieve pipe to increase the plug flow speed of the mixed liquor, and the filler near the perforated sieve pipe is pushed into the main flow gallery to circularly flow.
In some embodiments, the reactor further comprises a plurality of submersible propellers 10, the plurality of submersible propellers 10 are disposed in the middle and lower part of each reaction tank, and the submersible propellers 10 are disposed upstream of the perforated screen 3. The diving propeller 10 is arranged at the middle lower part of the reactor, and at least one diving propeller 10 is arranged in each gallery, so that the mixed liquid in the reaction tank circularly flows along the galleries. In some embodiments, the flow velocity of the mixed liquid is kept to be 0.25-0.5 m/s by referring to the parameters of the oxidation ditch, and no aeration head is arranged at a certain distance between the upstream and the downstream of the submersible propeller 10 so as to avoid mutual interference. Meanwhile, the submersible propeller 10 is arranged at the upstream of the perforated sieve pipe 3, so that the plug flow speed of the mixed liquid in the reaction tank can be increased, the filler near the perforated sieve pipe 3 is pushed into the main flow to flow circularly, and the filler is effectively prevented from being accumulated near the perforated sieve pipe 3 and blocking the water through holes of the perforated sieve pipe 3 to influence the sewage treatment effect.
The internal reflux device in some embodiments of the present invention employs an air stripping reflux device 8, as shown in fig. 4, which specifically comprises a water collecting pipe 8-1, 2 90-degree elbows 8-2, a riser pipe 8-3, and an air delivery pipe 8-4. The top of the water collecting pipe 8-1 and the top of the lifting pipe 8-3 are not closed, and the air is communicated to maintain an atmospheric pressure. The mixed liquid collected by the third perforated sieve tube 3-3 enters the water collecting pipe, after the air of the air conveying pipe 8-4 enters the lifting pipe 8-3, the density of the gas-water mixed liquid in the lifting pipe 8-3 is smaller than that of the mixed liquid in the water collecting pipe 8-1, under the action of atmospheric pressure, the liquid level of the gas-water mixed liquid in the lifting pipe 8-3 rises, the mixed liquid flows back to the first reaction tank, and redundant air escapes through an opening at the top of the lifting pipe 8-3, so that the oxygen-deficient environment of the first reaction tank is prevented from being damaged. Compared with a reflux pump, the gas stripping reflux device obviously reduces the power consumption and has good economical efficiency. If stripping reflux is inconvenient to implement, a reflux pump can still be used. For the denitrification of domestic sewage, the internal reflux ratio is preferably 2-6.
The utility model discloses an avoid interior reflux system to take place the jam and the loss of filler, also adopt the water collector of perforation screen pipe as interior backward flow, be equipped with underwater propulsor simultaneously. The utility model discloses the principle of air stripping backward flow is: after the gas is led to the bottom of the riser, the density of the gas-water mixed liquid in the riser is less than that of water (the relative density of the gas-water mixed liquid which generally rises is about 0.25-0.35), and according to the principle of a communicating vessel, under the action of the pressure of a water column with the height of H, the liquid level height of the gas-water mixed liquid is L, as follows:
ρ1H＝ρ2L
where ρ is1-the density of the sewage;
ρ2raising the density of the gas-water mixed liquid in the pipe;
h-submergence depth of the gas inlet;
l is the lifting height + the submerging depth, and H/L is the submerging rate.
With the above equation in mind, the elevation height (L-H) or minimum submergence depth H can be calculated as follows:
the amount of the stripping air is generally 3-5 times of the lifting amount.
In some embodiments, the multistage circulating flow moving bed biofilm reactor further comprises an aeration system, wherein the aeration device comprises a blower, an aeration pipe 9-1 and an aeration head 9-2, and the aeration pipe 9-1 and the aeration head 9-2 are arranged at the bottom of the aerobic reaction tank, namely the second reaction tank 1-2. The aeration system adopts blast aeration, and the blast aeration can increase the longitudinal turbulence degree of the reactor and improve the mixing effect. The height of the reactor adopting blast aeration can be 0.5-1.0 m.
In some embodiments, the reactor further comprises a water distributor 11, the bottom of the water distributor 11 is perforated, the water distributor 11 is disposed in each of the first reaction tank 1-1 and the second reaction tank 1-2, and one end of the first water outlet pipe 5 away from the first reaction tank 1-1 is communicated with the water distributor 11 disposed in the second reaction tank 1-2; one end of the return pipe 7, which is far away from the second reaction tank 1-2, is communicated with a water distributor 11 arranged in the first reaction tank 1-1. The utility model discloses communicating system between the reaction tank and interior reflux system's water distribution adopt the fenestrate water-locator in bottom, guarantee the homogeneity of intaking, avoid the too big and form the water conservancy blind spot that the vortex leads to of the velocity of flow of intaking.
