CN105417678A - Ozone catalytic oxidation method and device - Google Patents
Ozone catalytic oxidation method and device Download PDFInfo
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- CN105417678A CN105417678A CN201511013150.7A CN201511013150A CN105417678A CN 105417678 A CN105417678 A CN 105417678A CN 201511013150 A CN201511013150 A CN 201511013150A CN 105417678 A CN105417678 A CN 105417678A
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 171
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 48
- 230000003647 oxidation Effects 0.000 title claims abstract description 38
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 78
- 239000010865 sewage Substances 0.000 claims abstract description 73
- 239000003054 catalyst Substances 0.000 claims abstract description 55
- 238000011049 filling Methods 0.000 claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 229910052751 metal Inorganic materials 0.000 claims abstract description 7
- 239000002184 metal Substances 0.000 claims abstract description 7
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 7
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 52
- 238000006385 ozonation reaction Methods 0.000 claims description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 238000004090 dissolution Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 230000003381 solubilizing effect Effects 0.000 claims description 7
- -1 haydite Chemical compound 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 5
- 239000000470 constituent Substances 0.000 claims description 4
- 239000000356 contaminant Substances 0.000 claims description 4
- 229910021536 Zeolite Inorganic materials 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 238000011068 loading method Methods 0.000 claims description 3
- 229910052748 manganese Inorganic materials 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 238000004148 unit process Methods 0.000 claims description 3
- 239000010457 zeolite Substances 0.000 claims description 3
- 229910052725 zinc Inorganic materials 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract 3
- 238000000926 separation method Methods 0.000 abstract 3
- 238000006555 catalytic reaction Methods 0.000 abstract 1
- 238000007210 heterogeneous catalysis Methods 0.000 abstract 1
- 230000015556 catabolic process Effects 0.000 description 9
- 238000006731 degradation reaction Methods 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- 239000002957 persistent organic pollutant Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000006378 damage Effects 0.000 description 3
- 230000007812 deficiency Effects 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000009303 advanced oxidation process reaction Methods 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 239000010841 municipal wastewater Substances 0.000 description 2
- 230000020477 pH reduction Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 125000006615 aromatic heterocyclic group Chemical group 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000010786 composite waste Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 125000000623 heterocyclic group Chemical group 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000010893 paper waste Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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 an ozone catalytic oxidation method and device. The device comprises a contact oxidation tank, a water input pipe, a booster pump, a high-efficiency dissolved-air ejector, a perforated pipe water distributor, a catalyst filling material separation plate, a catalyst filling material, an ozone air inlet pipe, an ozone tail gas air inlet pipe and an ozone tail gas destroying device. The contact oxidation tank has a multi-section shunting type, sewage flows into the contact oxidation tank from the bottom and flows out from the top, and an up-flow contact oxidation reaction route is formed. Ozone is fully mixed with sewage and dissolved through the high-efficiency dissolved-air ejector, and is distributed at the bottom of the reaction tank through the perforated pipe water distributor. The catalyst filling material separation plate is arranged at the bottom of the reaction tank, and a catalyst layer is arranged on the separation plate. The catalyst is a high-efficiency load-type catalyst with metal and metal oxide loaded on a porous carrier. Sewage and ozone are subjected to a heterogeneous catalysis reaction in the contact oxidation tank under catalysis of the load catalyst, the ozone utilization efficiency and the oxidation efficiency are raised greatly, the ozone addition amount is reduced, and the operation cost is lowered.
Description
Technical field
The present invention relates to a kind of method and apparatus of catalytic ozonation, belong to sewage treatment area.
Background technology
Wastewater treatment in China industry, through the development of decades, has achieved the achievement of advancing by leaps and bounds.Current the planned city wastewater treatment rate has fulfiled the target of 70% ahead of schedule, and city down-stream processing item has progressively been tending towards saturated, but the actual compliance rate of China's town sewage is no more than 70%.Still a lot of Sewage Treatment Project is had because being mixed with a variety of causes such as industrial sewage can not to normal qualified discharge, there is a lot of municipal sewage plant water inlet standard comparing fuzzy, especially in some two, three line city and samll cities and towns, due to a variety of causes, trade effluent mixing municipal wastewater enters municipal sewage plant.Completely can not be mixed with the Processing tasks of trade effluent water inlet according to the municipal sewage plant of sanitary sewage standard design construction, cause water outlet to exceed standard.
