CN109179630B - Ozone aeration type electro-Fenton fluidized bed - Google Patents
Ozone aeration type electro-Fenton fluidized bed Download PDFInfo
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- CN109179630B CN109179630B CN201811333305.9A CN201811333305A CN109179630B CN 109179630 B CN109179630 B CN 109179630B CN 201811333305 A CN201811333305 A CN 201811333305A CN 109179630 B CN109179630 B CN 109179630B
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- fenton
- hydrogen peroxide
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 238000005273 aeration Methods 0.000 title claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000010865 sewage Substances 0.000 claims abstract description 40
- 239000012028 Fenton's reagent Substances 0.000 claims abstract description 19
- 239000000126 substance Substances 0.000 claims abstract description 11
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 154
- 239000011790 ferrous sulphate Substances 0.000 claims description 60
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 60
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 59
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 59
- 239000007788 liquid Substances 0.000 claims description 40
- 239000003814 drug Substances 0.000 claims description 29
- 238000010992 reflux Methods 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 14
- 239000000945 filler Substances 0.000 claims description 13
- 238000009826 distribution Methods 0.000 claims description 12
- 239000003792 electrolyte Substances 0.000 claims description 12
- 238000002360 preparation method Methods 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 7
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 6
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 5
- 235000011152 sodium sulphate Nutrition 0.000 claims description 4
- 238000002203 pretreatment Methods 0.000 claims 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 32
- 238000007254 oxidation reaction Methods 0.000 abstract description 26
- 230000003647 oxidation Effects 0.000 abstract description 25
- 238000000034 method Methods 0.000 abstract description 22
- 229910052742 iron Inorganic materials 0.000 abstract description 17
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 abstract description 13
- 229910001448 ferrous ion Inorganic materials 0.000 abstract description 13
- 230000000694 effects Effects 0.000 abstract description 10
- 125000002887 hydroxy group Chemical group [H]O* 0.000 abstract description 10
- 150000001491 aromatic compounds Chemical class 0.000 abstract description 5
- 230000003311 flocculating effect Effects 0.000 abstract description 3
- 238000005189 flocculation Methods 0.000 abstract description 3
- 230000016615 flocculation Effects 0.000 abstract description 3
- 238000005188 flotation Methods 0.000 abstract description 2
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 abstract 1
- 229910001447 ferric ion Inorganic materials 0.000 abstract 1
- 230000006872 improvement Effects 0.000 description 11
- 150000003254 radicals Chemical class 0.000 description 10
- 238000005243 fluidization Methods 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- -1 small-molecule fatty acids Chemical class 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 238000005868 electrolysis reaction Methods 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000012856 packing Methods 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 238000002848 electrochemical method Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-M hydrogensulfate Chemical compound OS([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-M 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002101 nanobubble Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- 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
- C02F1/465—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electroflotation
-
- 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
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Landscapes
- 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)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to the technical field of sewage treatment, in particular to an ozone aeration type electro-Fenton fluidized bed which comprises a fluidized bed tank body, wherein a split-phase jet flow chemical feeder and a three-dimensional electro-Fenton system are arranged in the fluidized bed tank body, a water distributor for inputting sewage is arranged in the fluidized bed tank body, fenton reagent is conveyed by the split-phase jet flow chemical feeder to enter the fluidized bed tank body to be mixed with the sewage, and an ozone pretreatment tank for generating ozone is arranged at the bottom of the fluidized bed tank body. According to the technical scheme, high molecular organic matters can be degraded through ozone aeration; meanwhile, hydroxyl radicals generated by the Fenton reagent attack small molecular organic matters, so that the dosage of ozone and Fenton reagent is effectively reduced; the three-dimensional electro-Fenton system can also generate electric flotation and electric flocculation, can further induce hydroxyl free radicals and ferrous ions to be generated, and avoids the ferric ions from flocculating into iron mud to be settled; combines an ozone oxidation method, a Fenton fluidized bed and an electro-Fenton system, and improves the removal effect of unsaturated organic matters and aromatic compounds in sewage.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an ozone aeration type electro-Fenton fluidized bed.
Background
In the current sewage treatment technology, after the biological treatment of industrial wastewater, the residual organic matters are generally difficult to biodegrade, and the low-concentration refractory organic matters are mainly removed by adopting an advanced oxidation technology. The advanced oxidation technology which is widely applied in industry at present is advanced oxidation technology related to Fenton oxidation and ozone oxidation.
The simple ozone oxidation has selectivity, has good treatment effect on some unsaturated organic matters and aromatic compounds in sewage, but has poor treatment effect on some small-molecule fatty acids and other organic matters, and is difficult to completely mineralize and decompose the organic matters. Meanwhile, an oxygen source ozone generator is generally adopted for ozone oxidation to obtain higher ozone concentration, and the treated tail gas still has ozone with a certain concentration because the ozone is difficult to fully react, and the tail gas is further required to be treated, so that the waste of oxygen and ozone is caused. And the cost for preparing and storing ozone is high, and the cost for industrial use is high.
