CN204058048U - For the device of heterogeneous catalysis ozone Oxidation Treatment water - Google Patents
For the device of heterogeneous catalysis ozone Oxidation Treatment water Download PDFInfo
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- CN204058048U CN204058048U CN201420452864.2U CN201420452864U CN204058048U CN 204058048 U CN204058048 U CN 204058048U CN 201420452864 U CN201420452864 U CN 201420452864U CN 204058048 U CN204058048 U CN 204058048U
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Abstract
The utility model relates to a kind of device for heterogeneous catalysis ozone Oxidation Treatment water, and described device is primarily of 1 central contact tower, 1 ~ 4 catalyzed oxidation tower and 1 ~ 4 radial-flow pipe connecting composition.Pending water is flowed into by central contact top of tower water inlet manifold, and the streams of ozone passed into bottom aeration head is reverse to be contacted, then through water conservancy diversion inclined-plane, pipe connecting delivers to catalyzed oxidation tower.Streams of ozone enters in catalyzed oxidation tower through aeration plate, with current coflow, makes solid catalyst be complete fluidized state.Be provided with membrane separation assemblies and rising pipe in the middle part of catalyzed oxidation tower, be separated for realizing water outlet, collection bucket and drain are equipped with in bottom.On-line monitoring dissolved ozone concentration, to control ozone dosage.Utilize venting pressure to realize the pressurized operation of each tower, tail gas is discharged by the delivery pipe on gas skirt.Compared with prior art, micron order solid catalyst can be used for continuous process by the utility model, has the advantages such as purification efficiency is high, applied widely, stable, flexible operation.
Description
Technical field
The utility model relates to a kind of water treatment device, is specifically related to a kind of device for heterogeneous catalysis ozone Oxidation Treatment water, belongs to environmental technology field.
Background technology
In purificating raw water and field of waste water treatment, ozone (O
3) because having strong oxidizing property (E
0=2.07V), be often used to realize sterilization and disinfection, decolouring and deodorizing, removal Recalcitrant chemicals and improve the objects such as former water biodegradability.According to direct oxidation principle, the O in water
3unsaturated, aromatics structure in energy preferential destruction organism, macromolecular substance is converted into small molecules product, but along with the carrying out reacted, the removal speed of system to total organic carbon (TOC) significantly will reduce.Now, add ozone if continue, processing cost not only can be made significantly to increase, limit its practical value, even may cause the accumulation of potential oncogene products (as aldehydes and bromate), cause secondary pollution.
When there is OH in reaction system
-, UV-light, hydrogen peroxide, gac, transition-metals and their oxides time, dissolved ozone can decompose generate hydroxy radical qiao (OH), the latter has extremely strong mineralization ability to organic pollutant.Wherein, taking solid catalyst as the heterogeneous catalysis Ozonation of core, dirty removal capacities is strong, ozone utilization rate is high because having, without the need to adding chemical agent and process low power consumption and other advantages, and becoming the investigation and application focus of domestic and international water treatment field.
Heterogeneous catalysis water treatment device by ozone oxidation is the place of carrying out water treatment, and it is the key factor of water treatment efficiency, efficiency.Existing heterogeneous catalysis water treatment device by ozone oxidation cannot give full play to the advantage of heterogeneous catalysis ozone oxidation water treatment, reason comprises (1), and existing apparatus all adopts atmospheric operation, and the solubleness that ozone molecule is lower in water significantly limit the growing amount of OH; (2) in existing apparatus, solid catalyst directly contacts with aromatics, hydrophobic organic compound in water, can cause the minimizing of catalytic site position, weaken its reactive behavior because of strong adsorption; (3) in existing apparatus, solid catalyst generally exists with fixed bed form, and so design solid catalyst and water engaging surface amass little, cause catalytic effect to fully demonstrate, and process also can be caused uneven, also add the treatment time.It is generally acknowledged, when solid catalyst particle diameter is less than 500 μm, and when being in complete fluidized state, ozone within it, the resistance to mass transfer of outside surface will be effectively eliminated, and reaction unit treatment efficiency significantly promotes, and hydraulic detention time can significantly reduce; But small size solid catalyst very easily runs off with water outlet, this makes the gas, the liquid two-phase reactor that configure traditional effluent weir (pipe), as traverse baffle contact tank, spray column, packing tower and sieve-tray tower etc., all safeguards system cannot obtain good operational stability, this is also that current distributing solid catalyst cannot the main reason of practical application.