Referring to fig. 5, in some embodiments, the perforated screen 3 includes a water collecting part 3-1 and a connector part 3-2, the water collecting part 3-1 is a cylindrical water collector with a plurality of circular water passing holes uniformly distributed on the surface, one end of the cylinder is closed, the other end of the cylinder is an open end, and the open end is configured as a circular connector part 3-2 for connecting a pipeline. For suspended biological fillers with the side length of 2cm, the diameter of the water passing hole is preferably 8-10 mm, so that the filler loss can be avoided, and the water passing efficiency is higher. When the perforated sieve tube 3 is arranged at the water outlet of the first reaction tank 1-1, the water collecting part 3-1 is connected with one end of the first water outlet pipe 5 extending into the first reaction tank 1-1 through the connector part 3-2, so that suspended biological filler in the first reaction tank 1-1 is effectively prevented from flowing into the second reaction tank 1-2; when the perforated sieve tube 3 is arranged at the water outlet of the second reaction tank 1-2, the water collecting part 3-1 is connected with one end of the second water outlet pipe 6 extending into the second reaction tank 1-2 through the connector part 3-2, so that the suspended biological filler in the second reaction tank 1-2 is effectively prevented from flowing out; when the perforated sieve tube 3 is arranged at the return port between the two stages of reaction tanks, the water collecting part 3-1 is connected with the water collecting pipe 8-1 in the inner return device 8 through the connector part 3-2, the mixed liquid in the second reaction tank 1-2 collected by the perforated sieve tube 3 flows into the water collecting pipe 8-1 for air stripping and backflow, and the suspended biological filler in the second reaction tank 1-2 is effectively prevented from flowing into the first reaction tank 1-1. To avoid packing build up near the perforated screen 3, the flow rate at the water holes should be controlled to be no more than 0.2m/s, for which purpose the length of the perforated screen can be increased, or groups of perforated screens can be provided. The water passing holes of the perforated screen pipe 3 are less susceptible to clogging by packing than conventional plate and tubular grids. Preferably, the surface of the upstream surface of the perforated sieve tube 3 is smooth so as to reduce the abrasion of the filler and the attachment of impurities such as hair and the like; the back water surface is provided with a reinforcing rib to ensure that the perforated sieve tube 3 has no obvious deformation under the hydraulic action.
In practical application, the utility model provides a multistage circulating flow removes biological membrane reactor concrete operation as follows: raw sewage enters a first reaction tank 1-1 through a water inlet pipe 4 and is fully mixed with mixed liquor to carry out anoxic denitrification reaction or anaerobic ammonia oxidation denitrification reaction, a submersible propeller 10 enables the mixed liquor to circularly flow along a gallery, and the mixed liquor is partially circulated after the majority of circulation flowThe mixed liquid is collected by the perforated sieve tube 3 in the first reaction tank 1-1 and then enters the second reaction tank 1-2 through the water distributor 11, and the filler of the first reaction tank 1-1 is blocked by the perforated sieve tube 3 and cannot flow into the second reaction tank 1-2, so that the loss of the filler is avoided, and the first reaction tank 1-1 can keep enough microbial biomass. Mixed liquor flowing out of the first reaction tank 1-1 enters the second reaction tank 1-2, is fully mixed and flows along the gallery, aeration quantity can be adjusted according to process requirements, complete nitration reaction or short-range nitration (nitrosation) reaction is carried out, after most of the circulation flow, part of the mixed liquor is collected by a perforated sieve tube 3 which is arranged in the second reaction tank and communicated with the second water outlet pipe and then enters the subsequent treatment process by a second water outlet pipe 6, and in addition, part of the mixed liquor is collected by the perforated sieve tube 3 which is arranged in the second reaction tank 1-2 and communicated with a gas reflux device and then is lifted by a gas stripping reflux device 8 and then enters the first reaction tank 1-1 by a reflux pipe 7 and a water distributor 11, so that nitrate Nitrogen (NO) generated in the second reaction tank 1-2 can be generated3- -N) or nitrous Nitrogen (NO)2- -N) to the first reaction tank 1-1 for anoxic denitrification or anaerobic ammoxidation denitrification to improve denitrification efficiency.
