CN205527940U - Two -stage ozone catalytic oxidation's effluent treatment plant - Google Patents
Two -stage ozone catalytic oxidation's effluent treatment plant Download PDFInfo
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- CN205527940U CN205527940U CN201620061049.2U CN201620061049U CN205527940U CN 205527940 U CN205527940 U CN 205527940U CN 201620061049 U CN201620061049 U CN 201620061049U CN 205527940 U CN205527940 U CN 205527940U
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Abstract
The utility model provides a two -stage ozone catalytic oxidation's effluent treatment plant. The device includes the 1st ozone catalytic oxidation reactor (1) and the 2nd ozone catalytic oxidation reactor (2), the first clear water district (105) of the 1st ozone catalytic oxidation reactor (1) and second water distribution gas distribution district (203) the intercommunication of the 2nd ozone catalytic oxidation reactor (2), perhaps the first water distribution gas distribution district (103) of the 1st ozone catalytic oxidation reactor (1) and second water distribution gas distribution district (203) the intercommunication of the 2nd ozone catalytic oxidation reactor (2). The utility model discloses can improve sewage treatment's stability and efficiency, the engineering gross investment that can significantly reduce moreover, maintenance management are easy.
Description
Technical field
The invention belongs to technical field of sewage, relate to a kind of industrial waste water disposal device, particularly relate to use the advanced waste treatment apparatus of catalytic ozonation.
Background technology
Along with China's water pollution problems highlights day by day, the raising of sewage disposal discharge standard has been trend of the times.In recent years, after especially " ten, water " proposes, the mark retrofit work that carries of various places sewage treatment plant is carried out the most successively.Proposing mark transformation, the mark that carries of the sewage treatment plant especially containing industrial wastewater is transformed, and only by upgrading biochemical processing process, is extremely difficult to required standard, certainly will need to increase advanced oxidation processes after biochemistry.
The method of advanced oxidation includes the high-level oxidation technologies such as Fenton process, Ozonation, electrolytic catalysis method, wet oxidation process, photochemistry synergistic oxidation method at present.Wherein, Fenton process can produce substantial amounts of iron cement to be difficult to process, and needs to add substantial amounts of soda acid and other medicaments in course of reaction simultaneously, and operating cost is higher.Electrochemical oxidation process application treatment scale is restricted, it is impossible to large-scale application is in big yield processing item.Wet Oxidation Process operating cost is the highest, applies less in Treatment of Industrial Water.Synergistic oxidation method covers several different method for oxidation, impact each other is complex, and it being in the laboratory research stage, its congenital restraining factors such as, course of reaction complexity harsh to water condition of water quality, effect instability, the feasibility of through engineering approaches are all the barriers that its development and application needs to capture.In Ozonation, the oxidability of ozone is relatively strong, and ozone is oxidized is decomposed into oxygen, and to environment non-secondary pollution, overall operation cost is relatively low.O3Typically to be combined with catalyst, promote O3Decompose and generate OH, make O3Organic pollutant degradation rate is significantly improved, and catalytic ozonation technology has the advantages such as operating cost is low, easy to operate.
Utility model content
This utility model is solved the technical problem that to be: for the deficiency of sewage disposal device, advanced waste treatment system associated with a kind of novel two-stage catalytic ozonation is proposed, can not only improve stability and the efficiency of sewage disposal, and it is easy to greatly reduce total investment of engineering, maintenance management.
Single ozonation technology has significant limitation, in processing procedure, and O3Pollutant that can be the fastest with reaction rate react, and show O3Removal to pollutant is selective, so that the low pollutant of reaction rate can not be removed.Use single catalytic ozonation technical finesse many industrial wastewaters, exist and once invest high shortcoming, and every kind of catalyst has its suitable high efficiency range, once exceedes high efficiency range, operating cost and investment cost and just increases by geometric progression.
Specifically, the utility model proposes following technical scheme.
