CN110668620A - Jet fluidized bed type electro-Fenton treatment system - Google Patents
Jet fluidized bed type electro-Fenton treatment system Download PDFInfo
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- CN110668620A CN110668620A CN201911082701.3A CN201911082701A CN110668620A CN 110668620 A CN110668620 A CN 110668620A CN 201911082701 A CN201911082701 A CN 201911082701A CN 110668620 A CN110668620 A CN 110668620A
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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
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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
- C02F1/006—Water distributors either inside a treatment tank or directing the water to several treatment tanks; Water treatment plants incorporating these distributors, with or without chemical or biological tanks
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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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
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic 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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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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
- C02F7/00—Aeration of stretches of water
Abstract
The invention discloses a jet fluidized bed type electro-Fenton treatment system, wherein a jet medicine adding aeration water distribution system introduces waste water and carries out aeration treatment to form gas-liquid mixed flow; the waste water after the electro-Fenton treatment by the electro-Fenton treatment system is output to a sedimentation water outlet pool, and the waste gas is output to a gas collection treatment system; the wastewater is discharged to a filler recovery preparation system after being precipitated by the precipitation water outlet tank; the filler recycling preparation system adds iron mud recycling particles into an electro-Fenton treatment system; the gas collecting and processing system introduces a part of waste gas into the jet medicine adding aeration water distribution system for aeration processing. According to the technical scheme, the electro-Fenton removal rate is greatly broken through, the electro-Fenton method realizes zero emission of chemical sludge, the fluidized bed mode promotes chemical oxidation reaction and electric proton efficiency, a fluidized environment is created while aeration dosing is carried out, energy is saved, consumption is reduced, the removal rate is greatly improved, and the separated iron is recycled.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a jet fluidized bed type electro-Fenton treatment system.
Background
The electro-Fenton technology (E Fenton) is a novel electrochemical advanced oxidation technology based on Fenton chemical reaction, the basic principle is that when waste water is treated, current is introduced into a solution, all or part of reagents required by Fenton are generated through negative and positive pole reactions, and the reaction principle is as follows: 1) the oxygen dissolved in water generates hydrogen peroxide at the cathode (formula 1-1), and the COD degradation efficiency is increased: 2) adding hydrogen peroxide into the tank, and electrolyzing the hydrogen peroxide and the anode iron plate to obtain Fe2+Constituting a Fenton agent (formula 1-2); 3) fe3+Can be reduced at the cathode to thereby reduce the subsequent iron sludge production (equations 1-3). The electric decomposition generates hydroxyl free radical (0H) with strong oxidizing property in the reaction process, and the purpose of removing the refractory organic pollutants is achieved by utilizing the non-selective strong oxidizing property of the 0H. The electro-Fenton method can effectively reduce the sludge yield, and the treatment process is relatively clean; in addition, the electro-Fenton method also has the advantages of relatively simple processing equipment, high processing efficiency, small occupied area and the like.
The currently widely used electro-Fenton adopts a soluble iron anode plate and a graphite electrode cathode plate, and a Fenton reaction system is formed by adding hydrogen peroxide and aerating the cathode in an electrolytic cell to generate hydrogen peroxide. The reaction equation is as follows:
O2+2e-+2H+→H2O2(E0＝0.695V/SHE) (1-1)
H2O2+Fe2+→(Fe3++-OH+·OH) (1-2)
Fe3++e-→Fe2+(E0＝0.77V/SHE) (1-3)
the aeration systems of the electro-Fenton treatment system which are widely used at present are mostly tubular aeration, and generated bubbles are large and are difficult to attach to a cathode to participate in a reduction reaction; the electro-Fenton treatment system has limited removal rate due to the fixed area of the iron plate, so that hydrogen peroxide and anode Fe are achieved2+After the optimum reagent ratio, it is difficult to further increase(ii) a Low electrical transmission efficiency of the whole system, Fe3+Reduction to Fe2+Very little, the system will also produce iron mud.
Disclosure of Invention
In view of at least one of the above problems, the present invention provides a jet fluidized bed type electro-Fenton treatment system, which uses the advantages of the fluidized bed carrier filler in the electro-Fenton technology, and uses the precipitated iron mud from the electro-Fenton effluent system to prepare the fluidized filler, so as to make Fe3+Not only can be reduced at the cathode, but also can be coated on the surface of a fluidized filler carrier by crystallization or precipitation to form hydroxyl complex iron, can further catalyze the Fenton reaction, and can be reduced into Fe2+The removal rate of electro-Fenton is greatly broken through, the electro-Fenton method is enabled to realize zero discharge of chemical sludge, the mode of the fluidized bed promotes chemical oxidation reaction and electric proton transfer efficiency, a fluidization environment is created while aeration dosing is carried out, energy is saved, consumption is reduced, the removal rate is greatly improved, and the separated iron is recycled.