Along with the needs of urban development and environment protection, no matter be municipal wastewater processing item or industrial sewage project, emission standard will progressively improve, and such as Beijing has been promoted to surface water four class water body standard.Current conventional processes can not meet the emission standard progressively improved, no matter be that water outlet exceeds standard or the raising of emission standard, need the COD removed not high, be generally about 20-60mg/L, and this type of COD is difficult to the hardly degraded organic substance by microbiological treatment.Selection adds medicament or uses charcoal absorption process, and the operation cost of great number is difficult to again bear.
Ozone in advanced oxidation processes is a kind of strong oxidizer, and redox potential is 2.07V, is the oxygenant that in current general oxygenant, oxidisability is the strongest.Its oxidation capacity is the twice of chlorine, Ozonation system device is relatively simple, floor space is little, Operation and Maintenance expense is lower, can not produce a large amount of mud, effectively can avoid secondary pollution, and reaction controllable degree is high, be convenient to realize industrial automation, the degradation efficiency of ozone high grade oxidation to the utilization ratio of ozone and organic pollutant is all lower.Ozone high grade oxidation technique, can not thorough chain rupture organics removal, and COD clearance is not high, and process organism has selectivity, and range of application is not extensive.Ozone is extremely unstable at normal temperatures and pressures, and decay is very fast, and ozone solubleness in water is not high.Ozone is used for needing in sewage disposal to experience the mass transfer process between the two-phase from gas phase to liquid phase, some has resolved into oxygen to be dissolved into ozone water from gas phase, some could not with target organic, react, so cause the utilization ratio of ozone in ozone high grade oxidation technique very low.
Summary of the invention
For the deficiency of existing sewage disposal technology, the invention provides a kind of method and apparatus of catalytic ozonation, for the treatment of the organism in lower concentration difficult degradation sewage disposal, the difficult degradation of solution organism, the difficult problem that ozone utilization rate is low, and kinds of processes combination and all kinds of sewage treatment project can be applicable to.
Technical scheme of the present invention is achieved in that
A kind of device for catalyzing and oxidating ozone, comprising:
Contact-oxidation pool, disposes of sewage for O3 contacted oxidation;
Water inlet pipe, for introducing described contact-oxidation pool by treatment sewage;
Ozone inlet pipe, for introducing described contact-oxidation pool by ozone;
Topping-up pump, for boosting, is connected with described water inlet pipe;
High-efficiency dissolued-air ejector, for fully mixing of ozone and sewage after supercharging, is connected with ozone inlet pipe with described water inlet pipe;
Perforated pipe water distributor, for being evenly distributed of ozone and sewage gas and liquid mixture, is connected with described high-efficiency dissolued-air ejector;
Ozone tail gas inlet pipe, for ozone tail gas backflow air inlet, is connected with described high-efficiency dissolued-air ejector;
Ozone tail gas breaking plant, for the discharge of oxygen in system and residue ozone, is connected with described ozone tail gas inlet pipe;
Catalyst filling dividing plate, for bearing catalyst filler, is positioned at bottom described contact-oxidation pool;
Catalyst filling, for O3 catalytic oxidation reaction, is positioned on the catalyst filling dividing plate of described contact-oxidation pool.
Further, described contact-oxidation pool is designed to multistage shunting, and sewage flows into bottom reaction tank, and top is flowed out, and forms upflowing contact oxidation route.
Further, described high-efficiency dissolued-air ejector water-in is connected with topping-up pump, makes ozone and the abundant mixed dissolution of sewage, evenly enter reaction tank from the water distributor bottom reaction tank by pressure.
Further, the exhaust port at described contact-oxidation pool top is connected with high-efficiency dissolued-air ejector by ozone tail gas inlet mouth, by pump by non-solubilizing reaction completely ozone return to in sewage, realize repeatedly adding of ozone.
Further, be provided with catalyst filling dividing plate bottom described high-efficient contact pond, described dividing plate is fixed on bottom described contact-oxidation pool by support, and catalyst filling placed by described dividing plate.
Further, described catalyst filling is active constituent loading high efficiency load type catalyzer on porous support.
Further, described support of the catalyst is one or more in activated alumina, gac, zeolite, haydite, molecular sieve.
Further, described catalyst activity component is one or more in the metal of Cu, Fe, Mn, Zn or metal oxide.
Further, the gas that ozonizer produces is all generally the mixed gas of oxygen and ozone, ozone can be utilized by dissolving, and oxygen is except being partly dissolved, some can overflow the top being accumulated in reactor, system pressure can be caused after oxygen gas buildup to increase, to a certain degree can be discharged by ozone tail gas breaking plant when system oxygen pneumatic is increased to.
