CN215102279U - High-efficient low energy consumption EMBR biochemical treatment system - Google Patents
High-efficient low energy consumption EMBR biochemical treatment system Download PDFInfo
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Abstract
The utility model relates to a high-efficiency low-energy consumption EMBR biochemical treatment system, which comprises a biochemical anoxic zone, a biochemical aerobic zone, a sludge settling zone and a membrane tank which are connected in sequence, wherein the membrane tank is used for carrying out membrane treatment on the sewage treated by the sludge settling zone to realize membrane water production; the biochemical aerobic zone is also connected to the biochemical anoxic zone through an air stripping reflux device and is used for refluxing the nitrified liquid treated by the biochemical aerobic zone to the biochemical anoxic zone in a large proportion for biological denitrification; the sludge settling zone and the membrane tank are also connected to the biochemical aerobic zone through a gas stripping reflux device and are used for refluxing the sludge in the sludge settling zone and the membrane tank to the biochemical aerobic zone. Compared with the prior art, the utility model discloses high-efficient low energy consumption EMBR biochemical treatment system has synthesized biochemical system, membrane technology and physicochemical technology's advantage, greatly reduced the operation energy consumption.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, especially, relate to a high-efficient low energy consumption EMBR biochemical treatment system.
Background
The current mature and widely applied biological treatment technology in the market is mainly A2The conventional treatment process is well applied to various sewage plants all over the world at present.
However, under the condition of facing continuous improvement of the productivity and severely limiting the unit water consumption and the occupied area, the traditional biological treatment process also has a plurality of technical problems which are difficult to overcome, and the treatment process is urgently needed to be optimized. For example, in the traditional biological treatment process, the impact load on the system is large when the quality fluctuation of raw water is large; the traditional aeration device has low oxygen transfer efficiency, so that the energy consumption of a fan is overhigh; the MBR process fan has high operation energy consumption and poor process flexibility; when the quality of raw water has a large deviation from the design value and the denitrification requirement is very strict, the denitrification efficiency cannot be improved.
Chinese patent CN103011395A discloses a membrane bioreaction system, a mud-water separation device is arranged between an aerobic tank of a biological treatment unit and a membrane tank of an immersed membrane treatment unit, the mud-water separation device comprises a tank body, a first guide wall, a second guide wall, a third guide wall and an aeration device, an aeration device is arranged on one side of the bottom of the tank body, mud-water separation is realized in the system through a guide wall structure, the separated mud-water mixed liquid with higher concentration flows back to the biological treatment unit through a submersible pump, and the submersible pump for backflow of the mud-water mixed liquid with higher concentration needs to consume great energy.
SUMMERY OF THE UTILITY MODEL
Based on the current situation that among the prior art sewage treatment process mud backward flow needs high energy consumption, the utility model provides a high-efficient low energy consumption EMBR biochemical treatment system.
The purpose of the utility model can be realized through the following technical scheme:
the utility model provides a high-efficient low energy consumption EMBR biochemical treatment system, including biochemical anoxic zone, biochemical aerobic zone, sludge settling zone and the membrane cisterna that the order links to each other, biochemical anoxic zone is used for carrying out the oxygen deficiency to sewage and handles, biochemical aerobic zone is used for carrying out aerobic treatment to sewage, sludge settling zone is used for carrying out sludge settling treatment to the treatment fluid after biochemical aerobic zone handles, the membrane cisterna is used for carrying out membrane treatment to the sewage after sludge settling zone handles, set up immersed membrane processing unit in the membrane cisterna, immersed membrane processing unit is used for realizing that the membrane produces water;
the biochemical aerobic zone is also connected to the biochemical anoxic zone through an air stripping reflux device, and the air stripping reflux device between the biochemical aerobic zone and the biochemical anoxic zone is used for refluxing the nitrified liquid treated by the biochemical aerobic zone to the biochemical anoxic zone for biological denitrification;
the sludge settling zone and the membrane tank are also connected to a biochemical aerobic zone through a gas stripping reflux device;
and the gas stripping reflux device connected with the sludge settling zone and the membrane tank is used for refluxing the sludge in the sludge settling zone and the membrane tank to the biochemical aerobic zone.