To achieve the above object, the present invention provides a jet fluidized bed electro-fenton treatment system, comprising: the system comprises a jet flow dosing aeration water distribution system, an electro-Fenton treatment system, a sedimentation water outlet pool, a filler recovery preparation system and a gas collection treatment system; the jet flow dosing aeration water distribution system introduces wastewater, hydrogen peroxide is pumped into the wastewater, air is input to carry out aeration treatment on the wastewater to form gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electro-Fenton treatment system; adding a fluidized filler into the electro-Fenton treatment system, performing electro-Fenton treatment on the wastewater after adding the chemicals and aerating, outputting the treated wastewater to the sedimentation water outlet tank, and outputting waste gas generated by the electro-Fenton treatment to the gas collection treatment system; the sedimentation water outlet tank is used for carrying out alkali treatment and sedimentation on the wastewater after electro-Fenton treatment, and discharging the precipitated sludge to the filler recovery preparation system; the filler recovery preparation system circularly adds the particles after drying, adding the viscose auxiliary agent and granulating and calcining into the electro-Fenton treatment system to serve as fluidized fillers; the gas collecting and processing system introduces a part of the collected waste gas into the jet flow dosing aeration water distribution system to carry out aeration treatment on the waste water, and the rest part is subjected to combustion consumption treatment.
In the above technical solution, preferably, the electro-fenton treatment system includes a power supply, an anode plate, a cathode plate and a fenton reaction tank, the anode plate and the cathode plate are respectively connected with a positive electrode and a negative electrode of the power supply, and the anode plate and the cathode plate are respectively arranged in the fenton reaction tank at intervals in a staggered manner.
In the above technical scheme, preferably, the jet dosing aeration water distribution system comprises a water diversion pump, a hydrogen peroxide storage tank, a hydrogen peroxide dosing pump, a self-oscillation jet dosing mixer, an induced draft fan, a gas-liquid exit pipeline, an aeration water distribution nozzle and a fluidized filler; waste water is input at the inlet of the diversion pump, the outlet of the diversion pump is communicated with the self-oscillation jet-flow dosing mixer, the inlet of the hydrogen peroxide dosing pump is communicated with the hydrogen peroxide storage tank, the outlet of the hydrogen peroxide dosing pump is communicated with the outlet channel of the diversion pump, the outlet of the induced draft fan is communicated with the air suction pipe of the self-oscillation jet-flow dosing mixer, the outlet of the self-oscillation jet-flow dosing mixer is connected to the aeration water distribution nozzle through a gas-liquid outgoing pipeline, the aeration water distribution nozzle is arranged at the bottom in the Fenton reaction tank, and the fluidization filler is filled in the Fenton reaction tank.
In the above technical solution, preferably, the self-oscillating jet chemical dosing mixer includes a fluid driving nozzle, the air intake pipe, a gas mixing chamber, a self-oscillating chamber, a collision wall and a diffusion pipe, the fluid driving nozzle is communicated with outlets of the water inducing pump and the hydrogen peroxide chemical dosing pump, the gas mixing chamber is arranged at an outlet of the fluid driving nozzle, a side wall of the gas mixing chamber is communicated with the air intake pipe, a mixture of air, wastewater and hydrogen peroxide is sucked by the air intake pipe to form a gas-liquid mixed flow in the gas mixing chamber, the self-oscillating chamber is arranged at an outlet of the gas mixing chamber, the collision wall is formed inside the self-oscillating chamber, the gas-liquid mixed flow is self-oscillated and sheared in the self-oscillating chamber to form a discrete vortex ring, and pressure oscillation waves are generated under the action of the collision wall, an outlet of the self-oscillating chamber is communicated with the, the diffusion pipe is communicated with the gas-liquid emergent pipeline, and the gas-liquid mixed flow is sprayed out from the diffusion pipe.
In the above technical scheme, preferably, the sedimentation water outlet tank includes a neutralization tank, an alkali adding subsystem, a sedimentation tank, an inclined plate sedimentation, a mud scraper and a mud outlet pipe, the wastewater in the fenton reaction tank is introduced into the neutralization tank, the alkali adding subsystem adds an alkaline reagent into the neutralization tank for neutralization reaction, the wastewater enters the sedimentation tank after the neutralization reaction, the inclined plate sedimentation is obliquely arranged in the sedimentation tank, the sedimentated sludge is sedimentated to the bottom of the sedimentation tank along with the inclined plate sedimentation, the mud scraper outputs the sludge to the filler recovery preparation system through the mud outlet pipe, and the mud outlet pipe is provided with a mud discharge valve.