Present invention also offers a kind of method adopting device for catalyzing and oxidating ozone to carry out water treatment, it is characterized in that, comprise the following steps:
Step one, ozone gas is connected with the high-efficiency dissolued-air ejector of each section of processing unit of contact-oxidation pool by ozone inlet pipe, and the ozone after shunting fully mixes with sewage and dissolves in high-efficiency dissolued-air ejector;
Step 2, the sewage of mixed dissolution ozone is uniformly distributed in bottom contact-oxidation pool by perforated pipe water distributor, with certain upflow velocity by catalyst filling layer, in this process, in the surface that a large amount of pollutent and ozone are attracted to porous supported catalyst and duct, by the synergy of catalyzer, by target contaminant oxygenolysis;
Step 3, sewage after oxide treatment is discharged by the water outlet of contact-oxidation pool top-side, and the sufficient ozone gas of the non-solubilizing reaction in contact-oxidation pool top is turned back in sewage again by ozone tail gas discharge outlet, air pump and ozone tail gas inlet pipe, until ozone is dissolved utilization to greatest extent.
Further, described ozone air inlet is divided into N part (N is the unit process pond quantity of contact-oxidation pool), and ozone is by after evenly distribute, and the tolerance of every part reduces, and more contributes to improving ozone utilization rate.
Further, described high-efficiency dissolued-air ejector is connected with ozone tail gas inlet pipe with ozone inlet pipe respectively, forms bidirection air intake mode.
Further, described contact-oxidation pool useful volume meets minimum hydraulic detention time.
Further, described ozone dosage is adjustable.
Further, described ozone tail gas adopts jet-pump or air pump to enter high-efficiency dissolued-air ejector.
Further, the filling ratio of described catalyst filling is adjustable, and filling ratio variable range is 8%-75%.
Compared with prior art, technological advantage of the present invention is:
1, the method and apparatus of a kind of catalytic ozonation of the present invention adopts multistage shunting contact-oxidation pool, adopt the high-efficiency dissolued-air ejector of the bidirection air intake mode of ozone inlet pipe and ozone tail gas inlet pipe, high-efficiency dissolued-air ejector is by topping-up pump and two inlet line, improve rate of ozone dissolution and utilization ratio, the sufficient ozone gas of the non-solubilizing reaction in contact-oxidation pool top is turned back in sewage again by ozone tail gas discharge outlet, air pump and ozone tail gas inlet pipe, achieve the Reusability of ozone, achieve ozone and farthest effectively utilize.
2, high-efficiency dissolued-air ejector is connected with perforated pipe water distributor, is uniformly distributed in bottom reaction tank by the sewage dissolving ozone, fully contacts and mass transfer with the catalyst filling bottom reaction tank, can increase substantially ozone transfer ratio and transfer efficiency.
3, special high-efficient carrier catalyzer is adopted significantly to adsorb and enrichment pollutent and ozone, under the effect of catalyzer, make ozone decompose in a large number produce hydroxyl radical free radical [HO] thus the chain reaction caused, this reaction also can produce antozone [O] that is very active, that have Strong oxdiative ability.Catalytic ozonation technology effective compensate for simple ozone oxidation to the utilization ratio of ozone and the lower deficiency of organic pollutant degradation rate, and the utilization of metal and metal oxide catalyst can improve the clearance of ozone utilization rate and Recalcitrant chemicals greatly.
The present invention can be widely used in sewage treatment area, especially lower concentration difficult degradation sewage, every ozone that utilizes carries out catalytic oxidation treatment difficult degradation sewage or pre-treatment organics removal, can adopt the method and apparatus of a kind of catalytic ozonation of the present invention.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation of a kind of device for catalyzing and oxidating ozone of the present invention;
In figure: 1. ozone inlet pipe; 2. water inlet pipe; 3. ozone tail gas inlet pipe; 4. high-efficiency dissolued-air ejector; 5. perforated pipe water distributor; 6. rising pipe; 7. contact-oxidation pool; 8. catalyst filling; 9. catalyst filling dividing plate; 10. ozone tail gas breaking plant.
Embodiment
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, to be briefly described embodiment below, apparently, example in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other application can also be obtained according to the present invention and these examples.
As shown in Figure 1, a kind of device for catalyzing and oxidating ozone of the present invention, comprising:
Contact-oxidation pool 7;
Water inlet pipe 2, is arranged at below contact-oxidation pool 7, is connected with high-efficiency dissolued-air ejector 4;
Ozone inlet pipe 1;
High-efficiency dissolued-air ejector 4, is connected with ozone tail gas inlet pipe 3 with water inlet pipe 2, ozone inlet pipe 1;
Perforated pipe water distributor 5, is connected with high-efficiency dissolued-air ejector 4;
Ozone tail gas inlet pipe 3, is connected with high-efficiency dissolued-air ejector 4;
Ozone tail gas breaking plant 10, is arranged at above contact-oxidation pool 7;
Catalyst filling dividing plate 9, is arranged at bottom contact-oxidation pool 7;
Catalyst filling 8, is positioned on the catalyst filling dividing plate 9 of contact-oxidation pool 7.