In one embodiment of the present invention, the gas stripping reflux device comprises a tank body, the tank body is provided with a feed inlet and a discharge outlet, a first wall and a second wall are arranged in the tank body, a feed area is arranged between the feed inlet and the first wall, a discharge area is arranged between the discharge outlet and the second wall, a gas stripping device is further arranged between the first wall and the second wall, a gas stripping area is arranged between the first wall and the second wall,
the top of the first wall body exceeds the liquid level of the tank body, and a reserved hole is formed in the bottom of the first wall body and is not closed for water passing; a gap is reserved between the top of the second wall and the top of the tank body, and the bottom of the second wall is not crossed with water, namely the top of the second wall is lower than the liquid level;
the first wall body and the second wall body are arranged so that material flow in the feeding area enters the gas stripping area from a reserved hole between the first wall body and the bottom of the tank body, and the gas stripping device is used for driving the material flow in the gas stripping area to ascend and flows out of the reserved hole between the second wall body and the top of the tank body to the discharging area.
In an embodiment of the present invention, the gas stripping device in the gas stripping reflux device includes a gas stripping aeration pipeline and a fan for introducing gas into the gas stripping aeration pipeline.
In one embodiment of the present invention, the aeration pipeline in the air stripping device is an aerator.
The utility model discloses an in one embodiment biochemical anoxic zone bottom sets up first aeration equipment biochemical aerobic zone bottom sets up second aeration equipment, first aeration equipment is used for realizing the stirring of biochemical anoxic zone interior material through gaseous, second aeration equipment is used for realizing the stirring of biochemical aerobic zone interior material through gaseous on the one hand, and on the other hand is used for letting in oxygen to biochemical aerobic zone.
In one embodiment of the present invention, the first aeration device and the second aeration device each include an aeration pipeline and a blower for introducing gas into the aeration pipeline.
In an embodiment of the present invention, the air stripping device, the first aeration device and the second aeration device in the air stripping reflux device may adopt the following preferred design schemes:
in an embodiment of the present invention, the first aeration device adopts a perforated aeration pipe and maintains an anoxic state, and the gas stripping device and the second aeration device adopt microporous aeration to improve the transfer efficiency of oxygen.
The aeration pipelines in the air stripping device, the first aeration device and the second aeration device adopt low-flux high-efficiency aerators, and the unit ventilation volume is 0.5-1.0m3And the fans in the air stripping device, the first aeration device and the second aeration device adopt efficient single-stage high-speed centrifugal fans. In one embodiment of the present invention, the method is as followsAn inclined plate or an inclined pipe is arranged in the sludge settling zone.
In one embodiment of the present invention, an aeration pipe is provided at the bottom of the sludge settling zone for washing the inclined plate or the inclined pipe to prevent the inclined plate or the inclined pipe from being clogged.
In one embodiment of the present invention, the submerged membrane treatment unit is selected from submerged ultrafiltration SMF or membrane bioreactor MBR.
Compared with the prior art, the utility model has the advantages of it is following and beneficial effect:
1. the utility model discloses in adopt air stripping reflux unit, based on unique air stripping circulation backward flow, realize the big proportion backward flow of biochemical aerobic zone to biochemical anoxic zone on the basis that does not increase power equipment, can realize the denitrogenation of high-efficient low energy consumption, the backward flow of big proportion can increase substantially the shock resistance of system simultaneously.
2. The utility model discloses in adopt efficient bottom aeration technique and efficient single-stage high-speed centrifugal fan's use, realized reducing by a wide margin of sewage factory operation energy consumption.
3. The utility model discloses a high-efficient sludge sedimentation tank's setting can reduce investment and the high-efficient sedimentation tank of energy consumption by a wide margin and can improve surface load, and it is controllable to produce water suspended solid concentration, provides more possibilities for follow-up membrane technology, the utility model discloses effectively combine high-efficient sedimentation tank and membrane tank, as the part of the low energy consumption's of high flux EMBR technology, can effectively improve membrane flux and reduce the operation energy consumption of membrane.
4. The utility model discloses produce the water suspended solid to high-efficient sedimentation tank in the system and detect control, can effectively switch the seamless switching of two kinds of technologies of submergence formula ultrafiltration SMF technology and membrane bioreactor MBR.
5. The utility model discloses the system can add chemical agent in the membrane pond, can realize the advanced treatment of membrane technology.
6. The utility model discloses except that immersed membrane processing unit need use the pump, other links can all not use the pump, practice thrift a large amount of energy consumptions.
In summary, the following steps: high-efficient EMBR system, the advantage of biochemical system, membrane technology and materialization technology has been synthesized. The biochemical system is optimized through an aeration system and a large-proportion backflow system, so that the operation energy consumption is greatly reduced; meanwhile, due to the arrangement of the high-efficiency sludge sedimentation tank, the operation mode of the membrane process can be flexibly switched according to the quality of the incoming water; when the COD and the chromaticity of the produced water have higher requirements, the quality of the product water can be further improved through the separation effect of a physicochemical process and a membrane process by adding a chemical agent, and the method can adapt to different requirements.