In the above technical scheme, preferably, the filler recycling preparation system includes a dryer, a granulator, an auxiliary subsystem, and a calciner, an inlet of the dryer is communicated with the sludge outlet pipe, an outlet of the dryer is communicated with an inlet of the granulator, the auxiliary subsystem adds an adhesive auxiliary agent into the granulator, dried sludge is formed into bars under the action of the adhesive auxiliary agent and is output in a granulation manner, an outlet of the granulator is communicated with the calciner, an outlet of the calciner is communicated with a feed hole on the fenton reaction tank, and calcined porous iron particles are recycled to the fenton reaction tank as the fluidized filler.
In the above technical scheme, preferably, the gas collection and treatment system includes a gas collecting hood, an induced air duct and a combustion tower, the gas collecting hood is sealed and covered on the fenton reaction tank, one end of the induced air duct is communicated with the inside of the gas collecting hood, and the other end of the induced air duct is connected to an inlet of the induced air duct through a return valve and communicated to the combustion tower through an electric valve.
In the above technical solution, preferably, the axial center line of the aeration water distribution nozzles intersects the horizontal surface downward at an angle of 30 ° to 60 °, and the plurality of aeration water distribution nozzles are circumferentially arranged at the bottom of the fenton reaction tank at a preset angle.
At the upper partIn the technical scheme, preferably, the current density of the anode plate is 0.25-12.5 mA, the current density of the cathode plate is 2-15 mA, and Fe in the Fenton reaction tank2+The concentration of the catalyst is 0.2-12 mol/L, the concentration of hydrogen peroxide is 0.04-3 mol/L, and the distance between the anode plate and the cathode plate is 15-40 mm.
In the above technical scheme, preferably, the required air supply of the backflow air pipe where the backflow valve is located is insufficient, when negative pressure exists in the backflow air pipe, the electric valve is reversely opened to supplement the air supply to the induced draft fan, and when positive pressure exists in the backflow air pipe, the combustion tower is opened to consume the residual tail gas.
Compared with the prior art, the invention has the beneficial effects that: the advantages of the fluidized bed supporter filler are used in the electro-Fenton technology, and the precipitated iron mud in the electro-Fenton water outlet system is used for preparing the fluidized filler, so that Fe3+Not only can be reduced at the cathode, but also can be coated on the surface of a fluidized filler carrier by crystallization or precipitation to form hydroxyl complex iron, can further catalyze the Fenton reaction, and can be reduced into Fe2+The removal rate of electro-Fenton is greatly broken through, the electro-Fenton method is enabled to realize zero discharge of chemical sludge, the mode of the fluidized bed promotes chemical oxidation reaction and electric proton transfer efficiency, the fluidized environment is created while aeration dosing is carried out, energy is saved, consumption is reduced, the removal rate is greatly improved, and the separated iron is recycled.
Drawings
Fig. 1 is a schematic diagram illustrating an overall configuration of a jet fluidized bed electro-fenton treatment system according to an embodiment of the present invention;
FIG. 2 is a schematic view of a combined structure of an electro-Fenton treatment system and a jet medicine-adding aeration water distribution system according to an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of an electro-Fenton processing system according to an embodiment of the present invention;
FIG. 4 is a schematic cross-sectional view of a self-oscillating jet-dosing mixer according to an embodiment of the present invention;
fig. 5 and fig. 6 are schematic diagrams of application modes of two embodiments of the fenton reaction tank disclosed by the invention.