A kind of two-stage catalytic ozonation wastewater treatment equipment, including the first catalytic ozonation reactor 1 and the second catalytic ozonation reactor 2；
Described first catalytic ozonation reactor 1 includes the first catalysis tank body or cell body 101, is arranged on the first the 104, first clear water zone, the 103, first catalyst zone, the 102, first water distribution gas distribution district of ozone district 105 and the first gas collection district 106 within the first catalysis tank body or cell body 101 the most from down to up；Described first clear water zone 105 is interconnected with the first water distribution gas distribution district 103；
Described second catalytic ozonation reactor 2 includes the second catalysis tank body or cell body 201, is arranged on the second the 204, second clear water zone, the 203, second catalyst zone, the 202, second water distribution gas distribution district of ozone district 205 and the second gas collection district 206 within the second catalysis tank body or cell body 201 the most from down to up；
First clear water zone 105 of described first catalytic ozonation reactor 1 connects with the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2；Or the first water distribution gas distribution district 103 of described first catalytic ozonation reactor 1 connects with the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2.
Preferably, wherein, the second described clear water zone 205 does not mutually connect with the second water distribution gas distribution district 203.
Preferably, wherein, described first catalytic ozonation reactor 1 also includes the first ozone tail gas destructor 107, is arranged on the first catalysis tank body or top outer of cell body 101 of the first catalytic ozonation reactor 1；Described second catalytic ozonation reactor 2 also includes the second ozone tail gas destructor 207, is arranged on the second catalysis tank body or top outer of cell body 201 of the second catalytic ozonation reactor 2.
Preferably, wherein, described first clear water zone 105 and the first water distribution gas distribution district 103 are interconnected by being arranged on the first water circulating pump 109 outside the first catalysis tank body or cell body 101.
Preferably, wherein, described first ozone district 102 connects ozonator by the first ozone import 1021；Described second ozone district 202 connects ozonator by the second ozone import 2021.
Preferably, wherein, the whole height of described first catalysis tank body or cell body 101 and the second catalysis tank body or cell body 201 is 4-9 rice, and the first water distribution gas distribution district 103 and the second water distribution gas distribution district 203 that arrange bottom it are highly 0.5-0.8 rice.
Preferably, wherein, by volume, described first catalyst zone 104 volume accounts for the first catalysis tank body or the 30%-70% of cell body 101 cumulative volume；Second catalyst zone 204 accounts for the second catalysis tank body or the 30%-70% of cell body 201 cumulative volume.
Preferably, wherein, described first water distribution gas distribution district 103 sidepiece is provided with the first waste water inlet 108；Described second water distribution gas distribution district 203 sidepiece is provided with the second waste water inlet 208.
The beneficial effects of the utility model are: a kind of two-stage catalytic ozonation advanced waste treatment apparatus, have that disposal ability is strong and the feature of high treating effect.Using native system, water outlet COD to can reach one-level A even surface water IV class standard in the treatment of waste water, compared with existing high-level oxidation technology, water percentage ratio up to standard is greatly improved, and operating cost is substantially reduced, and has good economic benefit.
Accompanying drawing explanation
The schematic diagram of Fig. 1 (a) this utility model the first catalytic ozonation reactor 1.
The schematic diagram of Fig. 1 (b) this utility model the second catalytic ozonation reactor 2.
This utility model two-stage catalytic ozonation advanced waste treatment apparatus schematic diagram of a kind of detailed description of the invention of Fig. 2.
This utility model two-stage catalytic ozonation advanced waste treatment apparatus schematic diagram of Fig. 3 another kind detailed description of the invention.
Detailed description of the invention
In order to be better understood from content of the present utility model, below in conjunction with being embodied as being described further the technical solution of the utility model, but specific embodiment is not the restriction being done this utility model.
As shown in Fig. 1 (a) and (b), the first catalytic ozonation reactor 1 and schematic diagram of the second catalytic ozonation reactor 2 of this utility model two-stage catalytic ozonation advanced waste treatment apparatus.