Drawings
FIG. 1 is a schematic structural diagram of an efficient and low-energy-consumption EMBR biochemical treatment system in embodiment 1 of the present invention.
Fig. 2 is a schematic structural view of the air stripping reflux unit of the present invention. The direction of the arrows in fig. 2 indicates the direction of liquid flow.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.
Example 1
Referring to fig. 1, the embodiment provides a high-efficiency low-energy-consumption EMBR biochemical treatment system, which includes a biochemical anoxic zone 1, a biochemical aerobic zone 2, a sludge settling zone 3 and a membrane tank 4, which are connected in sequence, where the biochemical anoxic zone 1 is used for anoxic treatment of sewage, the biochemical aerobic zone 2 is used for aerobic treatment of sewage, the sludge settling zone 3 is used for sludge settling treatment of treatment liquid treated by the biochemical aerobic zone 2, the membrane tank 4 is used for membrane treatment of sewage treated by the sludge settling zone 3, an immersed membrane treatment unit 6 is arranged in the membrane tank 4, and the immersed membrane treatment unit 6 is used for realizing membrane water production;
the biochemical aerobic zone 2 is also connected to the biochemical anoxic zone 1 through a gas stripping reflux device 5, and the gas stripping reflux device 5 between the biochemical aerobic zone 2 and the biochemical anoxic zone 1 is used for refluxing the nitrified liquid treated by the biochemical aerobic zone 2 to the biochemical anoxic zone 1;
the sludge settling zone 3 and the membrane tank 4 are also connected to the biochemical aerobic zone 2 through a gas stripping reflux device 5;
and the gas stripping reflux device 5 connected with the sludge settling zone 3 and the membrane tank 4 is used for refluxing the sludge in the sludge settling zone 3 and the membrane tank 4 to the biochemical aerobic zone.
Referring to fig. 2, in the present embodiment, the stripping reflux unit 5 includes a tank 51, the tank 51 is provided with a feed inlet and a discharge outlet, a first wall 52 and a second wall 53 are arranged in the tank 51, a feed area 55 is arranged between the feed inlet and the first wall 52, a discharge area 56 is arranged between the discharge outlet and the second wall 53, a stripping unit 54 is further arranged between the first wall 52 and the second wall 53, a stripping area 57 is arranged between the first wall 52 and the second wall 53,
the top of the first wall 52 exceeds the liquid level of the pool body 51, and the bottom is not closed and provided with a reserved hole for water passing; a gap is reserved between the top of the second wall 53 and the top of the tank body 51, and the bottom of the second wall 53 is not crossed with water, namely the top of the second wall 53 is lower than the liquid level;
the first wall 52 and the second wall 53 are arranged so that liquid in the feeding area 55 enters the stripping area 57 from a reserved hole between the first wall 52 and the bottom of the tank body 51, and the stripping device 54 is used for driving the material flow in the stripping area 57 to ascend and flow out to the discharging area 56 from a reserved hole between the second wall 53 and the top of the tank body 51.
In this embodiment, the gas stripping device 54 in the gas stripping reflux device 5 includes a gas stripping aeration line and a blower for introducing gas into the gas stripping aeration line.
In this embodiment, a first aeration device 7 is disposed at the bottom of the biochemical anoxic zone 1, a second aeration device 8 is disposed at the bottom of the biochemical aerobic zone 2, the first aeration device 7 is used for stirring materials in the biochemical anoxic zone 1 through gas, and the second aeration device 8 is used for stirring materials in the biochemical aerobic zone 2 through gas and introducing oxygen into the biochemical aerobic zone 2.
In this embodiment, each of the first aeration apparatus 7 and the second aeration apparatus 8 includes an aeration pipeline and a blower for introducing gas into the aeration pipeline.
In this embodiment, the air stripping device 54, the first aeration device 7 and the second aeration device 8 in the air stripping reflux device 5 are all adoptedThe following preferred design: the aeration pipelines in the air stripping device 54, the first aeration device 7 and the second aeration device 8 adopt low-flux high-efficiency aerators, and the unit ventilation volume is 0.5-1.0m3The ratio of the water to the water is/m/h; the fans in the air stripping device 54, the first aeration device 7 and the second aeration device 8 adopt high-efficiency single-stage high-speed centrifugal fans.
In this embodiment, an inclined plate or pipe 9 is provided in the sludge settling zone 3.
In this embodiment, an aeration pipe is provided at the bottom of the sludge settling zone 3 for washing the inclined plate or inclined pipe 9 to prevent the inclined plate or inclined pipe 9 from being clogged.
In this embodiment, the submerged membrane treatment unit 6 is selected from submerged ultrafiltration SMF or membrane bioreactor MBR.
