CN104478067B - Interior circulating sewage processes catalytic ozonation reactor and sewage water treatment method thereof - Google Patents
Interior circulating sewage processes catalytic ozonation reactor and sewage water treatment method thereof Download PDFInfo
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- CN104478067B CN104478067B CN201410775219.9A CN201410775219A CN104478067B CN 104478067 B CN104478067 B CN 104478067B CN 201410775219 A CN201410775219 A CN 201410775219A CN 104478067 B CN104478067 B CN 104478067B
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- 239000010865 sewage Substances 0.000 title claims abstract description 136
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 69
- 238000006385 ozonation reaction Methods 0.000 title claims abstract description 64
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 36
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000010992 reflux Methods 0.000 claims abstract description 10
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 8
- 231100000719 pollutant Toxicity 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 68
- 239000003054 catalyst Substances 0.000 claims description 34
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 238000010926 purge Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 239000008188 pellet Substances 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims 1
- 230000003647 oxidation Effects 0.000 description 17
- 238000007254 oxidation reaction Methods 0.000 description 17
- 238000012360 testing method Methods 0.000 description 12
- 238000006555 catalytic reaction Methods 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 238000011160 research Methods 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000005189 flocculation Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 238000009287 sand filtration Methods 0.000 description 3
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000003403 water pollutant Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 235000010044 Hernandia moerenhoutiana Nutrition 0.000 description 1
- 244000084296 Hernandia moerenhoutiana Species 0.000 description 1
- 229910018162 SeO2 Inorganic materials 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000000356 contaminant Substances 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
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- -1 hydroxyl radical free radical Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- VASIZKWUTCETSD-UHFFFAOYSA-N manganese(II) oxide Inorganic materials [Mn]=O VASIZKWUTCETSD-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- JPJALAQPGMAKDF-UHFFFAOYSA-N selenium dioxide Chemical compound O=[Se]=O JPJALAQPGMAKDF-UHFFFAOYSA-N 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000003437 trachea Anatomy 0.000 description 1
- 230000007306 turnover Effects 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
- C02F1/72—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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
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)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
In the invention discloses one, circulating sewage processes catalytic ozonation reactor, including shell of reactor, inner core it is provided with in shell of reactor, inner core top is less than cover top portion, higher than outer casing bottom bottom inner core, it is provided with return flow line between inner core and outer casing inner wall, bottom inner core and between outer casing bottom, is provided with backflow window；Shell of reactor is provided with offgas duct, and offgas duct is provided with tail gas return duct, in tail gas return duct pipeline connection to reactor；The invention also discloses a kind of sewage water treatment method, reactor internal reflux sewage uses the endless form of reflux pump without regular circulation, saves power consumption；By circulation and tail gas outer circulation in sewage, make full use of undissolved ozone in the ozone and tail gas dissolved in sewage and process the pollutant in sewage further, raising processes the degree of depth, can be used for the fields such as the advanced treating of sewage, reusing sewage and high concentration difficulty biochemical sewage pretreatment.
Description
Technical field
The invention belongs to technical field of sewage, relate to sewage disposal catalytic ozonation reactor apparatus,
It is specially a kind of interior circulating sewage and processes catalytic ozonation reactor and sewage water treatment method thereof.
Background technology
Along with day by day improving and the requirement of reusing sewage, at the most traditional sewage of national environmental standard
Reason technology has been difficult to meet the demand of technology, thus proposes the technical need of advanced treatment of wastewater.High
Level oxidation technology is an emerging water technology, can produce hydroxyl radical free radical etc. by force in course of reaction
Oxyradical group, substantially increases oxidability, water pollutant of effectively degrading.As senior oxygen
One of change technology, ozone oxidation or catalytic ozonation are due to its high treating effect, simple to operate and obtain
Develop faster, no matter ozone oxidation or catalytic ozonation, all have industrialization case running.
