CN206512041U - A kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water - Google Patents
A kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water Download PDFInfo
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- CN206512041U CN206512041U CN201720192093.1U CN201720192093U CN206512041U CN 206512041 U CN206512041 U CN 206512041U CN 201720192093 U CN201720192093 U CN 201720192093U CN 206512041 U CN206512041 U CN 206512041U
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 104
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 58
- 238000006385 ozonation reaction Methods 0.000 claims abstract description 29
- 230000001590 oxidative effect Effects 0.000 claims abstract description 19
- 239000007800 oxidant agent Substances 0.000 claims abstract description 18
- 238000005276 aerator Methods 0.000 claims abstract description 15
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 10
- 239000003054 catalyst Substances 0.000 claims description 78
- 239000002245 particle Substances 0.000 claims description 10
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 abstract description 25
- 230000003647 oxidation Effects 0.000 abstract description 24
- 239000010865 sewage Substances 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 description 43
- 230000000694 effects Effects 0.000 description 17
- 238000000034 method Methods 0.000 description 16
- 239000007789 gas Substances 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- 229910044991 metal oxide Inorganic materials 0.000 description 7
- 150000004706 metal oxides Chemical class 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000009826 distribution Methods 0.000 description 5
- 238000010992 reflux Methods 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 210000005056 cell body Anatomy 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 150000003254 radicals Chemical group 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 2
- 239000010931 gold Substances 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 229910052748 manganese Inorganic materials 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010919 dye waste Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- -1 hydroxyl radical free radical Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052500 inorganic mineral Chemical class 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011707 mineral Chemical class 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model discloses a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water, belong to sewage advanced treatment field.Device of the present utility model includes first-stage reactor and second reactor, wherein, first-stage reactor, which is provided with water inlet, the reactor, is provided with aerator, and the delivery port of first-stage reactor is connected by outlet pipe with the water inlet of second reactor；Provided with least two layers catalytic ozonation oxidant layer in second reactor, the top of second reactor is provided with delivery port, circulating outlet is additionally provided with below the delivery port, the circulating outlet is connected by circulating line and water pump with the circulation water inlet of second reactor bottom.The utilization rate and the catalysis oxidation efficiency for improving ozone are handled biochemical tail water progress using device of the present utility model, makes catalytic oxidation more efficient, complete.
Description
Technical field
The utility model belongs to water-treatment technology field, is related to a kind of two-stage gradient ozone catalytic fluidized bed deep treatment life
Change the device of tail water, this method is applied to processing micro-polluted water, the depth of waste water, the particularly waste water containing refractory organic
Spend process field.
Background technology
With developing rapidly for industrial technology, the discharge capacity of industrial wastewater is on the increase, and its composition also becomes more and more multiple
It is miscellaneous and also increasingly extensively and serious to the pollution of water body.Using simple bioanalysis to concentration height, the industrial wastewater of biodegradability difference
Direct progress processing is extremely difficult to reuse or discharge standard, it is necessary to used water difficult to degradate is pre-processed using physical chemistry means
Or advanced treating, to improve wastewater biodegradability or finally be degraded.High-level oxidation technology can be produced with Strong oxdiative
High stability, persistent organic pollutants carry out serial radical chain reaction in the free radical of ability, water, so as to destroy its knot
Structure, the organic matter for making it be gradually degraded as harmless low molecule amount, is finally degraded to CO2、H2O and other mineral salts.Therefore, mesh
Preceding high-level oxidation technology turns into the important means for administering bio-refractory toxic organic pollutantses.
Wherein, ozonation technology is a kind of efficient advanced oxidation water technology, due to the redox electricity of ozone
Position is higher, can be with the majority of organic pollutants in oxidation Decomposition water body, so as to reach the mesh of purification of water quality to a certain extent
's.Ozonation technology has a wide range of applications in fields such as decoloring dye waste water, sterilizing and drink water purifyings.So
And, ozonation technology still suffers from a series of problems in application process, and such as ozone utilization rate is low, mineralization ability is low, organic matter
Decompose not thorough etc..In recent years, catalytic ozonation has been developed again, catalytic ozonation technology is the work using catalyst
With the generation of strong oxidizing property free radical (predominantly hydroxyl radical free radical) in promotion course of reaction, so as to improve the utilization of ozone
Efficiency, adds the oxidation Decomposition and mineralising efficiency of organic pollution, and then at normal temperatures and pressures can be difficult to those ozone
The oxidation operation of oxidation or degraded even mineralising.
