CN115818862A - Cold water area mariculture tail water treatment system - Google Patents
Cold water area mariculture tail water treatment system Download PDFInfo
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Abstract
The invention relates to the technical field of water treatment, in particular to a cold water area mariculture tail water treatment system, which comprises a pretreatment unit, a biochemical treatment unit, a membrane treatment unit, a disinfection treatment unit and a sludge treatment unit which are sequentially connected; the pretreatment unit comprises a coarse grating, a fine grating, a grit chamber and a membrane grating which are connected in sequence; the biochemical treatment unit comprises an anaerobic zone, an anoxic zone, an aerobic zone and a post-anoxic zone which are sequentially connected; the membrane treatment unit is a membrane bioreactor. Compared with the prior art, the cold water area mariculture tail water treatment system provided by the invention adopts a highly enriched enhanced microorganism treatment process with a denitrification function, and ensures that the total nitrogen of effluent is stably below the standard limit on the premise of sufficient front-end nitration reaction and sufficient organic carbon source.
Description
Technical Field
The invention relates to the technical field of water treatment, in particular to a cold water area mariculture tail water treatment system.
Background
The treatment technology of the seawater culture tail water at home and abroad is in vogue, a lot of researches are carried out, the level is different, and no large successful case is completely counted at home at present, and the first seawater culture tail water treatment plant of 2000m < 3 >/d built in Hainan at home is put into production and good in trial run at the day before.
However, the annual average seawater temperature of Hainan is 23-25 ℃, the average seawater temperature of the sea in the Bohai region of China is 9-11 ℃, and the mariculture tail water treatment scheme of Hainan is not suitable for the mariculture tail water treatment of cold water areas in the Bohai region through study and small trials.
The seawater culture tail water contains various nitrogen and phosphorus, COD, antibiotics and heavy metal substances with relatively high pollution concentration, so that the water quality of the culture water body around farmers is rapidly deteriorated, the excellent aquatic culture environment of sensitive fishes is artificially damaged, and the total nitrogen is most difficult to remove in the process of removing various pollutants.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a cold water area mariculture tail water treatment system, which solves the problem of total nitrogen removal, ensures that the indexes of various pollutants in effluent are lower than the standard limit, and solves the problem of removal of various pollutants in cold water area mariculture tail water.
In order to achieve the purpose, the invention provides the following technical scheme:
a cold water area mariculture tail water treatment system comprises a pretreatment unit, a biochemical treatment unit, a membrane treatment unit, a disinfection treatment unit and a sludge treatment unit which are sequentially connected;
the pretreatment unit comprises a coarse grating, a fine grating, a grit chamber and a membrane grating which are connected in sequence;
the biochemical treatment unit comprises an anaerobic zone, an anoxic zone, an aerobic zone and a rear anoxic zone which are sequentially connected;
the membrane treatment unit is a membrane bioreactor.
Preferably, in the pretreatment unit, the coarse grid is a rotary coarse grid, and the fine grid and the membrane grid are both inward-flowing mesh plate type fine grids.
Preferably, in the biochemical treatment unit, the anoxic zone is provided with a sludge return pipe communicated with a water inlet pipe of the anaerobic zone; the aerobic zone is provided with a return pipe which is communicated with a water outlet pipe of the anaerobic zone.
Preferably, in the membrane treatment unit, a sludge return pipe is arranged in the membrane treatment unit and communicated with a water outlet pipe of the anoxic zone.
Preferably, in the membrane treatment unit, the membranes in the membrane bioreactor all adopt hollow fiber membranes, and the material is PVDF.
Preferably, in the biochemical treatment unit, a secondary sedimentation tank is connected after the post-anoxic zone.
Preferably, chemical phosphorus removal agents need to be added into the grit chamber and the secondary sedimentation tank.
Preferably, the chemical phosphorus removal agent is aluminum chlorohydrate PAC.
Preferably, the sterilization treatment unit is an ultraviolet sterilization device.
Preferably, the sludge treatment unit is a screw-stacking dehydrator.
Compared with the prior art, the cold water area mariculture tail water treatment system provided by the invention adopts a high enrichment reinforced microorganism treatment process with a denitrification function, and ensures that the total nitrogen of effluent is stably below the standard limit on the premise of sufficient front-end nitration reaction and sufficient organic carbon source.
In order to make the aforementioned and other objects, features and advantages of the present invention comprehensible, preferred embodiments accompanied with figures are described in detail below.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and those skilled in the art can also obtain other related drawings based on the drawings without inventive efforts.
