CN110316861A - Strengthen up flow type multiphase wastewater oxidation treatment process and processing system - Google Patents
Strengthen up flow type multiphase wastewater oxidation treatment process and processing system Download PDFInfo
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- CN110316861A CN110316861A CN201910551143.4A CN201910551143A CN110316861A CN 110316861 A CN110316861 A CN 110316861A CN 201910551143 A CN201910551143 A CN 201910551143A CN 110316861 A CN110316861 A CN 110316861A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 121
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 71
- 230000003647 oxidation Effects 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 51
- 238000012545 processing Methods 0.000 title claims abstract description 47
- 230000008569 process Effects 0.000 title claims abstract description 42
- 239000007788 liquid Substances 0.000 claims abstract description 93
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 81
- 238000007872 degassing Methods 0.000 claims abstract description 71
- 238000005189 flocculation Methods 0.000 claims abstract description 47
- 230000016615 flocculation Effects 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 47
- 238000004062 sedimentation Methods 0.000 claims abstract description 45
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910052742 iron Inorganic materials 0.000 claims abstract description 19
- 230000000694 effects Effects 0.000 claims abstract description 13
- 239000004568 cement Substances 0.000 claims abstract description 12
- 239000006228 supernatant Substances 0.000 claims abstract description 12
- 238000003825 pressing Methods 0.000 claims abstract description 6
- 230000003472 neutralizing effect Effects 0.000 claims description 36
- 238000007172 homogeneous catalysis Methods 0.000 claims description 23
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 22
- 238000005273 aeration Methods 0.000 claims description 19
- 230000001590 oxidative effect Effects 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 14
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 13
- 230000003197 catalytic effect Effects 0.000 claims description 12
- 238000006386 neutralization reaction Methods 0.000 claims description 11
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 10
- 239000003814 drug Substances 0.000 claims description 10
- 230000015556 catabolic process Effects 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 9
- 238000006731 degradation reaction Methods 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 229910017052 cobalt Inorganic materials 0.000 claims description 7
- 239000010941 cobalt Substances 0.000 claims description 7
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 7
- 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 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000000377 silicon dioxide Substances 0.000 claims description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000011017 operating method Methods 0.000 claims description 2
- 238000005728 strengthening Methods 0.000 claims 9
- 239000004744 fabric Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 7
- 230000001376 precipitating effect Effects 0.000 abstract description 6
- 239000012028 Fenton's reagent Substances 0.000 abstract description 4
- 230000003014 reinforcing effect Effects 0.000 abstract description 4
- 239000010802 sludge Substances 0.000 abstract description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 25
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000003054 catalyst Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 6
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 6
- 230000000593 degrading effect Effects 0.000 description 5
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 5
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 5
- 239000005416 organic matter Substances 0.000 description 5
- 238000007792 addition Methods 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 4
- 238000006385 ozonation reaction Methods 0.000 description 4
- 230000032258 transport Effects 0.000 description 4
- -1 Hydroxyl radical free radical Chemical class 0.000 description 3
- 239000000356 contaminant Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 229910052603 melanterite Inorganic materials 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910021580 Cobalt(II) chloride Inorganic materials 0.000 description 2
- 229910021380 Manganese Chloride Inorganic materials 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000011790 ferrous sulphate Substances 0.000 description 2
- 235000003891 ferrous sulphate Nutrition 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- 239000011565 manganese chloride Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 238000009938 salting Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000005518 electrochemistry Effects 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012806 monitoring device Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910001453 nickel ion Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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
The invention discloses a kind of reinforcing up flow type multiphase wastewater oxidation treatment process and processing system, which includes the up flow type multiphase wastewater oxidation system successively to connect, solid-liquid separation system, neutralizes degassing system and flocculation sedimentation system.The treatment process includes the following steps: that 1) waste water enters up flow type multiphase wastewater oxidation system progress oxidation processes；2) waste water is sent into solid-liquid separation system and is separated by solid-liquid separation, the heterocatalysis carrier isolated is returned into up flow type multiphase wastewater oxidation system, waste water is sent into and neutralizes degassing system；3) waste water is sent into the degassing system that neutralizes, adjusting wastewater pH to 5.5~7.5, then is stirred degassing；4) waste water is sent into flocculation sedimentation system and carries out mud-water separation, by supernatant outlet, harmless treatment will be transported outward after precipitating iron cement filters pressing.Using present invention process and system, the treatment effect of multiphase wastewater oxidation processing system can be improved, Fenton reagent dosage is reduced, effectively reduces the generation of chemical sludge.
Description
Technical field
The present invention relates to method for processing organic wastewater, specifically a kind of reinforcing up flow type multiphase wastewater oxidation treatment process and
Processing system.
Background technique
The technology of processing bio-refractory waste water includes Ozonation, active carbon adsorption, Fenton oxidation method etc. at present,
Wherein Fenton oxidation method (H2O2/Fe2+) it is a kind of most efficient, simple and economic method.