In the drawings, the correspondence between each component and the reference numeral is:
1. an electro-Fenton treatment system, 11, a power supply, 12, an anode plate, 13, a cathode plate, 14, a Fenton reaction tank,
2. jet flow medicine adding aeration water distributing system, 21, water introducing pump, 22, hydrogen peroxide storage tank, 23, hydrogen peroxide medicine adding pump, 24, self-oscillation jet flow medicine adding mixer, 241, fluid driving nozzle, 242, air suction pipe, 243, air mixing chamber, 244, self-oscillation chamber, 245, collision wall, 246, diffusion pipe, 25, induced draft fan, 26, gas-liquid exit pipeline, 27, aeration water distributing nozzle, 28, fluidization filler,
3. a sedimentation water outlet tank, 31, a neutralization tank, 32, an alkali adding subsystem, 33, a sedimentation tank, 34, inclined plate sedimentation, 35, a mud scraper, 36, a mud discharge valve, 37, a mud outlet pipe,
4. a filler recovery preparation system, 41, a dryer, 42, a granulator, 43, an auxiliary agent subsystem, 44, a calciner, 45, a feed hole,
5. the system comprises a gas collecting and processing system, 51 a gas collecting hood, 52 an induced draft tube, 53 an electric valve, 54 a return valve, 55 a return gas tube and 56 a combustion tower.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
The invention is described in further detail below with reference to the attached drawing figures:
as shown in fig. 1 and 2, a jet fluidized bed type electro-fenton treatment system according to the present invention includes: the device comprises a jet flow dosing aeration water distribution system 2, an electro-Fenton treatment system 1, a sedimentation water outlet tank 3, a filler recovery preparation system 4 and a gas collection treatment system 5; the jet flow medicine adding aeration water distribution system 2 introduces wastewater, hydrogen peroxide is pumped into the wastewater, air is input to carry out aeration treatment on the wastewater to form gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electro-Fenton treatment system 1; adding a fluidized filler 28 into the electro-Fenton treatment system 1, performing electro-Fenton treatment on the wastewater after adding the chemicals and aerating, outputting the treated wastewater to a precipitation water outlet pool 3, and outputting waste gas generated by the electro-Fenton treatment to a gas collection treatment system 5; the precipitation water outlet pool 3 is used for carrying out alkali treatment and precipitation on the wastewater after electro-Fenton treatment, and discharging precipitated sludge to the filler recovery preparation system 4; the filler recovery preparation system 4 circularly adds the particles after drying, adding the viscose auxiliary agent and granulating and calcining into the electro-Fenton treatment system 1 to be used as fluidized fillers 28; the gas collecting and processing system 5 introduces a part of the collected waste gas into the jet medicine adding aeration water distribution system 2 to carry out aeration treatment on the waste water, and the rest part is carried out combustion consumption treatment.
In the embodiment, industrial wastewater enters the electro-Fenton treatment system 1 through the jet medicine adding aeration water distribution system 2, hydrogen peroxide (hydrogen peroxide) and gas used by the system are pumped into the jet medicine adding aeration water distribution system 2, fluidized filler 28 is added into the electro-Fenton treatment system 1 to realize the fluidization effect, effluent of the electro-Fenton treatment system 1 enters the sedimentation water outlet tank 3 for neutralization and sedimentation, and iron sludge at the bottom of the tank enters the filler recovery preparation system 4 for drying, granulation and calcination to obtain the fluidized filler 28 required by the electro-Fenton treatment system 1 for recycling. The waste gas generated by the electro-Fenton treatment system 1 is recycled by the gas collecting and treating device, and a part of tail gas is used for supplying gas to the jet flow dosing aeration water distribution system 2, so that the redundant gas is consumed by combustion.
Specifically, by using the advantages of the fluidized bed carrier filler in the electro-Fenton technology, the precipitated iron mud in the electro-Fenton effluent system is used for preparing the fluidized filler 28, so that Fe3+Not only can be reduced at the cathode, but also can be coated on the surface of a carrier of the fluidized filler 28 by crystallization or precipitation to form hydroxyl complex iron, can further catalyze the Fenton reaction, and can be reduced into Fe2+Greatly breaks through the removal rate of electro-Fenton, leads the electro-Fenton method to realize zero discharge of chemical sludge, promotes the chemical oxidation reaction and the electric proton transfer efficiency in the fluidized bed mode, and adds medicaments in the aeration processThe method creates a fluidization environment, saves energy, reduces consumption, greatly improves the removal rate, and realizes the recycling of the separated iron.
As shown in fig. 3, in the above embodiment, preferably, the electro-fenton treatment system 1 includes a power source 11, an anode plate 12, a cathode plate 13 and a fenton reaction tank 14, the anode plate 12 and the cathode plate 13 are respectively connected to the positive electrode and the negative electrode of the power source 11, and the anode plate 12 and the cathode plate 13 are respectively arranged in the fenton reaction tank 14 at intervals and in a staggered manner.
In the above embodiment, preferably, the pH of the industrial wastewater inlet water is adjusted to 3-6, a micron-sized gas-liquid mixed flow is injected into the electro-fenton treatment system 1 through the jet chemical-adding aeration water distribution system 2, the two-port direct-current power supply 11 is turned on, the current density of the anode plate 12 diffused to the anode plate is controlled to be 0.25-12.5 mA, the current density of the cathode plate 13 is controlled to be 2-15 mA, and the hydraulic retention time is controlled to be 30-480 min, so that the treatment of the organic wastewater is completed. Control of Fe in Fenton reaction cell 142+The concentration of the catalyst is 0.2-12 mol/L, and the concentration of the hydrogen peroxide is 0.04-3 mol/L. Preferably, the iron electrode anode plate 12 and the graphite electrode cathode plate 13 are arranged near the oxygen evolution electrode, and the distance between the iron electrode anode plate 12 and the graphite electrode cathode plate 13 is preferably 15-40 mm. Under the action of current, the iron electrode and the graphite electrode simultaneously generate two-electron reaction, and the iron electrode generates Fe2+The graphite electrode receives the oxygen generated by the oxygen evolution electrode to generate a small amount of H202，Fe2+With in situ generated and pumped H2O2The reaction generates OH with strong oxidizing property, thereby oxidizing and removing organic pollutants.