Fenton oxidation technology is more common at present and has the photoFenton, electro-Fenton and Fenton fluidized beds, the Fenton fluidized bed has low operation cost, the equipment is simply and widely applied in industry, but the post-treatment cost is increased due to the fact that iron mud is generated during operation; while photoFenton greatly reduces the yield of iron mud, but has low treatment efficiency; and the equipment investment cost and the operation cost of the electro-Fenton are high.
The electro-Fenton method is generated by an electrochemical method and is used as a continuous source of Fenton reagent, and the electro-Fenton method and the Fenton reagent act immediately after being generated to generate hydroxyl free radicals with high activity, so that organic matters are degraded, and the Fenton reagent is directly generated in the electrolytic process. Compared with the traditional Fenton method, the electro-Fenton method has the unique advantages that a small amount of chemical agents are not needed or only needed to be added, the treatment cost can be greatly reduced, the treatment process is clean, secondary pollution to water quality can not be generated, the equipment is relatively simple, the parameters to be controlled in the electrolysis process are only current and voltage, and the automatic control is easy to realize. Besides the oxidation of hydroxyl free radicals, the electro-Fenton method has the accompanying purification effects of anodic oxidation, electro-adsorption and the like, so that the treatment efficiency is higher than that of the traditional Fenton method, the occupied area is small, the treatment period is short, the condition requirement is not harsh, the electro-Fenton method is easy to combine with other methods, and an effective way is provided for comprehensive treatment of wastewater. However, the electro-Fenton technology also has the problems of low free radical yield, slow pollutant degradation rate, incomplete mineralization and the like. Therefore, how to improve the prior Fenton oxidation technology is to design a sewage treatment device with a plurality of oxidation methods in cooperation so as to avoid the defects of a single oxidation method, and the method has important significance.
Disclosure of Invention
The embodiment of the invention aims to provide an ozone aeration type electro-Fenton fluidized bed which is combined with an ozone oxidation method to deeply remove unsaturated organic matters and aromatic compounds in sewage.
In order to achieve the above purpose, the embodiment of the invention provides an ozone aeration type electro-Fenton fluidized bed, which comprises a fluidized bed tank body, wherein a split-phase jet flow chemical feeder and a three-dimensional electro-Fenton system are arranged in the fluidized bed tank body, a water distributor for inputting sewage is arranged in the fluidized bed tank body, fenton reagent is conveyed by the split-phase jet flow chemical feeder to enter the fluidized bed tank body to be mixed with the sewage, and an ozone pretreatment tank for generating ozone is arranged at the bottom of the fluidized bed tank body.
As an improvement of the technical scheme, an aeration disc is arranged at the bottom of the ozone pretreatment tank, a nano homogenizing generator, an air accommodating pump and an ozone generator are connected to the aeration disc, and ozone generated by the ozone generator sequentially passes through the air accommodating pump, the nano homogenizing generator and the aeration disc according to the gas flow sequence and finally enters the ozone pretreatment tank.
As an improvement of the technical scheme, a screen for passing micro-nano ozone bubbles and sewage is arranged between the ozone pretreatment tank and the fluidized bed tank body.
As an improvement of the technical scheme, the water distributor is arranged at the bottom of the fluidized bed tank body, and a water distribution nozzle close to the screen is arranged on the water distributor.
As an improvement of the technical scheme, at least one mixed dosing jet flow arm pointing to the inside of the fluidized bed tank body is arranged on the split-phase jet flow doser, and a hydrogen peroxide runner and a ferrous sulfate runner which are communicated with the mixed dosing jet flow arm are arranged on the split-phase jet flow doser.
As an improvement of the technical scheme, the hydrogen peroxide runner is connected with a hydrogen peroxide medicament mixing tank through a pipeline, and the hydrogen peroxide runner and the hydrogen peroxide medicament mixing tank are sequentially provided with a hydrogen peroxide dosing metering pump, a hydrogen peroxide dosing control valve, a hydrogen peroxide dosing device, a hydrogen peroxide dosing return pipe and a hydrogen peroxide return liquid inlet pump according to the fluid flow direction; the ferrous sulfate runner is connected with a ferrous sulfate medicament blending pool through a pipeline, and a ferrous sulfate dosing metering pump, a ferrous sulfate dosing control valve, a ferrous sulfate dosing device, a ferrous sulfate dosing return pipe and a ferrous sulfate return liquid inlet pump are sequentially arranged between the ferrous sulfate runner and the ferrous sulfate medicament blending pool according to the fluid flow direction.