But when being handled using the ozone catalytic reaction tank in existing engineering waste water, ozone is difficult to fully with catalyst
The micropore ozone bubbles that itself is produced in hybrid reaction, and its catalytic oxidation process easily become big in catalyst surface aggregation again,
So as to cause the utilization rate of ozone and catalyst still relatively low, it is difficult to water treatment effect is effectively ensured.It is to waste water simultaneously
Handling process it is relative complex, processing cost is higher, it is difficult to real to realize engineering application.Therefore, how further to improve and urge
Change the utilization rate of ozone and catalyst in ozonation technique, it is ensured that its water treatment effect has obtained the wide model concern of researcher.
Through retrieval, the patent report on improving ozone utilization rate in catalytic ozonation technology is existing related open.Such as, in
State's number of patent application for 201110356245.4 application case disclose a kind of catalysis ozone processing pulp-making waste-water device and its
Processing method, (corresponding structure is respectively with the first He including the reactor of structure identical first and second for the device of this application case
Second makes a distinction), storage cistern and exhaust collection bottle；Active adsorbing material load transitions are carried on cell body inner support air distribution plate
Metal oxide catalyst, cell body bottom, which is provided with aerator, cell body, to be provided with intake-outlet, enters ozone mouthful and sample tap,
Tail gas mouthful is provided with top cover.First enters ozone mouthful is connected with the first aerator by pipeline, and the first delivery port enters with storage cistern
The mouth of a river, storage cistern delivery port are connected with pump and the second water inlet by pipeline；First tail gas mouthful, second enter ozone mouthful, second
Aerator passes sequentially through pipeline connection；Blast pipe is provided with exhaust collection bottle, tail gas bottle is connected with the second tail gas mouthful.
And for example, Chinese Patent Application No. discloses a kind of organic wastewater with difficult degradation thereby multistage for 2016108912090 patent
Catalytic ozonation processing unit, the device includes multistage catalytic ozonation system, every grade of catalytic ozonation system by
Ozone gas distribution system and the obligate solid catalyst system above ozone gas distribution system are constituted；Wherein every grade ozone gas distribution system
System is connected by pipeline with ozone generator, and ozone dosage successively decreases multistage ozone gas distribution system step by step from bottom to top；Device
Top is provided with ozone tail gas outlet, and ozone tail gas outlet is connected by pipeline with ozone breaker, and multistage obligate solid is urged
Agent system loads a variety of different obligate solid catalysts respectively, and respectively by catalyst support member support.Above-mentioned two application
Case to industrial wastewater by carrying out multistage catalytic ozone Oxidation Treatment, so as to improve the resolution ratio of hardly degraded organic substance,
Ozone microbubble in the treatment effect of waste water, but its processing procedure is improved to a certain extent to be still inevitably catalyzed
Agent surface aggregation becomes big, and the utilization rate of catalyst and ozone is relatively low, thus cause the improvement of water treatment effect by compared with
Big limitation.
Utility model content
1. the utility model technical problem to be solved
The purpose of this utility model is to overcome when being handled using existing ozone catalytic reaction tank waste water, catalyst
Utilization rate with ozone is relatively low, its treatment effect to waste water need further to be improved not enough there is provided a kind of two-stage
The device of gradient ozone catalytic fluidized bed deep treatment biochemical tail water.It can be effectively improved using the technical solution of the utility model
The utilization rate of ozone and catalyst, so as to ensure water treatment effect.
2. technical scheme
To reach above-mentioned purpose, the technical scheme that the utility model is provided is：
A kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model, including one-level
Reactor and second reactor, wherein, the first-stage reactor, which is provided with water inlet, the reactor, is provided with aerator, and
The delivery port of first-stage reactor is connected by outlet pipe with the water inlet of second reactor；Provided with least in the second reactor
Two layers of catalytic ozonation oxidant layer, the top of second reactor, which is provided with below delivery port, the delivery port, is additionally provided with cyclic water outlet
Mouthful, the circulating outlet is connected by circulating line and water pump with the circulation water inlet of second reactor bottom.