In the above embodiment, preferably, the jet dosing aeration water distribution system 2 includes a water pump 21, a hydrogen peroxide storage tank 22, a hydrogen peroxide dosing pump 23, a self-oscillation jet dosing mixer 24, an induced draft fan 25, a gas-liquid exit pipeline 26, an aeration water distribution nozzle 27 and a fluidization filler 28; the waste water is input from the inlet of the priming pump 21, the outlet of the priming pump 21 is communicated with the self-oscillation jet dosing mixer 24, the inlet of the hydrogen peroxide dosing pump 23 is communicated with the hydrogen peroxide storage tank 22, the outlet of the hydrogen peroxide dosing pump 23 is communicated with the outlet channel of the priming pump 21, the outlet of the induced draft fan 25 is communicated with the air suction pipe 242 of the self-oscillation jet dosing mixer 24, the outlet of the self-oscillation jet dosing mixer 24 is connected to the aeration water distribution nozzles 27 through the gas-liquid outgoing pipeline 26, the aeration water distribution nozzles 27 are arranged at the bottom in the Fenton reaction tank 14, and the fluidized filler 28 is filled in the Fenton reaction tank 14.
As shown in fig. 4, in the above embodiment, preferably, the self-oscillating jet dosing mixer 24 includes a fluid-driven nozzle 241, an air suction pipe 242, an air mixing chamber 243, a self-oscillating chamber 244, an impact wall 245 and a diffusion pipe 246, the fluid-driven nozzle 241 is communicated with the outlets of the water-induced pump 21 and the hydrogen peroxide dosing pump 23, the air mixing chamber 243 is arranged at the outlet of the fluid-driven nozzle 241, the side wall of the air mixing chamber 243 is communicated with the air suction pipe 242, the air sucked by the air suction pipe 242 forms an air-liquid mixed flow with the mixture of wastewater and hydrogen peroxide in the air mixing chamber 243, the self-oscillating chamber 244 is arranged at the outlet of the air mixing chamber 243, the impact wall 245 is formed inside the self-oscillating chamber 244, the air-liquid mixed flow forms a discrete vortex ring in the self-oscillating chamber 244 by self-oscillating shear and generates a pressure oscillation wave under the action of, the diffuser 246 communicates with the gas-liquid exit line 26, and the gas-liquid mixture flow is ejected from the diffuser 246.
Specifically, the industrial wastewater is introduced into the self-oscillation jet dosing mixer 24 by the priming pump 21, and is injected by the fluid driving nozzle 241 after the hydrogen peroxide dosing pump 23 adds a certain amount of hydrogen peroxide, so that a negative pressure is formed in the gas mixing chamber 243, a part of the tail gas of the gas collecting and processing system 5 is sucked by the air suction pipe 242, and the induced draft fan 25 plays a role in tail gas traction. The gas-liquid mixed flow is disturbed by the vorticity within a certain frequency range in the self-oscillation chamber 244, is amplified in the self-oscillation chamber 244, forms a violent shearing field by the self-oscillation action, forms a series of discrete vortex rings in a shearing layer, and when the discrete vortex rings reach and interact with the collision wall 245, pressure oscillation waves are generated in the area near the collision wall 245, and the waves propagate upstream at the speed of sound and induce new vorticity pulsation upstream. The process is repeated continuously, strong self-oscillation is formed in the cavity, after a certain cycle number, repeated and violent shearing is carried out on the gas-liquid mixed liquid flowing through the self-oscillation cavity, the size of generated bubbles is reduced, the uniform mixing of the raw water and the hydrogen peroxide is realized, and micron-sized bubbles are generated. The two-phase gas-liquid stream is ejected from diffuser 246 in pulses.
As shown in fig. 5 and 6, specifically, the gas-liquid mixed flow is introduced into the electro-fenton treatment system 1 through the gas-liquid outlet line 26, and further gas and water distribution is performed through the plurality of aeration water distribution nozzles 27, and a fluidized state of the fluidized packing 28 is realized. Preferably, a plurality of aeration water distribution nozzles 27 are arranged around the bottom of the Fenton reaction tank 14 of the electro-Fenton treatment system 1 at a predetermined angle of incidence. Further preferably, the axial center line of the aeration water distribution nozzles 27 and the horizontal surface are intersected downwards to form a angle of 30-60 degrees, the combined arrangement of the aeration water distribution nozzles 27 controls the flowing state of the fluid in the Fenton reactor, the uniformity of gas distribution and water distribution can be further realized, the fluidized state without dead angles is realized, and the electric transmission efficiency is improved.