Preferably, described high-efficient contact oxidation pond is designed to multistage shunting, and sewage flows into bottom reaction tank, and top is flowed out, and forms upflowing contact oxidation route.
Preferably, described high-efficiency dissolued-air ejector water-in is connected with topping-up pump, makes ozone and the abundant mixed dissolution of sewage, evenly enter reaction tank from the water distributor bottom reaction tank by pressure.
Preferably, the exhaust port at described high-efficient contact oxidation pond top is connected with high-efficiency dissolued-air ejector by ozone tail gas inlet mouth, by pump by non-solubilizing reaction completely ozone return to in sewage, realize repeatedly adding of ozone.
Preferably, be provided with catalyst filling dividing plate with holes bottom described high-efficient contact pond, described dividing plate is fixed on bottom described high-efficient contact oxidation pond by support, and catalyst filling placed by described dividing plate.
Preferably, described catalyst filling is active constituent loading high efficiency load type catalyzer on porous support.
Preferably, described support of the catalyst is one or more in activated alumina, gac, zeolite, haydite, molecular sieve.
Preferably, described catalyst activity component is one or more in the metal of Cu, Fe, Mn, Zn or metal oxide.
Preferably, the gas that ozonizer produces is all generally the mixed gas of oxygen and ozone, ozone can be utilized by dissolving, and oxygen is except being partly dissolved, some can overflow the top being accumulated in reactor, system pressure can be caused after oxygen gas buildup to increase, to a certain degree can be discharged by ozone tail gas breaking plant when system oxygen pneumatic is increased to.
Present invention also offers a kind of method of catalytic ozonation, comprise the following steps:
Step one, ozone gas is connected with the high-efficiency dissolued-air ejector 4 of each section of processing unit of contact-oxidation pool 7 by ozone inlet pipe 1, and the ozone after shunting fully mixes with sewage and dissolves in high-efficiency dissolued-air ejector 4;
Step 2, the sewage of mixed dissolution ozone is uniformly distributed in bottom contact-oxidation pool 7 by perforated pipe water distributor 5, with certain upflow velocity by catalyst filling 8, in this process, in the surface that a large amount of pollutent and ozone are attracted to porous supported catalyst and duct, by the synergy of catalyzer, by target contaminant oxygenolysis;
Step 3, sewage after oxide treatment is discharged by the water outlet 6 of contact-oxidation pool 7 top-side, and the sufficient ozone gas of the non-solubilizing reaction in contact-oxidation pool 7 top is turned back in sewage again by air pump and ozone tail gas inlet pipe 3, until ozone is dissolved utilization to greatest extent.
Preferably, described ozone air inlet is divided into N part (N is the unit process pond quantity of contact-oxidation pool), and ozone is by after evenly distribute, and the tolerance of every part reduces, and more contributes to improving ozone utilization rate.
Preferably, described high-efficiency dissolued-air ejector is connected with ozone tail gas inlet pipe with ozone inlet pipe respectively, forms bidirection air intake mode.
Preferably, described contact-oxidation pool useful volume meets minimum hydraulic detention time.
Preferably, described ozone dosage is adjustable.
Preferably, described ozone tail gas adopts jet-pump or air pump to enter high-efficiency dissolued-air ejector.
Preferably, the filling ratio of described catalyst filling is adjustable, and filling ratio variable range is 8%-75%.
Embodiment one:
Certain sewage work designed water inlet originally for sanitary sewage, and actual water inlet major part is paper waste now.Water inlet biodegradability is lower, and main Recalcitrant chemicals is xylogen.The major part discharge enterprise of water factory's service is all provided with enterprise's sewage works, draining is according to municipal sewage system emission standard, but BOD is not specially required, so cause can biochemical part easily mostly removing in the sewage works process of enterprise self treating part in sewage, and flow into the sewage of sewage work, although COD does not exceed water drain emission standard, but intractability is far above water drain emission standard.
Water inlet is Ge Jia enterprise of certain economic and technological development zone composite waste, and water-quality constituents is complicated, biodegradability extreme difference, and indivedual enterprises exist night arranges phenomenon steathily, has part oil-containing, colloidal type waste water enters biochemical system.Influent COD mean value is 480mg/L, and water inlet maximum is 1350mg/L, and average effluent COD is 82mg/L, and water outlet exceeds standard, and water outlet maximum value is 123mg/L.BOD is lower in water inlet, and mean value is only 70mg/L, and B/C is about 0.15 than mean value.