Further, provided with two layers of catalytic ozonation oxidant layer in the second reactor, wherein, the first catalyst layer
Positioned at the top of the second catalyst layer and its filling height be second reactor height 5%~10%, the second catalyst layer
Filling height is the 5%~20% of second reactor height.
Further, the particle diameter of the catalytic ozonation agent is 3~8mm, and density is 0.8~1.6g/cm3。
Further, the top and bottom of every layer of catalytic ozonation oxidant layer are equipped with supporting layer, and supporting layer
It is even to be provided with filter opening.
Further, described aerator is connected with ozone generation system.
Further, offgas outlet, and offgas outlet are equipped with the top of the first-stage reactor and second reactor
It is provided with ozone tail gas decomposer.
3. beneficial effect
The technical scheme provided using the utility model, compared with prior art, with following remarkable result：
(1) device of a kind of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model, including
First-stage reactor and second reactor, carry out preliminary ozone Oxidation Treatment, and make to give up by first-stage reactor to pending waste water
Water is well mixed with ozone, and carrying out multistage catalytic ozonation subsequently into second reactor is handled, so as to significantly improve
The degradation rate of hardly degraded organic substance in waste water, is conducive to improving water treatment effect.Meanwhile, pass through circulation pipe in the utility model
The setting on road is fluidized the catalyst in second reactor, so as to effectively prevent ozone microbubble in catalyst surface
Assemble, significantly improve the utilization rate of ozone and catalyst, the hardly degraded organic substance in pending waste water is obtained fully
Degraded；In addition, circulation catalytic oxidation treatment can also be carried out to waste water, by the setting of circulation line so as to further increase
The treatment effect of waste water.
(2) a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model, described
Provided with two layers of catalytic ozonation oxidant layer in second reactor, wherein, the first catalyst layer is located at the top of the second catalyst layer
And its filling height is the 5%~10% of second reactor height, the filling of the second catalyst layer is highly high for second reactor
The 5%~20% of degree, optimizes design, so as to which difficult degradation thing is effectively ensured by the packed height to two layers of catalyst
The abundant degraded of matter, and due to the raising of ozone and catalyst utilization, only set two layers of catalyst to be that can reach processing requirement,
So as to reduce requirement and the equipment cost of equipment.
(3) a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model, every layer
The top and bottom of catalytic ozonation oxidant layer, which are equipped with supporting layer, and supporting layer, is uniformly provided with filter opening, passes through supporting layer
Setting can effectively prevent the loss of catalyst, and increase recirculated water further increases ozone to the impact of catalyst
With the utilization rate of catalyst.
(4) a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model, described
Offgas outlet is equipped with the top of first-stage reactor and second reactor, and offgas outlet is provided with ozone tail gas decomposer,
So as to effectively prevent residual ozone to be exhausted directly in air pollute environment.
Brief description of the drawings
Fig. 1 is a kind of knot of the device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model
Structure schematic diagram.
In figure：1st, first-stage reactor；101st, water inlet；102nd, the first offgas outlet；2nd, aerator；3rd, outlet pipe；4、
Valve；5th, second reactor；501st, delivery port；502nd, the second offgas outlet；601st, the first catalyst layer；602nd, the second catalyst
Layer；7th, supporting layer；8th, circulating line；9th, water pump.
