CN107162158B - Fenton fluidized bed reactor and method - Google Patents
Fenton fluidized bed reactor and method Download PDFInfo
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- CN107162158B CN107162158B CN201710597174.4A CN201710597174A CN107162158B CN 107162158 B CN107162158 B CN 107162158B CN 201710597174 A CN201710597174 A CN 201710597174A CN 107162158 B CN107162158 B CN 107162158B
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- 238000000034 method Methods 0.000 title claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 128
- 238000009826 distribution Methods 0.000 claims abstract description 78
- 238000006243 chemical reaction Methods 0.000 claims abstract description 70
- 239000003054 catalyst Substances 0.000 claims abstract description 36
- 239000010865 sewage Substances 0.000 claims abstract description 32
- 239000007800 oxidant agent Substances 0.000 claims abstract description 30
- 230000001590 oxidative effect Effects 0.000 claims abstract description 28
- 238000005273 aeration Methods 0.000 claims abstract description 25
- 239000000945 filler Substances 0.000 claims abstract description 25
- 239000013078 crystal Substances 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 37
- 238000007254 oxidation reaction Methods 0.000 claims description 24
- 230000003647 oxidation Effects 0.000 claims description 23
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 150000002500 ions Chemical group 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 230000007797 corrosion Effects 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 230000007547 defect Effects 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 239000012028 Fenton's reagent Substances 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 241000544051 Damasonium alisma Species 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- 229910002588 FeOOH Inorganic materials 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000007210 heterogeneous catalysis Methods 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000009827 uniform distribution 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses a fluidized bed Fenton reactor and a method, which solve the problems of crystal loss and uneven water distribution in the prior art, and have the beneficial effects of reducing the operation cost and improving the removal rate of refractory organic matters in sewage, and the scheme is as follows: the fluidized bed Fenton reactor comprises a reaction tank body, wherein a catalyst inlet for raw water and a catalyst to enter and an oxidant inlet for raw water and an oxidant to enter are formed in the bottom of the reaction tank body, the catalyst inlet is connected with a first water distribution head, the oxidant inlet is connected with a second water distribution head, a microporous aeration head is arranged on the side part of the first water distribution head in the reaction tank body, a main reaction zone is arranged above the microporous aeration head in the reaction tank body, a filler is arranged in the main reaction zone, and a three-phase separator is arranged above the main reaction zone.
Description
Technical Field
The invention relates to the field of environmental protection equipment, in particular to a fluidized bed Fenton reactor and a method.
Background
In sewage treatment, particularly in some industrial sewage treatment, some water quality which is difficult to biochemically degrade is often encountered, and the current common methods for treating the water quality are as follows:
1. advanced oxidation methods, including ozone oxidation, fenton reagent oxidation, hydrogen peroxide oxidation and the like, are used for directly oxidizing and degrading refractory organic matters in the wastewater;
2. micro-electrolysis methods, such as iron-carbon micro-electrolysis, utilize electrons generated by micro-electrolysis to open some groups of organic matters and decompose the groups into small molecular substances, thereby being beneficial to subsequent biochemical treatment;
3. the distillation method distills the mother solution containing salt with high concentration, reduces inorganic salt with inhibiting effect on biochemical bacteria in the wastewater, and is convenient for subsequent biochemical treatment.
The advanced oxidation method is mostly adopted at present by combining the factors of the operation cost and the investment cost, and particularly the Fenton reagent oxidation method is most adopted.
At present, the Fenton reagent oxidation method mainly comprises two types, namely a traditional Fenton oxidation method and a fluidized bed Fenton oxidation method represented by Taiwan water star, wherein the Fenton fluidized bed can enable most of ferric iron generated by the Fenton method to be coated on the surface of a filler (a carrier) of a fluidized bed in a crystallization or precipitation way, and FeOOH formed on the surface of the carrier has heterogeneous catalysis effect, and the chemical oxidation reaction and mass transfer efficiency are promoted by the fluidized bed mode, so that the COD removal rate is improved.
Compared with the traditional oxidation method, the fluidized bed Fenton oxidation method has the greatest advantages of medicament saving and low sludge yield, and is also increasingly applied.