The group of ferrous salt (such as ferrous sulfate) and hydrogen peroxide (hydrogen peroxide) is collectively referred to as Fenton reagent, it can the efficient oxidation
The hardly degraded organic substance that removal conventional waste water processing technique not can be removed, its essence is H2O2In Fe2+Catalytic action under generate
Hydroxyl radical free radical (OH) with high reaction activity, OH can be reacted with most of organic matters makes its degradation.
In a broad sense, the effects of Fenton method is using catalyst or electrochemistry, passes through H2O2It is organic to generate OH processing
The technology of object.But a large amount of Fe is needed during simple Fenton oxidation method2+Dosage to maintain enough OH to generate,
A large amount of iron cements can be generated in treatment process, need additional processing cost.It is likely present the extremely difficult degradation of organic substances in part simultaneously
Or remaining organic matter is not degraded.The Fenton iron cement of conventional homogeneous is more, and oxidation efficiency is low；The catalyst loss of traditional out-phase Fenton
Greatly, it produces and processes newly generated iron cement in operational process and adheres to more metal bondings into catalyst, catalyst efficiency is caused to decline.
Summary of the invention
The technical problems to be solved by the invention provide a kind of reinforcing up flow type multiphase wastewater oxidation treatment process and processing
System, the treatment process combine homogeneous catalysis technology, carrier heterocatalysis technology, ozonation aerated catalysis technique, fully urge
Change Fenton's reaction process, and utilize the secondary degradation residual organic matter of remaining hydrogen peroxide, enhances traditional up flow type multiphase waste water
The processing capacity of processing system.
The present invention solves above-mentioned technical problem with following technical solution:
The present invention strengthens up flow type multiphase wastewater oxidation treatment process, including following operating procedure:
(1) oxidation processes: organic wastewater with difficult degradation thereby is sent into up flow type multiphase wastewater oxidation system, which includes upstream
Formula multiphase wastewater oxidation tower adds Fenton medicament, homogeneous catalysis promotor and heterocatalysis carrier in oxidizing tower；
(2) solid-liquid separation treatment: the waste water after will be oxidation-treated, which is sent into solid-liquid separation system, to carry out at separation of solid and liquid
The liquid isolated is sent into and neutralizes degassing system, while the heterocatalysis carrier for isolating the overlay film in oxidizing tower being sent by reason
It is back in oxidizing tower, realizes the effect of enriched catalytic agent；
(3) it neutralizes degassing process: solid-liquid separation system treated waste water being sent into and neutralizes degassing system, neutralize degassing system
System includes the neutralizing tower and degassing tower being connected, and waste water first mixes in neutralizing tower with the lye added, is adjusted to wastewater pH
5.5~7.5, degassing is then stirred in degassing tower；
(4) flocculation sedimentation is handled: the waste water after neutralization degassing process being sent into flocculation sedimentation system and carries out mud-water separation, wadding
Solidifying settling system includes flocculation sedimentation tank, and waste water, by the supernatant outlet on flocculation sedimentation tank top, will flocculate after flocculation sedimentation
Harmless treatment is transported outward after precipitating the iron cement filters pressing of bottom of pond portion.
In the step 1), the dosage of Fenton medicament routinely requires to add, and heterocatalysis carrier is before system starting
It adds, dosage is the 1/10~1/3 of up flow type multiphase wastewater oxidation tower volume.
In step 1), the homogeneous catalysis promotor is liquid homogeneous catalysis promotor, contains iron, manganese, cobalt, micro-Ni
Element, wherein 10~20mg/L of concentration of iron, 5.0~15mg/L of concentration of manganese, 1.0~3.0mg/L of concentration of cobalt, the concentration of nickel
0.5~1.0mg/L.
In the step 1), heterocatalysis carrier is diagonal in the spherical heterocatalysis carrier of 2~5mm or maximum using diameter
Distance is the polyhedron heterocatalysis carrier of 2~5mm, and material is the inorganic carrier of ceramics, silica or activated alumina,
Or the organic inert carrier for PVA or PVE.
In step 1), up flow type multiphase wastewater oxidation system in the process of running, when homogeneous catalysis promotor adds for the first time,
It is added according to 1~the 5 ‰ of processing water, and continuous 5~10 days benefits throw and maintain this amount；Hereafter after every subsystem sediment outflow, continue by
It mends to throw according to 1~the 5 ‰ of processing water and maintain, and continuously add 3~5 days.
In step 2), the solid-liquid separation system carries out the separate mode that fluid blocks using inclined plate, inclined tube or arresting net,
Or by the way of eddy flow centrifuge separation, gravity separation separation.
In step 3), the bottom of the neutralizing tower and degassing tower be passed through containing ozone mass concentration be 1%~10% it is mixed
It closes air and carries out aeration stirring and gas stripping, the processing time in neutralizing tower is 15~25min, and the processing time of degassing tower is
20~30min.
In the step 4), the processing time of flocculation sedimentation tank is 2~3 hours.