Embodiment
As shown in figure 1, a kind of dress of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model
Put, including first-stage reactor 1 and second reactor 5, wherein, the first-stage reactor 1 is provided with water inlet 101, the reactor
Interior to be provided with aerator 2, aerator 2 is connected with ozone generation system.The delivery port of above-mentioned first-stage reactor 1 passes through outlet pipe
3 are connected with the water inlet of second reactor 5, and valve 4 is provided with outlet pipe 3.At least two are provided with the second reactor 5
Layer catalytic ozonation oxidant layer, the particle diameter of catalytic ozonation agent is 3~8mm, and density is 0.8~1.6g/cm3, and every layer smelly
The top and bottom of oxygen catalysis oxidation oxidant layer are equipped with supporting layer 7, and supporting layer 7 and are uniformly provided with filter opening, will by supporting layer 7
Second reactor 5 is divided into reaction of high order region, and ozone concentration changes with differential responses series in gradient, order of reaction
Number is bigger, and ozone concentration is smaller.Due to catalyst layer in the utility model number be two layers when can meet the processing of waste water
It is required that, therefore illustrated herein and in specific embodiment with two layers.Wherein, the first catalyst layer 601 is located at the second catalysis
The top of oxidant layer 602 and its filling height is the 5%~10% of the height of second reactor 5, the filling of the second catalyst layer 602 is high
Spend for the 5%~20% of the height of second reactor 5, the catalyst in above-mentioned catalytic ozonation oxidant layer is ordinary ceramsite or gold
Belong to oxide type catalyst (manganese dioxide or aluminum oxide), and every layer of catalyst is loaded with different metal (manganese, iron, copper and mickel
In at least two), form many metal component ozone catalysts.The top of second reactor 5 is provided with delivery port 501, the water outlet
The lower section of mouth 501 is additionally provided with circulating outlet, and the circulating outlet passes through circulating line 8 and water pump 9 and the bottom of second reactor 5
The circulation water inlet in portion is connected, and so as to which catalyst is fluidized, significantly improves the utilization rate of ozone, has been effectively ensured useless
Water treatment efficiency.The top of first-stage reactor 1 and second reactor 5 is equipped with offgas outlet in the utility model, and tail gas goes out
Mouth is provided with ozone tail gas decomposer, so as to carry out resolution process to residual ozone, prevents from being exhausted directly to dirty in air
Contaminate environment.With reference to accompanying drawing, the top of first-stage reactor 1 is provided with the first offgas outlet 102, and the top of first-stage reactor 5 is provided with the
Two offgas outlets 502.
Start the device of ozone catalytic fluidized bed deep treatment biochemical tail water of the present utility model to biochemical tail water at
Manage, its detailed process is：Pending waste water enters first-stage reactor 1, ozone generation system production through water pump of intaking by water inlet 101
The raw ozone for being mixed with oxygen is aerated through aerator 2, and the mass ratio of the aeration quantity of ozone and COD in pending waste water is
1：(0.2~1).One side waste water and ozone are sufficiently mixed in first-stage reactor 1, on the other hand carry out preliminary ozone to waste water
Oxidation processes.Then valve 4 is opened, makes waste water and ozone through entering second reactor 5 together with outlet pipe 3, flows through different ozone
Sufficiently catalytic oxidation Decomposition is carried out to waste water during catalysis oxidation oxidant layer.The utility model by waste water carry out multistep treatment, from
And the degradation rate of hardly degraded organic substance in waste water can be significantly improved, be conducive to improving water treatment effect.
Then flow to delivery port 501 on the waste water after fully oxidized decomposition and discharge reactor, wherein there is effluent part
Extracted out through water pump 9 and the circulation water inlet by circulating line 8 and the bottom of second reactor 5 reenters second reactor 5, so that
Fluidization treatment can be carried out to the catalyst in second reactor 5, and then can effectively prevent ozone microbubble in catalyst table
Face is assembled, and the utilization rate of ozone and catalyst is significantly improved, and it is relatively low to overcome ozone utilization rate in the prior art,
Water treatment effect is difficult to meet desired deficiency, i.e., catalyst can be effectively ensured and smelly using method of the present utility model
The utilization rate of ozone and catalyst is significantly improved while oxygen is sufficiently mixed, the treatment effect of waste water is significantly improved.Together
When, cyclic oxidation processing can also be carried out to waste water by the backflow of recirculated water, its treatment effect is further increased.Due to this
The top and bottom of every layer of catalytic ozonation oxidant layer are equipped with supporting layer 7 in utility model, so as on the one hand can effectively prevent
The only loss of catalyst, on the other hand can increase impact of the recirculated water to catalyst, further increase ozone with urging
The utilization rate of agent.