However, the fluidized bed Fenton oxidation method has the following defects:
firstly, in order to keep crystals in sewage in a fluidized state, the wastewater needs to keep a relatively high flow rate, and in order to ensure certain reaction time, a method for increasing the reflux quantity of the wastewater is generally adopted at present to increase the flow rate, so that the energy consumption is increased;
secondly, due to inconsistent size and density of crystals in water, some crystals can run off along with water outlet, the water quality of the water outlet is affected, and the difficulty and cost of subsequent treatment are increased;
thirdly, the most uniform water distribution mode at present is a multi-point water distribution mode, but because the lengths of pipelines reaching each point are different, the used elbow, the variable diameter number and the size are also different, the uniform water distribution quantity of each water distribution point is difficult to ensure, and the flow velocity in the tank is uneven and the fluidization effect is poor;
fourth, the mixing of oxidant and catalyst in Fenton reactor is in front of the main reaction zone at present, the hydroxyl radical produced too early produces the oxidation corrosion to pipeline, pipe fittings and apparatus, has reduced the efficiency of removing the difficult organic matter of degradation in the water.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a fluidized bed Fenton reactor, which has the advantages of less crystal loss, uniform water distribution and capability of avoiding oxidation corrosion to pipelines, pipes and equipment.
The fluidized bed Fenton reactor has the following specific scheme:
a fluidized bed Fenton reactor comprising:
the reaction tank body, the reaction tank body bottom is equipped with the catalyst entry that is used for raw water and catalyst to get into and is used for raw water and the oxidant entry that the oxidant got into, the catalyst entry is connected with first water distribution head, the oxidant entry is connected with the second water distribution head, first water distribution head lateral part is equipped with the micropore aeration head in the reaction tank body, be equipped with main reaction zone in the reaction tank body above the micropore aeration head, be equipped with the filler in the main reaction zone, be equipped with the three-phase separator above the main reaction zone, the setting of three separator can prevent crystalline solid loss to discharge the gas in the jar through the blast pipe.
The gas in the reactor is used for improving the water flow speed in the reaction tank body, and fully stirring and mixing the mixed solution of the catalyst, the oxidant and raw water (sewage), so that the catalyst and the oxidant are uniformly mixed, hydroxyl free radicals are generated, in addition, the gas is air, and partial COD in the sewage can be oxidized by oxygen in the air. The flow rate in the tank body is lifted by using air, so that the energy can be saved greatly compared with the increase of the sewage reflux ratio.
The bottom of the main reaction zone is provided with a supporting plate, and the first water distribution head and the second water distribution head are arranged on the supporting plate.
The first water distribution heads and the second water distribution heads are respectively provided with a plurality of water distribution heads, the first water distribution heads and the second water distribution heads are uniformly and alternately arranged, the staggered arrangement is favorable for further uniform distribution of sewage, the first water distribution heads and the second water distribution heads keep a certain pressure of about 0.15-0.2 MPa, the pressure at the water inlet end of each water distribution head can be ensured to be the same, the water yield of each water distribution head is consistent, the water distribution is uniform, the first water distribution heads are long-handle water distribution heads, and the second water distribution heads are short-handle water distribution heads.
The microporous aeration head is arranged on the supporting plate, two cavities are arranged below the supporting plate of the reaction tank body, a catalyst inlet is arranged on the side part of the cavity at the lowest part, and the oxidant inlet is arranged in the cavity at the upper part.
The microporous aeration head is connected with an air inlet pipe, an air inlet of the air inlet pipe is arranged at the upper part of the supporting plate in the main reaction zone, the air inlet is used for introducing air, and the air is provided by external equipment such as an air compressor.
And an overflow weir is arranged at the upper part of the three-phase separator in the reaction tank body, and the overflow weir is arranged to facilitate drainage.
The overflow weir is provided with a water outlet.
The three-phase separator is communicated with an exhaust pipe penetrating through the reaction tank body and used for exhausting gas, and is provided with a gas collecting cover which is used for collecting the gas.
The microporous aeration heads are provided with a plurality of microporous aeration heads which are uniformly arranged, and the microporous aeration heads can also be microporous aeration pipes, perforated pipes and the like.