Ozone oxidation or catalytic ozonation currently mainly use the mode of perforated pipe or micro-pore aeration by ozone
Being passed through in sewage, owing to ozone forms bubble relatively greatly in sewage, and dissolution rate is relatively low, thus causes smelly
Coefficient of oxygen utilization is low, and in outer last person's gas, ozone content is more.
For improving ozone utilization rate and sewage treating efficiency, the side of current commonly used catalytic ozonation
Formula carries out sewage disposal.Catalytic ozonation has been successfully applied to advanced treatment of wastewater, reusing sewage, height
The more independent ozone oxidation of aspect, ozone utilization rate and sewage treating efficiency such as concentration difficulty biochemical sewage pretreatment
Improve a lot.But the research of catalytic ozonation is concentrated mainly on catalyst research and development aspect at present, opens
Have issued different carriers and load different activities component catalyst, as with activated carbon, activated alumina,
Molecular sieves etc. are carrier, and load MnO, CuO, ZnO, TiO2, CeO2, SeO2 etc. up to more than ten plant and live
Property component, carries out the catalyst that various combination is developed；The catalyst range of application developed is different,
Treatment effect is each variant.Research Emphasis is placed on exploitation effective catalyst to improve by current each research institution
In ozone utilization rate and sewage treating efficiency, and seldom have by research, design and develop high efficiency reactor
Improve ozone utilization rate and sewage treating efficiency.The reactor of research and application is mainly two kinds at present,
One be sewage ozone co-flow, by reactor bottom from bottom to top by reactor catalyst bed, send out
Raw catalytic oxidation；Another kind be sewage ozone reverse flow, sewage from top to bottom, ozone from lower and
On by reactor catalyst bed, there is catalytic oxidation.
The subject matter that existing catalytic ozonation reactor exists has:
1, ozone undissolved in tail gas after reaction, reaction is unrecovered, discharges after ozone decomposed device processes,
Cause the waste of ozone so that ozone utilization rate is relatively low.
2, the dissolubility ozone having not enough time to reaction in sewage is expelled directly out, if follow-up sewage disposal connects
There is biological processing unit, also need that sewage is carried out ozone stripping etc. and process, on the one hand add treatment process,
On the other hand the waste of ozone is caused.
3, sewage time of staying in reactor is generally 0.5～1.0 hour, the difficult oxidation of part in sewage
Material has not enough time to oxidized just be discharged, and reaction depth is inadequate, causes sewage treating efficiency the highest.
A kind of oil refining sewerage catalytic ozonation depth disclosed in Chinese patent literature CN203625104U
Reason device, is to use two catalytic ozonation tower series connection, by first ozone catalytic of waste water processes
Oxidizing tower uses high pressure, second catalytic ozonation tower to use normal pressure, and its principle is high by first
Pressure catalytic ozonation tower, utilizes high pressure, high-concentrated ozone that macromolecule contaminant is first degraded to little molecule
Pollutant, then with low pressure, low concentration ozone degradation of small molecular pollutant.Its essence is really by using
Two catalytic ozonation towers improve ozone with the waste water time to improve pollutant catalysis degree of oxidation,
And initial stage smellyization is to be completed by high pressure, high-concentrated ozone, i.e. improve ozone and sewage or pollutant
Ratio, and in the tail gas in final normal pressure catalytic ozonation tower, ozone content is by normal pressure ozone catalytic oxygen
The process conditions changing tower determine, the most this mode can improve the degree for the treatment of of dirty water pollutant, but
Can not really reduce ozone concentration i.e. ozone discharge amount in tail gas, ozone utilization rate the most really improves.
Simultaneously as use two towers, particularly first is high-pressure tower, and equipment investment is multiplied, and not
Easily operation.
