CN114751560A - Air-floated water treatment device and treatment method thereof - Google Patents
Air-floated water treatment device and treatment method thereof Download PDFInfo
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- CN114751560A CN114751560A CN202210533657.9A CN202210533657A CN114751560A CN 114751560 A CN114751560 A CN 114751560A CN 202210533657 A CN202210533657 A CN 202210533657A CN 114751560 A CN114751560 A CN 114751560A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000005189 flocculation Methods 0.000 claims abstract description 94
- 230000016615 flocculation Effects 0.000 claims abstract description 94
- 238000006243 chemical reaction Methods 0.000 claims abstract description 73
- 238000005345 coagulation Methods 0.000 claims abstract description 56
- 230000015271 coagulation Effects 0.000 claims abstract description 56
- 239000007788 liquid Substances 0.000 claims abstract description 48
- 238000000926 separation method Methods 0.000 claims abstract description 35
- 238000005188 flotation Methods 0.000 claims abstract description 34
- 239000002245 particle Substances 0.000 claims abstract description 30
- 238000005276 aerator Methods 0.000 claims abstract description 29
- 238000005273 aeration Methods 0.000 claims abstract description 28
- 230000000694 effects Effects 0.000 claims abstract description 28
- 239000010802 sludge Substances 0.000 claims abstract description 28
- 239000012528 membrane Substances 0.000 claims abstract description 25
- 239000008213 purified water Substances 0.000 claims abstract description 17
- 238000005192 partition Methods 0.000 claims abstract description 15
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- 238000007599 discharging Methods 0.000 claims abstract description 8
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- 239000002131 composite material Substances 0.000 claims abstract description 7
- 239000004810 polytetrafluoroethylene Substances 0.000 claims abstract description 7
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims abstract description 7
- 239000010865 sewage Substances 0.000 claims description 31
- 230000003311 flocculating effect Effects 0.000 claims description 23
- 239000000470 constituent Substances 0.000 claims description 18
- 239000000701 coagulant Substances 0.000 claims description 14
- 239000000084 colloidal system Substances 0.000 claims description 13
- 239000003344 environmental pollutant Substances 0.000 claims description 13
- 231100000719 pollutant Toxicity 0.000 claims description 13
- 230000003068 static effect Effects 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 11
- 238000012544 monitoring process Methods 0.000 claims description 10
- 238000001179 sorption measurement Methods 0.000 claims description 10
- 238000013461 design Methods 0.000 claims description 9
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- 238000012423 maintenance Methods 0.000 claims description 5
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- 230000003993 interaction Effects 0.000 claims description 4
- 238000006386 neutralization reaction Methods 0.000 claims description 4
- 229920000642 polymer Polymers 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 3
- 230000005856 abnormality Effects 0.000 claims description 3
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 3
- 238000010276 construction Methods 0.000 claims description 3
- 238000001514 detection method Methods 0.000 claims description 3
- 125000001165 hydrophobic group Chemical group 0.000 claims description 3
- 238000011065 in-situ storage Methods 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- 239000013307 optical fiber Substances 0.000 claims description 3
- 229920002401 polyacrylamide Polymers 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
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- 239000007789 gas Substances 0.000 description 9
- 238000010992 reflux Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000009300 dissolved air flotation Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5209—Regulation methods for flocculation or precipitation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/03—Pressure
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/42—Liquid level
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
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- General Chemical & Material Sciences (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
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Abstract
The invention relates to an air flotation water treatment device and a treatment method thereof, wherein the device integrates coagulation, flocculation and flotation and comprises the following components: the system comprises a coagulation reaction zone, a flocculation turbulent flow zone, a flow guide zone, a bubble adhesion zone, a solid-liquid separation zone, a sludge discharge channel, a purified water flow guide channel, a water outlet channel, a coagulation reaction zone stirrer, a weir plate, a flocculation turbulent flow zone partition plate, a micron aerator, a purified water flow guide channel flow turbulent flow plate, a flow guide wall, a mud scraper and a high-level mud discharging weir. The flocculation turbulence area partition plate and the micron aerator are adopted, so that the power consumption is saved by 70-85%, and the operating cost is reduced; the hollow fiber membrane of the PTFE composite ceramic particles is adopted for aeration, the removal rate of suspended matters is 90-99%, the turbidity of effluent is less than or equal to 4NTU, and the air floatation turbidity removal treatment effect is good; the hollow fiber membrane of the PTFE composite ceramic particles is a high-strength flexible membrane, and can be disturbed along with water flow washing, so that the micron aerator is prevented from being polluted and blocked; the aeration mode of the invention is continuous stable pressure aeration, and the aeration device can be started and stopped at any time without influencing the service life of the device.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an air-floated water treatment device and a treatment method thereof.
Background
The air floatation is a water purification method which is characterized in that a large amount of highly dispersed micro-bubbles are introduced into a water body to be adhered with light colloid in the water to form floating slag with the specific gravity smaller than that of the water to float on the water surface, so that solid-liquid separation is carried out. The key point influencing the treatment effect of the air floatation process is the design of the state and the flow state of bubbles.
According to the principle of bubble generation, the method can be divided into electrolytic air flotation process, pressurized dissolved air decompression air flotation process, dispersed air flotation process and the like. The electrolysis air floatation process is mainly a method for floating and removing light flocs in water by utilizing electrolytic reaction generated on two sides of an electrode and by utilizing the generated hydrogen nano bubbles to contact and adhere the light flocs, but the method has high energy consumption and needs to replace electrode plates in time, so the method is generally suitable for the micro bubble application field with higher precision requirement; the pressurized dissolved air decompression air-float technology is the most common technology, also called dissolved air-float technology, the technology is to dissolve the gas in the water under certain pressure condition, and reach the saturation state of the gas under the temperature, then release the high-pressure and high-saturation dissolved air water through decompression air-release device, the reduction of the pressure will promote the part of the gas dissolved in the water by the high pressure to continuously separate out, and then form the micro-nano bubble, adhere to the floc in the air-float contact chamber, then float to the water surface, use the scum scraping technology of the scum machine, the technology is widely applied at present; the dispersed air floatation process is that air is sheared, mixed and dissolved in water through a high-speed rotating machine, large bubbles are split into tiny bubbles, and the tiny bubbles are stabilized in a pressure stabilizing tank and then are introduced into an air floatation tank to achieve the effect of removing pollutants. At present, micropore aeration is not adopted in the industry, because the micropore aeration is limited to aeration aperture diameter more than micron, the generated bubbles generally belong to millimeter level, and the flotation effect is poor.