Adopt conventional ozone high grade oxidation technique, major equipment comprises: ozonizer, ozone gas source system, contact-oxidation pool, ozone tail gas destruction system etc.Major experimental data: contact oxidation time 1.5h, ozone dosage is 70mg/L, and water outlet just can be made to reach one-level emission standard A, and COD < 50mg/L, ozone utilization rate is lower.
Adopt the method and apparatus of a kind of catalytic ozonation of the present invention, major experimental data: contact oxidation time 1h, packed catalyst rate is 12%, and ozone dosage is when 30mg/L, COD average removal rate 50.41%, water outlet can reach one-level emission standard A completely.Substantially increase ozone utilization rate, reduce the ozone dosage of 57%.
Embodiment two
Certain sewage work treatment scale 30000m
3/ sky, its technical process is: coarse rack-lift pump-fine fack-aerated grit chamber-hydrolysis acidification pool-A/O pond-second pond-uv sterilisation pond-water outlet.Trade effluent accounts for more than 60%, and dyeing waste water accounts for about 85% of trade effluent, and water inlet biodegradability is poor, B/C < 0.25.Influent COD mean value is 298mg/L, and maximum value is 621mg/L, and minimum value is 189mg/L; Water inlet SS mean value is 130mg/L, and maximum value reaches 350mg/L, and Schwellenwert is 50mg/L; The mean value of water inlet NH3-N is at 12.5mg/L, and maximum value is reached for 25mg/L, and minimum value is 5.7mg/L.Water inlet colourity is higher, higher than 100 times.Water outlet COD exceeds standard, and mean value is 89mg/L, and effluent color dilution exceeds standard, and mean value is 50 times.
Adopt conventional ozone high grade oxidation technique, major equipment comprises: ozonizer, ozone gas source system, contact-oxidation pool, ozone tail gas destruction system etc.Major experimental data: contact oxidation time 1.5h, ozone dosage is 60mg/L, and after process, average water outlet COD is 45mg/L, and average COD removal 48%, water outlet reaches one-level emission standard A, and effluent color dilution is lower than 20 times, and ozone utilization rate is lower.
Adopt the method and apparatus of a kind of catalytic ozonation of the present invention, major experimental data: contact oxidation time 1h, packed catalyst rate is 15%, ozone dosage is when 30mg/L, average water outlet COD37mg/L, COD clearance ranges up to 54%, average 43%.Ozone dosage at 20mg/L, average water outlet COD46mg/L, COD average removal rate 36%.Water outlet can reach one-level emission standard A, and effluent color dilution is lower than 20 times.Reduce ozone dosage 66%.
Embodiment three
Certain industrial park Engineering of Sewage Treatment Plant total scale 40000m
3/ d, first phase design scale is 20000m
3/ d, mainly processes the trade effluent of oil, petrochemical industry, mechanic factory workers, Designing Sewage Treatment Plant day treatment scale 20000m
3/ d.Trade effluent accounts for the ratio of total water inlet up to 97.2%, and trade effluent is based on petrochemical wastewater.Sewage disposal plant process flow is: coarse rack-sewage lifting pump house-fine fack-horizontal-flow grit chamber-hydrolysis acidification pool-AAO biochemistry pool-second pond-second lift pump house-coagulative precipitation tank-fibre turntable filter chamber-uv sterilisation pond.
Water factory intakes at present and mainly contains following problem: in (1) water inlet, sanitary sewage accounts for total ratio of intaking only has 2.8%, and sanitary sewage ratio is less than 50%; (2) influent quality exceeds standard, and water inlet is containing hazardous and noxious substances such as toluene, dimethylbenzene, volatile phenols, and chloride ion content is very high, has a strong impact on biochemical system and runs.
Influent COD mean value is 450mg/L, and maximum value reaches 1350mg/L; Water inlet BOD5 mean value is 72mg/L, and maximum value reaches 180mg/L; Water inlet SS mean value is 125mg/L, and maximum value reaches 329mg/L; Water inlet muriate mean value is 1900mg/L, and maximum value reaches 3500mg/L.
Because service garden enterprise of this water factory relates to the multiple industries such as oil, petrochemical industry, mechanical workout, water factory's influent quality is very complicated, sewage is after the process of enterprises sewage works, and easily biodegradable organics is preferentially gone out, and entering major part in water factory's sewage is all Recalcitrant chemicals.