As an improvement of the technical scheme, a reflux weir plate is arranged on the upper side of the inside of the fluidized bed tank body, one end, far away from the hydrogen peroxide reflux liquid inlet pump, of the hydrogen peroxide dosing reflux pipe extends into one side of the reflux weir plate in the inside of the fluidized bed tank body, and sewage in the reflux weir plate is refluxed into the hydrogen peroxide reflux liquid inlet pump through the hydrogen peroxide dosing reflux pipe; one end of the ferrous sulfate dosing return pipe, which is far away from the ferrous sulfate reflux liquid inlet pump, extends into one side of a reflux weir plate in the fluidized bed tank body, and sewage in the reflux weir plate flows back into the ferrous sulfate reflux liquid inlet pump through the ferrous sulfate dosing return pipe.
As the improvement of the technical scheme, the packing sieve plate is arranged in the fluidized bed tank body, the three-dimensional electro-Fenton system is positioned above the packing sieve plate and comprises an electrode, an anode, a cathode and a particle electrode, and the split-phase jet doser and the ozone pretreatment tank are positioned on one side, away from the three-dimensional electro-Fenton system, of the packing sieve plate.
As an improvement of the technical scheme, the three-dimensional electro-Fenton system further comprises an electrolyte inlet, and the electrolyte inlet is connected with a sodium sulfate liquid inlet tank and an electrolyte liquid inlet pump.
As the improvement of the technical scheme, the upper side of the three-dimensional electro-Fenton system is provided with a filter screen, a water outlet weir plate is arranged above the filter screen, and a water outlet pipe extending to one side of the water outlet weir plate is arranged at the outer side of the fluidized bed tank body.
The Fenton fluidized bed device has the following advantages:
(1) The ozone degradation tank is arranged at the lower end of the Fenton fluidized bed, redundant ozone gas can enter the fluidized bed tank body through the screen, and a large amount of suspended matters can be taken away by the ozone gas in the oxidation reaction process, so that a good environment is provided for the Fenton reaction, hydroxyl radicals generated by Fenton reagent attack small molecular organic matters, the consumption of ozone and Fenton reagent is effectively reduced, an ozone oxidation method is combined with the Fenton fluidized bed, and the removal effect of unsaturated organic matters and aromatic compounds in sewage is improved;
(2) The water distributor of the Fenton fluidized bed and the jet stirring mode of the split-phase jet doser greatly improve the mixing efficiency of the medicament in the whole fluidized bed tank body, can realize rapid mixing among multiple fluids, has high fluidization efficiency of a filler carrier, has no dead angle in a fluidization area in the fluidized bed tank body, and fully and rapidly reacts;
(3) The three-dimensional electro-Fenton system is arranged at the upper part in the fluidized bed tank body, COD is degraded by utilizing the electro-Fenton principle, the addition amount of the medicament is saved, meanwhile, residual ozone and iron ions are consumed by utilizing a three-dimensional electrode in the three-dimensional electro-Fenton system, meanwhile, the three-dimensional electro-Fenton system can also generate electric floatation and electric flocculation, hydroxyl free radicals and ferrous ions can be further induced to generate, the ferrous ions are combined with hydrogen peroxide again to form Fenton reagent to participate in fluidization reaction, the iron ions are prevented from flocculating into iron mud to be settled, and the iron mud is cooperatively matched with the ozone oxidation and the Fenton fluidized bed, so that the iron mud in the fluidized bed tank body is greatly reduced;
(4) The water distributor not only improves the water distribution uniformity, but also continuously breaks up redundant ozone, so that redundant ozone oxidation tail gas is further reacted and absorbed in a fluidized bed, and a large amount of suspended matters can be taken away by the tiny oxidation tail gas;
(5) The whole system is ingenious in design, the structures are matched with each other, the multiple oxidation methods are matched with each other, the sewage treatment efficiency is high, no dead angle exists in the whole stirring process, the reaction is sufficiently and rapidly, the homogenization degree is high, the overall pipeline layout is reasonable, the hidden trouble of mechanical faults is few, the service life is long, the maintenance is convenient, the production cost is saved, and the market prospect is wide.
Drawings
Fig. 1 is a schematic structural diagram of an ozone aeration type electro-Fenton fluidized bed in an embodiment of the invention.