The flotation area has the function that the air-entrained flocs float up to the water surface and are scraped by mud scraping equipment. The air-entrained flocs are subjected to the interaction of gravity, buoyancy and resistance in the water body. The integral density of the air-entrained flocs is reduced along with the increase of the content of bubbles in the flocs, the volume of the air-entrained flocs is relatively increased, the rising speed is also increased, and the air-entrained flocs are easier to float to the water surface. The flotation area is divided into a horizontal flow type flotation tank, a vertical flow type flotation tank, a shallow layer high-efficiency flotation tank, a copolymerization flotation tank, an ion flotation tank, a circular flotation tank, a reverse-cocurrent flow flotation tank and the like according to the structure type. The structural design of the flotation area influences the flow state of water flow, and further influences the upward floating of air-entrained flocs. If the flow state is disordered, the air-entrained flocs can enter the produced water along with the water flow, and the quality of the discharged water is influenced.
At present, the widely used air floatation device has the following problems:
1. during air floatation, the grain size of micro bubbles is a key factor influencing the treatment efficiency, and the dissolved air pressure of a widely applied pressurized dissolved air decompression method directly influences the size of the grain size of the bubbles. The working pressure of the dissolved air tank is 0.3-30 MPa, the working pressure of the dissolved air releaser is 0.1-5 MPa, the working pressure of the air compressor is 0.08-33 MPa, and the reflux water is set as the dissolved air water, and the reflux ratio is 5-16%. Therefore, equipment such as a dissolved air compressor, a reflux pump and the like needs to be arranged, and the main power consumption is in the part.
2. The pressure releaser belongs to a vulnerable part because of pressure change. The filler type air dissolving tank has different types and specifications of fillers, and the filler is easy to block when the inlet water turbidity is high, so that the air dissolving efficiency of equipment is reduced; in the initial operation stage of the air floatation process, more impurities in water cause more sediment deposition in a dissolved air water pipeline, and blockage can be caused to a releaser.
3. Due to the structural design of the air floatation tank, the size of bubbles and the air floatation treatment effect are influenced by turbulence in the tank.
4. If the air floatation equipment is used for a discontinuous time, the idle period is longer, and if the air floatation equipment is not cleaned properly, the inner walls of the dissolved air tank and the dissolved air pipeline are corroded; the air compressor can be opened and closed frequently along with the fluctuation of the pressure stabilizing tank, and the equipment loss is large.
5. The conventional micropore aeration is limited to the aeration aperture diameter more than micron, the generated bubbles generally belong to millimeter level, the coalescence and rupture of the bubbles are serious, and the flotation effect is poor.
Disclosure of Invention
Aiming at the defects of the air floatation device in the prior art, the invention aims to: the air flotation water treatment device and the air flotation water treatment method have the advantages of being reasonable in structural design, capable of reducing air flotation process energy consumption, low in maintenance cost, capable of improving air flotation treatment effect, capable of being started and stopped at any time by the whole device and the like.
In order to achieve the purpose, the invention adopts the following technical scheme:
an air flotation water treatment device, which integrates coagulation, flocculation and flotation and comprises: the system comprises a coagulation reaction zone, a flocculation turbulent flow zone, a flow guide zone, a bubble adhesion zone, a solid-liquid separation zone, a sludge discharge channel, a purified water flow guide channel, a water outlet channel, a coagulation reaction zone stirrer, a weir plate, a flocculation turbulent flow zone partition plate, a micron aerator, a purified water flow guide channel flow turbulent flow plate, a flow guide wall, a mud scraper and a high-level mud discharging weir; wherein, a coagulation reaction zone stirrer is arranged in the coagulation reaction zone, the coagulation reaction zone stirrer is fixed with the top of the coagulation reaction zone through bolts, the coagulation reaction zone is connected with the flocculation reaction zone through a high-position water through hole, and the flocculation reaction zone is connected with the flocculation turbulent flow zone through a low-position water through hole; a static flocculation turbulence area clapboard is arranged in the flocculation turbulence area, and the fixed position of the static flocculation turbulence area clapboard is positioned at the top of the flocculation turbulence area and is fixed by bolts; the flocculation turbulent flow area is connected with the flow guide area through a high-position water passing hole, and the flow guide area is connected with the bubble adhesion area through a low-position water passing hole; the micron aerator is arranged in the bubble adhesion zone, laid in the middle of the bubble adhesion zone and fixed with the tank wall of the bubble adhesion zone through bolts, the bubble adhesion zone is connected with the solid-liquid separation zone, the connection part is a guide wall positioned between the bubble adhesion zone and the solid-liquid separation zone, and the height of the guide wall is lower than the highest liquid level of the bubble adhesion zone; the solid-liquid separation zone is connected with the sludge discharge channel through a high-level sludge discharge weir, and the upper part of the tank body of the solid-liquid separation zone is provided with a sludge scraper; the bottom of the solid-liquid separation zone is provided with a diversion canal diversion turbulent flow plate which is connected with a purified water diversion canal, the purified water diversion canal is connected with a water outlet canal through a high-level water tunnel, and the opening of the high-level water tunnel is provided with a weir plate.
As a further optimization of the scheme, a coagulant adding tank is arranged in the coagulation reaction zone, one of aluminum sulfate, polyaluminium chloride, ferric trichloride and polyferric sulfate is arranged in the coagulant adding tank, and the coagulant adding tank reacts with pollutants under the stirring of a stirrer in the coagulation reaction zone to form a flocculating constituent;
and an anion high-molecular flocculant dosing tank is arranged in the flocculation reaction zone, and polyacrylamide is arranged in the anion high-molecular flocculant dosing tank and used for providing an adsorption bridging effect to improve the flocculation effect.
As a further optimization of the scheme, the included angle between the axis of the guide wall and the vertical direction is 5-15 degrees.
As a further optimization of the scheme, the micron aerator adopts a hollow fiber membrane of PTFE composite ceramic particles, nano-scale micropores with the diameter of 10-40nm are uniformly distributed on the surface of a membrane wire of the hollow fiber membrane, air is supplied to the interior of the membrane wire through a fan or an air compressor, the air is released from the membrane hole, and the size of bubbles is stabilized between 10-40 mu m.