The first described catalytic ozonation reactor 1 includes the first catalysis tank body or cell body 101, it is arranged on the first the 104, first clear water zone, the 103, first catalyst zone, the 102, first water distribution gas distribution district of ozone district 105 and the first gas collection district 106 within the first catalysis tank body or cell body 101 the most from down to up, and is arranged on the first ozone tail gas destructor 107 of the first catalysis tank body or cell body 101 top outer.The first described water distribution gas distribution district 103 sidepiece is provided with the first waste water inlet 108.The first described clear water zone 105 and the first water distribution gas distribution district 103 are to be interconnected by being arranged on the first water circulating pump 109 outside the first catalysis tank body or cell body 101.The sidepiece in described first ozone district 102 is provided with the first ozone import 1021；The first described clear water zone 105 sidepiece is provided with the first clear water output 1051.Described first ozone district 102 connects ozonator by the first ozone import 1021.Being provided with ozone gas distributing pipeline in first ozone district 102, preferred ozone gas distributing pipeline is provided with aeration plate DN150 (titanium dish).
First catalyst zone 104 is filled with activated alumina as carrier, the heterogeneous ozone catalytic oxidation catalyst of one or more in the metal-oxide such as Supported Manganese, copper, ferrum, cerium, zirconium, nickel.By volume, described first catalyst zone 104 accounts for the first catalysis tank body or the 30%-70% of cell body 101 cumulative volume.
The second described catalytic ozonation reactor 2 includes the second catalysis tank body or cell body 201, it is arranged on the second the 204, second clear water zone, the 203, second catalyst zone, the 202, second water distribution gas distribution district of ozone district 205 and the second gas collection district 206 within the second catalysis tank body or cell body 201 the most from down to up, and is arranged on the second ozone tail gas destructor 207 of the second catalysis tank body or cell body 201 top outer.The second described water distribution gas distribution district 203 sidepiece is provided with the second waste water inlet 208.The sidepiece in described second ozone district 202 is provided with the second ozone import 2021；The second described clear water zone 205 sidepiece is provided with the second clear water output 2051.Described second ozone district 202 connects ozonator by the second ozone import 2021.Being provided with ozone gas distributing pipeline in first ozone district 102, preferred ozone gas distributing pipeline is provided with aeration plate DN150 (titanium dish).
Second catalyst zone 204 is filled with activated carbon as carrier, the heterogeneous ozone catalytic oxidation catalyst of one or more in the metal-oxide such as Supported Manganese, copper, ferrum, cerium, zirconium, nickel.By volume, described catalyst zone 204 accounts for catalysis tank body or the 30%-70% of cell body 201 cumulative volume.
The whole height of described first catalysis tank body or cell body 101 and the second catalysis tank body or cell body 201 is 4-9 rice, and the first water distribution gas distribution district 103 and the second water distribution gas distribution district 203 that arrange bottom it are highly 0.5-0.8 rice.
Ozonator used by this utility model and ozone tail gas destructor are commercially available conventional equipment.
It it is this utility model two-stage catalytic ozonation advanced waste treatment apparatus schematic diagram of a kind of detailed description of the invention shown in Fig. 2.In this embodiment, the first clear water zone 105 of described first catalytic ozonation reactor 1 connects with the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2, it is possible to stream operational mode processes waste water continuously.Concrete, waste water enters the first water distribution gas distribution district 103 of the first catalytic ozonation reactor 1 from the first waste water inlet 108, through matrix pattern perforated pipe water distribution.Ozone is produced by ozone generating-device (not shown), then enters the first ozone district 102 through the first ozone import 1021.Through ozone gas distributing pipeline and titanium dish gas distribution, the service area of single titanium dish is 0.5～1.0 square metre, ozone enters the first water distribution gas distribution district 103 from the first ozone district 102, the first catalyst zone 104 is entered together with the waste water in the first water distribution gas distribution district 103, first catalyst zone 104 is filled with activated alumina as carrier, the heterogeneous ozone catalytic oxidation catalyst of one or more in the metal-oxides such as Supported Manganese, copper, ferrum, cerium, zirconium, nickel, waste water and ozone, catalyst haptoreaction, remove the COD in waste water.