Therefore, how to innovate reaction unit configured, farthest optimize gas, liquid, solid three-phase mass transfer reaction process, consolidation system treatment efficiency is the key promoting heterogeneous catalysis Ozonation practicalization.
Summary of the invention
The purpose of this utility model is to provide a kind of device for heterogeneous catalysis ozone Oxidation Treatment water, and it gives full play to the superiority of heterogeneous catalysis Ozonation, and water treatment efficiency is high, stable effluent quality, flexible operation mode, the scope of application are wider.
For achieving the above object, the technical solution adopted in the utility model is:
Comprise 1 central contact tower, 1 ~ 4 catalyzed oxidation tower, radial-flow pipe connecting and solid catalyst, water inlet manifold; Described central contact tower is connected by radial-flow pipe connecting with catalyzed oxidation tower;
Described central contact tower tower body is cylindrical structural, and aspect ratio is 6 ~ 8: 1;
Described central contact top of tower is provided with gas skirt; This gas skirt is provided with tail gas discharging pipe; Described tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve;
Described water inlet manifold stretches in central contact tower through gas skirt; Described water inlet manifold is positioned at 20 ~ 25% of contact tower tower body height centered by central contact Ta Tanei length partly;
Described central contact tower bottom is provided with titanium aeration head; The aperture of described titanium aeration head is 2 ~ 5 μm; Described titanium aeration head periphery is provided with water conservancy diversion inclined-plane; The upper end on described inclined-plane contacts with the bottom surface of titanium aeration head, and lower end contacts with radial-flow pipe connecting;
Described catalyzed oxidation tower tower body is cylindrical structural, and its virtual height is consistent with the virtual height of central contact tower, and aspect ratio is 4 ~ 6: 1;
Described catalyzed oxidation top of tower is provided with gas skirt; This gas skirt is provided with tail gas discharging pipe; Described tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve;
Cylindrical membrane separation assembly is provided with in the middle part of described catalyzed oxidation tower; The length of described membrane separation assemblies is 30 ~ 60% of catalyzed oxidation tower tower body height; The diameter of described membrane separation assemblies is 30 ~ 50% of catalyzed oxidation tower tower body diameter; The filtering accuracy of described membrane separation assemblies is 0.1 ~ 1.0 μm;
Described membrane separation assemblies top is provided with rising pipe; Described rising pipe passes catalyzed oxidation tower, and pass part be provided with vacuum meter;
Described catalyzed oxidation tower middle and lower part is provided with circular cylindrical solid catalyst addition tube; Described solid catalyst filling tube is provided with stopping valve;
Described catalyzed oxidation tower bottom is provided with titanium aeration plate; The aperture of described titanium aeration plate is 2 ~ 5 μm; Described titanium aeration plate diameter is 1.0 ~ 1.5 times of membrane separation assemblies diameter; The top of described titanium aeration plate is lower than the bottom of radial-flow pipe connecting;
Described catalyzed oxidation tower bottom is provided with collection bucket; Drain and stopping valve is provided with bottom described collection bucket;
Described solid catalyst is positioned at catalyzed oxidation tower;
Closed dissolved ozone scale tank is equipped with in the middle part of described central contact tower, catalyzed oxidation tower.
In technique scheme, dissolved ozone scale tank is positioned at outside tower, is communicated with tower; On-line computing model is established in dissolved ozone scale tank.
In technique scheme, central contact tower, catalyzed oxidation tower are all cylindrical structural, and virtual height is consistent, and aspect ratio arranges rationally, and thus, device can obtain high gas, liquid mass-transfer efficiency.
In technique scheme, described gas skirt is connected with tower body by flange; Described collection bucket is connected with tower body by flange.
In technique scheme, the gas skirt of described central contact top of tower is frustro-pyramidal; The gas skirt of described catalyzed oxidation top of tower is conical; The collection bucket of described catalyzed oxidation tower bottom is turbination.
In technique scheme, described membrane separation assemblies is fixed on support; Described support is fixed on catalyzed oxidation inner wall of tower.
In technique scheme, described radial-flow pipe connecting is provided with electromagnetic throttle valve, for regulating the working quantity of hydraulic detention time and control catalyzed oxidation tower; Described radial-flow pipe connecting is also provided with thief hole, for collecting central contact tower water outlet water sample, or as blow-down pipe.