As a further optimization of the scheme, the device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, and a pressure sensor assembly, a flow sensor assembly, a liquid level sensor assembly, a concentration sensor assembly, a display assembly, an abnormality alarm assembly, an in-situ control station and a central monitoring station which are respectively connected with the programmable PLC controller; the pressure sensor assembly includes: the pressure sensor is arranged on the air inlet pipeline; the flow sensor assembly includes: the flow sensor is arranged on the water inlet pipeline; the level sensor assembly includes: the liquid level sensor is arranged in the flow guide area; the concentration sensor assembly includes: a turbidity sensor arranged in the water outlet channel; the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the pressure sensor assembly, the flow sensor assembly, the liquid level sensor assembly and the concentration sensor assembly to the field control station and the industrial personal computer; the display component comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button and a protection and safety interlocking device of the equipment, and the emergency stop button, the protection and safety interlocking device are all connected to the electric control loop by adopting hard wires; the field control station comprises an operation terminal control cabinet, and is used for manually controlling the equipment or adjusting the equipment to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen connected with the industrial personal computer.
The operation level of the equipment is divided into three levels, namely local operation, field control station operation and central monitoring station operation, and the priority level is decreased in turn. The on-site operation is the control of the equipment through an on-site button of the equipment; the operation of the field control station is to manually control the equipment through a terminal control cabinet by an operator or to automatically control the adjustment through a PLC program. The central monitoring station operation refers to the operation of field equipment through a mouse or a keyboard matched with the industrial personal computer.
The controlled equipment is provided with an automatic/manual/stop mode selection switch, and when the switch is in an automatic position, the equipment is controlled by the output of the PLC (namely, the operation mode of the field control station). When the switch is in the 'manual' position, the equipment is controlled by an on-site button (namely, an on-site operation mode), and an emergency stop button, a protection and safety interlocking device of the equipment are connected to an electric control loop by hard wires and are not limited by a mode selection switch. When the switch is in the "off" position, the device is off-line and cannot be controlled at all.
The field control station has a manual/automatic mode selection function, and in the manual mode, the equipment is manually controlled by function keys on an operator terminal or on a touch screen, and in the automatic mode, the equipment is controlled by a PLC according to a pre-programmed program.
All control is realized by feedback of the control command, when the control command is inconsistent with the feedback information, an alarm is given, and a fault processing program is executed.
The treatment method of the air floatation tank treatment device comprises the following steps:
1) a coagulation stage: the sewage firstly enters a coagulation reaction zone, the designed retention time of the coagulation reaction zone is 1-6min, and the sewage is formed by adding a coagulant and reacting with pollutants under the stirring of a stirrer in the coagulation reaction zoneThe stirring speed gradient of the stirrer in the flocculation body and the coagulation reaction zone is 250-350s-1；
2) A flocculation stage: sewage enters a flocculation reaction zone after passing through a coagulation reaction zone, an anionic high-molecular flocculant is added for 5-20min of residence time of the flocculation reaction zone to provide an adsorption bridging effect to improve a flocculation effect, the sewage mixed with a primary flocculating constituent enters the flocculation turbulent flow zone through a water drop weir plate, a static flocculation turbulent flow zone partition plate is arranged in the flocculation turbulent flow zone instead of a conventional flocculation zone stirrer, and the width of the flocculation turbulent flow zone partition plate is 100 mm; through the mixing of the flocculation turbulence area partition plate, a flocculating agent is mixed and flocculated with colloid particles, suspended matters and the like in water in the area, and high molecular polymers with different charges are adsorbed on the surfaces of the colloid particles in the water, so that an electrical neutralization effect is generated, the zeta potential of the surfaces of pollutants is reduced, and the colloid particles and the suspended matters are destabilized and gathered;
3) a flotation stage: the sewage after flocculation enters a flow guide area, enters a bubble adhesion area from the bottom, a micron aerator is arranged in the bubble adhesion area, provides micron-sized aeration bubbles, is laid in the middle of the bubble adhesion area, is 1.8-2m away from the liquid level, is vertically and uniformly arranged, is transversely arranged in a staggered manner, has a projection interval of 2-5cm, has an aeration pressure of 0.2MPa, has an aeration amount of 4% -5% of total suspended matters of inflow water so as to uniformly disperse the bubbles and be rapidly and fully contacted with the sewage, destabilizing particles can provide 'nucleus' for micro-bubbles after the micro-bubbles meet floc particles, the bubbles and the floc particles are hydrophobic substances, have hydrophobic attraction, have the tendency of reducing the mutual adsorption of free energy of self interfaces, have sufficient kinetic energy and can be mutually pushed under a specific flow state, and water films with poor adhesive force on the surfaces of the micro-bubbles and the floc particles are pushed away, when the two are close to each other, the residual hydrophobic groups of the flocs collide with the water films orderly arranged in the microbubbles, and the two adhere to each other under the interaction of van der Waals acting force to complete the combination of the microbubbles and the flocs; the sewage of the mixed micro-bubble and flocculating constituent crosses the guide wall and enters the solid-liquid separation zone, the guide wall weakens the disturbance and the damage of water jump behind a weir to a micro-bubble sludge layer, the surface load of the solid-liquid separation zone is 20-40m/h, the designed water depth is 5-6m, and the rising speed of the entrained gas flocculating constituent is higher than the surface load of the separation zone, so the entrained gas flocculating constituent cannot be taken away by the falling water flow and floats upwards to be separated from the water phase; clean water enters the clean water diversion channel through the diversion channel diversion turbulent flow plate, the flow aperture of the diversion turbulent flow plate of the clean water diversion channel is designed to be 15-50mm, and then the flow aperture falls into the water outlet channel through the weir plate and is discharged outside, the weir plate is designed to be adjustable, the height range can be adjusted up and down within 100 plus and 200mm, the width of the water outlet channel is 600 plus and 800mm, and the construction and the maintenance are convenient; and a mud scraper is arranged at the upper part of the solid-liquid separation zone, the operation period of the mud scraper is 4-8 h, the mud discharging time is 4-10min, the gas-entrained flocs are scraped into a sludge discharge channel through a high-position mud outlet weir, the design width of the sludge discharge channel is 600-800mm, and the sludge is discharged out of the system through a pipeline.