Fig. 1 is a structural diagram of a tail water treatment system for mariculture in a cold water area according to an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without making any creative effort, shall fall within the protection scope of the present invention.
In the scheme, the treated raw water is the tail water of mariculture discharged from a demonstration park of a certain ocean high and new industry in the Bohai Bay region.
The system specifically comprises polluted seawater discharged from an aquatic product industrial culture demonstration area, an aquatic product seedling raising base, an outdoor circulating water culture demonstration area, an aquatic product processing area, a leisure fishery vacation area, an aquatic product trading area, a storage and stream area and the like.
The treated effluent reaches the standard IV class (TN is less than or equal to 10) of the environmental quality standard of surface water (GB 3838-2002). The main water quality indexes of inlet and outlet water are shown in a table 1:
TABLE 1 water quality index table
| Serial number | Index (I) | Quality of inlet water | Quality of effluent water |
| 1 | Chemical oxygen demand CODcr (mg/L) | ≤350 | ≤30 |
| 2 | Biochemical oxygen demand BOD5 (mg/L) for 5 days | ≤160 | ≤6 |
| 3 | Suspended Substance (SS) (mg/L) | ≤120 | ≤5 |
| 4 | Ammonia nitrogen (mg/L) | ≤47 | ≤1.5 |
| 5 | TN(mg/L) | ≤70 | ≤1.5 |
| 6 | TP(mg/L) | ≤5 | ≤0.3 |
As shown in fig. 1, an embodiment of the present invention provides a tail water treatment system for mariculture in cold water areas, which includes a pretreatment unit, a biochemical treatment unit, a membrane treatment unit, a disinfection treatment unit, and a sludge treatment unit connected in sequence.
The pretreatment unit comprises a coarse grating, a fine grating, a grit chamber and a membrane grating which are connected in sequence.
In the pretreatment unit, according to the characteristics of the quality of raw water, the main task of the pretreatment unit is to remove floating matters and suspended matters in sewage by a physical separation method and improve the biodegradability of the sewage, and main facilities and structures comprise a grid, a grit chamber and the like.
The grid is used for getting rid of great suspended solid, floater, fibrous material and solid particle material in the sewage to guarantee the normal operating of follow-up processing unit and water pump, alleviate the processing load of follow-up processing unit, prevent to block row mud pipeline. The device is divided into a coarse grating, a middle grating and a fine grating according to the gaps of the grating bars, the coarse grating is generally provided with two coarse gratings and the fine gratings are generally provided with two coarse gratings, large-size floaters and suspended matters are removed by the coarse grating, the fine grating is used for further removing the suspended matters and the floaters of smaller particles in sewage, and the trapped matters of the gratings are transported out of a factory.
The membrane grille is used for further removing fine hair and fiber substances in water and is a key pretreatment device of an MBR membrane method. The film grids are of various types, and are divided into a screen slit type and a screen hole type according to the types of screens, and are divided into a drum type, a stepped type, an internal inflow type and the like according to the structural forms.
In this scheme, thick grid adopts the thick grid of rotation, and the thin grid adopts the interior net board formula thin grid that flows of intaking, and the membrane grid adopts the interior net board formula thin grid that flows of intaking.
Because the sewage entering the sewage treatment plant contains certain inorganic silt, a grit chamber is necessary to be arranged in terms of protecting the normal and stable operation of the subsequent biological treatment working section, ensuring and improving the effective utilization rate of the biological reaction tank, enabling the process flow to have greater operation flexibility and the like.
The grit chamber occupies a small proportion in the aspects of investment, occupied land and the like of a sewage treatment plant, but the effect of the grit chamber is not ignored. If the grit removal effect of the grit chamber is not good and no ideal grit removal effect exists, a large amount of sand particles enter each subsequent processing unit, and a great deal of hidden danger is brought to the normal operation of a sewage plant: in engineering design, the efficiency of a grit chamber system is usually measured as the sand removal efficiency for d ≧ 0.2 mm. The most common types of grit chambers at present include aerated grit chambers and cyclone grit chambers.
Earlier in domestic application, aeration grit chambers, sewage treatment plants of different types and specifications are widely applied. The main advantages of the grit chamber are:
1) The removal rate of fine sand particles is high, and the design can be changed according to the water inlet condition and the water outlet requirement to meet different requirements.
2) The operation is stable, and the adaptability to the impact load of flow and sand amount is strong.