Adopt conventional Fenton advanced oxidation processes, major equipment comprises: dosing mixing pit, main body reaction tank, plus-minus mixing pit, settling tank, medicine system etc.Major experimental data: dosing mixing pit hydraulic detention time 20min, main body reaction tank hydraulic detention time 1h, plus-minus mixing pit hydraulic detention time 20min, settling tank hydraulic detention time 2h, Fenton added amount of chemical is: hydrogen peroxide dosage 300mg/L, ferrous sulfate 275mg/L, sulfuric acid 0.2mL/L, sodium hydroxide 400mg/L.Water factory's secondary clarifier effluent is chosen in Fenton water inlet, and secondary clarifier effluent average COD is 135mg/L, and after Fenton process, average water outlet COD is 95mg/L, on average can remove about 40mg/LCOD, and average COD removal is 29.6%.Because water factory water water quality is unstable, have some heterocyclic aromatics hard-degraded substances may with hydrogen peroxide generation special reaction, the more high reason of secondary clarifier effluent SS, after Fenton process, there is COD and raise phenomenon in sewage.Increase adding of agent, COD can not continue to reduce substantially, and treatment effect is poor.
Adopt conventional ozone high grade oxidation technique, major equipment comprises: ozonizer, ozone gas source system, contact-oxidation pool, ozone tail gas destruction system etc.Major experimental data: contact oxidation time 1.5h, ozone dosage is 50-100mg/L, water factory's secondary clarifier effluent is chosen in water inlet, secondary clarifier effluent average COD is 135mg/L, and after process, average water outlet COD is 120mg/L, owing to containing heterocyclic and the complicated organism of long-chain in sewage, there is oxidation barrier in ozone high grade oxidation, increasing ozone dosage can not oxidize contaminants further, and also there is the scene of COD rising after process, the non-constant for the treatment of effect.
Adopt the method and apparatus of a kind of catalytic ozonation of the present invention, major experimental data: contact oxidation time 1h, packed catalyst rate is 30%, and ozone dosage is when 30mg/L, and average water outlet COD43mg/L, COD clearance mean value is 68%.Water outlet can reach one-level emission standard A.The present invention, for process difficult degradation sewage, can effectively break oxidizing reaction barrier, and oxygenolysis conventional high level oxidation technology can not the complicated pollutent of oxygenolysis.
The method and apparatus of a kind of catalytic ozonation of the present invention is the ozone high grade oxidation technique adopting special carrier catalyzer auxiliary, produces the chemical oxidation of hydroxyl radical free radical [HO], greatly can reduce selectivity, improve speed of reaction.Principle is exactly under surface catalyst existent condition, utilizes strong oxidizer-O
3organic pollutant at normal temperatures and pressures in catalyzed oxidation waste water, or direct oxidation organic pollutant, or macromole organic pollutant is oxidized to small molecules organic pollutant, improve the biodegradability of waste water, remove organic pollutant preferably.The carried catalyst of loaded metal or metal oxide mixes by microscopic grains and non-crystallized part the mixture formed, the present invention adopts specific loads method evenly to be plated on porous support by catalyzer, and by the catalyzer after the stabilization treatment method process loads such as high-temperature roasting, catalyzer is immersed in surface in sewage and contains a large amount of acidity or basic group.The existence of the existence of these acid or basic groups particularly hydroxyl, phenolic hydroxyl group, makes catalyzer not only have adsorptive power, but also has catalytic capability.In ozone/catalyzer synergy process, first adsorption and enrichment is carried out to pollutent, a large amount of ozone and pollutent are enriched in catalyst surface and hole, under the effect of catalyzer, make ozone decomposed produce hydroxyl radical free radical [HO] thus the chain reaction caused, this reaction also can produce antozone [O] that is very active, that have Strong oxdiative ability.Catalytic ozonation technology effective compensate for simple ozone oxidation to the utilization ratio of ozone and the lower deficiency of organic pollutant degradation rate, and the utilization of metal and metal oxide catalyst can improve the clearance of ozone utilization rate and Recalcitrant chemicals greatly.