The air flotation water treatment device and the air flotation water treatment method have the following beneficial effects:
the structural design is more reasonable, the power consumption is saved by 70-85% by adopting the flocculation turbulence area partition plate and the micron aerator, and the operating cost is reduced; the hollow fiber membrane of PTFE composite ceramic particles is adopted for aeration, micropores with the diameter of 10-40nm are uniformly distributed on the surface of the membrane filaments, air is released from the membrane pores, the size of bubbles is stabilized between 10-40 mu m, the removal rate of suspended matters is 90-99%, the turbidity of effluent is less than or equal to 4NTU, and the air floatation turbidity removal treatment effect is good; the hollow fiber membrane of the PTFE composite ceramic particles is a high-strength flexible membrane, can be disturbed along with water flow washing, and can provide power for desorption of pollutants attached to the surface of the membrane wire in the disturbing process so as to prevent the micro-aerator from being polluted and blocked; the aeration mode of the invention is continuous stable pressure aeration, and the aeration device can be started and stopped at any time without influencing the service life of the device. In addition, the whole device has the advantages of reducing the energy consumption of the air floatation process, lowering the maintenance cost, improving the air floatation treatment effect, being capable of stopping along with the start and the stop and the like in the actual operation process.
Drawings
FIG. 1 is a schematic structural view of an air flotation water treatment device of the present invention.
Detailed Description
The present invention will be described in detail with reference to fig. 1.
The utility model provides an air supporting water treatment facilities, the device collects and thoughtlessly congeals, flocculation, flotation as an organic whole, includes: the system comprises a coagulation reaction zone 1, a flocculation reaction zone 2, a flocculation turbulent flow zone 3, a flow guide zone 4, a bubble adhesion zone 5, a solid-liquid separation zone 6, a sludge discharge channel 7, a purified water flow guide channel 8, a water outlet channel 9, a coagulation reaction zone stirrer 10, a weir plate 11, a flocculation turbulent flow zone partition plate 12, a micron aerator 13, a purified water flow guide channel flow distribution turbulent flow plate 14, a flow guide wall 15, a mud scraper 16 and a high-level mud outlet weir 17; wherein, a coagulation reaction zone stirrer 10 is arranged in the coagulation reaction zone 1, the coagulation reaction zone stirrer 10 is fixed with the top of the coagulation reaction zone through a bolt, the coagulation reaction zone 1 is connected with a flocculation reaction zone 2 through a high-level water tunnel, and the flocculation reaction zone 2 is connected with a flocculation turbulence zone 3 through a low-level water tunnel; a static flocculation turbulence area clapboard 12 is arranged in the flocculation turbulence area 3, and the fixed position of the static flocculation turbulence area clapboard 12 is positioned at the top of the flocculation turbulence area and is fixed by bolts; the flocculation turbulence area 3 is connected with the flow guide area 4 through a high-level water through hole, and the flow guide area 4 is connected with the bubble adhesion area 5 through a low-level water through hole; the micron aerator 13 is arranged in the bubble adhesion zone 5, the micron aerator 13 is laid in the middle of the bubble adhesion zone 5 and is fixed with the tank wall of the bubble adhesion zone 5 through bolts, the bubble adhesion zone 5 is connected with the solid-liquid separation zone 6, the connection part is a flow guide wall 15 positioned between the bubble adhesion zone and the solid-liquid separation zone, and the height of the flow guide wall 15 is lower than the highest liquid level of the bubble adhesion zone; the solid-liquid separation zone 6 is connected with the sludge discharge channel 7 through a high-level sludge discharge weir 17, and the upper part of the tank body of the solid-liquid separation zone 6 is provided with a sludge scraper 16; the bottom of the solid-liquid separation zone 6 is provided with a diversion canal diversion turbulent plate 14, the diversion canal diversion turbulent plate 14 is connected with a purified water diversion canal 8, the purified water diversion canal 8 is connected with a water outlet canal 9 through a high-level water passing hole, and a weir plate 11 is arranged at the opening of the high-level water passing hole. A coagulant adding tank is arranged in the coagulation reaction zone, one of aluminum sulfate, polyaluminium chloride, ferric trichloride and polyferric sulfate is arranged in the coagulant adding tank, and the coagulant adding tank reacts with pollutants under the stirring of a stirrer 10 in the coagulation reaction zone to form a flocculating constituent;
and an anion high-molecular flocculant dosing tank is arranged in the flocculation reaction zone, and polyacrylamide is arranged in the anion high-molecular flocculant dosing tank and used for providing an adsorption bridging effect to improve the flocculation effect. The included angle between the axis of the guide wall and the vertical direction is 5-15 degrees, and 8 degrees is preferred. The micron aerator adopts a hollow fiber membrane of PTFE composite ceramic particles, nano-scale micropores of 10-40nm are uniformly distributed on the surface of a membrane wire of the hollow fiber membrane, air is supplied to the interior of the membrane wire through a fan or an air compressor, the air is released from the membrane hole, and the size of the air bubbles is stabilized between 10-40 mu m.
The device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, and a pressure sensor assembly, a flow sensor assembly, a liquid level sensor assembly, a concentration sensor assembly, a display assembly, an abnormality alarm assembly, an in-situ control station and a central monitoring station which are respectively connected with the programmable PLC controller; the pressure sensor assembly includes: the pressure sensor is arranged on the air inlet pipeline; the flow sensor assembly includes: the flow sensor is arranged on the water inlet pipeline; the level sensor assembly includes: the liquid level sensor is arranged in the flow guide area; the concentration sensor assembly includes: a turbidity sensor arranged in the water outlet channel; the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the pressure sensor assembly, the flow sensor assembly, the liquid level sensor assembly and the concentration sensor assembly to the field control station and the industrial personal computer; the display component comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button and a protection and safety interlocking device of the equipment, and the emergency stop button, the protection and safety interlocking device are all connected to the electric control loop by adopting hard wires; the field control station comprises an operation terminal control cabinet, and is used for manually controlling the equipment or adjusting the equipment to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen connected with the industrial personal computer.
The operation level of the equipment is divided into three levels, namely local operation, field control station operation and central monitoring station operation, and the priority level is decreased in turn. The local operation is the control of the equipment through a local button of the equipment; the operation of the field control station is that an operator controls the equipment manually through a terminal control cabinet or the adjustment is automatically controlled by a PLC program. The central monitoring station operation refers to the operation of field equipment through a mouse or a keyboard matched with the industrial personal computer.