A kind of oil refining sewerage catalytic ozonation pretreatment disclosed in Chinese patent literature CN203625105U
Device is also to use two towers i.e. to pre-oxidize tower and catalysis oxidizing tower series connection, different from CN203625105U
Time its sewage and ozone be counter current contacting, be included in adverse current in tower, and be the most also adverse current,
I.e. sewage from pre-oxidation tower to catalysis oxidizing tower, and ozone be from catalysis oxidizing tower to pre-oxidation tower.It is not
Foot remains and adds equipment investment and operation easier, and ozone from catalysis oxidizing tower tail gas out
After concentration (content) reduces, at pre-oxidation tower internal oxidition declines, therefore its pre-oxidation column efficiency is relatively
Low, improve ozone utilization rate by increasing this tower, invest with it compared with the most do not preponderate.
Summary of the invention
For the problems referred to above, present invention aim at providing a kind of interior circulating sewage to process catalytic ozonation
Reactor, is greatly improved ozone utilization rate, improves the sewage disposal degree of depth, reduces energy consumption.
Technical scheme is as follows:
In a kind of, circulating sewage processes catalytic ozonation reactor, and including shell of reactor, its feature exists
In, it being provided with inner core in shell of reactor, inner core top is less than cover top portion, higher than at the bottom of shell bottom inner core
Portion, is provided with sewage backflow passage between inner core and outer casing inner wall, be provided with bottom inner core and between outer casing bottom
Sewage backflow window；Reactor head is provided with exhaust collection cover, and exhaust collection cover is provided with offgas duct, tail
Trachea is provided with tail gas return duct, and tail gas return duct pipeline connection is to water sprayer gas phase import.
Further, it is sequentially provided with water inlet distributor, ozone gas distribution from bottom up in shell of reactor
Device, catalyst support grid, catalyst bed course and described beds；Water inlet distributor pipeline is even
Water flowing emitter exports, the aqueous phase inlet communication sewage water inlet pipe of water sprayer, the gas phase inlet communication of water-blaster
Described tail gas return duct, sewage water inlet pipe is provided with booster pump；Ozone gas pipe pipeline connection air inlet pipe；
Being provided with tail gas control valve between tail gas return duct and offgas duct outlet, offgas duct outlet controls with tail gas
Ozone decomposed device it is communicated with between valve；Shell of reactor wall below exhaust collection cover is provided with overfall,
Overfall connection sewage drainage pipe, sewage drainage pipe is provided with draining control valve.
Further, backwash water inlet distributor and backwash inlet air distribution device, backwash water inlet water distribution are also included
Device and backwash inlet air distribution device are arranged in inner core, are positioned at below water inlet distributor, backwash water inlet distributor
Connection backwash water inlet pipe, backwash inlet air distribution device connection backwash air inlet pipe；Inner core above beds
Wall is provided with backwash drain pipe, and backwash drain pipe passes to outside reactor through shell of reactor；Backwash draining
Pipe is provided with backwash water draining control valve.
Further, the inner tube wall top of described reactor is provided with a circle downflow weir, downflow weir
Described overfall is arranged on shell of reactor wall.
At a kind of sewage utilizing above-mentioned interior circulating sewage to process catalytic ozonation reactor for treatment sewage
Reason method, it is characterised in that comprise the following steps:
(1) by water inlet distributor in interior circulation dirt after treatment sewage enters water inlet pipe intensified pump supercharging
Water is upper equably in processing catalytic ozonation reactor inner core, and ozone passes through ozone after air inlet pipe
Distributor is uniform upper in reactor inner core, is filled with catalyst in reactor inner core；Pending dirt
Water and ozone all enter beds, catalytic ozonation reaction occurs under catalyst action, removes
Pollutant in sewage；
(2) sewage overflowed through downflow weir after step (1) reaction, a part enters row from overfall
Water pipe is expelled to outside reactor, and it discharges the water yield by draining control valve control；Step (1) reaction after through
Another part sewage that downflow weir overflows is back to reactor bottom by sewage backflow passage, then by dirt
Water backflow window enters in reactor inner core, and sewage is upper to be entered through water inlet distributor, ozone gas pipe
Beds participates in catalytic ozonation reaction again；
(3) in step (1) course of reaction produce containing ozone tail gas through exhaust collection cover collect after, one
Partial tail gas enter pass to after exhaustor ozone decomposed device process up to standard after be emitted into the external world, exhaust emissions amount
Controlled by tail gas control valve；Another part that step (1) produces is entered by tail gas return duct containing ozone tail gas
Enter water sprayer gas phase entrance, mix with the treatment sewage entering water sprayer, form air-water mixture and enter
Reactor inner core participates in catalytic ozonation reaction again.