Contact-oxidation pool of the present invention can effectively improve ozone utilising efficiency again, strengthens COD removal effect.The method and apparatus of a kind of catalytic ozonation of the present invention effectively can solve the process problem of lower concentration difficult degradation sewage, and can ozone utilization rate be increased substantially, reduce ozone dosage, strengthen COD removal effect, reduce the selectivity of catalytic ozonation, broaden application scope.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. a device for catalyzing and oxidating ozone, comprising:
Contact-oxidation pool, disposes of sewage for O3 contacted oxidation;
Water inlet pipe, for introducing described contact-oxidation pool by treatment sewage;
Ozone inlet pipe, for introducing described contact-oxidation pool by ozone;
Topping-up pump, for boosting, is connected with described water inlet pipe;
High-efficiency dissolued-air ejector is connected, and for fully mixing of ozone and sewage after supercharging, is connected with ozone inlet pipe with described water inlet pipe;
Perforated pipe water distributor, for being evenly distributed of ozone and sewage gas and liquid mixture, is connected with described high-efficiency dissolued-air ejector;
Ozone tail gas inlet pipe, for ozone tail gas backflow air inlet, is connected with described high-efficiency dissolued-air ejector;
Ozone tail gas breaking plant, for the discharge of oxygen in system and residue ozone, is connected with described ozone tail gas inlet pipe;
Catalyst filling dividing plate, for bearing catalyst filler, is positioned at bottom described contact-oxidation pool;
Catalyst filling, for O3 catalytic oxidation reaction, is positioned on the catalyst filling dividing plate of described contact-oxidation pool.
2. device for catalyzing and oxidating ozone according to claim 1, is characterized in that: described contact-oxidation pool is designed to multistage shunting, and sewage flows into bottom reaction tank, and top is flowed out, and forms upflowing contact oxidation route.
3. device for catalyzing and oxidating ozone according to claim 1, is characterized in that: described high-efficiency dissolued-air ejector water-in is connected with topping-up pump, makes ozone and the abundant mixed dissolution of sewage, evenly enter reaction tank from the water distributor bottom reaction tank by pressure.
4. device for catalyzing and oxidating ozone according to claim 1, it is characterized in that: the exhaust port at described contact-oxidation pool top is connected with high-efficiency dissolued-air ejector by ozone tail gas inlet pipe, by pump by non-solubilizing reaction completely ozone return to in sewage, realize repeatedly adding of ozone.
5. device for catalyzing and oxidating ozone according to claim 1, it is characterized in that: bottom described high-efficient contact pond, be provided with catalyst filling dividing plate, described catalyst filling dividing plate is Perforated clapboard, described catalyst filling dividing plate is fixed on bottom described contact-oxidation pool by support, and catalyst filling placed by described catalyst filling dividing plate.
6. device for catalyzing and oxidating ozone according to claim 1, is characterized in that: described catalyst filling is active constituent loading high efficiency load type catalyzer on porous support; Described support of the catalyst is one or more in activated alumina, gac, zeolite, haydite, molecular sieve; Described catalyst activity component is one or more in the metal of Cu, Fe, Mn, Zn or metal oxide.
7. use device for catalyzing and oxidating ozone as claimed in claim 1 to carry out a method for water treatment, it is characterized in that, comprise the following steps:
Step one, ozone gas is connected with the high-efficiency dissolued-air ejector of each section of processing unit of contact-oxidation pool by ozone inlet pipe, and the ozone after shunting fully mixes with sewage and dissolves in high-efficiency dissolued-air ejector;
Step 2, the sewage of mixed dissolution ozone is uniformly distributed in bottom contact-oxidation pool by perforated pipe water distributor, catalyst filling is passed through with certain upflow velocity, in this process, in the surface that a large amount of pollutent and ozone are attracted to high-efficient carrier catalyzer and duct, by the synergy of catalyzer, by target contaminant oxygenolysis;
Step 3, sewage after oxide treatment is discharged by the water outlet of contact-oxidation pool top-side, and the sufficient ozone gas of the non-solubilizing reaction in contact-oxidation pool top is turned back in sewage again by ozone tail gas discharge outlet, air pump and ozone tail gas inlet pipe, until ozone is dissolved utilization to greatest extent.
8. the method for catalytic ozonation according to claim 7, it is characterized in that: ozone air inlet is divided into N part (N is the unit process pond quantity of contact-oxidation pool), ozone is by after evenly distribute, and the tolerance of every part reduces, and more contributes to improving ozone utilization rate.
9. the method for catalytic ozonation according to claim 7, is characterized in that: described high-efficiency dissolued-air ejector is connected with ozone tail gas inlet pipe with ozone inlet pipe respectively, forms bidirection air intake mode.
10. the method for catalytic ozonation according to claim 7, is characterized in that: the filling ratio of described catalyst filling is adjustable, and filling ratio variable range is 8%-75%.