3) High organic matter separating effect and less organic matter.
4) Has better function of removing grease and scum, which is particularly remarkable for a system without a separate primary sedimentation tank.
The disadvantages of this grit chamber are mainly two-fold:
1) The occupied area is large.
2) The aeration process may increase the dissolved oxygen value of the wastewater and may consume some of the rapidly degraded organic matter in the wastewater, which may adversely affect the subsequent operation of the anaerobic biological tank. Cyclone grit chamber
As for the scheme, the aeration grit chamber is adopted, and the shape of the chamber can ensure stable sand removing effect, can give full play to the good sand removing effect and the oil skimming and scum removing effect, ensures the smooth proceeding of the subsequent procedures, and is beneficial to the operation management of the whole plant and the comprehensive improvement of the effluent quality.
The biochemical treatment unit comprises an anaerobic zone, an anoxic zone, an aerobic zone and a post-anoxic zone which are sequentially connected;
according to the requirements of the water quality of inlet water and the water quality of outlet water, the biochemical treatment unit adopts a biological nitrogen and phosphorus removal treatment process. The biological nitrogen and phosphorus removal treatment process adopts an A/A/O process.
The A/A/O process is an anaerobic-anoxic-aerobic activated sludge process, i.e. the dephosphorization and denitrification reaction is completed in an environment with alternate change of anaerobic and aerobic, anoxic and aerobic. In the process, the anaerobic tank is used for biological phosphorus removal, the anoxic tank is used for biological nitrogen removal, carbon source substances in raw water firstly enter the anaerobic tank, phosphorus accumulating bacteria preferentially utilize easily biodegradable substances in sewage to become dominant strains, conditions are created for phosphorus removal, sewage then enters the anoxic tank, and denitrifying bacteria utilize other carbon sources which can be utilized to reduce nitrate nitrogen which flows back to the anoxic tank into nitrogen, so that the purpose of nitrogen removal is achieved.
The method is characterized in that the anaerobic section, the anoxic section and the aerobic section have clear functions and clear boundary lines, the space-time proportion and the running condition of the three sections can be artificially created and controlled according to the water inlet condition and the water outlet requirement, and higher dephosphorization and denitrification effects can be achieved as required as long as the carbon source is sufficient. The back anoxic zone can further improve the effects of phosphorus removal and nitrogen removal.
The membrane treatment unit is a membrane bioreactor.
The Membrane-Bioreactor (MBR) is a product of the organic combination of Membrane separation technology and biological sewage treatment technology, and is generally regarded as a sewage treatment technology with stable performance, good effect and great development potential. The technology is characterized in that the gravity settling separation process of mud and water in the traditional activated sludge treatment process is replaced by the ultrafiltration and microfiltration membrane separation process, and the membrane separation is adopted, so that the high biological concentration and the excellent water outlet effect can be kept. Can effectively remove pollutants such as organic matters, ammonia nitrogen and the like in water.
The membrane treatment unit adopts an immersed MBR, and is characterized in that a special membrane component is immersed in mixed liquid, water (permeating a microporous membrane) is discharged out of the biochemical reaction tank under the suction action of a water pump or the push of water level difference, and microorganisms, cells and other particles are intercepted in the biochemical reaction tank. Wherein, the membranes are all hollow fiber membranes and are made of PVDF. Each grid membrane pool is provided with a water inlet gate, a water outlet gate and an emptying pipe. The effluent of the membrane pool is designed according to the suction and outflow, and a permeate pump is arranged corresponding to each grid of membrane pool. The water outlet main pipe is connected to the membrane pool through a water outlet connecting pipe, and the water outlet main pipe is connected with a membrane pool water pump. And the membrane pool is subjected to frequency conversion control by a permeate pump.
The MBR process mainly has the following characteristics:
(1) The effluent quality is good, the solid-liquid separation can be efficiently carried out, the effluent quality is good and stable, the suspended matters and turbidity are close to zero, and compared with the traditional biological treatment process, the biological activity-activated sludge concentration is improved by 2-3 times, so the biochemical efficiency is greatly improved, the effluent quality is good, and the effluent quality can be ensured to be comprehensively superior to the first-level A standard.
(2) The occupied area is small, about 1/2-1/3 of the occupied area of the traditional process, the concentration of microorganisms in the reactor is high and can reach more than 10,000 mg/L, and the volume load (can reach 2-5 KgCOD/m) is greatly improved 3 D), the biochemical pool volume is reduced. One treatment structure of the membrane bioreactor is adopted to replace a plurality of treatment structures of primary sedimentation, aeration, secondary sedimentation, coagulation, filtration and the like in the traditional sewage treatment process, so that the land occupation is greatly reduced.