Further, above-mentioned sewage water treatment method, it is characterised in that further comprising the steps of:
(4) after catalytic ozonation reaction runs 6～7 days, beds need to be carried out backwash, first
By backwash air inlet pipe air inlet, by under backwash inlet air distribution device beds in reactor inner core
Side's uniformly air inlet carries out independent air purge, is intake by backwash water inlet pipe while the most not stopping air purge again,
By backwash water inlet distributor beds carried out gas water associating backwash；Then stop air inlet, pass through
Beds is individually washed by the water inlet of backwash water inlet pipe；
(5) backwash waste that step (4) produces is discharged by backwash drain pipe, and backwash waste gas is by tail gas
Collecting hood is discharged by offgas duct after collecting.
Further, in step (4), the independent air purge time is 3～10 minutes, air purge intensity be 12～
25L/(m2·s)；Gas the water associating backwash time be 3～5 minutes, air purge intensity 10～15L/ (m2·s)、
Washing intensity 4～6L/ (m2·s)；Individually washing time is 3～10 minutes, washes intensity 8～16L/
(m2·s)。
Further, in catalytic ozonation course of reaction, interior circulating sewage reflux ratio be 100%～
300%, tail gas reflux ratio is 100%～400%.
Further, in described catalytic ozonation course of reaction, the catalyst in reactor is granule
Shape catalyst, particle diameter is 2～8mm.
Further, in described catalytic ozonation course of reaction, in reactor, the effective waterpower of sewage is stopped
Staying the time is 0.5～1.0 hour.The invention has the beneficial effects as follows that a kind of interior circulating sewage of offer processes ozone
Catalyst oxidation reactor, reasonable in design, reactor internal reflux sewage uses reflux pump without regular circulation
Endless form, saves power consumption；Present invention also offers a kind of this interior circulating sewage process ozone to urge
Oxidation device processes the method for sewage, by circulation and tail gas outer circulation in sewage, makes full use of dirt
In the ozone dissolved in water and tail gas, undissolved ozone processes the pollutant in sewage further, improves anti-
Answering the degree of depth, relatively conventional catalyst oxidation reactor, ozone utilization rate improves more than 20%, can be used for sewage
The fields such as advanced treating, reusing sewage and high concentration difficulty biochemical sewage pretreatment.
Accompanying drawing explanation
Fig. 1 processes structure when catalytic ozonation reactor runs for the interior circulating sewage that the present invention provides
Schematic diagram；
In figure:
1. treatment sewage；2. water inlet pipe；3. booster pump；4. water sprayer；5. water inlet distributor；6. dirty
Water backflow window；7. backwash inlet air distribution device；8. backwash water inlet distributor；9. backwash air inlet pipe；10.
Backwash water inlet pipe；11. air inlet pipe；12. ozone gas pipes；13. catalyst support grids；14. catalyst
Bed course；15. beds；16. reactor inner cores；17. shell of reactor；18. backwash drain pipies；
19. backwash waste；20. backwash draining control valves；21. effluent sewerages；22. draining control valves；23.
Sewage drainage pipe；24. downflow weirs；25. exhaust collection covers；26. offgas duct；27. tail gas control valves；28.
Ozone decomposed device；29. tail gas outlets；30. tail gas return ducts；31. sewage backflow passages.
Detailed description of the invention
In order to make those skilled in the art be more fully understood that the present invention program, below in conjunction with the accompanying drawings and specifically
The present invention is described in further detail for embodiment.