The circulation water inlet flow velocity of above-mentioned second reactor 5 is adjustable, and fluidisation can not be formed to prevent the too small catalyst layer of fluid stopping speed
State, and catalyst can then be lost in the excessive catalyst layer of flow velocity.By adjusting circulation water inlet flow velocity so that catalyst fluidization
Expansion rate is 5%~100%, and it is 20%~100% to control the reflux ratio of recirculated water, and is taken for the waste water of various concentrations
Different expansion rates and reflux ratio, so as to make catalyst be in optimal fluidized state, and makes waste strength and power consumption
Reach balance, it is to avoid the too high power loss brought of expansion rate.Pending waste water is anti-in two reactors in the utility model
Add up to 0.5~2 hour between seasonable, wherein its reaction time in second reactor 5 is 0.3~1 hour, so as to enter
One step ensures the abundant degraded of hardly degraded organic substance in waste water.
In addition, the utility model also passes through the packed height to catalyst layer, the compounding of different catalysts species and anti-
Parameter optimizes design between seasonable etc., so as to be effectively ensured the abundant degraded of hard-degraded substance, and due to ozone with urge
The raising of agent utilization rate, only sets two layers of catalyst to be that can reach processing requirement, so that reduce equipment wants summation device
Cost.Meanwhile, the catalyst in the utility model is not discharged with waste water, can be recycled, easy to use, is reduced secondary
Pollution, improves ozone utilization ratio, so as to reduce operating cost.
To further appreciate that content of the present utility model, detailed is made to the utility model in conjunction with the drawings and specific embodiments
Description.
Embodiment 1
As shown in figure 1, a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water of the present embodiment,
Including first-stage reactor 1 (ozone oxidation area) and second reactor 5 (catalytic ozonation area), first-stage reactor 1 be provided with into
Aerator 2 is provided with the mouth of a river 101, the reactor, aerator 2 is connected with ozone generation system, and the ozone of the present embodiment is
What the ozone generation system for making the partial oxidation in air or pure oxygen be converted into ozone by voltolising method was produced.Above-mentioned one-level
The delivery port of reactor 1 is connected by outlet pipe 3 with the water inlet of second reactor 5, and valve 4 is provided with outlet pipe 3.Institute
State provided with two layers of catalytic ozonation oxidant layer in second reactor 5, the top and bottom of every layer of catalytic ozonation oxidant layer are all provided with
Have and be uniformly provided with filter opening on supporting layer 7, and supporting layer 7.Wherein, the first catalyst layer 601 is located at the upper of the second catalyst layer 602
Side and its filling height be the height of second reactor 5 5%, the catalyst be metal oxide (activated alumina), particle diameter is 3
~5mm.The filling height of second catalyst layer 602 is the 10% of the height of second reactor 5, and the catalyst is ordinary ceramsite, grain
Footpath is 6~8mm.The top of second reactor 5 is provided with delivery port 501, and the lower section of the delivery port 501 is additionally provided with circulating outlet,
The circulating outlet is connected by circulating line 8 and water pump 9 with the circulation water inlet of the bottom of second reactor 5.The present embodiment
The top of middle first-stage reactor 1 is provided with the first offgas outlet 102, and the top of first-stage reactor 5 is provided with the second offgas outlet 502,
And two offgas outlet be provided with ozone tail gas decomposer.
Using the present embodiment two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water device to certain chemical industry garden
Region two-stage bio-chemical effluent carries out advanced treating, by the chemical industrial park secondary biochemical effluent by intaking water pump and water inlet 101 leads to
Enter first-stage reactor 1, and be aerated by aerator 2, the COD Ratio controls in ozone dosage and waste water are 1:0.2.
Waste water carries out after ozone oxidation carrying out sufficiently catalytic oxidation processes, which part into second reactor 5 in first-stage reactor 1
Waste water is internally formed circulating water flow from bottom to top in the presence of circulating line 8 and water pump 9 in second reactor 5, so that
Catalyst expansion is obtained, expansion rate is 5%, now reflux ratio is 20%.