(3) The sewage treatment system has the advantages of strong impact resistance, stable operation, no sludge loss due to high sludge concentration and rich biological phases, no influence of factors such as sludge expansion and the like, strong impact resistance, stable operation and remarkable advantages especially when being used for sewage treatment plants containing more industrial sewage.
(4) The biological phase is rich: the efficient interception function of the membrane enables microorganisms to be completely intercepted in the reactor, so that the microorganisms with longer generation period and the microorganisms which are not easy to form zoogloea can be enriched and propagated, the biological enrichment and co-metabolism function can be formed in the whole biological phase, a more complete microorganism chain is formed, the treatment efficiency and the stability of the system are greatly improved, and the process is less common in the traditional biochemical process.
(4) The biological phase is rich: the efficient interception function of the membrane ensures that microorganisms are completely intercepted in the reactor, so that microorganisms with longer generation period and microorganisms which are not easy to form zoogloea can be enriched and propagated, the biological enrichment and co-metabolism function can be formed in the whole organism, a more complete microorganism chain is formed, the treatment efficiency and the stability of the system are greatly improved, and the process is rare in the traditional biochemical process. (5) The design and the automatic control are easy to expand due to the modular characteristic of the membrane bioreactor technology, and can respond to the increase of water treatment capacity by adding necessary modules. The process equipment is centralized, all the process equipment adopts computer automation control, and the operation management is simple and convenient.
(5) The design and the automatic control are easy to expand due to the modular characteristic of the membrane bioreactor technology, and can respond to the increase of water treatment capacity by adding necessary modules. The process equipment is centralized, all the process equipment adopts computer automation control, and the operation management is simple and convenient.
(6) 1+1 >. Therefore, the membrane bioreactor is not simply the superposition of biological treatment and membrane separation technology, but has the effect of 1+1 >.
Working procedure of the membrane separation system:
the submerged membrane blocks are placed in separate membrane tanks. The membrane block is immersed in the mixed liquor, and under the condition of negative pressure produced by the osmotic (effluent) pump, the water can be passed through the membrane so as to implement filtration treatment. The membrane tank replaces the functions of separating suspended matters and liquid in the secondary sedimentation tank and carrying out deep filtration treatment.
Aeration plays an important role in the operation of membrane plants. The bottom of the membrane block is aerated by large bubbles to generate turbulence to scour the surfaces of the hollow fibers and enable particles to fall off the surfaces of the membranes. Another approach is to combine gas and water at the bottom of the membrane monolith to produce the same effect. Each of these measures reduces the frequency of chemical cleaning of the membrane block.
When the membrane tank is aerated, the membrane tank can be used as a second aerobic tank, so that the oxidation of BOD5 and the nitrification of ammonia nitrogen are completely finished, and the effluent is ensured to reach the standard.
The micro-filtration membrane is also a barrier for biological flocs, suspended matters and pathogens, clear effluent can be obtained, the SS concentration is nearly zero, and the separation effect does not depend on the sedimentation performance of sludge.
Each membrane pool is provided with a water outlet pump. The effluent is sent to the next treatment process by an effluent pump. By the operation of the pump, a negative pressure can be generated at the head of the membrane module coupling. The treated water is passed through a porous fibrous microfiltration membrane into a suction pump.
The concentrated mixed liquor produced in the membrane tank continuously flows back to the previous biological tank by gravity through the mixed liquor to maintain the sludge concentration in the biochemical tank and reduce the accumulation of the biological sludge in the membrane tank.
And transferring the mixed liquid as a part of the residual sludge to a sludge thickening and dewatering machine room for dewatering.
After a period of use, the permeability of the membrane decreases due to clogging with organic and inorganic substances, which leads to an increase in the filtration resistance of the membrane and thus to an increase in the transmembrane pressure difference (TMP). The following measures will control membrane fouling, thereby achieving long-term, stable operation of the system:
(1) Positive air sweeping
The forward air sweeping means that when the system filters, the air blowers matched with the system are simultaneously started, corresponding control valves are started, and the air blowers perform aeration to sweep the surfaces of the membrane filaments so as to prevent a large amount of particulate matters on the surfaces of the membranes from being deposited.