In preferred technical scheme, the tap density of described solid catalyst is 450 ~ 900 kg/m
3, the flaky material that it can be the particle of 0.05 ~ 0.30 mm for particle diameter, long limit is 1 ~ 20 mm or length are the filamentary material of 1 ~ 20 mm.It drops into concentration and selects according to water quality treatment.Finished commercial prod's ozone catalyst can be selected.Filling tube outside catalyzed oxidation tower middle and lower part, for supplementing new catalyzer; The collection bucket of bottom and drain, for collecting and discharge old catalyzer.
In technique scheme, in described central contact tower, titanium aeration head service area be 1.5 times of tower body sectional area, the inclination angle on water conservancy diversion inclined-plane is 45 degree, and water inlet manifold is positioned at position, gas skirt axis.The setting of guide face can make current enter pipe connecting with larger flow velocity, and avoids water to reflux.
In the utility model, described membrane separation assemblies is in parallel by multiple tubular membrane unit, and film unit number is determined according to actual water production rate; In described membrane separation assemblies, film unit is tubular type aluminum oxide ceramic membrane, tubular type zirconium white ceramic membrane, tubular type titanium dioxide ceramic membrane or tubular type titanium metal film.
Utilize said apparatus to carry out ozone Oxidation Treatment water, comprise the following steps:
(1) will send in central contact tower by water inlet manifold after pending water pressurization; Ozone passes in central contact tower by the titanium aeration head of central contact tower bottom simultaneously; Water and ozone is reverse to be contacted, mixing;
In described central contact tower, working pressure 0.15 ~ 0.2 MPa, dissolved ozone concentration 1.0 ~ 3.0 mg/L;
(2) water being dissolved with ozone enters in catalyzed oxidation tower by radial-flow pipe connecting, and simultaneously the titanium aeration plate of catalyzed oxidation tower bottom passes into ozone, air-flow and current by under move upward; After the mixing of ozone, water, solid catalyst, reaction, process water is discharged by rising pipe through membrane separation assemblies, namely completes water treatment procedure;
In described catalyzed oxidation tower, working pressure 0.15 ~ 0.2 MPa, dissolved ozone concentration 0.2 ~ 0.5 mg/L; In described membrane separation assemblies, cross-film working pressure is 0.15 ~ 0.3 MPa.
In technique scheme, in described central contact tower, hydraulic detention time is 0.5 ~ 3 min; In described catalyzed oxidation tower, hydraulic detention time is 2 ~ 20 min.The working pressure of central contact tower and catalyzed oxidation tower controls by regulating the throttling valve on ozone air input and tail gas discharging pipe.When working pressure continues to increase, should suitably turn down ozone air input, heighten free air delivery, otherwise, heighten ozone air input, turn down free air delivery.After water treatment, residual ozone is discharged after being collected by top gas skirt, and solid catalyst is trapped in tower.
In technique scheme, the dissolved ozone concentration in central contact tower and catalyzed oxidation tower is by establishing on-line computing model to measure in dissolved ozone scale tank; Control by regulating hydraulic detention time and inlet gas ozone concentration.When dissolved ozone concentration continues to increase, should suitably turn down inlet gas ozone concentration, heighten hydraulic detention time, otherwise, heighten inlet gas ozone concentration, turn down hydraulic detention time.
In the utility model, the connection of titanium aeration head take air or oxygen as the ozonizer of source of the gas, can control ozone dosage by regulating machine power and source of the gas tolerance.Described central contact tower, catalyzed oxidation tower and radial-flow pipe connecting are all preferably AISL-316L stainless steel or other withstand voltage, resistance to ozone corrosion materials.
In the utility model, solid catalyst is complete fluidized state under the acting in conjunction of air-flow, current; Membrane separation assemblies adopts external pressure mode to run, utilize the combined action that in tower, pressurization and rising pipe vacuumize, there is provided cross-film working pressure, this makes micron order solid catalyst also can be used to continuous print water treatment procedure, is conducive to the scrubbing usefulness and the operational stability that significantly promote reactor; In addition, by means of the film surface shearing force of gas, liquid and the strong oxidizing property of ozone, the problems such as Pore Blocking and generation gel coat will be effectively suppressed, and membrane module water permeability is good, longer service life.
The utility model can run in the mode of multitower combination, and namely 1 central contact tower connects 1 ~ 4 catalyzed oxidation tower, is parallel way, is positioned at central contact tower surrounding, make central contact tower be positioned at reaction unit central position between catalyzed oxidation tower; Current, after central contact tower, enter radial-flow pipe connecting by water conservancy diversion inclined-plane, then divide in each catalyzed oxidation tower of inflow; Greatly expand the scope of application of the present utility model, improve its flexibility of operation and process economy; And according to treatment capacity, the quantity of coupling tower can be selected, be obviously different from the traditional reactor that effective volume is fixing.