Total residence time is 0.5 hour to waste water in the reactor in the present embodiment, the average 65mg/L of COD of original water inlet, place
COD value is 40mg/L after reason, and COD clearances are 38%, compared to more former ozone catalytic fixed bed, and water outlet COD is 45mg/L, COD
Clearance improves 8%, with preferable treatment effect.
Embodiment 2
Using reaction unit same as Example 1, change each operational factor, carrying out practically is as follows：It is smelly in first-stage reactor 1
COD Ratio controls are 1 in oxygen dosage and waste water:0.5, the catalyst in second reactor 5 in second catalyst layer 602 is gold
Belong to oxide carried thing (activated alumina load iron, manganese), particle diameter is 5~6mm, and the filling of the catalyst is highly second order reaction
The 15% of device 5；Catalyst in first catalyst layer 601 is metal oxide (activated alumina), and particle diameter is in 3~4mm, and this is urged
The filling height of agent is the 8% of second order reaction pillar height degree.Meanwhile, in wastewater treatment process, the expansion rate of catalyst layer
For 50%, now reflux ratio is 100%, and the residence time is 1 hour to waste water in the reactor, the average 65mg/L of COD of original water inlet,
COD value is 30mg/L after processing, and COD clearances are 54%, compared to more former ozone catalytic fixed bed, and water outlet COD is 45mg/L,
COD clearances improve 23%, with preferable treatment effect.
Embodiment 3
Using reaction unit same as Example 1, change each operational factor, carrying out practically is as follows：It is smelly in first-stage reactor 1
COD Ratio controls are 1 in oxygen dosage and waste water:1, the catalyst in second reactor 5 in second catalyst layer 602 is metal
Oxide carried thing (activated alumina supported copper, nickel), particle diameter is 5~6mm, and it is the height of second reactor 5 that it, which loads height,
20%.Catalyst in first catalyst layer 601 is metal oxide (activated alumina), and particle diameter is in 3~4mm, and it loads high
Spend for the 10% of the height of second reactor 5.Meanwhile, the expansion rate for controlling catalyst layer in second reactor 5 is 70%, and waste water exists
The residence time is 1 hour in reactor, the average 135mg/L of COD of original water inlet, and COD value is 70mg/L, COD clearances after processing
For 48%, compared to more former ozone catalytic fixed bed, water outlet COD is 90mg/L, and COD clearances improve 15%, with preferable
Treatment effect.
Embodiment 4
Using reaction unit same as Example 1, change each operational factor, carrying out practically is as follows：Ozone dosage and useless
COD Ratio controls are 1 in water:1, the catalyst that the second catalyst layer 602 is used in second reactor 5 is metal oxide supported
Thing (activated alumina load iron, manganese and copper), particle diameter is 5~6mm, and it loads 20% that height is second reactor 5；First urges
The catalyst that agent layer 601 is used is metal oxide (manganese dioxide), and particle diameter is in 3~4mm, and it is second order reaction that it, which loads height,
The 10% of device 5, catalyst layer expansion rate is 100%, and now reflux ratio is 200%, and the residence time is 2 small to waste water in the reactor
When, the average 135mg/L of COD of original water inlet, COD value is 60mg/L after processing, and COD clearances are 56%, are urged compared to more former ozone
Change fixed bed, water outlet COD is 90mg/L, and COD clearances improve 22%, with preferable treatment effect.
According to embodiment 1-4, when handling waste water using apparatus and method of the present utility model, the water from water inlet water pump is first
First-stage reactor is introduced into, the ozone for then and in ozone generation system being mixed with oxygen carries out ozone in first-stage reactor
Oxidation reaction, during subsequent waste water enters second reactor from first-stage reactor bottom, second reactor is internally formed interior circulation, makes
The catalyst that must be filled reaches fluidisation state, improves the effective collision of ozone and catalyst, then occurs ozone catalytic reaction.Its
In, catalyst selects the ozone catalyst with different catalytic performances in second reactor, and being formed has different gradient effects
Catalytic effect, so as to can reach effective processing for different waste water.It can be significantly improved using method of the present utility model
The utilization rate and the catalysis oxidation efficiency of ozone, make catalytic oxidation more efficient, complete.