The present invention strengthens the processing system that up flow type multiphase wastewater oxidation treatment process uses, including the upstream successively to connect
Formula multiphase wastewater oxidation system, neutralizes degassing system and flocculation sedimentation system at solid-liquid separation system；
The up flow type multiphase wastewater oxidation system includes up flow type multiphase wastewater oxidation tower, up flow type multiphase wastewater oxidation
The bottom of tower is equipped with water distribution cover, and inside is filled with heterocatalysis carrier, and top is equipped with solid-liquid separator, water distribution cover and separation of solid and liquid
Device is located at the following above and of heterocatalysis carrier, the top of solid-liquid separator be equipped with water inlet A and with water inlet A phase
The fill cycle slot of connection, fill cycle slot are connected through circulation pipe with the water distribution cover of bottom, and circulation is equipped on the circulation pipe
The top of pump, solid-liquid separator is equipped with water outlet A；
The solid-liquid separation system includes cyclone separator, and the top of cyclone separator is equipped with and up flow type multiphase waste water oxygen
Change the water inlet B that the water outlet A of tower is connected, bottom is equipped with drain pipe, and the inside of cyclone separator, which is equipped with, is delivered up waste water
Central tube, the top of central tube is equipped with water outlet B；
The neutralization degassing system includes neutralizing tower and degassing tower, and the bottom of neutralizing tower and degassing tower is respectively equipped with and can be passed through
The top of the microporous aeration disc of ozone-air and pure oxygen, neutralizing tower and degassing tower is respectively equipped with gas-liquid two-phase separator, gas-liquid two
The top of phase separator connects gas-liquid separator through pipeline, and gas-liquid separator is equipped with the down-comer for protruding into tower lower part, neutralizing tower
Lower part is equipped with the water inlet C being connected with the water outlet B of solid-liquid separation system, and the top of neutralizing tower is equipped with positioned at gas-liquid two-phase point
From the water outlet C above device, the bottom of degassing tower is equipped with the water inlet D being connected with water outlet C, and the top of degassing tower is equipped with position
Water outlet D above gas-liquid two-phase separator；
The flocculation sedimentation system includes flocculation sedimentation tank, and flocculation sedimentation tank is connected with the water outlet D of degassing tower, flocculation
The top of sedimentation basin is equipped with supernatant discharge outlet, and bottom is equipped with mud discharging mouth.
The gas discharge outlet of the gas-liquid separator connects two pipeline branches with parallel way, wherein a branch and two
Manganese oxide sizer is connected, and another branch is connected by the air inlet pipe of booster fan and microporous aeration disc.
Compared with prior art, the present invention having the following beneficial effects:
1) present invention is in original up flow type multiphase wastewater oxidation system by adding homogeneous catalysis promotor and out-phase
The mode of catalytic carrier improves the ability of oxidative system catalytic degradation organic matter, reduces Fenton added amount of chemical；
2) present invention can constantly supplement carrier surface by using the mode of regular addition homogeneous catalysis promotor
Catalytic activity point, keeps the catalytic performance of different-phase catalyst；
3) heterocatalysis carrier can be retained preferably in systems, be made by increasing solid-liquid separation system by the present invention
It persistently plays a role；
4) present invention in and and degassing process in mixed and expose jointly using certain density ozone and air, in maintenance one
While determining aeration quantity, the ozone being passed through can occur catalysis with hydrogen peroxide remaining in water and react, and secondary oxidation process occurs,
The treatment effect of raising system reduces medicament residual.
Detailed description of the invention
Fig. 1 is the operating process schematic diagram that the present invention strengthens up flow type multiphase wastewater oxidation treatment process.
Fig. 2 is that the present invention strengthens the up flow type multiphase wastewater treatment oxygen used in up flow type multiphase wastewater oxidation processing system
Change the structural schematic diagram of tower.
Fig. 3 is the structural representation that the present invention strengthens the cyclone separator used in up flow type multiphase wastewater oxidation processing system
Figure.
When Fig. 4 is that the neutralizing tower used in present invention reinforcing up flow type multiphase wastewater oxidation processing system is connect with degassing tower
Structural schematic diagram.
Fig. 5 is the structural representation that the present invention strengthens the flocculation sedimentation tank used in up flow type multiphase wastewater oxidation processing system
Figure.
In figure: 1- up flow type multi-phase waste-water processing oxidation tower；2- water outlet A；3- fill cycle slot；4- water inlet A；5- is different
Phase catalytic carrier；6- solid-liquid separator；7- circulation pipe；8- circulating pump；9- water distribution cover；10- cyclone separator；11- central tube；
12- drain pipe；13- neutralizing tower；14- gas-liquid two-phase separator；15- gas-liquid separator；16- down-comer；17- microporous aeration disc；
18- manganese dioxide sizer；19- degassing tower；20- flocculation sedimentation tank, 21- water inlet B, 22- water outlet B, 23- water inlet C,
24- water outlet C, 25- water inlet D, 26- water outlet D, 27- supernatant discharge outlet, 28- mud discharging mouth, 29- booster fan.
Specific embodiment
In order to illustrate more clearly for the treatment of process of the present invention, in the following with reference to the drawings and specific embodiments to technology of the invention
Scheme makees further unrestricted detailed description.
As shown in Figure 1, the processing system that treatment process of the present invention uses includes up flow type multiphase waste water treatment system, solid-liquid
Separation system neutralizes degassing system, flocculation sedimentation system.