(2) Intermittent suction
Intermittent pumping means that the osmotic suction pump of the membrane continuously operates for a certain time (such as 7 min), stops operating for a certain time (such as 1 min), and the forward air sweeping blower of the membrane wire still operates at the moment, and the membrane wire obtains vibration with enough strength under the disturbance of severe gas-water two-phase turbulence formed by bubbles, so that a small amount of particles deposited on the surface of the membrane wire during filtration are separated from the surface of the membrane, and pollutants on the surface of the membrane are removed.
(3) Maintenance cleaning
A medicated chemical backwash, known as a maintenance clean (the frequency of cleaning is also dependent on the nature of the wastewater and may be performed once every 10-30 days), is typically performed weekly. When the system is running, the automatic backwashing process is carried out on each membrane pool respectively without the input of operators. The development of high strength, high chemical resistance PVDF membranes has made this frequent maintenance on-line cleaning possible. The maintenance cleaning agent is common acid and sodium hypochlorite, and is prepared into a low-concentration solution for use. The cleaning operation becomes very simple by the automatic control of the PLC, and the on-line maintenance Cleaning (CIP) process can be designed to be fully automatic without manual intervention. The time for each cleaning of the maintenance cleaning does not exceed 2 hours, and the normal production is not influenced.
(4) Recovery cleaning
Even with these maintenance measures, the TMP will slowly reach a maximum or end value. Once the stop value is reached, each membrane block needs to be removed from the cell and chemically cleaned to remove fouling materials and restore permeability. This procedure, called recovery cleaning, is usually performed once in 12 to 24 months depending on the clogging. Once the membrane modules need to be cleaned, the individual membrane modules are removed and immersed in a cleaning tank. Depending on the type of scale, different chemical solvents can be used for cleaning, sodium hypochlorite for organic scale and weak acids for inorganic scale. After a period of soaking, the filtration performance of the membrane is restored, and the membrane module is reinstalled on the production line. Since the operation of the system is affected little in a short period of time by the removal of a single membrane module, the resumption of chemical cleaning does not affect the production either.
The main characteristics are that:
(1) The MBR process has good effluent quality, can efficiently carry out solid-liquid separation, has good and stable effluent quality, has suspended matters and turbidity close to zero, and has the advantages that the concentration of biological phase-activated sludge is improved by 2-3 times compared with the traditional biological treatment process, so the biochemical efficiency is greatly improved, the effluent quality is good, the effluent quality can be ensured to be comprehensively superior to the first-level A standard, and the effluent can have wider application. The process for treating the reclaimed water is relatively simple. In addition, the membrane separation technology has strong modularization characteristics, so the membrane separation technology has the characteristic of easy extension and is very convenient for extension. The method can conveniently realize the improvement of the treatment capacity by means of adding a microfiltration membrane treatment unit in a biological treatment structure, improving the sludge concentration and the like.
(2) Generally, in the early stage of the application of the MBR technology, the traditional MBR technology has the disadvantages of high engineering investment, high power consumption and high operation cost. However, with the development of MBR technology and the increasing expansion of engineering application in recent years, we know that a novel MBR technology which can make the engineering investment and operation cost equal to the traditional process is available in China and China. It is characterized in that: a. the double-layer membrane component is adopted, so that the filling density of the membrane component is higher, and the occupied area is saved; b. the pulse superposition type membrane purging technology is adopted, so that the energy consumption of membrane purging is further reduced; c. and a multi-phase combination form of multi-point water inflow, multi-point backflow and the like is adopted, so that the biochemical treatment efficiency is higher, and the energy consumption is lower compared with the traditional MBR operation.
(3) For MBR technology, the membrane for sewage treatment is mainly a solid-phase asymmetric membrane prepared from an organic polymer material, and the structural form of the engineering membrane is a hollow fiber type membrane. The hollow fiber type has an outer diameter of 40 to 250 μm and an inner diameter of 25 to 42 μm. The advantages are that: high compression strength and difficult deformation. The combination mode of the membrane component and the bioreactor is a split-type membrane-bioreactor, namely the membrane component and the bioreactor are separately arranged, mixed liquor in the bioreactor is pressurized by a circulating pump and then is pumped to the filtering end of the membrane component, and liquid in the mixed liquor permeates through the membrane under the action of pressure to become system treated water; solid matter, macromolecular substance, etc. are intercepted by the membrane and return to the bioreactor along with the concentrated solution. The split-type membrane-bioreactor has the characteristics of stable and reliable operation, and easy cleaning, replacement and addition of the membrane; and membrane flux is generally large. However, in order to reduce the deposition of pollutants on the membrane surface and prolong the cleaning period of the membrane under the general conditions, a circulating pump is required to provide higher cross flow velocity of the membrane surface, and the water circulation amount is large. The assembly is directly placed into a reactor in a membrane pool without a pressure container, and the immersed membrane-bioreactor is formed. Typically an external pressure membrane module. The advantages are that: the packing density is high; the manufacturing cost is relatively low; the service life is long, and a nylon hollow fiber membrane with stable physicochemical property and low water permeability can be adopted; the membrane has good pressure resistance and does not need supporting materials.