Specifically, as shown in fig. 5, if the fenton reaction tank 14 is circular, the gas-liquid outlet pipeline 26 is also circular and surrounds the circumferential edge of the bottom in the circular fenton reaction tank 14, the aeration water distribution nozzles 27 are respectively and uniformly arranged on the gas-liquid outlet pipeline 26 at preset intervals, because the anode plate 12 and the cathode plate 13 of the electro-fenton treatment system 1 are also arranged at the bottom in the fenton reaction tank 14, the anode plate 12 and the cathode plate 13 are arranged in the diameter direction of the circular fenton reaction tank 14, the aeration water distribution nozzles 27 are respectively arranged on the circumference of the gas-liquid outlet pipeline 26 and both face a preset injection angle direction relative to the tangential direction of the current position, so that the entire fenton reaction tank 14 has injection liquid flow in each direction under the arrangement of the aeration water distribution nozzles 27 surrounding one circle, and the axial center line of the aeration water distribution nozzles 27 intersects with the horizontal plane at an angle of 30 to 60 degrees, therefore, the fluidized filler in the Fenton reaction tank 14 is fluidized, and can be fully mixed under the impact of the liquid column sprayed by the aeration and water distribution nozzle 27. The stirring and mixing of the fluid just mainly occur in the regions of the anode plate 12 and the cathode plate 13 which are subjected to reaction, so that a dead-corner-free fluidized state is realized, and the proton efficiency of the Fenton reaction is improved.
As shown in fig. 6, if the fenton reaction tank 14 is rectangular or square, the gas-liquid outlet pipe 26 is also rectangular or square, and is disposed at the edge of the tank wall at the bottom of the fenton reaction tank 14, the aeration water distribution nozzles 27 are respectively and uniformly disposed on the gas-liquid outlet pipe 26 at predetermined intervals, because the anode plate 12 and the cathode plate 13 of the electro-fenton treatment system 1 are also disposed at the bottom of the fenton reaction tank 14, the anode plate 12 and the cathode plate 13 are transversely disposed at the middle of the rectangular or square fenton reaction tank 14, the aeration water distribution nozzles 27 are respectively disposed on each segment of the gas-liquid outlet pipe 26 along the tank wall direction and both face a predetermined injection angle direction relative to the tank wall direction at the current position, so that the entire fenton reaction tank 14 has injection liquid flows in each direction under the arrangement of the aeration water distribution nozzles 27 surrounding one circle and the axial center line thereof intersects the horizontal plane at an angle of 30 to 60 degrees, therefore, the fluidized filler in the Fenton reaction tank 14 is fluidized, and can be fully mixed under the impact of the liquid column sprayed by the aeration and water distribution nozzle 27. The stirring and mixing of the fluid are just mainly generated in the regions of the anode plate 12 and the cathode plate 13 which are in the middle for reaction, thereby realizing a fluidized state without dead angles and improving the proton efficiency of Fenton reaction.
Wherein, the jet flow medicine adding aeration water distribution system 2 leads the fluidized filler 28 in the Fenton reaction tank 14 to flow in multi-dimensional longitudinal and annular directions, and the complex iron generated by the electro-Fenton reaction is coated on the surface of the fluidized bed filler in a crystallization or precipitation way to form a supporter, so that the Fe generated by the reaction3+Most of the FeOOH heterogeneous crystal grows on the filler in the form of crystal growth, and the heterogeneous crystal is a good catalyst and promotes Fe on the surface of the carrier3+To Fe2+The conversion of (2) also increases the conductivity due to the existence of the Fe supporter in the reaction tank, forms a micro-battery structure, provides a catalytic action and a reaction site for the action of OH free radicals and COD, improves the contact frequency between sewage and the OH free radicals, simultaneously realizes no dead angle in an electro-Fenton reaction zone, provides a space for further increasing the concentration of the Fenton reagent, and has low energy consumption and high efficiency.