First clear water zone 105 and the first water distribution gas distribution district 103 are to be interconnected by being arranged on the first water circulating pump 109 outside the first catalysis tank body or cell body 101, waste water after the first catalyst zone 104 processes enters the first clear water zone 105, then the first water distribution gas distribution district 103 is looped back by the first water circulating pump 109, again the first catalyst zone 104 is entered together with ozone, in the process, waste water is constantly and ozone, catalyst haptoreaction, reaction is continuously, the most repeatedly, channel is not had in reactor, short stream, ensure that ozone repeatedly contacts cutting with catalyst, improve the utilization rate of ozone.
Ozone is after the first catalyst zone 104 is fully contacted with waste water, generate containing ozone, oxygen and the mixed gas of carbon dioxide, this mixed gas passes the first clear water zone 105, collect in the first gas collection district 106, it is then passed through after the first ozone tail gas destructor 107 destroys remaining ozone, being discharged in air.
First clear water zone 105 of the first catalytic ozonation reactor 1 is connected by the first clear water output 1051 with the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2.Through repeatedly contacting the waste water processed with ozone and catalyst from the first clear water zone 105, arrive the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2 through the first clear water output 1051, through matrix pattern perforated pipe water distribution.Ozone is produced by ozone generating-device (not shown), then enters the second ozone district 202 through the second ozone import 2021, and through ozone gas distributing pipeline and titanium dish gas distribution, the service area of single titanium dish is 0.5～1.0 square metre.Ozone enters the second water distribution gas distribution district 203 from the second ozone district 202, the second catalyst zone 204 is entered together with the waste water in the second water distribution gas distribution district 203, second catalyst zone 204 is filled with activated carbon as carrier, the heterogeneous ozone catalytic oxidation catalyst of one or more in the metal-oxides such as Supported Manganese, copper, ferrum, cerium, zirconium, nickel, waste water and ozone, catalyst haptoreaction, remove the COD in waste water.
Ozone is after the second catalyst zone 204 is fully contacted with waste water, generate containing ozone, oxygen and the mixed gas of carbon dioxide, this mixed gas passes the second clear water zone 205, collect in the second gas collection district 206, it is then passed through after the second ozone tail gas destructor 207 destroys remaining ozone, being discharged in air.
Second clear water zone 205 of the second catalytic ozonation reactor 2 is provided with the second clear water output 2051.Discharge the second catalytic ozonation reactor 2 through repeatedly contacting, with ozone and catalyst, the process water processed from the first clear water output 1051, flow to follow up device equipment.Water after process can reach one-level A or the discharge of surface water IV class standard, or enter follow-up reclaiming system and carry out desalting processing and be back to boiler feedwater.This detailed description of the invention energy Continuous Wastewater Treatment, has that disposal ability is strong and the feature of high treating effect.
It it is this utility model two-stage catalytic ozonation advanced waste treatment apparatus schematic diagram of another kind of detailed description of the invention shown in Fig. 3.In this embodiment, the first water distribution gas distribution district 103 of described first catalytic ozonation reactor 1 connects with the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2.This embodiment is with the difference of Fig. 2 illustrated embodiment, and present embodiment is intermittent flow operational mode.After waste water fully processes in the first catalytic ozonation reactor 1, waste water is incorporated into the second water distribution gas distribution district 203 of the second catalytic ozonation reactor 2, then, in the second catalytic ozonation reactor 2, waste water is constantly and ozone, catalyst haptoreaction.
This utility model the first catalytic ozonation reactor 1 and the second catalytic ozonation reactor 2 can use many series connection continuous processings or the mode of batch process according to situations such as the flows of waste water.