In the figure: the preparation method comprises the steps of 1-an ozone pretreatment tank, 2-a fluidized bed tank body, 3-a split-phase jet doser, 4-a water distributor, 5-a three-dimensional electro Fenton system, 6-a hydrogen peroxide dosing device, 7-a ferrous sulfate dosing device, 11-an ozone generator, 12-Rong Qibeng, 13-a nano homogenizing generator, 14-an aeration disk, 15-a screen, 21-a filler screen, 22-a water outlet weir plate, 23-a backflow weir plate, 24-an exhaust valve, 25-a water outlet pipe, 26-a blow-down valve, 27-a blow-down pipe, 31-a hydrogen peroxide runner, 32-a ferrous sulfate runner, 33-a mixed dosing jet arm, 34-a hydrogen peroxide backflow liquid inlet pump, 35-a ferrous sulfate backflow liquid inlet pump, 36-hydrogen peroxide dosing backflow pipe, 37-ferrous sulfate dosing backflow pipe, 41-a water distributor runner, 42-water distribution nozzle, 43-sewage liquid inlet pump, 44-liquid inlet valve, 45-liquid inlet pipe, 51-electrode, 52-anode, 53-cathode, 54-particle electrode, 55-electrolyte liquid inlet, 56-electrolyte liquid inlet pump, 57-sodium sulfate liquid pond, 58-sodium sulfate liquid inlet valve, 58-hydrogen peroxide, 58-62-hydrogen peroxide dosing valve, hydrogen peroxide control valve, and 71-hydrogen peroxide dosing tank, and controlling the hydrogen peroxide dosing valve to add the hydrogen peroxide to the hydrogen sulfate and the dosing tank to prepare the preparation method.
Detailed Description
Further advantages and effects of the present invention will become apparent to those skilled in the art from the disclosure of the present invention, which is described by the following examples.
It should be understood that the structures, proportions, sizes, etc. shown in the drawings are for illustration purposes only and should not be construed as limiting the invention to the extent that it can be practiced, since modifications, changes in the proportions, or otherwise, used in the practice of the invention, are not intended to be critical to the essential characteristics of the invention, but are intended to fall within the spirit and scope of the invention. Also, the terms "inner", "outer", "upper", "lower" and the like are used herein for descriptive purposes only and are not intended to limit the scope of the invention for practical purposes, but rather are intended to cover any adaptations or modifications of the present invention that may be made without substantial modification to the technical context.
In the description of the embodiments below, unless explicitly stated and limited otherwise, the terms "disposed," "connected," and the like are to be construed broadly, and for example, "connected" may be either fixedly connected, detachably connected, or integrated; either mechanically or indirectly, through intermediaries, or in communication with each other, or in interaction with each other, unless otherwise specifically defined. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
As shown in fig. 1, this embodiment provides an ozone aeration type electro-Fenton fluidized bed, which comprises a fluidized bed tank body 2, wherein a split-phase jet doser 3 and a three-dimensional electro-Fenton system 5 are arranged in the fluidized bed tank body 2, a water distributor 4 for inputting sewage is arranged in the fluidized bed tank body 2, the split-phase jet doser 3 conveys Fenton reagent into the fluidized bed tank body 2 to be mixed with the sewage, and an ozone pretreatment tank 1 for generating ozone is arranged at the bottom of the fluidized bed tank body 2.
The water distributor 4 is provided with a plurality of water distribution nozzles 42, the water distributor 4 also comprises a sewage inlet pump 43, a liquid inlet pipe 45, a liquid inlet valve 44 and a water distributor runner 41, wherein the water distribution nozzles 42 are arranged on the water distributor runner 41, and the number of the water distribution nozzles 42 can be multiple. The sewage inlet pump 43 pressurizes the sewage and then inputs the sewage into the fluidized bed tank 2 through the water distributor runner 41.
The split-phase jet doser 3 conveys Fenton reagent into the fluidized bed tank body 2 to be mixed with sewage, the main component of the Fenton reagent is a system with strong oxidizing property composed of hydrogen peroxide (hydrogen peroxide) and ferrous ions, wherein the hydrogen peroxide and the ferrous ions can be respectively and independently added into the fluidized bed tank body 2, or can be added into the fluidized bed tank body 2 after being premixed in the split-phase jet doser 3. In this embodiment, hydrogen peroxide and ferrous ions are premixed in the split-phase jet doser 3 and then added into the fluidized bed tank 2 for detailed description.
The split-phase jet doser 3 is provided with at least one mixed dosing jet arm 33 pointing to the inside of the fluidized bed tank body 2, the split-phase jet doser 3 is provided with a hydrogen peroxide runner 31 and a ferrous sulfate runner 32 which are communicated with the mixed dosing jet arm 33, the hydrogen peroxide conveyed by the hydrogen peroxide runner 31 and the ferrous sulfate ions conveyed by the ferrous sulfate runner 32 are mixed at the position of the mixed dosing jet arm 33, the mixed dosing jet arm 33 can spray the mixed ferrous ions and hydrogen peroxide, so that the mixed dosing jet arm 33 can continuously fill the fluidized bed tank body to generate fluidization, and then the mixed liquid in the fluidized bed tank body 2 is uniformly mixed through continuous stirring of the flow field.