As shown in Fig. 2, up flow type multiphase wastewater oxidation system of the present invention includes up flow type multiphase wastewater oxidation tower 1,
The bottom of up flow type multiphase wastewater oxidation tower 1 is equipped with water distribution cover 9, and inside is filled with heterocatalysis carrier 5, and top is equipped with solid-liquid point
From device 6, water distribution cover 9 and solid-liquid separator 6 are located at the following above and of heterocatalysis carrier 5, the top of solid-liquid separator 6
Equipped with water inlet A 4 and the fill cycle slot 3 being connected with water inlet A 4, fill cycle slot 3 is through circulation pipe 7 and bottom
Water distribution cover 9 is connected, and circulating pump 8 is equipped on the circulation pipe 7, and the top of solid-liquid separator 6 is equipped with water outlet A 2.
As shown in figure 3, the solid-liquid separation system includes cyclone separator 10, the top of cyclone separator 10 be equipped with it is upper
The water inlet B 21 that the water outlet A 2 of streaming multiphase wastewater oxidation tower 1 is connected, bottom are equipped with drain pipe 12, cyclone separator
10 inside is equipped with the central tube 10 for being delivered up waste water, and the top of central tube 10 is equipped with water outlet B 22.
As shown in figure 4, the neutralization degassing system includes neutralizing tower 13 and degassing tower 19, neutralizing tower 13 and degassing tower 19
Bottom is respectively equipped with the microporous aeration disc 17 that can be passed through ozone-air and pure oxygen, and the top of neutralizing tower 13 and degassing tower 19 is set respectively
There is gas-liquid two-phase separator 14, the top of gas-liquid two-phase separator 14 connects gas-liquid separator 15, gas-liquid separator 15 through pipeline
Equipped with the down-comer 16 for protruding into 19 lower part of neutralizing tower 13 and degassing tower, the lower part of neutralizing tower 13 is equipped with to be gone out with solid-liquid separation system
The water inlet C 23 that mouth of a river B 22 is connected, the top of neutralizing tower 13 are equipped with the water outlet C being located above gas-liquid two-phase separator
24, the bottom of degassing tower 19 is equipped with the water inlet D 25 being connected with water outlet C 24, and the top of degassing tower 19, which is equipped with, is located at gas
The gas discharge outlet of water outlet D 26 above liquid two phase separator, gas-liquid separator 15 connect two pipeline branch with parallel way
Road, wherein a pipeline branch is connected with manganese dioxide sizer 18, another pipeline branch passes through booster fan 29 and micropore
The air inlet pipe of aeration plate 17 connects.
As shown in figure 5, the flocculation sedimentation system includes flocculation sedimentation tank 20, flocculation sedimentation tank 20 goes out with degassing tower 19
Mouth of a river D 26 is connected, and the top of flocculation sedimentation tank 20 is equipped with supernatant discharge outlet 27, and bottom is equipped with mud discharging mouth 28.
The specific operation process that the present invention strengthens up flow type multiphase wastewater oxidation treatment process is as follows:
The first step, organic wastewater with difficult degradation thereby initially enter up flow type multiphase wastewater oxidation system, which includes up flow type
Multiphase wastewater oxidation tower 1.Organic wastewater with difficult degradation thereby enters up flow type multi-phase waste-water processing oxidation tower 1 through water inlet A 4 first and pushes up
The fill cycle slot 3 in portion, the interior addition of fill cycle slot 3 is by ferrous sulfate and H2O2The Fenton reagent and homogeneous catalysis of composition promote
Into agent, waste water enters the water distribution cover 9 of 1 bottom of up flow type multiphase wastewater oxidation tower through circulation pipe 7 after mixing with medicament, waste water is through oxygen
It is separated by solid-liquid separation again through solid-liquid separator 6 after change processing, subsequent processing is then discharged by water outlet A 2.
In this step, waste water is mixed with Fenton reagent first, is formed the OH with high reaction activity and is divided with organic matter
Son reacts, and macromolecule organic is degraded to small organic molecule, under the good fluidized state of system, Fenton medicine
Agent comes into full contact with homogeneous catalysis promotor, and more OH are generated under catalytic action and participate in reaction；Homogeneous catalysis promotees simultaneously
Into the metallic element and Fe in agent2+And H2O2The Fe of generation3+5 surface of heterocatalysis carrier is adsorbed onto a manner of crystallizing or precipitate
On, heterocatalysis particle, this part heterocatalysis particle and homogeneous catalysis promotor collective effect are formed, oxidative system is improved
Treatment effeciency.
The dosage of Fenton medicament described in the step routinely requires to add, and heterocatalysis carrier is before system starting
It adds, dosage is the 1/10~1/3 of up flow type multiphase wastewater oxidation tower volume；Heterocatalysis carrier is using diameter in 2~5mm
Spherical heterocatalysis carrier or maximum diagonal distance be 2~5mm polyhedron heterocatalysis carrier, material is ceramics, two
The inorganic carrier of silica or activated alumina, or the organic inert carrier for PVA, PVE.