It will be understood by those skilled in the art that the foregoing is merely a preferred embodiment of the present invention, and is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. A multi-stage circulating flow moving bed biofilm reactor is characterized by comprising a first reaction tank (1-1) and a second reaction tank (1-2) which are communicated, wherein the first reaction tank (1-1) is an anoxic reaction tank or an anaerobic reaction tank, and the second reaction tank (1-2) is an aerobic reaction tank; suspended biological fillers are arranged in the first reaction tank (1-1) and/or the second reaction tank (1-2);
one or more perforated sieve pipes (3) are respectively arranged in the first reaction tank (1-1) and the second reaction tank (1-2), one end of each perforated sieve pipe (3) is closed, the other end of each perforated sieve pipe is open, and the pipe wall of each perforated sieve pipe is provided with a plurality of water through holes; the water through holes are used for enabling sewage to enter the perforated sieve pipe (3) to be collected, and the suspended biological filler is blocked outside the perforated sieve pipe (3); the open end of the perforated sieve tube (3) arranged in the first reaction tank (1-1) is communicated with a first water outlet pipe (5), and the first water outlet pipe (5) is used for conveying the sewage in the first reaction tank (1-1) to the second reaction tank (1-2); the open end of the perforated sieve tube (3) arranged in the second reaction tank (1-2) is communicated with a second water outlet pipe (6), and the second water outlet pipe (6) is used for discharging sewage in the second reaction tank (1-2); the size of the suspended biological filler is larger than that of the water through holes;
and a backflow module is arranged in the second reaction tank and used for enabling the sewage part of the second reaction tank (1-2) to flow back into the first reaction tank (1-1).
2. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: a first guide plate (2-1) and a second guide plate (2-2) are arranged in the first reaction tank (1-1) and the second reaction tank (1-2); the first guide plate (2-1) is vertically arranged in the center of the first reaction tank (1-1) and/or the second reaction tank (1-2) along the length direction of the first reaction tank (1-1) and the second reaction tank (1-2), and divides the first reaction tank (1-1) and the second reaction tank (1-2) into two galleries respectively; the second guide plate (2-2) is arc-shaped and is arranged at two ends of the first reaction tank (1-1) and the second reaction tank (1-2), and the arc-shaped opening of the second guide plate (2-2) faces the first guide plate (2-1).
3. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: the reactor also comprises a primary reaction tank, wherein the primary reaction tank is communicated with the first reaction tank (1-1) through a water inlet pipe (4), the primary reaction tank is an anaerobic reaction tank, and the first reaction tank (1-1) is an anoxic reaction tank.
4. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: the backflow module comprises a backflow pipe (7) and an internal backflow device (8), and a water outlet of the internal backflow device (8) is communicated with the backflow pipe (7); the return pipe (7) is used for returning the sewage part of the second reaction tank (1-2) to the first reaction tank (1-1); the internal reflux device (8) is a gas stripping reflux device or a reflux pump.
5. The multi-stage circulating flow moving bed biofilm reactor of claim 4, wherein: the gas stripping reflux device is of a U-shaped structure and comprises a water collecting pipe (8-1), two 90-degree elbows (8-2), a lifting pipe (8-3) and a gas pipe (8-4), wherein the top ends of the water collecting pipe (8-1) and the lifting pipe (8-3) are provided with openings, the bottom end of the water collecting pipe (8-1) is communicated with the bottom end of the lifting pipe (8-3) through the two 90-degree elbows (8-2), and the gas pipe (8-4) penetrates through the side wall of the lifting pipe (8-3) and extends into the inner bottom of the lifting pipe (8-3);
a water inlet is arranged on the side surface of the water collecting pipe (8-1) and is communicated with the open end of another perforated sieve pipe arranged in the second reaction tank (1-2); a water outlet is arranged on the side surface of the lifting pipe (8-3) and is communicated with the return pipe (7); the height of the water outlet is higher than that of the water inlet, and the height of an opening of the gas pipe (8-4) in the lifting pipe (8-3) is lower than that of the water outlet.
6. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: the device also comprises an aeration system, wherein the aeration system comprises a blower, an aeration pipeline (9-1) and an aeration head (9-2), and the aeration pipeline (9-1) and the aeration head (9-2) are arranged at the bottom of the second reaction tank (1-2).
7. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: the device is characterized by further comprising a plurality of submersible propellers (10), wherein the submersible propellers (10) are arranged at the middle lower parts of the first reaction tank (1-1) and the second reaction tank (1-2).
8. The multi-stage circulating flow moving bed biofilm reactor of claim 7, wherein: the submersible propeller (10) is arranged at the upstream of the perforated sieve tube (3).
9. The multi-stage circulating flow moving bed biofilm reactor of claim 4, wherein: the water distributor (11) is arranged at the bottom of the water distributor (11), the water distributors (11) are arranged in the first reaction tank (1-1) and the second reaction tank (1-2), and one end, far away from the first reaction tank (1-1), of the first water outlet pipe (5) is communicated with the water distributor (11) arranged in the second reaction tank (1-2); one end of the return pipe (7) far away from the second reaction tank (1-2) is communicated with a water distributor (11) arranged in the first reaction tank (1-1).
10. The multi-stage circulating flow moving bed biofilm reactor of claim 1, wherein: the suspended biological filler is a flexible suspended filler which is a spongy porous cube made of hydrophilic materials.
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| CN113121010A (en) * | 2021-05-24 | 2021-07-16 | 华中科技大学 | Multistage circulating flow moving bed biofilm reactor and application thereof |
| CN113121010B (en) * | 2021-05-24 | 2024-04-23 | 华中科技大学 | Multistage circulating flow moving bed biomembrane reactor and application thereof |
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