In order to overcome the defects in the prior art, the invention also provides a sewage treatment method, which adopts a fluidized bed Fenton reactor and comprises the following steps:
1) The raw water with the pH value regulated is mixed with the catalyst uniformly, and the other part of the raw water is mixed with the oxidant uniformly, and enters the reaction tank body through the catalyst inlet and the oxidant inlet respectively, and then enters the main reaction zone of the tank body through the first water distribution head and the second water distribution head respectively;
2) The gas enters the reaction tank body through the microporous aeration head, and the two liquids are fully mixed under the stirring of the gas to react to generate hydroxyl free radicals, and the hydroxyl free radicals decompose or oxidize refractory substances in the sewage; meanwhile, the filler in the tank body is fluidized in the upward flowing process of water and gas, sewage is fully contacted with the filler, and catalyst ions form crystals on the surface of the filler;
3) When sewage, filler and gas flow to the three separators at the upper part of the reaction tank body, the filler is blocked and then falls back to the main reaction zone; the gas is collected through a three-phase separator and then discharged through an exhaust pipe; the water enters the water outlet through the overflow weir to be discharged after passing through the three separators, thus finishing the Fenton oxidation process of the sewage.
Compared with the prior art, the invention has the beneficial effects that:
1) The invention solves the problems of high energy consumption, crystal loss, uneven water distribution, oxidation corrosion of hydroxyl radicals generated prematurely on pipelines, pipes and equipment and the like in the existing fluidized bed Fenton oxidation method for treating sewage, reduces the operation cost and improves the removal rate of refractory organic matters in the sewage.
2) According to the invention, raw water, an oxidant and raw water are respectively mixed with a catalyst, and oxidation corrosion of pipe fittings and equipment caused by hydroxyl radicals generated in advance before a main reaction zone is avoided.
3) According to the invention, through the arrangement of a plurality of water distribution heads, the uniformity of water distribution is ensured, and the loss of crystals is avoided through the arrangement of the three-phase separator.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiments of the application and together with the description serve to explain the application and do not constitute an undue limitation to the application.
Fig. 1 is a schematic diagram of the general structure of the invention.
Fig. 2 is a cross-sectional view of fig. 1.
Wherein: 1. the reaction tank body 2, the three-phase separator 3, the main reaction zone 4, the micropore aeration head 5, the long handle water distribution head 6, the short handle water distribution head 7, the air inlet 8, the catalyst inlet 9, the oxidant inlet 10, the filling material 11, the water outlet 12, the overflow weir 13 and the exhaust pipe.
Detailed Description
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the present application. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the present application. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
As described in the background art, the present application provides a fluidized bed Fenton reactor and a method for solving the above technical problems.
In a typical embodiment of the present application, as shown in fig. 1, a fluidized bed Fenton reactor includes a reaction tank 1, a catalyst inlet 8 for raw water and catalyst to enter and an oxidant inlet 9 for raw water and oxidant to enter are provided at the bottom of the reaction tank 1, the catalyst inlet 8 is connected with a first water distribution head, the oxidant inlet 9 is connected with a second water distribution head, a microporous aeration head 4 is provided at the side of the first water distribution head in the reaction tank 1, a main reaction zone 3 is provided above the microporous aeration head 4 in the reaction tank 1, a packing 10 is provided in the main reaction zone 3, a three-phase separator 2 is provided above the main reaction zone 3, and the three-phase separator 2 is provided to prevent crystal loss and discharge gas in the reaction tank 1 through an exhaust pipe 13.
The gas distribution points of the gas distribution system are uniformly arranged in the reaction tank body 1, and the gas distribution points can be microporous aeration heads 4, microporous aeration pipes, perforated pipes and the like, and are preferably microporous aeration heads. The gas distribution system is used for improving the speed of water flow in the tank body, fully stirring and mixing the mixed solution of the catalyst, the oxidant and the raw water, so that the catalyst and the oxidant are uniformly mixed in the main reaction zone 3, hydroxyl free radicals are generated, in addition, the gas is air, oxygen in the air can oxidize part of COD in sewage, the flow rate in the reaction tank body 1 is improved by using the gas, the sewage reflux ratio is increased, and energy sources (generally electricity) can be saved greatly.
The first water distribution head is a long-handle water distribution head, the second water distribution head is a short-handle water distribution head, and the long-handle water distribution heads and the short-handle water distribution heads are distributed in a staggered manner. The two cavities of the structure respectively contain water inflow after raw water, catalyst and oxidant are mixed, and keep a certain pressure of about 0.15-0.2 MPa, so that the pressure at the water inlet end of each water distribution head is ensured to be the same, the water yield of each water distribution head is consistent, and water distribution is very uniform.