Because technique scheme is used, the utility model compared with prior art has following advantages:
(1), in the disclosed device for heterogeneous catalysis ozone Oxidation Treatment water of the utility model, central contact tower can improve the solubleness of ozone molecule in water on the one hand, is conducive to the treatment efficiency improving follow-up heterogeneous catalytic reaction; High-concentrated ozone can be utilized on the other hand to remove unsaturated, the larger molecular organics of part in water selectively, prevent it to be adsorbed in solid catalyst surface, cause the activity of catalyzer to reduce.
(2) membrane separation assemblies that the utility model utilizes can tolerate ozone corrosion, effectively can retain solid catalyst; And the combined action that in tower, pressurization and rising pipe vacuumize provides cross-film working pressure to membrane separation assemblies, further increases the ability that membrane separation assemblies retains solid catalyst, realizes the high efficiency separation of solid catalyst and water.
(3) device disclosed in the utility model is suitable for micron order solid catalyst, solid catalyst is complete fluidized state under the acting in conjunction of air-flow, current, while increasing catalytic effect, overcome the defect that catalyzer in prior art easily runs off, significantly promote water treatment usefulness and the operational stability of reaction unit; Also solve the problem such as Pore Blocking and generation gel coat in prior art, add the water permeability of membrane separation assemblies, longer service life.
(4) in the treatment process that the utility model provides, pressure is introduced first when ozonize, the solubleness of ozone in water is high, effectively can remove unsaturated, the larger molecular organics in sewage, avoid in prior art and cause due to catalyst surface adsorbed polymer the shortcoming that its catalytic performance declines.
(5), in the treatment process that the utility model provides, the regulate and control operation carrying out device based on dissolved ozone concentration is proposed first; Compared with the method for traditional monitoring gas phase ozone concn, control device of the present utility model is sensitiveer, reliable, be applicable to the multiple situation such as drink water purifying and wastewater treatment, can the hydraulic detention time of optimization device and ozone dosage to the full extent, realize object that is energy-conservation, consumption reduction.
(6) the utility model can run in the mode of multitower combination, and according to the quantity of pending water water quality, water yield gating catalytic oxidation tower, water treatment is flexible, gas, liquid mass-transfer efficiency are high, and method is simple, easy handling, treatment time is short, and cost is low, is applicable to industrial applications.
Accompanying drawing explanation
Fig. 1 is the structural representation for heterogeneous catalysis ozone Oxidation Treatment water device in embodiment one;
Fig. 2 is for central contact tower vertical section structure schematic diagram in heterogeneous catalysis ozone Oxidation Treatment water device in embodiment one;
Fig. 3 is for catalyzed oxidation tower vertical section structure schematic diagram in heterogeneous catalysis ozone Oxidation Treatment water device in embodiment one;
Fig. 4 is the vertical view for the device of heterogeneous catalysis ozone Oxidation Treatment water in embodiment two.
Embodiment
Below in conjunction with accompanying drawing, embodiment, the utility model is further described:
In embodiment during unreceipted concrete experimental technique, carry out in accordance with national standard method and condition.