As shown in Figure 1: in a kind of, circulating sewage processes catalytic ozonation reactor, including reactor
Shell 17, is provided with inner core 16 in shell of reactor 17, inner core 16 top is less than shell 17 top, interior
Higher than bottom shell 17 bottom cylinder 16, between inner core 16 and shell 17 inwall, it is provided with return flow line 31,
Backflow window 6 it is provided with between bottom inner core 16 and bottom shell 17；Set the most successively in inner core 16
Have water inlet distributor 5, ozone gas pipe 12, catalyst support grid 13, catalyst bed course 14 and
Described beds 15；Water inlet distributor 5 pipeline connection water sprayer 4 exports, and sewage water inlet pipe 2 is even
Logical described water sprayer 4 aqueous phase import, water inlet pipe 2 is provided with booster pump 3, and ozone gas pipe 12 pipeline is even
Logical ozone air inlet pipe 11.Shell of reactor 17 top is provided with exhaust collection cover 25, exhaust collection cover 25
Being provided with offgas duct 26, offgas duct 26 is provided with tail gas return duct 30, and tail gas return duct 30 connects described
The gas phase import of water sprayer 4, is provided with tail gas control between tail gas return duct 30 and offgas duct outlet 29
Valve 27.Wherein water sprayer is also referred to as ejector, it is possible to return anti-after making treatment sewage and backflow tail gas mixing
Answer device bottom so that backflow tail gas can be formed with treatment sewage in the case of normal pressure even negative pressure
Air-water mixture returns to reactor and again participates in catalytic oxidation.
Described offgas duct 26 connects ozone decomposed device 28；It is provided with a circle to overflow at reactor inner core 16 top
Stream weir 24, the externally discharged waste water overfall on downflow weir is arranged on shell of reactor 17 wall and is positioned at tail gas receipts
Below collection cover 25.Overfall connection sewage drainage pipe 23, sewage drainage pipe 23 is provided with draining control valve
22。
In the present invention, circulating sewage process catalytic ozonation reactor also includes backwash water inlet distributor 8 He
Backwash inlet air distribution device 7, backwash water inlet distributor 8 and backwash inlet air distribution device 7 are arranged in inner core 16,
It is positioned at below water inlet distributor 5；Backwash water inlet distributor connection backwash water inlet pipe 10, backwash inlet air distribution
Device connection backwash air inlet pipe 9；Inner core 16 wall above beds 15 is provided with backwash drain pipe 18,
Backwash drain pipe 18 passes to outside reactor through shell of reactor 17；Backwash drain pipe 18 is provided with backwash
Water draining control valve 20.
This interior circulating sewage processes the method for catalytic ozonation reactor for treatment sewage, it is characterised in that bag
Include following steps:
(1) by water sprayer 4 after treatment sewage 1 enters water inlet pipe 2 intensified pump 3 supercharging, afterwards
By water inlet distributor 5, in described interior circulating sewage processes catalytic ozonation reactor inner core 16 all
Even ground is upper, and ozone passes through ozone distributor 12 at reactor inner core 16 after ozone air inlet pipe 11
Interior uniform upper, treatment sewage and ozone are upper through catalyst grid 13 and catalyst bed course 14
Enter beds 15；Loading catalyst in beds 15, treatment sewage and ozone are being urged
Under agent effect, in beds 15, there is catalytic ozonation reaction, remove the pollution in sewage
Thing；In catalytic ozonation course of reaction, the catalyst in reactor is pellet type catalyst, and particle diameter is
2～8mm.