The homogeneous catalysis promotor is liquid homogeneous catalysis promotor, contains but be not limited to the sun of iron, manganese, cobalt, nickel
Ion microelement, wherein 10~20mg/L of concentration of iron, 5.0~15mg/L of concentration of manganese, cobalt 1.0~3.0mg/L of concentration,
0.5~1.0mg/L of concentration of nickel.
In up flow type multiphase wastewater oxidation tower operational process, dosage is according to processing water to homogeneous catalysis promotor for the first time
1~5 ‰ additions of amount, and continuous 5~10 days benefits throw and maintain this amount；Hereafter after every subsystem sediment outflow, continue according to processing water
1~5 ‰ mend to throw and maintain, and continuously add 3~5 days.
Up flow type multiphase wastewater oxidation system treated waste water is sent into solid-liquid separation system, the solid-liquid by second step
Cyclone separator 10 can be used in separation system.The water outlet of up flow type multiphase wastewater oxidation tower 1 enters cyclonic separation through water outlet A 2
Device 10, the heterocatalysis carrier 5 partially flowing to inside cyclone separator 10 are enriched in cyclone separator 10 by cyclonic action
Bottom, reach activating and regenerating and reuse can be discharged after certain amount by drain pipe 12, and the waste water isolated through central tube 10,
Water outlet B 24 enters subsequent processing after being discharged.
The solid-liquid separation system can carry out the separate mode that fluid blocks using inclined plate, inclined tube or arresting net, can also
In a manner of using eddy flow centrifuge separation, gravity separation separation.
The waste water isolated is entered and neutralizes degassing system by third step, and the neutralization degassing system includes in being connected
With tower 13 and degassing tower 19.Waste water initially enters neutralizing tower 13, lye is added in neutralizing tower 13, while at the bottom of neutralizing tower 13
Portion is passed through the mixing air for being 1%~10% containing ozone mass concentration through the air inlet pipe of microporous aeration disc 17 and its connection and carries out
Aeration stirring, processing time are 15~25min, and pH value of waste water is made to be adjusted to 5.5~7.5, then pass through gas-liquid two-phase separator
Waste water is carried out gas-liquid separation processing by 14, then waste water is sent into degassing tower 19, addition PAM solution in degassing tower 19, while
The mixing air that it is 1%~10% containing ozone mass concentration that the bottom of degassing tower 19, which is passed through, carries out gas stripping, handles the time
For 20~30min, waste water is then subjected to gas-liquid separation processing by gas-liquid two-phase separator 14, then waste water is sent into flocculation and is sunk
Shallow lake system.
The gas-liquid two-phase separator 14 can collect the carbon dioxide gas that reaction generates and unreacted is completely residual
Stay ozone gas.The gas-liquid separator 15 separates the waste water mixed liquor come in air lift and residue ozone or air, pure oxygen are mixed
Close gas.The settable ozone concentration in 15 top of gas-liquid separator and air pressure monitoring device, when ozone concentration in gas-liquid separator 15
When higher, the mixed gas in gas-liquid separator is delivered to neutralizing tower by booster fan 29 and degassing tower bottom carries out again
Aeration, so that remaining ozone is fully used, and is occurred advanced catalysis with hydrogen peroxide and is reacted, while neutralizing tower is added
The PAM solution that liquid alkaline and degassing tower are added plays stirring action, until monitoring ozone concentration and pressure in gas-liquid separator
Power is unsatisfactory for utilizing requirement again.When the mixed gas in gas-liquid separator is unsatisfactory for again using requiring, by mixed gas
It drains into manganese dioxide sizer 18 and absorbs remaining low concentration ozone, so that the mixed gas of discharge meets emission request.
Mass-transfer efficiency can be improved by micro-pore aeration in the step, and waste water makes wherein residual under the aeration effect of ozone
The hydrogen peroxide stayed is catalytically decomposed, and newborn OH is formed, and is further reacted in remaining small organic molecule, is realized secondary oxygen
Change degradation.
4th step will be sent into flocculation sedimentation system, flocculation sedimentation system packet by neutralizing degassing system treated waste water
Flocculation sedimentation tank 20 is included, waste water enters in flocculation sedimentation tank 20, and flocculation sedimentation occurs in pond with the flocculant added, precipitating
Sludge (iron cement) is ejected after gravity concentration by mud discharging mouth 28, and through being dehydrated filters pressing, then outward transport carries out innoxious place
Reason, and the supernatant on sedimentation basin top is through 27 qualified discharge of supernatant discharge outlet；The processing time of flocculation sedimentation tank 20 is 2~3
Hour.
The working principle that the present invention strengthens up flow type multiphase wastewater oxidation processing system is as follows:
The present invention introduces the liquid containing the microelements such as iron ion and manganese, cobalt, nickel in up flow type multiphase waste water treatment system
State homogeneous catalysis promotor, by being periodically added in oxidative system together with Fenton medicament, transition metal is utilized in reaction process
The d track of discontented electronics can be catalyzed to the affinity of electronics and promote the migration of electronics during Fenton's reaction, improve reaction
Efficiency.And introduce the polyhedron out-phase that diameter is 2~5mm in the spherical heterocatalysis carrier of 2~5mm or maximum diagonal distance
Catalytic carrier will be thrown by suction-operated during heterocatalysis carrier fluidizes in oxidative system with water distribution with medicament
The adsorption of metal ions in homogeneous catalysis promotor added forms different-phase catalyst on heterocatalysis carrier.Although traditional is different
It mutually in catalysis Fenton system, after catalyst can be because be covered by iron cement, loses activity, but in present invention process, periodically throws
The homogeneous catalysis promotor added can be adsorbed constantly by carrier and the iron cement being attached on carrier, so that the surface layer of catalyst is always
There is catalytic activity bodies, solve the problems, such as catalyst activity reduction.