Referring to fig. 1, this embodiment further provides a high-efficiency and low-energy-consumption EMBR biochemical treatment process, including the following steps:
the sewage enters a biochemical anoxic zone 1 and a biochemical aerobic zone 2 in sequence for biochemical treatment;
the nitrifying liquid treated in the biochemical aerobic zone 2 flows back to the biochemical anoxic zone 1 through the gas stripping reflux device 5 for biological denitrification, and the rest treating liquid enters the high-efficiency settling zone 3 for sludge settling treatment;
the sewage treated by the sludge settling zone 3 enters a membrane tank 4 for treatment, an immersed membrane treatment unit 6 is arranged in the membrane tank 4, membrane water production is realized by the immersed membrane treatment unit 6, and the sludge obtained in the sludge settling zone 3 and the membrane tank 4 flows back to the biochemical aerobic zone 2 through an air stripping reflux device 5.
In this embodiment, due to the special design of the first wall 52, the second wall 53 and the stripping device 54 in the stripping reflux device 5, when air is introduced into the stripping device 54, air stripping can drive water to move upwards during aeration because the density of the air is lower than that of the water, so that a micro negative pressure state is formed at the bottom; after the water flow moves upwards, the water flow can only move towards the second wall 53 because the first wall 52 blocks the water flow. Under the drive of the gas, the water flow formed by the micro negative pressure formed at the lower left side enters and moves upwards due to low gas density, so that continuous water inlet and outlet are formed. The lifting height of the liquid level is controlled within 200mm from the design, and the energy consumption requirement is reduced to the minimum while the maximum reflux quantity is realized.
In this embodiment, the first aeration device 7 is filled with oxygen-free gas, and the second aeration device 8 is filled with oxygen-containing gas for metabolism of microorganisms.
In this embodiment, if the concentration of suspended solids in the water produced by the sludge settling zone 3 is controlled to be above 5000mg/L, the submerged membrane treatment unit 6 selects the membrane bioreactor MBR, and the membrane process section operates according to the MBR process mode.
In this embodiment, if the concentration of suspended matters in the water produced in the sludge settling zone 3 is controlled within 100mg/L, the submerged ultrafiltration SMF is selected by the submerged membrane processing unit 6, and the membrane process section operates according to the submerged ultrafiltration SMF process mode.
In the embodiment, when the actual water quantity or water quality is far lower than the design in the previous period, an operation mode of immersed ultrafiltration SMF is adopted; when the actual water quantity or water quality reaches or slightly exceeds the original design standard, switching to an MBR operation mode; when the COD of the biochemical produced water reaches a certain bottleneck through biodegradation and can not be reduced any more and the water quality of the produced water needs to be improved, the mode is switched to the SMF mode.
In the embodiment, chemical agents are added into the membrane tank to form micro flocculation, and then membrane separation is directly carried out to further reduce COD and chroma so as to obtain water quality superior to biochemical and MBR produced water.
In the embodiment, the air stripping reflux device 5 is adopted to realize the reflux of the sewage and muddy water mixture, and the problem of high energy consumption caused by the fact that a material conveying pump is required to realize the reflux in the traditional process is solved.
The part of nitrifying liquid after 2 processings in biochemical aerobic zone through air stripping reflux unit 5 backward flows to biochemical anoxic zone 1 and explains the adoption the utility model discloses air stripping reflux unit 5 can bring the reason of the reduction of energy consumption:
in general, biological denitrification is realized by adopting an A/O (anoxic-aerobic) process, ammonia nitrogen in raw water is converted into nitrate nitrogen under the action of nitrifying bacteria in an aerobic environment by sewage, and then the mixed solution of the nitrate nitrogen flows back to an anoxic section and is mixed with the raw water under the action of denitrifying bacteria to realize the biological denitrification. The sludge reflux ratio for biological denitrification in the current design specifications is recommended to be 3-4 times, and the main reason is due to the limitation of denitrification efficiency, for example, 3 times Q of reflux has denitrification efficiency of 3/(1+3) ═ 75%; 4 times of Q, the denitrification efficiency is 80 percent (4/(1 + 4)); the denitrification efficiency of 5 times Q refluxing is 83 percent (5/(1 + 5)). When the reflux is increased from 3 times to 4 times, the theoretical denitrification efficiency is only improved by 5 percent; when the reflux is increased from 4 times to 5 times, the theoretical denitrification efficiency is only improved by 3 percent, and the marginal effect is reduced obviously.