(2) sewage overflowed through downflow weir 24 after step (1) reaction, a part enters from overfall
Drain pipe 23 is expelled to outside reactor, and the output of its sewage discharge water 21 is controlled by draining control valve 22；
Then sewage turnover dynamic equilibrium in interior circulating sewage capacity of returns and reactor is controlled；After step (1) reaction
Through another part sewage that downflow weir 24 overflows, lead to 31 by sewage backflow and be back to reactor bottom,
Enter in reactor inner core by sewage backflow window 6 again, sewage upper through water inlet distributor 5, smelly
Oxygen gas pipe 12 grade enters beds 15 and again participates in catalytic ozonation reaction, thus fully sharp
With the ozone dissolved in sewage, improve ozone utilization rate, and improve the sewage disposal degree of depth；
(3) in step (1) course of reaction produce containing ozone tail gas through exhaust collection cover 25 collect after,
A part of tail gas enter pass to after exhaustor 26 ozone decomposed device 28 process up to standard after be emitted into the external world, tail
Gas discharge capacity is controlled by tail gas control valve 27, so that while making full use of containing ozone tail gas, it is ensured that reaction
Air inflow and the dynamic equilibrium of capacity in device；Another part that step (1) produces passes through containing ozone tail gas
Tail gas return duct 30 enters water sprayer 4 gas phase entrance, mixes with the treatment sewage 1 entering water sprayer 4,
Formed and air-water mixture entrance reactor inner core 16 participates in catalytic ozonation reaction again, thus fully
Utilize remaining ozone in tail gas, improve ozone utilization rate；Tail gas reflux ratio passes through tail gas control valve 27
Control in the range of 100%～400%.
(4) after catalytic ozonation reaction runs 6～7 days, beds 15 space and catalyst table
Float, colloid blocking or the pollution that face can be brought in sewage or reaction produces, need to be to catalysis
Agent bed 15 carries out backwash.First passing through backwash air inlet pipe 9 air inlet, gas passes through backwash inlet air distribution device 7,
Below beds 15 in reactor inner core 16, air inlet carries out independent air purge, independent air purge time
Being 3～10 minutes, air purge intensity is 12～25L/ (m2·s)；Lead to again while the most not stopping air purge
Crossing backwash water inlet pipe 10 to intake, water passes through backwash water inlet distributor 8, carries out beds 15
Gas water associating backwash；Gas the water associating backwash time be 3～5 minutes, air purge intensity 10～15L/ (m2·s)、
Washing intensity 4～6L/ (m2·s)；Then stop air inlet, intake to catalysis by backwash water inlet pipe 10
Agent bed 15 is individually washed；Individually washing time is 3～10 minutes, washes intensity 8～16L/
(m2·s)。
(5) backwash waste 19 that step (4) produces is discharged by backwash drain pipe 18, backwash waste gas
Discharged by offgas duct 26 after being collected by exhaust collection cover 25.
The present invention is by the appropriate design to reactor, it is achieved circulation in sewage, it is not necessary to needed for regular circulation
Circulating pump, save power consumption.It is characterized in utilizing sewage and backflow tail gas to be formed at water sprayer
Bottom air-water mixture entrance with pressure reactor inner core, it is provided that flow up power, at sewage backflow window
Form certain pressure reduction, make the sewage after process bottom sewage backflow passage, Returning reactor inner core
Form inner circulating reflux.
Embodiment 1:
Certain Treatment of Sewage Reservoir of Chemical Plant Treatment stations second pond draining, CODcr is between 85～96mg/l, it is desirable to outer
Sewer CODcr is less than 50mg/l, need to carry out advanced treating further.Owing to this sewage is through biochemical treatment
After, secondary clarifier effluent BOD5Less than 8mg/l, B/C value less than 0.1, belong to difficult biochemical treatment sewage.Through opinion
Card, intends using flocculation sand filtration+catalytic ozonation to process technique, and carried out checking and contrast test.Examination
Testing result to show, sewage is after flocculation sand filtration processes, and CODcr is in about 80mg/l, flocculation sand filtration water outlet
After catalytic ozonation processes, COD of sewage cr is up to below 50mg/l.For catalytic ozonation,
Having carried out the contrast test of different reactor type, contrast test is at the interior circulating sewage that the present invention provides
Reason catalytic ozonation reactor and conventional concurrent catalytic ozonation reactor (sewage, ozone all from
Lower and on pass through beds) between carry out, the catalyst that two set reactors are loaded is active oxygen
Changing aluminum loaded catalyst, hydraulic detention time is 0.5 hour, and comparative test result is shown in Table 1.