The controlled equipment is provided with an automatic/manual/stop mode selection switch, and when the switch is in an automatic position, the equipment is controlled by the output of the PLC (namely, the operation mode of the field control station). When the switch is in the 'manual' position, the equipment is controlled by an on-site button (namely, an on-site operation mode), and an emergency stop button, a protection and safety interlocking device of the equipment are connected to an electric control loop by hard wires and are not limited by a mode selection switch. When the switch is in the "off" position, the device is off-line and cannot be controlled at all.
The field control station has a manual/automatic mode selection function, and in the manual mode, the equipment is manually controlled by function keys on an operator terminal or on a touch screen, and in the automatic mode, the equipment is controlled by a PLC according to a pre-programmed program.
All control is realized by feedback of the control command, when the control command is inconsistent with the feedback information, an alarm is given, and a fault processing program is executed.
The treatment method of the air floatation tank treatment device comprises the following steps:
1) a coagulation stage: the sewage firstly enters a coagulation reaction zone 1, the designed retention time of the coagulation reaction zone 1 is 1-6min, the sewage reacts with pollutants under the stirring of a stirrer 10 of the coagulation reaction zone to form a floccule body by adding a coagulant, and the stirring speed gradient of the stirrer 10 of the coagulation reaction zone is 250-350s-1；
2) A flocculation stage: sewage enters a flocculation reaction zone 2 after passing through a coagulation reaction zone, an anionic polymeric flocculant is added for 5-20min after the flocculation reaction zone 2 stays for providing an adsorption bridging effect to improve the flocculation effect, the sewage mixed with a primary flocculating constituent enters a flocculation turbulent flow zone 3 through a water drop weir plate 11, a static flocculation turbulent flow zone partition plate 12 is arranged in the flocculation turbulent flow zone 3 instead of a conventional flocculation zone stirrer, and the width of the flocculation turbulent flow zone partition plate 12 is 100 mm; through the mixing of the flocculation turbulence area partition plate 12, a flocculating agent is mixed and flocculated with colloid particles, suspended matters and the like in water in the area, and high molecular polymers with different charges are adsorbed on the surfaces of the colloid particles in the water, so that an electric neutralization effect is generated, the zeta potential of the surfaces of pollutants is reduced, and the colloid particles and the suspended matters are destabilized and aggregated;
3) a flotation stage: the sewage after flocculation enters a flow guide zone 4 and enters a bubble adhesion zone 5 from the bottom, a micron aerator 13 is arranged in the bubble adhesion zone 5, the micron aerator 13 provides micron-sized aeration bubbles, the micron aerator 13 is laid in the middle of the bubble adhesion zone 5 and is 1.8-2m away from the liquid level, the micron aerator is vertically and uniformly arranged and transversely arranged in a staggered manner, the projection interval is 2-5cm, the aeration pressure is 0.2MPa, the aeration amount is 4% -5% of total suspended matters of inflow water, so that the bubbles are uniformly dispersed and rapidly and sufficiently contacted with the sewage, destabilizing particles can provide 'nucleus' positions for micro-bubbles after the micro-bubbles meet floc particles, the bubbles and the floc particles are hydrophobic substances, have hydrophobic attraction, have the tendency of reducing the mutual adsorption of free energy of self interfaces, and have sufficient kinetic energy in a specific flow state and can be pushed and squeezed mutually, the water films with poor surface adhesion of the two are pushed away, when the two are close to each other, the residual hydrophobic groups of the flocs collide with the water films orderly arranged in the microbubbles, and the water films are mutually adhered under the interaction of van der Waals acting force to complete the combination of the microbubbles and the flocs; the sewage of the mixed micro-bubble and flocculating constituent crosses the guide wall 15 and enters the solid-liquid separation zone 6, the guide wall 15 weakens the disturbance and the damage of water jump behind a weir to a micro-bubble sludge layer, the surface load of the solid-liquid separation zone 6 is 20-40m/h, the designed water depth is 5-6m, and the rising speed of the entrained gas flocculating constituent is higher than the surface load of the separation zone, so the entrained gas flocculating constituent can not be taken away by the descending water flow and floats upwards to be separated from a water phase; clean water enters the clean water diversion channel 8 through the diversion channel diversion turbulent flow plate 14, the flow aperture of the diversion turbulent flow plate 14 of the clean water diversion channel is designed to be 15-50mm, and then falls into the water outlet channel 9 through the weir plate 11 and is discharged outside, the weir plate is designed to be adjustable, the height range can be adjusted up and down within 100 plus 200mm, the width of the water outlet channel 9 within 600 plus 800mm, and construction and maintenance are facilitated; the upper part of the solid-liquid separation zone 6 is provided with a mud scraper 16, the operation period of the mud scraper 16 is 4-8 h, the mud discharging time is 4-10min, the entrained gas floc is scraped into the sludge discharge channel 7 through a high-level mud outlet weir 17, the designed width of the sludge discharge channel 7 is 600-800mm, and the sludge is discharged out of the system through a pipeline.