Generally, the circulating reflux of the nitrified liquid needs to be realized through a water pump, and the power cost for realizing the denitrification by improving the reflux ratio is higher. The minimum lift of the centrifugal pump is about 6m, the lift of the axial pump can be 2-3m (the minimum power is 7.5kw), and the conventional centrifugal pump has a large amount of loss on the lift. E.g. 5000m3D wastewater to achieve 3 times of reflux (Q: 630 m)3H), the annual power consumption is about 7.5 multiplied by 24 multiplied by 365 to 6.57 ten thousand KWH according to the axial flow pump with the lowest energy consumption of 7.5 kw; to achieve 5 times the reflux amount (Q: 1050 m)3H) with a power of 15kw and an electrical consumption of about 7.5 × 2 × 24 × 365 ═ 13.14 ten thousand KWH per year.
The marginal effect that causes for the big proportion backward flow that avoids the high energy consumption of backwash pump and denitrogenation needs, the utility model discloses in adopt air stripping reflux unit to realize high-efficient air stripping circulation backward flow, can reduce the energy consumption by a wide margin.
In the embodiment, a gas stripping reflux device and a gas stripping system are adopted, wherein the gas stripping system is 1000m3Flow rate is only 1.0m3The air flow of the fan per minute is converted into energy consumption of 1.5kwh, and the annual operating power consumption is as follows: 1.5 is multiplied by 24 and 365 is 1.3 ten thousand KWH, and the energy is saved by over 90 percent. It is worth mentioning that the oxygen dissolved in the wastewater by gas stripping can still be utilized by the following microorganisms, so that this part of the energy is not wasted at all. Because a huge reflux ratio can be provided, the denitrification efficiency is greatly improved without being limited by the reflux ratio.
Meanwhile, due to the huge reflux ratio provided by the circulating system, the system realizes the advantage of complete mixing, and the impact resistance of the system is greatly improved by responding to the fluctuation of the water quality of raw water.
In the embodiment, when the air stripping reflux device is adopted to realize the reflux of the Sludge, an Enhanced-Cyclic Activated Sludge process (ECAST) is formed, and the operation energy consumption can be greatly reduced.
As is known, in the whole operation cost of a sewage plant, the power consumption occupies 50-60% of the operation cost of the water plant, and particularly, the fan adopted for aeration occupies 30-50% of the operation cost of the whole sewage plant, so that how to reduce the energy consumption of the fan of the sewage plant becomes the key for controlling the operation cost of the sewage plant, and the system effectively saves energy by more than 40% by adopting the following three ways:
1. the high-efficiency aeration system comprises: the test of the aeration system is carried out under the clear water condition of 6m water depth, and the deeper the water depth condition is, the higher the oxygen mass transfer efficiency of aeration is; the lower the aeration per unit membrane, the higher the oxygen mass transfer efficiency. At present, most of microporous aerators commonly used in the market are disc aerators and tubular aerators, and under the condition of 6m water depth, the oxygen mass transfer efficiency can reach 20-25%, and the unit ventilation volume is 4-8m3The ratio of the water to the water is/m/h. The high-efficiency dissolved oxygen aeration technology arranged in the system mainly adopts a low-flux high-efficiency aerator, and the unit ventilation volume is 0.5-1.0m3The oxygen mass transfer efficiency can be improved to 30-35% under the condition of 6m water depth, the oxygen transfer efficiency is improved by 30-50% through the optimization of aeration equipment, and the power of a fan is greatly reduced. Zhejiang Shaoxing certain printing and dyeing mill 5000m3The printing and dyeing wastewater is taken as an example (put into production), the oxygen transfer efficiency of the original aeration system is 20 percent, and the design is 2 tables with 42Nm3And the roots blower has the advantages of min (3 sets in total, 2 sets in 1 set), wind pressure of 7m, fan shaft power of 65kw and motor power of 75 kw. In 2017, by adopting the high-efficiency low-flux aeration system, the oxygen transfer efficiency reaches 35 percent, and the air quantity requirement is 42Nm3Min to 31Nm3And/min, the frequency of the fan is reduced from 48HZ to 38HZ, the shaft power is only 44kw, and the power consumption is greatly reduced.
2. High-efficient fan: the most mainstream fans applied in the current market are a multistage centrifugal fan and a Roots fan (or a screw fan), and if the fan is replaced by a high-efficiency single fanThe high-speed centrifugal fan has different structure forms, and adopts air bearing or magnetic suspension bearing, so that the idle loss of mechanical friction force is eliminated, and the power is greatly reduced. Zhejiang Shaoxing certain printing and dyeing mill 5000m3The original configuration is 42Nm through energy-saving transformation by taking the printing and dyeing wastewater of/d as an example3The Roots blower with the speed of min, wind pressure of 7m, fan shaft power of 65kw and motor power of 75kw is replaced by 31Nm3Min, wind pressure 7m, shaft power 38kw and motor power 44 kw.