For heterocatalysis carrier at overlay film initial stage since partial size is smaller, density is smaller in order to prevent, is easy to be raised stream and take out of
Oxidative system, the present invention are specially provided with solid-liquid separation system, and the effect of solid-liquid separation system can be to greatest extent by out-phase
Catalytic carrier is retained in oxidative system, is reduced carrier and is added the frequency with changing.
By solid-liquid separation system treated water outlet the enters degassing system that neutralizes, traditional neutralization deaerates system master the present invention
If by adding hydrogen ion that alkali neutralization Fenton's reaction adds in the process and newly-generated, and passing through aeration effect for small molecule
Volatile organic matter and remaining part hydrogen peroxide stripping go out system.And in present invention process, using containing ozone mass concentration
For 1%~10% waste water of the mixing air aeration stirring after alkali neutralization, in the process ozone can with it is residual in mixed liquor
Advanced oxidation reaction occurs for the hydrogen peroxide stayed, releases OH, and residual organic contaminants of degrading further increase effluent quality.
Finally, will neutralize degassing system treated, water outlet will enter flocculation sedimentation tank, and iron cement is further in flocculation sedimentation tank
Flocculation sedimentation occurs, outward transport harmless treatment, supernatant standard water discharge row are carried out after precipitating sludge gravity concentration and dehydration
It puts.
It is application example of the invention below:
Example 1
Certain paper mill bio-chemical effluent is handled using treatment process of the present invention, raw wastewater COD365mg/L, coloration 80
Times.Waste water is pumped into fill cycle slot at the top of oxidizing tower by being promoted, adds H in fill cycle slot2O2And FeSO4·7H2O。
Two kinds of added amount of chemical are as follows: H2O2It is 1.5:1, i.e. H with COD mass ratio to be processed in waste water2O2Dosage is 547.5mg/L,
H2O2With Fe2+Molar ratio be 5:1, i.e. FeSO4·7H2O dosage is 895mg/L.Hold before processing system starting according to reactor
Long-pending 1/5 adds the silica crystals for the even width that maximum diagonal distance is 2mm, and according to the 1 ‰ of design treatment water
The homogeneous promotor of liquid is added, liquid homogeneous catalysis promotor uses FeSO4、CoCl2、NiSO4And MnCl2Salting liquid dilution
Configuration, wherein the mass concentration of Fe is 10mg/L, and the mass concentration of Mn is 10mg/L, and the mass concentration of Co is 2mg/L, the matter of Ni
Amount concentration is 0.5mg/L, is continuously added 3 days.
Waste water enters cyclone separator after oxidizing tower is discharged and separates 3~5min, then enters neutralizing tower and carries out in soda acid
With put into liquid alkaline in neutralizing tower, adjust pH to 6~7.5, neutralize tower bottom during this period and carry out ozonation aerated stirring, simultaneously
Ozone is reacted with hydrogen peroxide remaining in waste water, and some organic pollutants of degrading, 15~20min of this stage residence time.Through
Waste water after neutralization enters degassing tower, and degassing tower bottom microporous aeration disc is passed through ozone, is stirred degassing, deaerate 20~
30min, the PAM for adding 0.05mg/L forms wadding body, while ozone generates advanced oxygen with the remaining hydrogen peroxide in mixed liquor
Change reaction, while residual organic contaminants of further degrading.Waste water after degassing enters flocculation sedimentation tank, and flocculation sedimentation tank stops
Time 2~3 hours, mud-water separation is carried out, supernatant is discharged outlet, transports outward harmless treatment after precipitating iron cement filters pressing.After processing
Water outlet COD be down to 50mg/L, coloration is reduced to 5 times.
Example 2
The water outlet of certain starch factory biochemical waste water is handled using treatment process of the present invention, raw wastewater COD472mg/L, color
75 times of degree.Waste water is pumped into fill cycle slot at the top of oxidizing tower by being promoted, adds H in fill cycle slot2O2And FeSO4·
7H2O.Two kinds of added amount of chemical are as follows: H2O2It is 1.8:1, i.e. H with COD mass ratio to be processed in waste water2O2Dosage is 850mg/
L, H2O2With Fe2+Molar ratio be 12:1, i.e. FeSO4·7H2O dosage is 579mg/L.According to reaction before processing system starting
The 1/10 of device volume adds heterocatalysis carrier, heterocatalysis carrier by the silica crystals that maximum diagonal distance is 2mm and
The activated alumina ball that diameter is 5mm is mixed according to volume ratio 1:3 to be formed, and adds liquid according to the 3 ‰ of design treatment water
Homogeneous promotor, liquid homogeneous catalysis promotor use FeSO4、CoCl2、NiSO4And MnCl2Salting liquid dilute configuration, wherein
The mass concentration of Fe is 10mg/L, and the mass concentration of Mn is 10mg/L, and the mass concentration of Co is 2mg/L, and the mass concentration of Ni is
0.5mg/L is continuously added 3 days.