The upper part of the reaction tank body 1 is provided with a set of gas, liquid and solid separators which can prevent crystal loss and discharge the gas in the tank through an exhaust pipe.
The filler in the reaction tank 1 is quartz sand with the particle size of 0.5-1.0 mm.
When the reactor runs, raw water with a regulated PH value is mixed with a catalyst and an oxidant outside a Fenton reactor and then enters two cavities at the lower part of a reaction tank body 1 respectively, the catalyst enters a lower cavity, the oxidant enters an upper cavity, and then enters a main reaction zone 3 of the reaction tank body 1 respectively through long and short handle water distribution heads which are uniformly and alternately distributed, and the two liquids are fully mixed under the stirring of gas to react to generate hydroxyl free radicals, so that the hydroxyl free radicals decompose or oxidize refractory substances in sewage; meanwhile, the filler in the reaction tank body 1 is fluidized in the upward flowing process of water and gas, sewage is fully contacted with the filler, catalyst ions form crystals on the surface of the filler, the catalyst is prevented from running away along with the water flow, the investment of the catalyst is saved, the running cost is reduced, and the generation of sludge is reduced.
When sewage, filler and gas (including gas generated by the reaction of air) flow to the three separators 2 at the upper part of the reaction tank body 1, the filler is blocked and then falls back to the main reaction zone 3; the gases are collected together through a gas collecting hood of the three-phase separator 2 and then discharged through an exhaust pipe 13; the water enters the water outlet 11 through the overflow weir 12 to be discharged after passing through the three separators 2, and the Fenton oxidation process is completed.
The invention solves the problems of high energy consumption, crystal loss, uneven water distribution, oxidation corrosion of hydroxyl radicals generated prematurely on pipelines, pipes and equipment and the like in the existing fluidized bed Fenton oxidation method for treating sewage, reduces the operation cost and improves the removal rate of refractory organic matters in the sewage.
In order to overcome the defects in the prior art, the invention also provides a sewage treatment method, which adopts a fluidized bed Fenton reactor and comprises the following steps:
1) The raw water with the pH value regulated is mixed with the catalyst uniformly, and the other part of the raw water is mixed with the oxidant uniformly, and enters the reaction tank body through the catalyst inlet and the oxidant inlet respectively, and then enters the main reaction zone of the tank body through the first water distribution head and the second water distribution head respectively;
2) The gas enters the reaction tank body through the microporous aeration head, and the two liquids are fully mixed under the stirring of the gas to react to generate hydroxyl free radicals, and the hydroxyl free radicals decompose or oxidize refractory substances in the sewage; meanwhile, the filler in the tank body is fluidized in the upward flowing process of water and gas, sewage is fully contacted with the filler, and catalyst ions form crystals on the surface of the filler;
3) When sewage, filler and gas flow to the three separators at the upper part of the reaction tank body, the filler is blocked and then falls back to the main reaction zone; the gas is collected through a three-phase separator and then discharged through an exhaust pipe; the water enters the water outlet through the overflow weir to be discharged after passing through the three separators, thus finishing the Fenton oxidation process of the sewage.
The foregoing description is only of the preferred embodiments of the present application and is not intended to limit the same, but rather, various modifications and variations may be made by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application should be included in the protection scope of the present application.
Claims (6)
1. A fluidized bed Fenton reactor, comprising:
the reaction tank body, there are catalyst inlets used for raw water and catalyst entering and oxidizing agent inlet used for raw water and oxidizing agent entering at the bottom of reaction tank body, the catalyst inlet is connected with first water distribution head, the oxidizing agent inlet is connected with second water distribution head, there are micropore aeration heads at the first water distribution head lateral part in reaction tank body, there are main reaction areas above micropore aeration heads in reaction tank body, there are fillers in the main reaction area, there are three-phase separators above the main reaction area, in order to prevent crystal loss, and discharge the gas in the tank through the blast pipe; the bottom of the main reaction zone is provided with a supporting plate, and the first water distribution head and the second water distribution head are arranged on the supporting plate;
the first water distribution heads and the second water distribution heads are respectively provided with a plurality of water distribution heads, and the first water distribution heads and the second water distribution heads are uniformly staggered;
the first water distribution head is a long-handle water distribution head, the second water distribution head is a short-handle water distribution head, and the long-handle water distribution heads and the short-handle water distribution heads are distributed in a staggered manner; the two cavities of the first water distribution head and the second water distribution head respectively contain water inflow after raw water, catalyst and oxidant are mixed, and the pressure of 0.15-0.2 MPa is kept, so that the pressure of the water inlet end of each water distribution head is ensured to be the same, the water yield of each water distribution head is consistent, and the water distribution is very uniform;
the microporous aeration head is arranged on the supporting plate; the microporous aeration heads are provided with a plurality of microporous aeration heads which are uniformly arranged.