In the above embodiment, preferably, the sedimentation water outlet tank 3 includes a neutralization tank 31, an alkali adding subsystem 32, a sedimentation tank 33, an inclined plate sedimentation 34, a mud scraper 35 and a mud outlet pipe 37, the wastewater in the fenton reaction tank 14 is introduced into the neutralization tank 31, the alkali adding subsystem 32 adds an alkaline reagent into the neutralization tank 31 for neutralization reaction, and the PH value is controlled to be 7-7.5. And the sludge enters a sedimentation tank 33 after neutralization reaction, the inclined plate sedimentation 34 is obliquely arranged in the sedimentation tank 33, the precipitated sludge is settled to the bottom of the sedimentation tank 33 along with the inclined plate sedimentation 34 to realize sludge-water separation, the supernatant is discharged for further treatment, a mud scraper 35 outputs the sludge to a filler recovery preparation system 4 through a mud outlet pipe 37, and a mud discharge valve 36 is arranged on the mud outlet pipe 37.
In the above embodiment, preferably, the filler recycling preparation system 4 includes a dryer 41, a granulator 42, an auxiliary subsystem 43, and a calciner 44, an inlet of the dryer 41 is communicated with the sludge outlet pipe 37, an outlet of the dryer 41 is communicated with an inlet of the granulator 42, the auxiliary subsystem 43 adds a viscose auxiliary agent into the granulator 42, the dried sludge is formed into bars under the action of the viscose auxiliary agent and output in a granulation manner, an outlet of the granulator 42 is communicated with the calciner 44, an outlet of the calciner 44 is communicated with a feeding hole 45 on the fenton reaction tank 14, and the calcined porous iron particles are periodically circulated to the fenton reaction tank 14 as the fluidized filler 28 for recycling.
In the above embodiment, preferably, the gas collection and treatment system 5 includes the gas collection hood 51, the induced air duct 52 and the combustion tower 56, the gas collection hood 51 is hermetically covered on the fenton reaction tank 14, one end of the induced air duct 52 is communicated with the inside of the gas collection hood 51, and the other end is respectively connected to the inlet of the induced air fan 25 through the return valve 54 and is communicated to the combustion tower 56 through the electric valve 53.
In the above embodiment, preferably, when the gas source required by the return gas pipe 55 of the return valve 54 is insufficient and the pressure in the return gas pipe 55 is negative, the electric valve 53 is reversely opened to supplement the gas source to the induced draft fan 25, and when the pressure in the return gas pipe 55 is positive, the combustion tower 56 is opened to consume the remaining tail gas.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A jet fluidized bed electro-fenton treatment system, comprising: the system comprises a jet flow dosing aeration water distribution system, an electro-Fenton treatment system, a sedimentation water outlet pool, a filler recovery preparation system and a gas collection treatment system;
the jet flow dosing aeration water distribution system introduces wastewater, hydrogen peroxide is pumped into the wastewater, air is input to carry out aeration treatment on the wastewater to form gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electro-Fenton treatment system;
adding a fluidized filler into the electro-Fenton treatment system, performing electro-Fenton treatment on the wastewater after adding the chemicals and aerating, outputting the treated wastewater to the sedimentation water outlet tank, and outputting waste gas generated by the electro-Fenton treatment to the gas collection treatment system;
the sedimentation water outlet tank is used for carrying out alkali treatment and sedimentation on the wastewater after electro-Fenton treatment, and discharging the precipitated sludge to the filler recovery preparation system;
the filler recovery preparation system circularly adds the particles after drying, adding the viscose auxiliary agent and granulating and calcining into the electro-Fenton treatment system to serve as fluidized fillers;
the gas collecting and processing system introduces a part of the collected waste gas into the jet flow dosing aeration water distribution system to carry out aeration treatment on the waste water, and the rest part is subjected to combustion consumption treatment.
2. The jet fluidized bed electro-Fenton treatment system according to claim 1, comprising a power source, an anode plate, a cathode plate and a Fenton reaction tank, wherein the anode plate and the cathode plate are respectively connected with a positive pole and a negative pole of the power source, and the anode plate and the cathode plate are respectively arranged in the Fenton reaction tank at intervals in a staggered manner.
3. The jet fluidized bed electro-fenton treatment system of claim 1, wherein: the jet medicine adding aeration water distribution system comprises a water diversion pump, a hydrogen peroxide storage tank, a hydrogen peroxide medicine adding pump, a self-oscillation jet medicine adding mixer, a draught fan, a gas-liquid outgoing pipeline, an aeration water distribution nozzle and fluidized fillers;
waste water is input at the inlet of the diversion pump, the outlet of the diversion pump is communicated with the self-oscillation jet-flow dosing mixer, the inlet of the hydrogen peroxide dosing pump is communicated with the hydrogen peroxide storage tank, the outlet of the hydrogen peroxide dosing pump is communicated with the outlet channel of the diversion pump, the outlet of the induced draft fan is communicated with the air suction pipe of the self-oscillation jet-flow dosing mixer, the outlet of the self-oscillation jet-flow dosing mixer is connected to the aeration water distribution nozzle through a gas-liquid outgoing pipeline, the aeration water distribution nozzle is arranged at the bottom in the Fenton reaction tank, and the fluidization filler is filled in the Fenton reaction tank.