Two-stage catalytic ozonation advanced waste treatment system described in the utility model, has continuously stream operational mode and two kinds of tupes of intermittent flow operational mode, has that disposal ability is strong and the feature of high treating effect.This utility model equipment is applicable to process the waste water that COD (COD) content is high, can effectively reduce the COD content in waste water, the most also can apply to TDS content high, the difficult waste water that pH value is high.The water outlet COD that this utility model processes can reach one-level A even surface water IV class standard, and compared with existing high-level oxidation technology, water percentage ratio up to standard is greatly improved, and operating cost is substantially reduced, and has good economic benefit.
Above according to desirable embodiment of the present utility model for enlightening, by above-mentioned description, relevant staff can carry out various change and amendment completely in the range of without departing from this utility model technological thought.The content that the technical scope of this utility model is not limited in description, it is necessary to determine its poly-talented scope according to right.
Embodiment and comparative example measure COD (COD) with potassium dichromate for oxidant.
It is measured with the potassium bichromate solution of 0.25mol/L concentration.
Reflux: the full glass refluxing unit of band 250mL conical flask.
Heater: electric hot plate or variable resistance electric furnace.
Ferroin indicator solution: weigh 1.485g neighbour phenanthrene quinoline (C12H8N2H2O), 0.695g ferrous sulfate (FeSO4 7H2O) soluble in water, it is diluted to 100mL, is stored in brown bottle.
Ferrous ammonium sulfate standard solution: weigh 39.5g Ferrous ammonium sulfate (C (NH4)2Fe(SO4)2 6H2O) soluble in water, it is slowly added into 20mL concentrated sulphuric acid while stirring, moves in 1000mL volumetric flask after cooling, be diluted with water to graticule, shake up.Before use, demarcate with potassium dichromate standard solution.Scaling method: absorption 10.00mL potassium dichromate standard solution, in 500mL conical flask, is diluted with water to about 110mL, is slowly added to 30mL concentrated sulphuric acid, mixing.After cooling, adding 3 examinations ferrous iron record indicator solution (about 0.15mL), titrate with Ferrous ammonium sulfate, the color from yellow of solution is terminal through aeruginous to bronzing.
C=0.2500 × 10.00/V
In formula: C-Ferrous ammonium sulfate standard solution concentration, mol/L；The consumption of V-Ferrous ammonium sulfate standardized titration, mL.
Sulphuric acid-silver sulfate solution: add 25g silver sulfate in 2500mL concentrated sulfuric acid solution.Placing 1～2 day, shake frequently makes it dissolve.
Mercury bisulfate.: crystallization or powder.
Experimental procedure: take the water sample of 20.00mL mix homogeneously, put the backflow conical flask of 250mL ground, accurately add 10.00ml 0.25mol/L potassium dichromate standard solution and several clean beades or zeolite, connect ground reflux condensing tube, it is slowly added 30ml sulphuric acid-silver sulfate solution from condensing tube is suitable for reading, being shaken gently for conical flask makes solution mix, and is heated to reflux 2 hours (timing when certainly coming to life).
After cooling, slowly rinse condensation tube wall with 90mL water from top, take off conical flask.Overall solution volume must not be less than 140mL, and otherwise too big because of acidity, titration end-point is inconspicuous.
Solution cool down once again or, add three ferroin indicators, titrate with Ferrous ammonium sulfate standard solution, the color from yellow of solution is terminal through aeruginous to bronzing, the consumption of record Ferrous ammonium sulfate standard solution.
While measuring water sample, with 20.00mL distilled water, make blank assay by same operating procedure.The consumption of Ferrous ammonium sulfate standard solution when record titration is blank.
Data process CODcr concentration (with O2Meter) in the examination of (mg/L)=(V0-V1) × C × 8 × 1000/V: the concentration of C-Ferrous ammonium sulfate standard solution, mol/L；
The consumption of Ferrous ammonium sulfate standard solution, mL when V0-titration is blank；
The consumption of Ferrous ammonium sulfate standard solution, mL during V1-Titration Water Sample；
The volume of V-water sample, mL；
8-oxygen (1/2O) molal weight, g/mol.
Embodiment and comparative example, with TDS tester test TDS (total dissolved solidss), use Bante520 tester.
Embodiment and comparative example test pH value with pH meter, use the pH meter of model ECPH70042S of Thermo company.