In the above scheme, hydrogen peroxide and ferrous ions can be quickly mixed into Fenton reagent in the mixed dosing jet flow arm 33 of the split-phase jet flow dosing device 3, hydroxyl free radicals are generated, then the mixed reagent is quickly added into the fluidized bed tank 2 of the Fenton fluidized bed, and after the mixed reagent is contacted with a filler carrier, the hydroxyl free radicals generated by the reaction quickly and effectively attack COD, so that the COD degradation efficiency is greatly improved. Meanwhile, hydrogen peroxide and ferrous ions can be sprayed out through the mixed dosing jet arms 33 of different split-phase jet dosers 3, and hydroxyl free radicals are generated after the hydrogen peroxide and the ferrous ions meet in the fluidized bed tank body 2, so that the number of the split-phase jet dosers 3 is multiple.
Further, the hydrogen peroxide runner 31 is connected with a hydrogen peroxide medicament preparing pool 63 through a pipeline, and a hydrogen peroxide dosing metering pump 62, a hydrogen peroxide dosing control valve 61, a hydrogen peroxide dosing device 6, a hydrogen peroxide dosing return pipe 36 and a hydrogen peroxide return liquid inlet pump 34 are sequentially arranged between the hydrogen peroxide runner 31 and the hydrogen peroxide medicament preparing pool 63 according to the fluid flow direction; the ferrous sulfate runner 32 is connected with a ferrous sulfate medicament preparation tank 73 through a pipeline, and a ferrous sulfate dosing metering pump 72, a ferrous sulfate dosing control valve 71, a ferrous sulfate dosing device 7, a ferrous sulfate dosing return pipe 37 and a ferrous sulfate return liquid inlet pump 35 are sequentially arranged between the ferrous sulfate runner 32 and the ferrous sulfate medicament preparation tank 73 according to the fluid flow direction.
Firstly, hydrogen peroxide is configured in a hydrogen peroxide medicament preparation pond 63, then the medicament addition amount is precisely controlled through a hydrogen peroxide medicament adding metering pump 62, the hydrogen peroxide is added through a hydrogen peroxide medicament adding control valve 61 and a hydrogen peroxide medicament adding device 6, and the hydrogen peroxide enters a mixed medicament adding jet flow arm 33 through a hydrogen peroxide medicament adding return pipe 36, a hydrogen peroxide reflux liquid inlet pump 34 and a hydrogen peroxide flow channel 31. The preparation of ferrous sulfate is carried out in the ferrous sulfate medicament preparation pond 73, then the accurate control of medicament addition amount is carried out through the ferrous sulfate medicament adding metering pump 72, the ferrous sulfate adding operation is carried out through the ferrous sulfate medicament adding control valve 71 and the ferrous sulfate medicament adding device 7, the ferrous sulfate enters the mixed medicament adding jet flow arm 33 through the ferrous sulfate medicament adding return pipe 37, the ferrous sulfate reflux liquid inlet pump 35 and the ferrous sulfate flow channel 32, and the ferrous sulfate and the hydrogen peroxide are premixed and then enter the fluidized bed tank body 2.
In the scheme, the upper side of the inside of the fluidized bed tank body 2 is provided with the backflow weir plate 23, and one end, far away from the hydrogen peroxide backflow liquid inlet pump 34, of the hydrogen peroxide dosing backflow pipe 36 stretches into one side of the backflow weir plate 23 in the inside of the fluidized bed tank body 2, and sewage in the backflow weir plate 23 flows back into the hydrogen peroxide backflow liquid inlet pump 34 through the hydrogen peroxide dosing backflow pipe 36; one end of the ferrous sulfate dosing return pipe 37, which is far away from the ferrous sulfate reflux liquid inlet pump 35, extends into one side of the reflux weir plate 23 in the fluidized bed tank body 2, and sewage in the reflux weir plate 23 flows back into the ferrous sulfate reflux liquid inlet pump 35 through the ferrous sulfate dosing return pipe 37. By extending one ends of the hydrogen peroxide dosing return pipe 36 and the ferrous sulfate dosing return pipe 37 to one side of the reflux weir plate 23, sewage at the reflux weir plate 23 can be circulated to the lower part of the fluidized bed tank body 2 through the split-phase jet doser 3, and the uniformity of fluidization effect of each region in the fluidized bed tank body 2 is improved.