Taking the sewage treatment system of an industrial park as an example, the water quantity of the air inlet floating system is 1340m3H, water temperature of 10-25 ℃, pH of 6-8 and suspended matter concentration of 33 mg/L. The sewage firstly enters a coagulation reaction zone 1, a coagulant PAC is added at the inlet of the coagulation reaction zone 1, the adding concentration is 50mg/L, the sewage reacts with pollutants under the stirring of a stirrer 10 in the coagulation reaction zone to form a floccule, and the stirring speed gradient of the stirrer 10 in the coagulation reaction zone is 280s-1The designed retention time of the coagulation reaction zone 1 is 2 min; then the sewage enters a flocculation reaction zone 2, an anionic polymer flocculant is added at the inlet of the flocculation reaction zone 2 to provide an adsorption bridging effect to improve the flocculation effect, the retention time of the flocculation reaction zone 2 is 12min, the sewage mixed with the primary flocculating constituent enters a flocculation turbulence zone 3 through a water drop weir plate 11, a static flocculation turbulence zone clapboard 12 is arranged in the flocculation turbulence zone 3, the width of the flocculation turbulence zone clapboard 12 is 100mm, and if a stirrer is arranged, the power of the stirrer is 4kw, the static flocculation turbulence zone clapboard is adopted in the system, so that the energy consumption is reduced; through the mixing of the flocculation turbulence area partition plate 12, the flocculating agent is mixed and flocculated with colloid particles, suspended matters and the like in water in the area, and high molecular polymers with different charges are adsorbed on the surfaces of the colloid particles in the water, so that the electric neutralization effect is generated, the zeta potential on the surfaces of pollutants is reduced, and the colloid particles and the suspended matters are destabilized and gathered. The sewage after flocculation is fed into a flow guide area 4 and fed into a bubble adhesion area 5 from the bottom, a micron aerator 13 is arranged in the bubble adhesion area 5, the top of the micron aerator is 2m away from the liquid level, if dissolved air flotation is adopted, the aeration pressure is 0.2MPa, the pressure requirement of the dissolved air flotation is 1.0MPa, and a reflux pump is needed to provide dissolved air water, the aeration pressure of the system is lower, the aeration is direct, the reflux pump is not needed, the energy consumption of the system is saved, the aeration amount is 4% of total suspended matters of water inlet, membrane filaments are arranged in a staggered manner, and the density is 3cm at the projection interval, so that the bubbles are uniformly dispersed and rapidly and fully contacted with the sewage, and the combination of micro bubbles and a flocculating constituent is rapidly completed; the sewage mixed with the micro-bubbles and the flocculating constituent crosses the guide wall 15 to enter the solid-liquid separation zone 6, and the guide wall 15 is used for weakening the disturbance of hydraulic turbulence behind the weir on the micro-bubble sludge layerAnd the design angle of the guide wall 15 is 8 degrees when the guide wall is moved and damaged. The surface load of the solid-liquid separation zone 6 is 28m/h, and the design water depth is 5.7 m. Purified water enters the purified water diversion channel 8 through the diversion channel diversion turbulent plate 14, the flow aperture of the diversion channel diversion turbulent plate 14 is designed to be 25mm, the purified water falls into the water outlet channel 9 through the weir plate 11 and is discharged outside, and the width of the water outlet channel 9 is 600 mm. The upper part of the solid-liquid separation zone 6 is provided with a mud scraper 16, the running period of the mud scraper 16 is 6 hours, the mud discharging time is 4min, the entrained gas flocs are scraped into a mud discharging channel 7, the designed width of the mud discharging channel 7 is 600mm, and the mud is discharged out of the system through a pipeline.
The turbidity range of the effluent of the system is 2-3 NTU. Comparing the electric power of the project with the electric power of the dissolved air floatation process equipment with the same scale as follows:
in the above table, the mixer in the coagulation reaction zone is in accordance with the tank volume and the mixing speed gradient of 280s-1The retention time is 2min, and the power of the model selection stirrer is 4kw, so that the coagulation effect can be achieved; the conventional dissolved air flotation of a flocculation reaction zone stirrer needs to be set, the uniform flocculation can be realized by adopting a flocculation turbulence zone clapboard without a stirrer, and an electric stirrer does not need to be set; the air compressor is set to provide air for the system, micro-nano bubbles are provided for the micron aerator by using air supply of the air compressor, air is provided by the air compressor to be dissolved in water by using conventional dissolved air flotation, and the high-pressure and high-saturation dissolved air water is released through the pressure reduction and air release device to form the micro-nano bubbles. The work of the reflux circulating pump is to provide dissolved air water for the conventional dissolved air floatation, and the project system adopts direct aeration without the dissolved air water, thereby omitting the reflux circulating pump; the mud scraper is arranged to scrape the air-entrained flocs into the sludge discharge channel. The sludge discharge concentration is improved, the water loss is reduced, and the conventional dissolved air flotation system and the project air flotation system are required to be arranged.
Conversion per ton of water power consumption: the ton water power consumption of the project air floatation system is 7.5 multiplied by 10-3kw.h/ton water, electricity consumption of 44.1 x 10 per ton water by conventional dissolved air floatation-3kw · h/ton water. The annual energy saving power consumption is 429240 kw.h, and the electricity price is calculated according to 0.6 yuan/kw.hThe annual cost is saved by 25.75 ten thousand yuan, and the power consumption is saved by 82.91%.
The present invention is not limited to the above embodiments, and any modifications, equivalent substitutions, improvements, etc. within the spirit and principle of the present disclosure should be included in the scope of the present disclosure as long as the technical effects of the present invention are achieved by the same means. Are intended to fall within the scope of the present invention. The invention is capable of other modifications and variations in its technical solution and/or its implementation, within the scope of protection of the invention.
Claims (6)
1. An air-floated water treatment apparatus characterized in that: the device collects and thoughtlessly congeals, flocculation, flotation as an organic whole, includes: the device comprises a coagulation reaction zone (1), a flocculation reaction zone (2), a flocculation turbulence zone (3), a flow guide zone (4), a bubble adhesion zone (5), a solid-liquid separation zone (6), a sludge discharge channel (7), a purified water flow guide channel (8), a water outlet channel (9), a coagulation reaction zone stirrer (10), a weir plate (11), a flocculation turbulence zone partition plate (12), a micron aerator (13), a purified water flow guide channel flow distribution turbulence plate (14), a flow guide wall (15), a mud scraper (16) and a high-level mud outlet weir (17); wherein, a coagulation reaction zone stirrer (10) is arranged in the coagulation reaction zone (1), the coagulation reaction zone stirrer (10) is fixed with the top of the coagulation reaction zone through a bolt, the coagulation reaction zone (1) is connected with the flocculation reaction zone (2) through a high-level water through hole, and the flocculation reaction zone (2) is connected with the flocculation turbulence zone (3) through a low-level water through hole; a static flocculation turbulent flow area clapboard (12) is arranged in the flocculation turbulent flow area (3), and the fixed position of the static flocculation turbulent flow area clapboard (12) is arranged at the top of the flocculation turbulent flow area and is fixed by bolts; the flocculation turbulence area (3) is connected with the flow guide area (4) through a high-position water through hole, and the flow guide area (4) is connected with the bubble adhesion area (5) through a low-position water through hole; a micron aerator (13) is arranged in the bubble adhesion zone (5), the micron aerator (13) is laid in the middle of the bubble adhesion zone (5) and is fixed with the tank wall of the bubble adhesion zone (5) through a bolt, the bubble adhesion zone (5) is connected with the solid-liquid separation zone (6), a flow guide wall (15) is arranged at the joint between the bubble adhesion zone and the solid-liquid separation zone, and the height of the flow guide wall (15) is lower than the highest liquid level of the bubble adhesion zone; the solid-liquid separation zone (6) is connected with the sludge discharge channel (7) through a high-level sludge outlet weir (17), and the upper part of the tank body of the solid-liquid separation zone (6) is provided with a sludge scraper (16); the bottom of the solid-liquid separation zone (6) is provided with a diversion canal diversion turbulence plate (14), the diversion canal diversion turbulence plate (14) is connected with a purified water diversion canal (8), the purified water diversion canal (8) is connected with a water outlet canal (9) through a high-level water tunnel, and the mouth of the high-level water tunnel is provided with a weir plate (11).