Embodiment 1:
The intermittent duty mode shown in Fig. 3 of employing processes waste water.First catalytic ozonation reactor 1 uses 316L tank body, and a size of φ 3.6 × 8m (effective water level 7.5m), quantity is 6.Each reactor runs in turn, i.e. uses periodic running mode, every water inlet 0.5h, reacts 2h, draining 0.5h.Catalyst filling rate (catalyst zone volume accounts for catalysis tank body or the ratio of cell body cumulative volume) is 50%.Ozone dosage is 15kg/h.Water circulating pump flow is 50m3/ h, runs in the 2h of reactor reaction always.
Second catalytic ozonation reactor 2 uses 316L tank body, a size of φ 3.6 × 6.7m (effective water level 6.2m), quantity 2.Use continuously-running duty, current bottom in and top out, react 0.5h.Catalyst filling rate (catalyst zone volume accounts for catalysis tank body or the ratio of cell body cumulative volume) is 40%.Ozone dosage is 2kg/h.
Processing the dense water of RO (the dense water of first-stage reverse osmosis) of certain titanium dioxide industry waste water, the water yield is 100m3/ h, COD are 220-250mg/L, belong to the industrial wastewater of difficult degradation, can not biochemical treatment, require after process water outlet COD require below 60mg/L.
After described two-stage catalytic ozonation advanced waste treatment system, when water COD is 224mg/L～232mg/L, (TDS (total dissolved solidss) is 26700mg/L, pH is 11.2), the first catalytic ozonation reactor 1 water outlet COD after reaction 2h is 85～100mg/L, then the water outlet COD after the second catalytic ozonation reactor 2 reacts 30min is at about 45mg/L.
Embodiment 2:
The intermittent duty mode shown in Fig. 3 of employing processes waste water.First catalytic ozonation reactor 1 uses concrete sump, a size of 4 × 4 × 6.5m (effective water level 6.0m).First catalytic ozonation reactor 1 quantity totally 24, is divided into 4 series, each serial 6.4 series of the first catalytic ozonation reactor 1 are run simultaneously, and 6 block response devices of each series run in turn, i.e. use periodic running mode, every block response device water inlet 0.2h, react 0.8h, draining 0.2h.Every block response device catalyst filling rate (catalyst zone volume accounts for catalysis tank body or the ratio of cell body cumulative volume) is 40%.Ozone dosage is 60kg/h.Water circulating pump flow is 80m3/ h, runs in the 0.8h of reactor reaction always.
Second catalytic ozonation reactor 2 uses concrete sump, a size of 4 × 4 × 6.5m (effective water level 6.0m).Second catalytic ozonation reactor 2 quantity totally 12, is divided into 4 series, each serial 3.4 series of the second catalytic ozonation reactor 2 are run simultaneously, and each series uses continuously-running duty, current upper entering and lower leaving, reacts 0.4h.Catalyst filling rate (catalyst zone volume accounts for catalysis tank body or the ratio of cell body cumulative volume) is 42%.Ozone dosage is 10kg/h.
Processing certain chemical industrial park sewage qualified discharge, the water yield is 30000m3/ d, this garden is four big pillar industries with petrochemical industry, salt chemical engineering, fine chemistry industry, biochemical industry.Sewage water outlet COD after concentrating biochemical treatment in garden is 150～about 250mg/L, pH 7.0～8.0, TDS 6500～7500, but final COD discharge index requires as below 60mg/L.
After described two-stage catalytic ozonation advanced waste treatment system, when water COD is 200mg/L, (TDS is 6850mg/L, pH is 7.3), the first catalytic ozonation reactor 1 water outlet COD after reaction 0.8h is at about 90mg/L, then the water outlet COD after the second catalytic ozonation reactor 2 reacts 0.4h is at about 45mg/L.