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106495359A (en) * | 2016-11-23 | 2017-03-15 | 北京清大国华环境股份有限公司 | A kind of highly difficult advanced waste treatment apparatus and method |
| CN107162343A (en) * | 2017-06-29 | 2017-09-15 | 苏州科博思设备工程有限公司 | A kind of sewage disposal system |
| CN107879460A (en) * | 2017-12-26 | 2018-04-06 | 华东交通大学 | A kind of device of catalytic ozonation processing waste water |
| CN108114725A (en) * | 2016-11-28 | 2018-06-05 | 中国石油化工股份有限公司 | A kind of ozone catalytic oxidation catalyst, its preparation method and application |
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| CN114229987A (en) * | 2021-12-20 | 2022-03-25 | 北京化工大学 | Flat ceramic membrane catalytic oxidation device and process for treating biologically-nondegradable wastewater |
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| CN116462373A (en) * | 2023-05-25 | 2023-07-21 | 长江生态环保集团有限公司 | Emergency treatment method for pollution load of composite sewage treatment plant |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644527A (en) * | 2004-12-23 | 2005-07-27 | 哈尔滨工业大学 | Porous multi-site provided reactor for water treatment |
| CN1689981A (en) * | 2004-04-22 | 2005-11-02 | 株式会社东芝 | Water treatment system |
| WO2014201979A1 (en) * | 2013-06-17 | 2014-12-24 | 南京德磊科技有限公司 | Sewage treatment system and method thereof |
| CN104478066A (en) * | 2014-12-15 | 2015-04-01 | 浙江中凯瑞普环境工程股份有限公司 | Catalytic ozonation reactor for treatment of external circulating wastewater and wastewater treatment method |
| CN104478067A (en) * | 2014-12-15 | 2015-04-01 | 浙江中凯瑞普环境工程股份有限公司 | Ozone catalytic oxidation reactor for treatment of inner circulation sewage and sewage treatment method using reactor |
| CN104787869A (en) * | 2015-04-10 | 2015-07-22 | 锐博环保科技(北京)有限公司 | Treatment method and device for catalyzing and oxidizing degradation-resistant organic wastewater with heterogeneous ozone |
| CN205472870U (en) * | 2015-12-31 | 2016-08-17 | 北京清大国华环境股份有限公司 | Ozone catalytic oxidation's device |
-
2015
- 2015-12-31 CN CN201511013150.7A patent/CN105417678A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1689981A (en) * | 2004-04-22 | 2005-11-02 | 株式会社东芝 | Water treatment system |
| CN1644527A (en) * | 2004-12-23 | 2005-07-27 | 哈尔滨工业大学 | Porous multi-site provided reactor for water treatment |
| WO2014201979A1 (en) * | 2013-06-17 | 2014-12-24 | 南京德磊科技有限公司 | Sewage treatment system and method thereof |
| CN104478066A (en) * | 2014-12-15 | 2015-04-01 | 浙江中凯瑞普环境工程股份有限公司 | Catalytic ozonation reactor for treatment of external circulating wastewater and wastewater treatment method |
| CN104478067A (en) * | 2014-12-15 | 2015-04-01 | 浙江中凯瑞普环境工程股份有限公司 | Ozone catalytic oxidation reactor for treatment of inner circulation sewage and sewage treatment method using reactor |
| CN104787869A (en) * | 2015-04-10 | 2015-07-22 | 锐博环保科技(北京)有限公司 | Treatment method and device for catalyzing and oxidizing degradation-resistant organic wastewater with heterogeneous ozone |
| CN205472870U (en) * | 2015-12-31 | 2016-08-17 | 北京清大国华环境股份有限公司 | Ozone catalytic oxidation's device |
Non-Patent Citations (1)
| Title |
|---|
| 全国勘察设计注册工程师环保专业管理委员会: "《注册环保工程师专业考试复习资料.1》", 中国环境科学出版社, pages: 97 * |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106495359A (en) * | 2016-11-23 | 2017-03-15 | 北京清大国华环境股份有限公司 | A kind of highly difficult advanced waste treatment apparatus and method |
| CN108114725B (en) * | 2016-11-28 | 2021-01-05 | 中国石油化工股份有限公司 | Ozone catalytic oxidation catalyst, preparation method and application thereof |
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| CN109569292B (en) * | 2017-09-28 | 2021-09-07 | 中国石油化工股份有限公司 | Ozone oxidation treatment device and treatment method for waste gas and waste water |
| CN109569292A (en) * | 2017-09-28 | 2019-04-05 | 中国石油化工股份有限公司 | The ozone Oxidation Treatment device and processing method of exhaust gas and waste water |
| CN107879460A (en) * | 2017-12-26 | 2018-04-06 | 华东交通大学 | A kind of device of catalytic ozonation processing waste water |
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| CN108467100B (en) * | 2018-04-03 | 2020-07-07 | 杭州市城建设计研究院有限公司 | Activated carbon catalytic ozonation device and industrial wastewater treatment process |
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