Embodiment one
The utility model device is used for the lake water purifying moderate eutrophication.See accompanying drawing 1-3, heterogeneous catalysis ozone Oxidation Treatment water device is made up of 1 central contact tower, 10,2 radial-flow pipe connectings 30 and 2 catalyzed oxidation towers 20.Wherein, central contact tower 10 tower body height 900 mm, tower body diameter 120 mm; Catalyzed oxidation tower 20 tower body height 900 mm, tower body diameter 170 mm; Central contact tower is connected by radial-flow pipe connecting 30 with catalyzed oxidation tower, and radial-flow pipe connecting is provided with electromagnetic throttle valve 31, and radial-flow pipe connecting is also provided with thief hole 32, and thief hole arranges stopping valve 33; Central contact top of tower is provided with gas skirt 11; Gas skirt is connected with tower body by flange 15; This gas skirt is provided with tail gas discharging pipe 112; Tail gas discharging pipe is provided with tensimeter 113 and electromagnetic throttle valve 114; Water inlet manifold 111 stretches in central contact tower through gas skirt; The length that water inlet manifold is positioned at central contact Ta Tanei part is 200 mm; Central contact tower bottom is provided with titanium aeration head 13; The mean pore size of titanium aeration head is 5 μm; Titanium aeration head connects ozonizer by inlet pipe 131; Titanium aeration head periphery is provided with water conservancy diversion inclined-plane 14; The upper end on inclined-plane contacts with the bottom surface of titanium aeration head, and lower end contacts with radial-flow pipe connecting; Catalyzed oxidation top of tower is provided with gas skirt 27; Gas skirt is connected with tower body by flange 28; This gas skirt is provided with tail gas discharging pipe 271; Tail gas discharging pipe is provided with tensimeter 272 and electromagnetic throttle valve 273; Cylindrical membrane separation assembly 24 is provided with in the middle part of catalyzed oxidation tower; Membrane separation assemblies is fixed on support 243, and support 243 is fixed on catalyzed oxidation inner wall of tower; Membrane separation assemblies long 500 mm, cross-sectional diameter 80 mm, select 47 passage zirconia ceramics films, single film unit is of a size of Φ 30 × 450 mm, every root film unit spacing 20 mm; Filtering accuracy 0.2 μm; Membrane separation assemblies top is provided with rising pipe 241; Rising pipe passes catalyzed oxidation tower, and pass part be provided with vacuum meter 242; Catalyzed oxidation tower middle and lower part is provided with circular cylindrical solid catalyst addition tube 26; Solid catalyst filling tube is provided with stopping valve 261; Catalyzed oxidation tower bottom is provided with titanium aeration plate 21; Titanium aeration plate diameter 80 mm, mean pore size 5 μm; The top of titanium aeration plate is lower than the bottom of radial-flow pipe connecting; Titanium aeration head connects ozonizer by inlet pipe 211; Catalyzed oxidation tower bottom is provided with collection bucket 22; Drain 221 and stopping valve 222 is provided with bottom collection bucket; Solid catalyst 23 is positioned at catalyzed oxidation tower; Be equipped with closed dissolved ozone scale tank 12 in the middle part of central contact tower, in dissolved ozone scale tank, establish on-line computing model 121; Be provided with closed dissolved ozone scale tank 25 in the middle part of catalyzed oxidation tower, in dissolved ozone scale tank, establish on-line computing model 251.
Actual treatment step is:
(1) former water flows into central contact tower with 10 L/min flows by water inlet manifold after coagulation pretreatment, and the streams of ozone passed into bottom titanium aeration head is reverse contacts, and in tower, hydraulic detention time is 1.0 min, working pressure 0.15 MPa; According to the pressure gauge reading of top tail gas discharging pipe, regulate exhaust shutter and ozone air input, to realize pressure-controlling.Titanium aeration head mean pore size 5 μm, inlet pipe connects a CF-G-2-10g type ozonizer (Qingdao Guolin Industry Co., Ltd.), and the latter take air as source of the gas.Inlet gas ozone concentration 20 g/Nm of central contact tower
3, air flow rate 0.4 Nm
3/ h, controlling dissolved ozone concentration in water is 2.1 ± 0.5 mg/L, and tail gas delivers to tail gas breaking plant through gas skirt;
(2) current are in guide face uniformly distributing to 2 pipe connecting, then enter from catalyzed oxidation tower bottom, and single tower hydraulic detention time is 4.0 min, working pressure 0.15 MPa; According to the pressure gauge reading of top tail gas discharging pipe, regulate exhaust shutter and ozone air input, to realize pressure-controlling.Pressure combined action controlling diaphragm separation assembly cross-film working pressure 0.2 ~ 0.25 MPa vacuumized by tower internal pressure and rising pipe.Titanium aeration plate diameter 80 mm, mean pore size 5 μm, inlet pipe is connected to a CF-G-2-20g type ozonizer, and the latter take air as source of the gas.Inlet gas ozone concentration 10 g/Nm of single catalyzed oxidation tower
3, air flow rate 0.75 Nm
3/ h, controlling dissolved ozone concentration in water is 0.2 ± 0.1 mg/L, and tail gas delivers to tail gas breaking plant through gas skirt.Solid catalyst adopts square modified active carbon fiber (Shanghai gac Products Co., Ltd), the length of side 3 mm, tap density 500 kg/m
3, the dosage of unit tower volume is 200 g/m
3, it is complete fluidized state under air-flow, flow action.Process water, by membrane separation assemblies, enters rising pipe and discharges, namely complete water treatment procedure.
Use the utility model to process lake water 6 h of moderate eutrophication continuously, result is as shown in table 1.