Claims (8)
1. the wastewater treatment equipment of a two-stage catalytic ozonation, it is characterised in that include the first catalytic ozonation reactor (1) and the second catalytic ozonation reactor (2)；
Described first catalytic ozonation reactor (1) includes the first catalysis tank body or cell body (101), is arranged on the first catalysis tank body or the first ozone district (102), the first water distribution gas distribution district (103), the first catalyst zone (104), the first clear water zone (105) and the first gas collection district (106) of cell body (101) inside the most from down to up；Described first clear water zone (105) is interconnected with the first water distribution gas distribution district (103)；
Described second catalytic ozonation reactor (2) includes the second catalysis tank body or cell body (201), is arranged on the second catalysis tank body or internal the second ozone district (202), the second water distribution gas distribution district (203), the second catalyst zone (204), the second clear water zone (205) and the second gas collection district (206) of cell body (201) the most from down to up；
First clear water zone (105) of described first catalytic ozonation reactor (1) connects with the second water distribution gas distribution district (203) of the second catalytic ozonation reactor (2)；Or the first water distribution gas distribution district (103) of described first catalytic ozonation reactor (1) connects with the second water distribution gas distribution district (203) of the second catalytic ozonation reactor (2).
Wastewater treatment equipment the most according to claim 1, it is characterised in that described the second clear water zone (205) does not mutually connect with the second water distribution gas distribution district (203).
Wastewater treatment equipment the most according to claim 1, it is characterized in that, described first catalytic ozonation reactor (1) also includes the first ozone tail gas destructor (107), is arranged on the first catalysis tank body or top outer of cell body (101) of the first catalytic ozonation reactor (1)；Described second catalytic ozonation reactor (2) also includes the second ozone tail gas destructor (207), is arranged on the second catalysis tank body or top outer of cell body (201) of the second catalytic ozonation reactor (2).
Wastewater treatment equipment the most according to claim 3, it is characterized in that, described first clear water zone (105) and the first water distribution gas distribution district (103) are interconnected by being arranged on first water circulating pump (109) of the first catalysis tank body or cell body (101) outside.
Wastewater treatment equipment the most according to claim 1, it is characterised in that described first ozone district (102) connects ozonator by the first ozone import (1021)；Described second ozone district (202) connects ozonator by the second ozone import (2021).
Wastewater treatment equipment the most according to claim 1, it is characterized in that, described first catalysis tank body or cell body (101), being 4-9 rice with the whole height of the second catalysis tank body or cell body (201), the first water distribution gas distribution district (103) and the second water distribution gas distribution district (203) that arrange bottom it are highly 0.5-0.8 rice.
Wastewater treatment equipment the most according to claim 6, it is characterised in that by volume, described first catalyst zone (104) volume accounts for the first catalysis tank body or the 30%-70% of cell body (101) cumulative volume；Second catalyst zone (204) accounts for the second catalysis tank body or the 30%-70% of cell body (201) cumulative volume.
Wastewater treatment equipment the most according to claim 1, it is characterised in that described first water distribution gas distribution district (103) sidepiece is provided with the first waste water inlet (108)；Described second water distribution gas distribution district (203) sidepiece is provided with the second waste water inlet (208).
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| CN108069498A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of new organic wastewater treatment process |
| CN108069496A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of technique using catalytic wet ozone Oxidation Treatment organic wastewater |
| CN108069501A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of technique for handling organic wastewater |
| CN115784416A (en) * | 2022-11-30 | 2023-03-14 | 达斯玛环境科技（北京）有限公司 | Treatment method of characteristic pollutants in sewage and wastewater and application thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108069498A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of new organic wastewater treatment process |
| CN108069496A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of technique using catalytic wet ozone Oxidation Treatment organic wastewater |
| CN108069501A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of technique for handling organic wastewater |
| CN107010760A (en) * | 2017-05-26 | 2017-08-04 | 青岛华水节能环保科技有限公司 | The deep treatment method and device of Drinking Water |
| CN115784416A (en) * | 2022-11-30 | 2023-03-14 | 达斯玛环境科技（北京）有限公司 | Treatment method of characteristic pollutants in sewage and wastewater and application thereof |
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