Schematically the utility model and embodiments thereof are described above, the description does not have restricted, accompanying drawing
Shown in be also one of embodiment of the present utility model, actual structure is not limited thereto.So, if this area
Those of ordinary skill enlightened by it, do not departing from the case that the utility model creates objective, designed without creative
The frame mode similar to the technical scheme and embodiment, all should belong to protection domain of the present utility model.
Claims (6)
1. a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water, it is characterised in that：It is anti-including one-level
Device (1) and second reactor (5) are answered, wherein, the first-stage reactor (1) is provided with water inlet (101), the reactor and is provided with
Aerator (2), and the delivery port of first-stage reactor (1) is connected by outlet pipe (3) with the water inlet of second reactor (5)；
Provided with least two layers catalytic ozonation oxidant layer in the second reactor (5), the top of second reactor (5) is provided with delivery port
(501) circulating outlet, is additionally provided with below the delivery port (501), the circulating outlet passes through circulating line (8) and water pump
(9) circulation water inlet with second reactor (5) bottom is connected.
2. a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water according to claim 1, its
It is characterised by：Provided with two layers of catalytic ozonation oxidant layer in the second reactor (5), wherein, the first catalyst layer (601) position
In the top of the second catalyst layer (602) and its filling height be second reactor (5) height 5%~10%, second catalysis
The filling of oxidant layer (602) is highly the 5%~20% of second reactor (5) height.
3. a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water according to claim 2, its
It is characterised by：The particle diameter of the catalytic ozonation agent is 3~8mm, and density is 0.8~1.6g/cm3。
4. a kind of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water according to any one of claim 1-3
Device, it is characterised in that：The top and bottom of every layer of catalytic ozonation oxidant layer are equipped with supporting layer (7), and supporting layer (7)
On be uniformly provided with filter opening.
5. a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water according to claim 4, its
It is characterised by：Described aerator (2) is connected with ozone generation system.
6. a kind of device of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water according to claim 4, its
It is characterised by：Offgas outlet is equipped with the top of the first-stage reactor (1) and second reactor (5), and offgas outlet is set
There is ozone tail gas decomposer.
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| CN106746034A (en) * | 2017-03-01 | 2017-05-31 | 南京大学盐城环保技术与工程研究院 | A kind of device and method of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water |
| CN107814459A (en) * | 2017-10-18 | 2018-03-20 | 上海电气集团股份有限公司 | A kind of biochemical ozone method for treating water and its processing unit |
| CN109019824A (en) * | 2018-09-17 | 2018-12-18 | 北京南科大蓝色科技有限公司 | A kind of efficiently catalyzing and oxidizing organic wastewater treating system |
| CN112125387A (en) * | 2020-11-04 | 2020-12-25 | 中冶赛迪技术研究中心有限公司 | Ozone catalytic oxidation treatment device and process for wastewater |
| CN112759064A (en) * | 2021-01-04 | 2021-05-07 | 华东理工大学 | Ozone catalytic oxidation system and treatment method of coal chemical industry concentrated solution |
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2017
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106746034A (en) * | 2017-03-01 | 2017-05-31 | 南京大学盐城环保技术与工程研究院 | A kind of device and method of two-stage gradient ozone catalytic fluidized bed deep treatment biochemical tail water |
| CN107814459A (en) * | 2017-10-18 | 2018-03-20 | 上海电气集团股份有限公司 | A kind of biochemical ozone method for treating water and its processing unit |
| CN109019824A (en) * | 2018-09-17 | 2018-12-18 | 北京南科大蓝色科技有限公司 | A kind of efficiently catalyzing and oxidizing organic wastewater treating system |
| CN109019824B (en) * | 2018-09-17 | 2021-08-27 | 深圳市南科大资产经营管理有限公司 | High-efficient catalytic oxidation organic wastewater treatment system |
| CN112125387A (en) * | 2020-11-04 | 2020-12-25 | 中冶赛迪技术研究中心有限公司 | Ozone catalytic oxidation treatment device and process for wastewater |
| CN112759064A (en) * | 2021-01-04 | 2021-05-07 | 华东理工大学 | Ozone catalytic oxidation system and treatment method of coal chemical industry concentrated solution |
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