3. Accurate dissolved oxygen control system: in the operation process, because the water volume loads in different time periods are different, if the operation is carried out according to the conventional fixed frequency, the excessive dissolved oxygen at the low load can be caused, and the energy consumption of the fan is wasted. Because the system adopts large circulation reflux control, the dissolved oxygen at each point is relatively uniform, and the adjustment of the fan according to the dissolved oxygen is very stable and easy to realize. The operation frequency of the fan is synchronously adjusted through the feedback control of dissolved oxygen, and the operation energy consumption can be saved by 5-10%.
Therefore, because a high-efficiency aeration system and a single-stage high-speed centrifugal fan are adopted, and a dissolved oxygen accurate control system is adopted, the power of a motor is reduced to 44kw from 2 original tables of 75kw, the shaft power is reduced to 38kw from 2 tables of 65kw, the average energy consumption is reduced to (65-38)/65-41.5%, and the running power consumption (65-38) and 2 × 24 × 365 is saved to 47.3 ten thousand kwh one year.
By effectively combining the methods, the aerodynamic consumption of the sewage plant can be reduced by 40-50%, and the electric energy consumption can be effectively reduced in the sewage plant.
In the embodiment, the surface load of the sedimentation tank is greatly improved by adding the inclined pipe/inclined plate in the sludge sedimentation area, the surface load of the secondary sedimentation tank is 0.6-1.5m/h in the specification, and the actual design value is mostly 0.5-0.75 m/h. The surface load of the invention can be increased to 1.5-2.7m/h by adding the inclined tube, thus greatly reducing the occupied area. Meanwhile, in order to prevent the sludge from blocking the inclined plate, the bottom of the settling zone is provided with an aeration pipe, and the flushing inclined plate can be opened at regular time.
In general, in order to realize sludge-water separation of a biochemical system, either a traditional secondary sedimentation tank is selected for sludge-water separation, or an efficient MBR membrane process is selected for sludge-water separation. However, the traditional secondary sedimentation tank has low surface load and large occupied area, effluent suspended matters are not easy to control, and effluent quality is unstable; the effluent quality of the MBR process is guaranteed, but the equipment cost and the operation cost are increased. In the embodiment, the high-flux and low-energy-consumption EMBR process can be obtained by arranging the high-efficiency sedimentation tank. The efficient sludge sedimentation tank is arranged between the biochemical process and the membrane tank, and has the following advantages:
1. the high sludge concentration (6000-8000mg/L) of the biochemical system is maintained through the high-efficiency precipitation process, and the high sludge concentration is also obtained. Meanwhile, the sludge of the biochemical system can flow back through the high-efficiency sedimentation tank, the concentration value (such as 100-1000mg/L) of the sludge entering the membrane tank can be controlled, a small part of residual sludge enters the membrane tank, and the effluent is separated through the MBR to obtain the quality of the water produced by the MBR.
2. The submerged ultrafiltration SMF process can be operated at low sludge concentration, thereby greatly improving the operating flux of the membrane and reducing the operating energy consumption thereof. In a certain printing and dyeing wastewater project in Zhejiang, the operation flux of the membrane is improved from 15LMH to about 20LMH by the arrangement of the efficient sedimentation tank, and the water production flux performance is improved by 33%. When the investment cost is converted into the investment cost of a new project, the cost of the membrane product can be reduced by about 30 percent, and the investment cost is greatly reduced.
3. When the effluent quality requirement is high, the effluent suspended matter concentration of the high-efficiency sedimentation tank is controlled, the sludge in the sedimentation tank is totally refluxed, and the residual sludge is discharged into the membrane tank. Chemical agents are added into the membrane tank, and after micro flocculation is generated, the micro flocculation is directly separated through an MBR membrane, so that the water quality of product water is further improved, and residual sludge is directly concentrated and then discharged.
In conclusion, the efficient and low-energy-consumption EMBR process can be obtained through the arrangement of efficient precipitation.
In this embodiment, the membrane process can be seamlessly switched between the submerged ultrafiltration SMF and membrane bioreactor MBR processes by optimal design and control of the process.
In general, RO process is mostly used for desalination in order to realize reuse of reclaimed water. Before the RO, the membrane at ultrafiltration level is mostly needed to be pretreated, and the processes such as external ultrafiltration UF, submerged ultrafiltration SMF or membrane bioreactor MBR process are usually adopted.
Compared with pressure type ultrafiltration, the submerged type ultrafiltration SMF is characterized in that a membrane is placed in a membrane pool by submerged type ultrafiltration, the requirement of water inflow is wider than that of pressure type ultrafiltration UF, and the pollution resistance is strong. The membrane has high water yield and low operation energy consumption, but compared with MBR, the membrane has low requirement on the concentration of influent suspended matters and weak anti-pollution capability.