Preferably, in the biochemical treatment unit, the anoxic zone is provided with a sludge return pipe communicated with a water inlet pipe of the anaerobic zone; the aerobic zone is provided with a return pipe which is communicated with a water outlet pipe of the anaerobic zone.
In addition, in the embodiment of the invention, the membrane treatment unit is provided with a sludge return pipe which is communicated with a water outlet pipe of the anoxic zone. In the biochemical treatment unit, a secondary sedimentation tank is also connected behind the rear anoxic zone. Chemical agents for removing phosphorus need to be added into the grit chamber and the secondary sedimentation tank. The chemical phosphorus removal agent is basic aluminum chloride PAC. The disinfection processing unit is an ultraviolet disinfection device. The sludge treatment unit is a screw-overlapping dehydrator.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or the orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only used for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly stated or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
Claims (10)
1. A cold water area mariculture tail water treatment system is characterized by comprising a pretreatment unit, a biochemical treatment unit, a membrane treatment unit, a disinfection treatment unit and a sludge treatment unit which are sequentially connected;
the pretreatment unit comprises a coarse grating, a fine grating, a grit chamber and a membrane grating which are connected in sequence;
the biochemical treatment unit comprises an anaerobic zone, an anoxic zone, an aerobic zone and a rear anoxic zone which are sequentially connected;
the membrane treatment unit is a membrane bioreactor.
2. The tail water treatment system for mariculture in a cold water area according to claim 1, wherein in the pretreatment unit, the coarse grating is a rotary coarse grating, and the fine grating and the membrane grating are both inward-flowing mesh plate type fine gratings.
3. The tail water treatment system for cold water body mariculture according to claim 2, wherein a sludge return pipe is arranged in the anoxic zone and communicated with a water inlet pipe of the anaerobic zone in the biochemical treatment unit; the aerobic zone is provided with a return pipe which is communicated with a water outlet pipe of the anaerobic zone.
4. The tail water treatment system for cold water body mariculture according to claim 3, wherein the membrane treatment unit is provided with a sludge return pipe communicated with a water outlet pipe of the anoxic zone.
5. The tail water treatment system for cold water body mariculture according to claim 4, wherein in the membrane treatment unit, the membranes in the membrane bioreactor are all hollow fiber membranes made of PVDF.
6. The tail water treatment system for cold water body mariculture according to claim 5, wherein a secondary sedimentation tank is further connected to the back anoxic zone in the biochemical treatment unit.
7. The tail water treatment system for cold water body mariculture according to claim 6, wherein the grit chamber and the secondary sedimentation tank are required to be fed with chemical phosphorus removal agents.
8. The cold water body mariculture tail water treatment system according to claim 7, wherein the chemical phosphorus removal agent is basic aluminum chloride (PAC).
9. The cold water body mariculture tail water treatment system according to claim 8, wherein the disinfection treatment unit is an ultraviolet disinfection device.
10. The cold water body mariculture tail water treatment system according to claim 9, wherein the sludge treatment unit is a stack screw dehydrator.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116143353A (en) * | 2023-04-18 | 2023-05-23 | 江苏南大五维电子科技有限公司 | Treatment device and method for cultivation tail water |
| CN117164176A (en) * | 2023-11-02 | 2023-12-05 | 广东科清环境技术有限公司 | Method for treating mariculture tail water |
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2022
- 2022-10-26 CN CN202211315775.9A patent/CN115818862A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116143353A (en) * | 2023-04-18 | 2023-05-23 | 江苏南大五维电子科技有限公司 | Treatment device and method for cultivation tail water |
| CN117164176A (en) * | 2023-11-02 | 2023-12-05 | 广东科清环境技术有限公司 | Method for treating mariculture tail water |
| CN117164176B (en) * | 2023-11-02 | 2024-02-02 | 广东科清环境技术有限公司 | Method for treating mariculture tail water |
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