In table 1, circulating sewage processes catalytic ozonation reactor and conventional catalytic ozonation reactor
Comparative test result
By table 1 result of the test it can be seen that the present invention provides interior circulating sewage process catalytic ozonation anti-
Answering device more conventional catalytic ozonation reactor, ozone utilization rate is improved by a relatively large margin, and improves
The sewage disposal degree of depth.
Embodiment 2:
Certain Petrochemical Enterprises externally discharged waste water CODcr is 50～60mg/l, enterprise need to using externally discharged waste water reuse as
Circulating water system, it is desirable to CODcr is less than 40mg/l.Through demonstration, intend using catalytic ozonation to dirt
Water processes, to reach the purpose of reuse.For determining the feasibility of scheme, enterprise has carried out on-the-spot examination
Testing, during test, the interior circulating sewage process catalytic ozonation reactor that the present invention provides has been investigated in contrast
With conventional concurrent catalytic ozonation reactor (sewage, ozone pass through beds the most from bottom to top)
Operational effect, the catalyst that two set reactors are loaded is activated alumina loaded catalyst, waterpower
The time of staying is 0.5 hour, and comparative test result is shown in Table 2.
In table 2, circulating sewage processes catalytic ozonation reactor and conventional catalytic ozonation reactor
Comparative test result
By table 2 result of the test it can be seen that the present invention provides interior circulating sewage process catalytic ozonation anti-
Answering device more conventional catalytic ozonation reactor, ozone utilization rate obtains more than 20% and improves by a relatively large margin,
And improve the sewage disposal degree of depth.
Above the present invention is described in detail.Principle and embodiment to the present invention are carried out herein
Illustrate, the core concept being only intended to help to understand the present invention described above.It should be pointed out that, for this
For the those of ordinary skill of technical field, under the premise without departing from the principles of the invention, it is also possible to this
Invention carries out some improvement and modification, and these improve and modify the protection model also falling into the claims in the present invention
In enclosing.
Claims (4)
1. a sewage water treatment method, it is characterised in that comprise the following steps:
(1) by water inlet distributor in interior circulation dirt after treatment sewage enters water inlet pipe intensified pump supercharging
Water is upper equably in processing catalytic ozonation reactor inner core, and ozone is divided by ozone after air inlet pipe
Cloth device is uniform upper in reactor inner core, is filled with catalyst in reactor inner core；Treatment sewage and
Ozone all enters beds, catalytic ozonation reaction occurs under catalyst action, removes in sewage
Pollutant；
(2) sewage overflowed through downflow weir after step (1) reaction, a part enters draining from overfall
Pipe is expelled to outside reactor, and it discharges the water yield by draining control valve control；Through overflowing after step (1) reaction
Another part sewage that stream weir is overflowed is back to reactor bottom by sewage backflow passage, then is returned by sewage
Stream window enters in reactor inner core, and sewage is upper enters catalyst through water inlet distributor, ozone gas pipe
Bed participates in catalytic ozonation reaction again；
(3) in step (1) course of reaction produce containing ozone tail gas through exhaust collection cover collect after, one
Dividing tail gas to pass to after entering exhaustor be emitted into the external world after ozone decomposed device processes, exhaust emissions amount is by tail gas control
Valve processed controls；Another part that step (1) produces enters water sprayer containing ozone tail gas by tail gas return duct
Gas phase entrance, mixes with the treatment sewage entering water sprayer, forms air-water mixture and enters reactor inner core
In again participate in catalytic ozonation reaction；
(4), after catalytic ozonation reaction runs 6～7 days, beds need to be carried out backwash, first lead to
Cross backwash air inlet pipe air inlet, by equal below backwash inlet air distribution device beds in reactor inner core
Even air inlet carries out independent air purge, is intake by backwash water inlet pipe while the most not stopping air purge again, by instead
Wash water inlet distributor beds is carried out gas water associating backwash；Then stop air inlet, entered by backwash
Beds is individually washed by water pipe water inlet；
(5) backwash waste that step (4) produces is discharged by backwash drain pipe, and backwash waste gas is received by tail gas
Collection cover is discharged by offgas duct after collecting；
In step (4), the independent air purge time is 3～10 minutes, and air purge intensity is 12～25L/ (m2·s)；
Gas the water associating backwash time be 3～5 minutes, air purge intensity 10～15L/ (m2S), washing intensity 4～
6L/(m2·s)；Individually washing time is 3～10 minutes, washes intensity 8～16L/ (m2·s)。
2. sewage water treatment method as claimed in claim 1, it is characterised in that: catalytic ozonation reacts
During, interior circulating sewage reflux ratio is 100%～300%, and tail gas reflux ratio is 100%～400%.