The membrane bioreactor MBR is mainly applied to a sewage treatment process, and the membrane separation technology is organically combined with the traditional wastewater biological treatment technology, so that the solid-liquid separation efficiency is greatly improved; meanwhile, the generation amount of excess sludge is reduced by reducing the F/M ratio, so that a plurality of outstanding problems existing in the traditional activated sludge method are solved, but the membrane flux is lower, and the operation energy consumption is higher.
Meanwhile, in the beginning of design, a plurality of sewage plants are difficult to determine the real and accurate water quality and water quantity, and great difficulty is brought to the operation of the sewage plants. The actual water quantity or water quality in the early stage of operation may be far lower than the design standard under normal conditions; in the actual operation process, the deviation between the actual inlet water quality and the designed water quality is large, and the uncertainty of the system in operation and the flexibility of operation need to be fully considered.
In the embodiment, the concentration of suspended matters in the effluent of the high-efficiency sedimentation tank can be controlled through optimal design and process control, and the membrane process can operate under different suspended matter concentrations to adapt to different process conditions.
a) If the concentration of suspended matters in the precipitated water is controlled to be more than 5000mg/L, the membrane process section operates according to the MBR process mode, scrubbing, backwashing and chemical cleaning are carried out at regular time, and the produced water enters the subsequent advanced treatment process section.
b) If the concentration of suspended matters in the water produced by precipitation is controlled within 100mg/L, most of sludge flows back to the front section of the biochemical system through the sedimentation tank, the operation flux of the membrane can be greatly improved, and the operation energy consumption is reduced. According to the scheme, after the Zhejiang dyeing wastewater is reformed, the SMF mode is switched to the immersed ultrafiltration SMF mode. The running flux is improved from 15LMH to 20LMH, and the productivity is improved by 33%; meanwhile, the continuous operation of the aeration fan is changed into 1 hour of every 3 hours, and the operation energy consumption is reduced by 75 percent.
The optimal design of the biochemical system and the seamless switching of the membrane process in the embodiment can effectively cope with the working condition of large concentration variation range of suspended matters.
When the actual water quantity or water quality is far lower than the design in the previous period, the operation mode of the immersed ultrafiltration SMF can be adopted. Activated sludge is intercepted by the efficient sedimentation tank, and the concentration of low suspended matters in the effluent is controlled, so that the operation condition of obtaining SMF is adopted, the low aeration rate can be adopted, the quality of the produced water can meet the pretreatment requirement of reuse water, and the operation cost can be effectively reduced; when the actual water quantity or water quality reaches or slightly exceeds the original design standard (especially total nitrogen), the MBR operation mode can be switched. The sludge concentration in the biochemical tank is increased in advance through the high-efficiency sedimentation tank, the microorganism concentration is further increased through an MBR process, and the sludge load of the system is reduced. Meanwhile, the denitrification capability of the system can be improved through multi-point water inlet and multi-stage large-proportion circulating reflux in the ECAST system.
When the COD of the biochemical produced water reaches a certain bottleneck through biodegradation and can not be reduced any more and the water quality of the produced water needs to be improved, the mode can be switched to the SMF mode.
In the embodiment, ECAST can be independently operated, sludge of a biochemical system flows back through the high-efficiency sedimentation tank, effluent enters the membrane tank, chemical agents are added into the membrane tank to form micro flocculation and then are directly separated, COD (chemical oxygen demand) and chromaticity can be further reduced, and the water quality superior to that of biochemical and MBR (membrane bioreactor) produced water is obtained.
The embodiment discloses an efficient and low-energy-consumption EMBR biochemical treatment process (eco Membrane Biological Reactor) which mainly comprises a biochemical treatment Enhanced circulating Activated Sludge process ECAST (Enhanced-Cyclic Activated Sludge Technology) and a Membrane process Membrane Bioreactor (MBR) Technology, and realizes the optimization and upgrading of a water treatment process flow.
The embodiments described above are intended to facilitate the understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention according to the disclosure of the present invention.