2. An air-floated water treatment apparatus as claimed in claim 1, wherein: a coagulant adding tank is arranged in the coagulation reaction zone, one of aluminum sulfate, polyaluminium chloride, ferric trichloride and polyferric sulfate is arranged in the coagulant adding tank, and the coagulant adding tank reacts with pollutants under the stirring of a stirrer (10) in the coagulation reaction zone to form a flocculating constituent;
and an anion high-molecular flocculant dosing tank is arranged in the flocculation reaction zone, and polyacrylamide is arranged in the anion high-molecular flocculant dosing tank and used for providing an adsorption bridging effect to improve the flocculation effect.
3. An air-floated water treatment apparatus as claimed in claim 1, wherein: the included angle between the axis of the guide wall and the vertical direction is 5-15 degrees.
4. An air-floated water treatment apparatus as claimed in claim 1, wherein: the micron aerator adopts a hollow fiber membrane of PTFE composite ceramic particles, nano-scale micropores of 10-40nm are uniformly distributed on the surface of a membrane wire of the hollow fiber membrane, air is supplied to the interior of the membrane wire through a fan or an air compressor, the air is released from the membrane hole, and the size of the air bubbles is stabilized between 10-40 mu m.
5. An air-floated water treatment apparatus as claimed in any one of claims 1 to 4, wherein: the device also comprises an automatic control system, wherein the automatic control system comprises a programmable PLC controller, and a pressure sensor assembly, a flow sensor assembly, a liquid level sensor assembly, a concentration sensor assembly, a display assembly, an abnormality alarm assembly, an in-situ control station and a central monitoring station which are respectively connected with the programmable PLC controller; the pressure sensor assembly includes: the pressure sensor is arranged on the air inlet pipeline; the flow sensor assembly includes: the flow sensor is arranged on the water inlet pipeline; the level sensor assembly includes: the liquid level sensor is arranged in the flow guide area (4); the concentration sensor assembly includes: a turbidity sensor arranged in the water outlet channel (9); the programmable PLC controller is in communication connection with the field control station and the industrial personal computer through an optical fiber network and is used for sending detection results of the pressure sensor assembly, the flow sensor assembly, the liquid level sensor assembly and the concentration sensor assembly to the field control station and the industrial personal computer; the display assembly comprises an OLED display screen and is used for displaying the concentration value detected in real time; the abnormity warning component comprises a lamp tube flasher or an alarm; the local control assembly comprises an emergency stop button and a protection and safety interlocking device of the equipment, and the emergency stop button, the protection and safety interlocking device are all connected to the electric control loop by adopting hard wires; the field control station comprises an operation terminal control cabinet which is used for manually controlling the equipment or is adjusted to be automatically controlled by a PLC program; the central monitoring station comprises an industrial personal computer and a display screen connected with the industrial personal computer.
6. The treatment method of the air flotation tank treatment device according to any one of claims 1 to 5, characterized by comprising the following steps: the processing method comprises the following steps:
1) a coagulation stage: the sewage firstly enters a coagulation reaction zone (1), the designed retention time of the coagulation reaction zone (1) is 1-6min, a coagulant is added, the sewage reacts with pollutants under the stirring of a stirrer (10) in the coagulation reaction zone to form a floccule, and the stirring speed gradient of the stirrer (10) in the coagulation reaction zone is 250-350s-1；
2) A flocculation stage: the sewage enters the flocculation reaction zone (2) after passing through the coagulation reaction zone, the retention time of the flocculation reaction zone (2) is 5-20min, and anion high molecular weight is added
Coagulant providing adsorption bridging effectThe flocculation effect is high, sewage mixed with the primary flocculating constituent enters the flocculation turbulent flow area (3) through the water drop weir plate (11), a static flocculation turbulent flow area partition plate (12) is arranged in the flocculation turbulent flow area (3) instead of a conventional flocculation area stirrer, and the width of the flocculation turbulent flow area partition plate (12) is 100 mm; through the mixing of the flocculation turbulence area clapboard (12), a flocculating agent is mixed and flocculated with colloid particles, suspended matters and the like in water in the area, and high molecular polymers with different charges are adsorbed on the surfaces of the colloid particles in the water, so that the electric neutralization effect is generated, the zeta potential of the surfaces of pollutants is reduced, and the colloid particles and the suspended matters are destabilized and gathered;
3) a flotation stage: the sewage after flocculation is fed into a flow guide area (4), the sewage enters a bubble adhesion area (5) from the bottom, a micron aerator (13) is arranged in the bubble adhesion area (5), micron-sized aeration bubbles are provided by the micron aerator (13), the micron aerator (13) is laid in the middle of the bubble adhesion area (5), the distance between the micron-sized aeration bubbles and the liquid level is 1.8-2m, the micron aerator is vertically and uniformly arranged, the micron aerator is transversely arranged in a staggered manner, the projection interval is 2-5cm, the aeration pressure is 0.2MPa, and the aeration amount is 4% -5% of total suspended matters of inflow water, so that the bubbles are uniformly dispersed and are rapidly and fully contacted with the sewage, after the micro bubbles meet with floc particles, destabilization particles can provide 'core' positions for the micro bubbles, the bubbles and the floc particles are both hydrophobic substances, have hydrophobic attraction force and have the tendency of reducing mutual adsorption of free energy of self interfaces, and the kinetic energy of the micro bubbles and the floc particles is abundant