4. The jet fluidized bed electro-Fenton treatment system according to claim 3, wherein the self-oscillating jet chemical dosing mixer comprises a fluid driving nozzle, the air suction pipe, a gas mixing chamber, a self-oscillating chamber, a collision wall and a diffusion pipe, the fluid driving nozzle is communicated with the water suction pump and the outlet of the hydrogen peroxide chemical dosing pump, the gas mixing chamber is arranged at the outlet of the fluid driving nozzle, the side wall of the gas mixing chamber is communicated with the air suction pipe, the mixture of the suction gas, the wastewater and the hydrogen peroxide forms a gas-liquid mixed flow in the gas mixing chamber, the self-oscillating chamber is arranged at the outlet of the gas mixing chamber, the collision wall is formed inside the self-oscillating chamber, the gas-liquid mixed flow self-oscillates and shears in the self-oscillating chamber to form a discrete vortex ring, and pressure oscillation waves are generated under the action of the collision wall, the outlet of the self-oscillation chamber is communicated with the diffusion pipe, the diffusion pipe is communicated with the gas-liquid outgoing pipeline, and the gas-liquid mixed flow is sprayed out from the diffusion pipe.
5. The jet fluidized bed electro-Fenton treatment system according to claim 1, wherein the precipitation effluent tank comprises a neutralization tank, an alkalifying subsystem, a sedimentation tank, an inclined plate sedimentation, a mud scraper and a mud outlet pipe, the wastewater in the Fenton reaction tank is introduced into the neutralization tank, the alkalifying subsystem adds an alkaline reagent into the neutralization tank for neutralization reaction, the wastewater enters the sedimentation tank after the neutralization reaction, the inclined plate sedimentation is obliquely arranged in the sedimentation tank, the precipitated sludge is sedimentated to the bottom of the sedimentation tank along with the inclined plate sedimentation, the mud scraper outputs the sludge to the filler recovery preparation system through the mud outlet pipe, and the mud outlet pipe is provided with a mud discharge valve.
6. The jet fluidized bed electro-Fenton treatment system according to claim 5, wherein the filler recovery preparation system comprises a dryer, a granulator, an auxiliary subsystem and a calciner, an inlet of the dryer is communicated with the sludge outlet pipe, an outlet of the dryer is communicated with an inlet of the granulator, the auxiliary subsystem adds a viscose auxiliary agent into the granulator, dried sludge is formed into bars under the action of the viscose auxiliary agent and output in a granulation mode, an outlet of the granulator is communicated with the calciner, an outlet of the calciner is communicated with a feeding hole in the Fenton reaction tank, and calcined porous iron particles are recycled to the Fenton reaction tank as the fluidized filler.
7. The fluid-jet fluidized-bed electro-Fenton treatment system according to claim 1, wherein the gas collection treatment system comprises a gas collection hood, an air induction pipe and a combustion tower, the gas collection hood is hermetically covered on the Fenton reaction tank, one end of the air induction pipe is communicated with the inside of the gas collection hood, and the other end of the air induction pipe is respectively connected to an inlet of the induced draft fan through a reflux valve and is communicated to the combustion tower through an electric valve.
8. The jet fluidized bed electro-Fenton treatment system according to claim 3, wherein the axial center line of the aeration water distribution nozzles intersects the horizontal surface downward at an angle of 30 ° to 60 °, and the plurality of aeration water distribution nozzles are circumferentially arranged at the bottom of the Fenton reaction tank at a predetermined angle of incidence, respectively.
9. The jet fluidized bed electro-Fenton treatment system according to claim 2, wherein the current density of the anode plate is 0.25-12.5 mA, the current density of the cathode plate is 2-15 mA, and Fe in the Fenton reaction tank2+The concentration of the catalyst is 0.2-12 mol/L, the concentration of hydrogen peroxide is 0.04-3 mol/L, and the distance between the anode plate and the cathode plate is 15-40 mm.
10. The fluid-jet fluidized-bed electro-fenton treatment system according to claim 7, wherein the electric valve is reversely opened to supplement the air source to the induced draft fan when the air source required by the return air pipe in which the return valve is located is insufficient and the pressure in the return air pipe is negative, and the combustion tower is opened to consume the remaining tail gas when the pressure in the return air pipe is positive.
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| CN111635088A (en) * | 2020-05-25 | 2020-09-08 | 湖南隆辉环保有限公司 | Jet type medicine adding device |
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