The bottom of the ozone pretreatment tank 1 is provided with an aeration disc 14, the aeration disc 14 is connected with a nano homogenizing generator 13, an air accommodating pump 12 and an ozone generator 11, ozone generated by the ozone generator 11 sequentially passes through the air accommodating pump 12, the nano homogenizing generator 13 and the aeration disc 14 according to the gas flow sequence and finally enters the ozone pretreatment tank 1, a screen 15 for passing micro-nano ozone bubbles and sewage is arranged between the ozone pretreatment tank 1 and the fluidized bed tank 2, and the screen 15 can pass through sewage and micro-nano or nano bubbles but cannot pass through filler, so that the filler is prevented from entering the ozone pretreatment tank 1. Ozone pretreatment tank 1 is used for carrying out ozone aeration at the bottom of fluidized bed tank body 2, and ozone oxidation treatment is carried out on sewage in fluidized bed tank body 2, at this time, the PH of the sewage can be adjusted to be 3-6, the ozone adding amount is 100-400 mg/L, and the ozone oxidation residence time can be 2-20 min.
Further, the water distributor 4 is arranged at the bottom of the fluidized bed tank 2, and the water distribution nozzle 42 on the water distributor 4 is close to or directed towards the screen 15. The water distribution nozzle 42 functions in two ways: firstly, the sewage sprayed by the water distribution nozzle 42 can form a turbulent flow effect at the bottom of the fluidized bed tank body 2 to generate an upward impact flow field, so that the filler can not be deposited at the bottom of the tank, and the fluidization effect can be improved; second, the sewage sprayed by the water distribution nozzle 42 washes the screen 15 to prevent the screen 15 from being blocked, and the water distribution nozzle 42 can adopt a venturi throat structure.
On the basis of the scheme, a filler sieve plate 21 is arranged in the fluidized bed tank body 2, a three-dimensional electro-Fenton system 5 is arranged above the filler sieve plate 21, the three-dimensional electro-Fenton system 5 comprises an electrode 51, an anode 52, a cathode 53 and a particle electrode 54, and the split-phase jet doser 3 and the ozone pretreatment tank 1 are positioned on one side, away from the three-dimensional electro-Fenton system 5, of the filler sieve plate 21. Function of the packing screen 21The filler is blocked from entering the area of the three-dimensional electro-Fenton system 5. Anode 52 may be a serpentine mesh anode, which increases the contact area with the solution, thereby increasing the rate of anodic electrolysis; the cathode 53 adopts a hollow columnar cathode, so that the equal distance between the cathode and the anode is ensured, and the electrolysis efficiency is greatly improved; the particle electrode 54 is located in the region between the anode 52 and the cathode 53, and the particle electrode 54 has a greatly increased surface area of the granular electrode and a small particle spacing, compared with conventional plate-like and rod-like electrodes, and can increase mass transfer rate and current efficiency. In order to improve the electrolysis efficiency, scrap iron is filled between the anode 52 and the cathode 53, and a three-dimensional electrode space is formed inside the three-dimensional electro-Fenton system 5, so that the generation quantity and the generation speed of hydroxyl radicals can be increased. The three-dimensional electro-Fenton system 5 further comprises an electrolyte inlet 55, a sodium sulfate liquid inlet tank 57 and an electrolyte liquid inlet pump 56 are connected to the electrolyte inlet 55, and electrolyte Na is contained in the sodium sulfate liquid inlet tank 57 2 SO 4 。
In the three-dimensional electro-Fenton system 5, the electrode 51 is completely submerged by wastewater, the electrode 51 can regulate current and voltage through an external power supply control box, the current is controlled to be 3A-5A, the voltage is 10V-20V, and the corresponding current density is 2mA/cm in the wastewater treatment process 2 ～10mA/cm 2 The electrifying time is 0.5 h-1 h, the anode 52 can be supported by iron, for example, an iron plate or a polar plate containing iron elements can be used for manufacturing the anode 52. The cathode 53 may be a stainless steel mesh filled with carbon, wherein the stainless steel mesh may have various mesh sizes, and the stainless steel mesh may be selected from, but not limited to, 0Cr18Ni9, 0Cr19Ni10, 0Cr25Ni20, 0Cr17Ni12Mo2, etc.
In the working process of the three-dimensional electro-Fenton system 5, the liquid environment in the fluidized bed tank body 2 contains ozone floating from the ozone pretreatment tank 1 and oxygen decomposed by the ozone, and when the ozone and the oxygen travel to the cathode 53 of the three-dimensional electro-Fenton system 5, the reaction occurs at the cathode 53 to induce the generation of H 2 O 2 And hydroxyl free radicals, hydrogen peroxide can further react with ferrous ions in the solution to generate fendon.
Three-dimensional electro-Fenton system 5 and common electricityDifferent chemical devices, the three-dimensional electro-Fenton system 5 in the embodiment of the scheme does not need to add hydrogen peroxide and Fe 2+ Hydrogen peroxide and Fe 2+ The waste water is generated by electrolysis, and the organic waste water which is difficult to degrade after being subjected to ozone oxidation treatment and Fenton fluidization treatment in the area of the split-phase jet current chemical feeder 3 can be further degraded by only powering on and adjusting the proper pH value when the waste water is treated, for example, the pH value can be controlled to be 3-4.