Waste water enters cyclone separator after oxidizing tower is discharged and separates 3~5min, then enters neutralizing tower and carries out in soda acid
With, liquid alkaline is put into neutralizing tower, to adjust pH to 5.5~7.5, is neutralized tower bottom during this period and is carried out ozonation aerated stirring,
Ozone is reacted with hydrogen peroxide remaining in waste water simultaneously, and some organic pollutants of degrading, and this stage residence time 20~
25min.Waste water after neutralized enters degassing tower, and degassing tower bottom microporous aeration disc is passed through ozone, is stirred degassing, deaerates
25~30min, the PAM that 0.05mg/L is added forms wadding body, while ozone is advanced with the remaining hydrogen peroxide generation in mixed liquor
Oxidation reaction, while residual organic contaminants of further degrading.Waste water after degassing enters flocculation sedimentation tank, and flocculation sedimentation tank stops
It stays the time 2~3 hours, carries out mud-water separation, supernatant is discharged outlet, transports outward harmless treatment after precipitating iron cement filters pressing.Processing
Water outlet COD afterwards is down to 56mg/L, and coloration is reduced to 4.5 times.
It is pointed out that the technical concept of above-described embodiment only to illustrate the invention, its object is to allow be familiar with this
The personage of technology cans understand the content of the present invention and implement it accordingly, and it is not intended to limit the scope of the present invention.All
According to equivalent change or modification made by spirit of the invention, should be covered by the protection scope of the present invention.
Claims (10)
1. strengthening up flow type multiphase wastewater oxidation treatment process, which is characterized in that including following operating procedure:
1) oxidation processes: organic wastewater with difficult degradation thereby is sent into up flow type multiphase wastewater oxidation system, which includes that up flow type is more
Phase wastewater oxidation tower adds Fenton medicament, homogeneous catalysis promotor and heterocatalysis carrier in oxidizing tower；
2) solid-liquid separation treatment: the waste water after will be oxidation-treated, which is sent into solid-liquid separation system, carries out solid-liquid separation treatment, will
The liquid isolated, which is sent into, neutralizes degassing system, while the heterocatalysis carrier for isolating the overlay film in oxidizing tower is returned to oxygen
Change in tower, realizes the effect of enriched catalytic agent；
3) it neutralizes degassing process: solid-liquid separation system treated waste water being sent into and neutralizes degassing system, neutralize degassing system packet
Include the neutralizing tower and degassing tower being connected, waste water first mixes in neutralizing tower with the lye added, make wastewater pH be adjusted to 5.5~
7.5, degassing is then stirred in degassing tower；
4) flocculation sedimentation is handled: the waste water after neutralization degassing process being sent into flocculation sedimentation system and carries out mud-water separation, flocculation is heavy
Shallow lake system includes flocculation sedimentation tank, waste water after flocculation sedimentation by the supernatant outlet on flocculation sedimentation tank top, by flocculation sedimentation
Harmless treatment is transported outward after the iron cement filters pressing of bottom of pond portion.
2. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that the step 1)
In, the dosage of Fenton medicament routinely requires to add, and heterocatalysis carrier is added before system starting, and dosage is upstream
The 1/10~1/3 of formula multiphase wastewater oxidation tower volume.
3. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that in step 1), institute
Stating homogeneous catalysis promotor is liquid homogeneous catalysis promotor, containing iron, manganese, cobalt, micro-Ni element, the wherein concentration 10 of iron
~20mg/L, 5.0~15mg/L of concentration of manganese, 1.0~3.0mg/L of concentration of cobalt, 0.5~1.0mg/L of concentration of nickel.
4. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that the step 1)
In, heterocatalysis carrier uses diameter in the spherical heterocatalysis carrier of 2~5mm or maximum diagonal distance for the multi-panel of 2~5mm
Body heterocatalysis carrier, material are the inorganic carrier of ceramics, silica or activated alumina, or having for PVA or PVE
Machine inert carrier.
5. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that in step 1), on
Streaming multiphase wastewater oxidation system in the process of running, homogeneous catalysis promotor for the first time dosage be according to processing water 1~
5 ‰ add, and continuous 5~10 days benefits throw and maintain this amount；Hereafter after every subsystem sediment outflow, continue 1~5 ‰ according to processing water
It mends to throw and maintain, and continuously add 3~5 days.
6. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that in step 2), institute
It states solid-liquid separation system and the separate mode that fluid blocks is carried out using inclined plate, inclined tube or arresting net, or be centrifugated using eddy flow,
The mode of gravity separation separation.
7. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that in step 3), institute
The mixing air that it is 1%~10% containing ozone mass concentration that the bottom for stating neutralizing tower and degassing tower, which is passed through, carry out aeration stirring and
Gas stripping, the processing time in neutralizing tower are 15~25min, and the processing time of degassing tower is 20~30min.