Claims (10)
1. The high-efficiency low-energy-consumption EMBR biochemical treatment system is characterized by comprising a biochemical anoxic zone (1), a biochemical aerobic zone (2), a sludge settling zone (3) and a membrane pool (4) which are sequentially connected, wherein the biochemical anoxic zone (1) is used for carrying out anoxic treatment on sewage, the biochemical aerobic zone (2) is used for carrying out aerobic treatment on sewage, the sludge settling zone (3) is used for carrying out sludge settling treatment on treatment liquid treated by the biochemical aerobic zone (2), the membrane pool (4) is used for carrying out membrane treatment on sewage treated by the sludge settling zone (3), an immersed membrane treatment unit (6) is arranged in the membrane pool (4), and the immersed membrane treatment unit (6) is used for realizing membrane water production;
the biochemical aerobic zone (2) is also connected to the biochemical anoxic zone (1) through an air stripping reflux device (5), and the air stripping reflux device (5) between the biochemical aerobic zone (2) and the biochemical anoxic zone (1) is used for refluxing the nitrified liquid treated by the biochemical aerobic zone (2) to the biochemical anoxic zone (1);
the sludge settling zone (3) and the membrane tank (4) are further connected to the biochemical aerobic zone (2) through a gas stripping reflux device (5), and the gas stripping reflux device (5) connected with the sludge settling zone (3) and the membrane tank (4) is used for refluxing the sludge in the sludge settling zone (3) and the membrane tank (4) to the biochemical aerobic zone (2).
2. The high-efficiency low-energy-consumption EMBR biochemical treatment system according to claim 1, wherein the air stripping reflux device (5) comprises a tank body (51), the tank body (51) is provided with a feeding port and a discharging port, a first wall body (52) and a second wall body (53) are arranged in the tank body (51), a feeding area (55) is arranged between the feeding port and the first wall body (52), a discharging area (56) is arranged between the discharging port and the second wall body (53), an air stripping device (54) is further arranged between the first wall body (52) and the second wall body (53), an air stripping area (57) is arranged between the first wall body (52) and the second wall body (53),
the top of the first wall body (52) exceeds the liquid level of the tank body (51), and a reserved hole is formed in the bottom of the first wall body and is not closed for water passing; a gap is reserved between the top of the second wall body (53) and the top of the tank body (51), and the bottom of the second wall body is not crossed with water;
the first wall body (52) and the second wall body (53) are arranged so that the material flow of the feeding area (55) enters the stripping area (57) from a reserved hole between the first wall body (52) and the bottom of the tank body (51), and the stripping device (54) is used for driving the material flow of the stripping area (57) to ascend and flow out to the discharging area (56) from a reserved hole between the second wall body (53) and the top of the tank body (51).
3. The high-efficiency low-energy-consumption EMBR biochemical treatment system according to claim 2, characterized in that the gas stripping device (54) comprises a gas stripping aeration line and a fan for introducing gas into the gas stripping aeration line.
4. The high-efficiency low-energy-consumption EMBR biochemical treatment system according to claim 3, characterized in that the aeration pipeline in the air stripping device (54) adopts an aerator, and the unit aeration is 0.5-1.0m3/m/h；
An aeration pipeline in the air stripping device (54) is a microporous aeration pipe;
the fan in the air stripping device (54) adopts a single-stage high-speed centrifugal fan.
5. A high-efficiency low-energy-consumption EMBR biochemical treatment system according to claim 1, wherein a first aeration device (7) is arranged at the bottom of said biochemical anoxic zone (1), a second aeration device (8) is arranged at the bottom of said biochemical aerobic zone (2), said first aeration device (7) is used for stirring the materials in the biochemical anoxic zone (1) by gas, said second aeration device (8) is used for stirring the materials in the biochemical anoxic zone (2) by gas on one hand, and for introducing oxygen into the biochemical aerobic zone (2) on the other hand.
6. A high efficiency and low energy consumption EMBR biochemical treatment system according to claim 5, characterized in that the first aeration device (7) and the second aeration device (8) each comprise an aeration line and a blower for introducing gas into the aeration line.
7. A high efficiency and low energy consumption EMBR biochemical treatment system according to claim 6, wherein the aeration pipeline of said first aeration apparatus (7) and said second aeration apparatus (8) is composed of aerators with unit aeration rate of 0.5-1.0m3The ratio of the water to the water is/m/h; the fans in the first aeration device (7) and the second aeration device (8) adopt single-stage high-speed centrifugal fans;
the aeration pipe of the first aeration device (7) is a perforated aeration pipe, and the aeration pipeline in the second aeration device (8) is a microporous aeration pipe.
8. A high efficiency and low energy consumption EMBR biochemical treatment system according to claim 1, characterized in that an inclined plate or tube (9) is arranged in the sludge settling zone (3).
9. A high efficiency and low energy consumption EMBR biochemical treatment system according to claim 1, wherein an aeration pipe is provided at the bottom of the sludge settling zone (3).
10. A high efficiency, low energy consumption EMBR biochemical treatment system according to claim 1, wherein the submerged membrane treatment unit (6) is selected from submerged ultrafiltration SMF or membrane bioreactor MBR.
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