In the above scheme, when the suspended matters block the three-dimensional electro-Fenton system 5, the blocked suspended matters can be flushed by utilizing the water flow and the air flow by adjusting the water flow and the air flow, so that the blocking problem is solved, and the current efficiency of the three-dimensional electro-Fenton system 5 is recovered to be normal.
The three-dimensional electro-Fenton system 5 utilizes the electro-Fenton principle to degrade COD, so that the dosage of the medicament is saved; meanwhile, the three-dimensional electrode consisting of the anode 52, the cathode 53 and the particle electrode 54 is used for consuming residual ozone and iron ions, and meanwhile, the three-dimensional electro-Fenton system 5 can generate electric flotation and electric flocculation. Can further induce to generate hydroxyl free radicals and ferrous ions, the ferrous ions are combined with hydrogen peroxide again to form Fenton reagent to participate in fluidization reaction, iron ions are prevented from flocculating into iron mud to be settled, and the iron mud is cooperatively matched with the ozone oxidation and Fenton fluidized bed, so that the iron mud in the fluidized bed tank body 2 is greatly reduced.
The upper side of the three-dimensional electro-Fenton system 5 is provided with a filter screen 58, a water outlet weir plate 22 is arranged above the filter screen 58, the position of the water outlet weir plate 22 corresponds to that of the reflux weir plate 23, and a water outlet pipe 25 extending to one side of the water outlet weir plate 22 is arranged on the outer side of the fluidized bed tank body 2. The top of the fluidized bed tank body 2 is provided with an exhaust valve 24, and the exhaust valve 24 can exhaust the residual gas in the fluidized bed tank body 2. The bottom of the fluidized bed tank 2 is provided with a drain pipe 27 and a drain valve 26, and impurities deposited at the bottom of the fluidized bed tank 2 can be discharged through the drain pipe 27.
The ozone aeration Fenton fluidized bed utilizes the excellent high molecular organic matter degradation capability of ozone, utilizes an ozone generator 11, a gas-containing pump 12, a nano-homogenizing generator 13 and an aeration disc 14 to drive ozone into an ozone pretreatment tank 1, the ozone degrades unsaturated organic matters and aromatic compounds in sewage, then redundant ozone enters a fluidized bed tank body 2 along with the sewage, a split-phase jet chemical adder 3 conveys Fenton reagent into the fluidized bed tank body 2, hydroxyl free radicals generated by the Fenton reagent attack small molecular organic matters, so that the consumption of ozone and Fenton reagent is effectively reduced, the cost is reduced, the treatment efficiency is improved, a three-dimensional electrode is arranged at the upper part of a three-dimensional electric Fenton system 5, and the residual chemical in the container can further degrade COD by utilizing the electric Fenton principle, thereby saving the chemical addition.
After the redundant ozone oxidation tail gas in the ozone pretreatment tank 1 passes through the Fenton fluidized bed, a large amount of suspended matters can be taken away, meanwhile, residual ozone can be decomposed through the three-dimensional electro-Fenton system 5, the concentration of ozone in the tail gas is less than 1ppm, the tail gas treatment device of ozone is omitted while the deep removal of organic matters is realized, and the comprehensive utilization of ozone and oxygen resources is realized.
While the invention has been described in detail in terms of general description and specific embodiments, it will be apparent to those skilled in the art that modifications and improvements can be made to the embodiments of the invention. Accordingly, such modifications or improvements may be made without departing from the spirit of the invention and are intended to be within the scope of the invention as claimed.