in a specific flow state, the micro-bubble and the flocculating body can be pushed mutually, water films with poor surface adhesion force of the micro-bubble and the flocculating body are pushed away, when the micro-bubble and the flocculating body are close to each other, the residual hydrophobic groups of the flocs collide with the water films which are orderly arranged in the micro-bubble, and the micro-bubble and the flocculating body are adhered to each other under the interaction of van der Waals acting force to complete the combination of the micro-bubble and the flocculating body; the sewage of the mixed micro-bubbles and the flocculating constituent crosses the guide wall (15) and enters the solid-liquid separation zone (6), the guide wall (15) weakens the disturbance and the damage of water jump to a micro-bubble sludge layer after the weir, the surface load of the solid-liquid separation zone (6) is 20-40m/h, the designed water depth is 5-6m, and the rising speed of the entrained gas flocculating constituent is higher than the surface load of the separation zone, so the entrained gas flocculating constituent can not be taken away by the descending water flow and floats upwards to be separated from a water phase; clean water enters the clean water diversion channel (8) through the diversion channel diversion turbulent flow plate (14), the flow aperture of the clean water diversion channel diversion turbulent flow plate (14) is designed to be 15-50mm, and then the clean water falls into the water outlet channel (9) through the weir plate (11) and is discharged outside, the weir plate is designed to be adjustable, the height range can be adjusted up and down by 100 plus 200mm, the width of the water outlet channel (9) is 600 plus 800mm, and construction and maintenance are facilitated; the upper part of the solid-liquid separation zone (6) is provided with a mud scraper (16), the operation period of the mud scraper (16) is 4-8 h, the mud discharging time is 4-10min, the gas-entrained flocs are scraped into the sludge discharge channel (7) through the high-level mud outlet weir (17), the design width of the sludge discharge channel (7) is 600-800mm, and the sludge is discharged out of the system through a pipeline.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115259321A (en) * | 2022-08-23 | 2022-11-01 | 哈尔滨优方净水科技有限公司 | Adjustable gas-liquid multiphase anisotropic mixing flocculation integrated grid coagulation system |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8922425D0 (en) * | 1989-10-05 | 1989-11-22 | Spooner Ind Ltd | Air-float treatment apparatus |
| CN1617836A (en) * | 2002-01-30 | 2005-05-18 | 德格雷蒙公司 | Device for treating water by flotation |
| CN101746841A (en) * | 2009-12-22 | 2010-06-23 | 潍坊金丝达印染有限公司 | Sewage air-flotation treatment method and sewage treatment air flotation tank |
| CN101905930A (en) * | 2010-06-28 | 2010-12-08 | 胜利油田胜利勘察设计研究院有限公司 | Selective adsorbing and air-floating treatment method and device for sewage from oilfields |
| CN104030387A (en) * | 2014-05-27 | 2014-09-10 | 大庆高新区百世环保科技开发有限公司 | Efficient air floatation treatment integrated device for ternary composite flooding oilfield produced water |
| CN104291497A (en) * | 2014-11-03 | 2015-01-21 | 山东建筑大学 | Copolymerization pond integrating functions of air flotation and clarification |
| US20170297924A1 (en) * | 2014-10-02 | 2017-10-19 | Veolia Water Solutions & Technologies Support | Water treatment process employing dissolved air flotation to remove suspended solids |
| CN108439652A (en) * | 2018-04-27 | 2018-08-24 | 易能环境技术有限公司 | A kind of high-efficiency dissolued-air air-floating apparatus and its sewage water treatment method based on waterpower principle |
| CN213085547U (en) * | 2020-08-12 | 2021-04-30 | 福州海恒水务设备有限公司 | Improve whirl baffle combination reaction structure of flocculation reaction stroke and collision effect |
| CN113003864A (en) * | 2021-02-26 | 2021-06-22 | 北京首禾环保科技有限公司 | Improved sewage treatment device and method by nitrogen and phosphorus removal biomembrane method |
-
2022
- 2022-05-16 CN CN202210533657.9A patent/CN114751560A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8922425D0 (en) * | 1989-10-05 | 1989-11-22 | Spooner Ind Ltd | Air-float treatment apparatus |
| CN1617836A (en) * | 2002-01-30 | 2005-05-18 | 德格雷蒙公司 | Device for treating water by flotation |
| CN101746841A (en) * | 2009-12-22 | 2010-06-23 | 潍坊金丝达印染有限公司 | Sewage air-flotation treatment method and sewage treatment air flotation tank |
| CN101905930A (en) * | 2010-06-28 | 2010-12-08 | 胜利油田胜利勘察设计研究院有限公司 | Selective adsorbing and air-floating treatment method and device for sewage from oilfields |
| CN104030387A (en) * | 2014-05-27 | 2014-09-10 | 大庆高新区百世环保科技开发有限公司 | Efficient air floatation treatment integrated device for ternary composite flooding oilfield produced water |
| US20170297924A1 (en) * | 2014-10-02 | 2017-10-19 | Veolia Water Solutions & Technologies Support | Water treatment process employing dissolved air flotation to remove suspended solids |
| CN104291497A (en) * | 2014-11-03 | 2015-01-21 | 山东建筑大学 | Copolymerization pond integrating functions of air flotation and clarification |
| CN108439652A (en) * | 2018-04-27 | 2018-08-24 | 易能环境技术有限公司 | A kind of high-efficiency dissolued-air air-floating apparatus and its sewage water treatment method based on waterpower principle |
| CN213085547U (en) * | 2020-08-12 | 2021-04-30 | 福州海恒水务设备有限公司 | Improve whirl baffle combination reaction structure of flocculation reaction stroke and collision effect |
| CN113003864A (en) * | 2021-02-26 | 2021-06-22 | 北京首禾环保科技有限公司 | Improved sewage treatment device and method by nitrogen and phosphorus removal biomembrane method |
Non-Patent Citations (1)
| Title |
|---|
| 段云霞等, 天津大学出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259321A (en) * | 2022-08-23 | 2022-11-01 | 哈尔滨优方净水科技有限公司 | Adjustable gas-liquid multiphase anisotropic mixing flocculation integrated grid coagulation system |
| CN115259321B (en) * | 2022-08-23 | 2023-08-08 | 哈尔滨优方净水科技有限公司 | Adjustable gas-liquid multi-phase and multi-phase mixed flocculation integrated grid coagulation system |
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Address after: A3-1603, Area A, Lidu Shui'an, Yard 9, Fangyuan Nanli, Chaoyang District, Beijing 100000 Applicant after: Xia Fan Applicant after: Zhang Yanyan Address before: 300126 8-4-801, Meiyuan, Ruijiang garden, Hexi District, Tianjin Applicant before: Zhang Yanyan Applicant before: Xia Fan |
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