2. A fluidized bed Fenton reactor according to claim 1, wherein the microporous aeration head is connected with an air inlet pipe, and an air inlet of the air inlet pipe is arranged at the upper part of the supporting plate in the main reaction zone.
3. A fluidized bed Fenton reactor according to claim 1, wherein an overflow weir is provided at the upper part of the three-phase separator in the reaction tank.
4. A fluidized bed Fenton reactor according to claim 3, wherein said weir is provided with a water outlet.
5. A fluidized bed Fenton reactor according to claim 1, wherein said three-phase separator is in communication with an exhaust pipe passing through the reaction tank.
6. A method of sewage treatment, characterized by using a fluidized bed Fenton reactor according to any one of claims 1-5, comprising the steps of:
1) The raw water with the pH value regulated is mixed with the catalyst uniformly, and the other part of the raw water is mixed with the oxidant uniformly, and enters the reaction tank body through the catalyst inlet and the oxidant inlet respectively, and then enters the main reaction zone of the tank body through the first water distribution head and the second water distribution head respectively;
2) The gas enters the reaction tank body through the microporous aeration head, and the two liquids are fully mixed under the stirring of the gas to react to generate hydroxyl free radicals, and the hydroxyl free radicals decompose or oxidize refractory substances in the sewage; meanwhile, the filler in the tank body is fluidized in the upward flowing process of water and gas, sewage is fully contacted with the filler, and catalyst ions form crystals on the surface of the filler;
3) When sewage, filler and gas flow to the three separators at the upper part of the reaction tank body, the filler is blocked and then falls back to the main reaction zone; the gas is collected through a three-phase separator and then discharged through an exhaust pipe; the water enters the water outlet through the overflow weir to be discharged after passing through the three separators, thus finishing the Fenton oxidation process of the sewage.
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| CN201710597174.4A CN107162158B (en) | 2017-07-20 | 2017-07-20 | Fenton fluidized bed reactor and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108298635A (en) * | 2018-04-10 | 2018-07-20 | 浙江工业大学温州科学技术研究院 | A kind of reaction unit and its working method for recyclable magnetic photocatalyst |
| CN109179823A (en) * | 2018-11-09 | 2019-01-11 | 辽阳博仕流体设备有限公司 | A kind of photocatalysis Fenton fluidized bed |
| CN111498967B (en) * | 2020-04-30 | 2021-05-07 | 河南力诚环保科技有限公司 | Crystallization fluidized bed |
| CN114314890A (en) * | 2020-10-09 | 2022-04-12 | 南京工大开元环保科技（滁州）有限公司 | Organic phosphorus removing device |
| CN113371815A (en) * | 2021-07-20 | 2021-09-10 | 南京环保产业创新中心有限公司 | iron-series-Fenton degradation-resistant wastewater treatment reactor and method thereof |
| CN113634201B (en) * | 2021-08-26 | 2023-03-14 | 天津大学 | Upflow fluidized bed reaction device and method for treating antibiotic wastewater |
| CN114314740A (en) * | 2021-12-30 | 2022-04-12 | 福州大学 | Acousto-optic catalytic reaction device based on three-phase separation and water treatment process |
| CN114538596B (en) * | 2022-03-22 | 2023-04-28 | 中建环能科技股份有限公司 | Heterogeneous Fenton wastewater treatment device |
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| CN104787869A (en) * | 2015-04-10 | 2015-07-22 | 锐博环保科技(北京)有限公司 | Treatment method and device for catalyzing and oxidizing degradation-resistant organic wastewater with heterogeneous ozone |
| CN204714580U (en) * | 2015-05-08 | 2015-10-21 | 长沙威保特环保科技股份有限公司 | Upflowing Fenton fluidized-bed |
| CN205999108U (en) * | 2016-08-31 | 2017-03-08 | 湖南省科建市政工程有限公司 | A kind of oxidizing tower for advanced treatment of wastewater |
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