Claims (7)
1. The ozone aeration type electro-Fenton fluidized bed is characterized by comprising a fluidized bed tank body (2), wherein a split-phase jet flow chemical feeder (3) and a three-dimensional electro-Fenton system (5) are arranged in the fluidized bed tank body (2), a water distributor (4) for inputting sewage is arranged in the fluidized bed tank body (2), fenton reagent is conveyed by the split-phase jet flow chemical feeder (3) to enter the fluidized bed tank body (2) to be mixed with the sewage, and an ozone pretreatment tank (1) for generating ozone is arranged at the bottom of the fluidized bed tank body (2); the water distributor (4) is arranged at the bottom of the fluidized bed tank body (2); at least one mixed dosing jet flow arm (33) pointing to the inside of the fluidized bed tank body (2) is arranged on the split-phase jet flow doser (3), and a hydrogen peroxide runner (31) and a ferrous sulfate runner (32) which are communicated with the mixed dosing jet flow arm (33) are arranged on the split-phase jet flow doser (3); the hydrogen peroxide runner (31) is connected with a hydrogen peroxide medicament preparation tank (63) through a pipeline, and the hydrogen peroxide runner (31) and the hydrogen peroxide medicament preparation tank (63) are sequentially provided with a hydrogen peroxide dosing metering pump (62), a hydrogen peroxide dosing control valve (61), a hydrogen peroxide dosing device (6), a hydrogen peroxide dosing return pipe (36) and a hydrogen peroxide return liquid inlet pump (34) according to the fluid flow direction; the ferrous sulfate runner (32) is connected with the ferrous sulfate medicament preparation tank (73) through a pipeline, and a ferrous sulfate dosing metering pump (72), a ferrous sulfate dosing control valve (71), a ferrous sulfate dosing device (7), a ferrous sulfate dosing return pipe (37) and a ferrous sulfate return liquid inlet pump (35) are sequentially arranged between the ferrous sulfate runner (32) and the ferrous sulfate medicament preparation tank (73) according to the fluid flow direction; a backflow weir plate (23) is arranged on the upper side of the interior of the fluidized bed tank body (2), one end, far away from the hydrogen peroxide backflow liquid inlet pump (34), of the hydrogen peroxide dosing backflow pipe (36) stretches into one side of the backflow weir plate (23) in the interior of the fluidized bed tank body (2), and sewage in the backflow weir plate (23) flows back into the hydrogen peroxide backflow liquid inlet pump (34) through the hydrogen peroxide dosing backflow pipe (36); one end of the ferrous sulfate dosing return pipe (37) far away from the ferrous sulfate reflux liquid inlet pump (35) stretches into one side of a reflux weir plate (23) in the fluidized bed tank body (2), and sewage in the reflux weir plate (23) flows back into the ferrous sulfate reflux liquid inlet pump (35) through the ferrous sulfate dosing return pipe (37).
2. An ozone aeration type electro-Fenton fluidized bed as claimed in claim 1, wherein an aeration disc (14) is arranged at the bottom of the ozone pretreatment tank (1), a nano homogenizing generator (13), a Rong Qibeng (12) and an ozone generator (11) are connected to the aeration disc (14), and ozone generated by the ozone generator (11) sequentially passes through the air accommodating pump (12), the nano homogenizing generator (13) and the aeration disc (14) according to the gas flow sequence and finally enters the ozone pretreatment tank (1).
3. An ozone aerated electro-Fenton's fluidized bed according to claim 1, characterized in that a screen (15) for micro-nano size ozone bubbles and sewage to pass through is arranged between the ozone pretreatment tank (1) and the fluidized bed tank body (2).
4. An ozone aerated electro-Fenton fluidised bed according to claim 3, characterised in that the water distributor (4) is provided with water distribution nozzles (42) close to the screen (15).
5. An ozone aerated electro-Fenton fluidised bed as claimed in any of claims 1-4, characterised in that a filler screen (21) is provided in the fluidised bed tank (2), the three-dimensional electro-Fenton system (5) is located above the filler screen (21), the three-dimensional electro-Fenton system (5) comprises an electrode (51), an anode (52), a cathode (53) and a particle electrode (54), and the split-phase jet doser (3) and the ozone pre-treatment tank (1) are located on the side of the filler screen (21) facing away from the three-dimensional electro-Fenton system (5).
6. An ozone aerated electro-Fenton fluidised bed according to claim 5 characterised in that the three-dimensional electro-Fenton system (5) further comprises an electrolyte inlet (55), the electrolyte inlet (55) being connected with a sodium sulphate liquid inlet bath (57) and an electrolyte liquid inlet pump (56).
7. An ozone aeration type electro-Fenton fluidized bed as in claim 5, wherein a filter screen (58) is arranged on the upper side of the three-dimensional electro-Fenton system (5), a water outlet weir plate (22) is arranged above the filter screen (58), and a water outlet pipe (25) extending to one side of the water outlet weir plate (22) is arranged on the outer side of the fluidized bed tank body (2).
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| CN110668620A (en) * | 2019-11-07 | 2020-01-10 | 沈阳工业大学 | Jet fluidized bed type electro-Fenton treatment system |
| CN111470685A (en) * | 2020-05-06 | 2020-07-31 | 中国药科大学 | Method for removing and recovering phosphorus in pharmaceutical wastewater by homogeneous Fenton-iron-phosphorus precipitation enhanced flocculation method |
| CN113371798B (en) * | 2021-06-10 | 2022-09-20 | 华中师范大学 | Method for removing chemical oxygen demand in wastewater through ozone coupled electro-Fenton catalysis |
| CN113735227A (en) * | 2021-09-24 | 2021-12-03 | 西安建筑科技大学 | Aeration type three-dimensional electro-Fenton fluidized bed |
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