3. sewage water treatment method as claimed in claim 1, it is characterised in that: described catalytic ozonation
In course of reaction, the catalyst in reactor is pellet type catalyst, and particle diameter is 2～8mm.
4. sewage water treatment method as claimed in claim 3, it is characterised in that: described catalytic ozonation
In course of reaction, in reactor, the effective hydraulic detention time of sewage is 0.5～1.0 hour.
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| CN105417678A (en) * | 2015-12-31 | 2016-03-23 | 北京清大国华环境股份有限公司 | Ozone catalytic oxidation method and device |
| CN108408876A (en) * | 2018-05-30 | 2018-08-17 | 王德喜 | A kind of ozone oxidation system |
| CN110980918B (en) * | 2019-11-25 | 2022-05-31 | 哈尔滨工创环保科技有限公司 | Multistage ozone catalytic oxidation internal circulation device and use method |
| CN111302478B (en) * | 2020-03-03 | 2024-03-12 | 清华大学 | Sludge and wastewater treatment device and sludge or wastewater treatment method |
| CN112850876B (en) * | 2021-01-25 | 2021-11-02 | 江苏省环境科学研究院 | Three-phase reactor for catalytic oxidation of ozone |
| CN113877491A (en) * | 2021-10-26 | 2022-01-04 | 湖北惠大臭氧生物科技股份有限公司 | Ozonization oil reactor |
| CN114684972A (en) * | 2022-04-15 | 2022-07-01 | 东华工程科技股份有限公司 | Inner loop flow ozone catalytic oxidation reactor and method for treating wastewater by using same |
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| FR2861718B1 (en) * | 2003-10-30 | 2006-03-03 | Otv Sa | INSTALLATION AND METHOD FOR PURIFYING AQUEOUS EFFLUENT BY OXIDATION AND MEMBRANE FILTRATION |
| CN201347378Y (en) * | 2009-01-07 | 2009-11-18 | 南京师范大学 | Batch-type three-phase-fluidization ozone oxidation reactor |
| CN101993144B (en) * | 2010-12-17 | 2013-01-23 | 江苏江大环境工程有限责任公司 | Catalytic oxidation fluid bed |
| CN203200067U (en) * | 2012-07-13 | 2013-09-18 | 天津大港油田科远石油工程有限责任公司 | Sewage treatment device for improving utilization ratio of ozone by catalytic oxidation |
| CN203602394U (en) * | 2013-11-06 | 2014-05-21 | 九江学院 | Jet flow type ozone photocatalysis-membrane treatment organic wastewater device |
| CN203781901U (en) * | 2014-04-18 | 2014-08-20 | 世纪华扬环境工程有限公司 | Ozone catalytic oxidation device |
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Denomination of invention: Internal circulation sewage treatment ozone catalytic oxidation reactor and its sewage treatment method Effective date of registration: 20211015 Granted publication date: 20160914 Pledgee: South Taihu New Area sub branch of Huzhou Wuxing Rural Commercial Bank Co.,Ltd. Pledgor: ZHEJIANG CATHAYRIPE ENVIRONMENTAL ENGINEERING Co.,Ltd. Registration number: Y2021330001922 |
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