8. strengthening up flow type multiphase wastewater oxidation treatment process according to claim 1, which is characterized in that the step 4)
In, the processing time of the flocculation sedimentation tank is 2~3 hours.
9. according to claim 1 to 8 it is any it is described strengthen up flow type multiphase wastewater oxidation treatment process use processing systems,
It is characterized in that, including up flow type multiphase wastewater oxidation system, solid-liquid separation system, neutralization degassing system and the flocculation successively to connect
Settling system；
The up flow type multiphase wastewater oxidation system includes up flow type multiphase wastewater oxidation tower (1), up flow type multiphase wastewater oxidation
The bottom of tower is equipped with water distribution cover (9), and inside is filled with heterocatalysis carrier (5), and top is equipped with solid-liquid separator (6), water distribution cover
(9) and solid-liquid separator (6) is located at the following above and of heterocatalysis carrier (5), and the top of solid-liquid separator (6) is equipped with
Water inlet A (4) and the fill cycle slot (3) being connected with water inlet A, cloth of the fill cycle slot through circulation pipe (7) and bottom
Water cover is connected, and is equipped on the circulation pipe circulating pump (8), and the top of solid-liquid separator is equipped with water outlet A (2)；
The solid-liquid separation system includes cyclone separator (10), and the top of cyclone separator is equipped with and up flow type multiphase waste water oxygen
Change the water inlet B (21) that the water outlet A (2) of tower is connected, bottom is equipped with drain pipe (12), and the inside of cyclone separator (10) is set
There is the central tube (11) of upward transport wastewater, the top of central tube (11) is equipped with water outlet B (22)；
The neutralization degassing system includes neutralizing tower (13) and degassing tower (19), and the bottom of neutralizing tower and degassing tower is respectively equipped with can
It is passed through the microporous aeration disc (17) of ozone-air and pure oxygen, the top of neutralizing tower and degassing tower is respectively equipped with gas-liquid two-phase separator
(14), the top of gas-liquid two-phase separator connects gas-liquid separator (15) through pipeline, and gas-liquid separator (15) is equipped with and protrudes under tower
The down-comer (16) in portion, the lower part of neutralizing tower are equipped with the water inlet C being connected with the water outlet B (22) of solid-liquid separation system
(23), the top of neutralizing tower is equipped with the water outlet C (24) being located above gas-liquid two-phase separator, and the bottom of degassing tower is equipped with and goes out
The water inlet D (25) that mouth of a river C (24) is connected, the top of degassing tower are equipped with the water outlet D being located above gas-liquid two-phase separator
(26)；
The flocculation sedimentation system includes flocculation sedimentation tank (20), water outlet D (26) phase of flocculation sedimentation tank (20) and degassing tower
The top of connection, flocculation sedimentation tank (20) is equipped with supernatant discharge outlet (27), and bottom is equipped with mud discharging mouth (28).
10. strengthening the processing system that up flow type multiphase wastewater oxidation treatment process uses according to claim 9, feature exists
In the gas discharge outlet of the gas-liquid separator (15) connects two pipeline branches with parallel way, wherein a branch and two
Manganese oxide sizer (18) is connected, and another branch is connect by booster fan (29) with the air inlet pipe of microporous aeration disc (17).
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| CN201910551143.4A CN110316861A (en) | 2019-06-24 | 2019-06-24 | Strengthen up flow type multiphase wastewater oxidation treatment process and processing system |
| PCT/CN2019/094757 WO2020258359A1 (en) | 2019-06-24 | 2019-07-04 | Improved upflow multi-phase wastewater oxidation treatment process and system |
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| CN111018187A (en) * | 2019-12-25 | 2020-04-17 | 苏州希图环保科技有限公司 | Wastewater treatment process based on Fenton oxidation reaction |
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| CN106882866A (en) * | 2017-02-24 | 2017-06-23 | 河北科技大学 | The method that hydrogen peroxide synergy ozone heterogeneous catalytic oxidation processes waste water |
| KR20180006842A (en) * | 2017-06-05 | 2018-01-19 | 유흥케미칼(주) | Method of wastewater treatment using ferrous sulfate solution from industrial by-products |
| CN108191039B (en) * | 2018-02-24 | 2020-12-22 | 武汉纺织大学 | Efficient compound Fenton reagent and preparation method thereof |
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| CN101519251A (en) * | 2009-04-09 | 2009-09-02 | 广西大学 | Process for treating bio-refractory waste water by up-flow multi-phase oxidation column |
| CN202924850U (en) * | 2012-11-28 | 2013-05-08 | 北京市环境保护科学研究院 | Advanced wastewater oxidation system |
| JP2014198286A (en) * | 2013-03-29 | 2014-10-23 | 栗田工業株式会社 | Method for treating poorly biodegradable organic matter-containing water and treatment apparatus thereof |
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| CN111018187A (en) * | 2019-12-25 | 2020-04-17 | 苏州希图环保科技有限公司 | Wastewater treatment process based on Fenton oxidation reaction |
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Application publication date: 20191011 |
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