The device of table 1 the present embodiment is to the treatment effect of natural lake water
As shown in Table 1, former water is after the process of central contact tower, and the clearance of total organic carbon is not high, but ultraviolet absorptivity UV
254value and colourity obviously reduce, and this illustrates that in water, aromatic compounds is efficiently removed, and the formation potential of chloro detoxicated product significantly reduces.Meanwhile, there is obvious Accumulation Phenomenon in dissolved ozone, and colony-forming unit is in not detecting state.The catalytic oxidation process carried out subsequently is about 70% to the clearance of TOC in water, and dissolved ozone is almost totally consumed, aromaticity (SUVA value=UV that water sample is extremely low
254× 100/TOC) mean that organism is substantially oxidized.The result of embodiment 1 shows, the utility model energy device effectively removes the organic pollutant in natural water body enough at short notice, reaches " drinking water sanitary standard " (GB5749-2006) comprehensively require to create favourable condition for making water quality.
Embodiment two
The utility model device is used for advanced treatment municipal sewage plant bio-chemical effluent.See accompanying drawing 4, heterogeneous catalysis ozone Oxidation Treatment water device is made up of 1 central contact tower, 4 radial-flow pipe connectings and 4 catalyzed oxidation towers; Wherein, central contact tower tower body height 900 mm, tower body diameter 120 mm; Catalyzed oxidation tower tower body height 900 mm, tower body diameter 170 mm; Central contact tower is connected by radial-flow pipe connecting 30 with catalyzed oxidation tower, and radial-flow pipe connecting is provided with electromagnetic throttle valve 31, and radial-flow pipe connecting is also provided with thief hole, and thief hole arranges stopping valve; Central contact top of tower is provided with gas skirt 11; Gas skirt is connected with tower body by flange 15; This gas skirt is provided with tail gas discharging pipe 112; Tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve; Water inlet manifold 111 stretches in central contact tower through gas skirt; The length that described water inlet manifold is positioned at central contact Ta Tanei part is 200 mm; Central contact tower bottom is provided with titanium aeration head; The mean pore size of titanium aeration head is 5 μm; Titanium aeration head connects ozonizer by inlet pipe; Titanium aeration head periphery is provided with water conservancy diversion inclined-plane; The upper end on inclined-plane contacts with the bottom surface of titanium aeration head, and lower end contacts with radial-flow pipe connecting; Catalyzed oxidation top of tower is provided with gas skirt 27; Gas skirt is connected with tower body by flange 28; This gas skirt is provided with tail gas discharging pipe 271; Tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve; Cylindrical membrane separation assembly is provided with in the middle part of catalyzed oxidation tower; Membrane separation assemblies is fixed on support, and support is fixed on catalyzed oxidation inner wall of tower; Membrane separation assemblies selects 1 single passage titanium metallic membrane, is of a size of Φ 50 × 300 mm, filtering accuracy 0.5 μm; Membrane separation assemblies top is provided with rising pipe 241; Rising pipe passes catalyzed oxidation tower, and pass part be provided with vacuum meter; Catalyzed oxidation tower middle and lower part is provided with circular cylindrical solid catalyst addition tube; Solid catalyst filling tube is provided with stopping valve; Catalyzed oxidation tower bottom is provided with titanium aeration plate; Titanium aeration plate diameter 80 mm, mean pore size 5 μm; Titanium aeration head connects ozonizer by inlet pipe; The top of titanium aeration plate is lower than the bottom of radial-flow pipe connecting; Catalyzed oxidation tower bottom is provided with collection bucket; Drain and stopping valve is provided with bottom collection bucket; Solid catalyst is positioned at catalyzed oxidation tower; Be equipped with closed dissolved ozone scale tank in the middle part of central contact tower, catalyzed oxidation tower, in dissolved ozone scale tank, establish on-line computing model.
Actual treatment step is:
(1) bio-chemical effluent flows into central contact tower with 5 L/min flows by water inlet manifold after coagulation pretreatment, and the streams of ozone passed into bottom titanium aeration head is reverse contacts, and in tower, hydraulic detention time is 2.0 min, working pressure 0.15 MPa.According to the pressure gauge reading of top tail gas discharging pipe, regulate exhaust shutter and ozone air input, to realize pressure-controlling.Titanium aeration head mean pore size 5 μm, inlet pipe connects a CF-G-2-20g type ozonizer (Qingdao Guolin Industry Co., Ltd.), and the latter take air as source of the gas.Inlet gas ozone concentration 28 g/Nm of central contact tower
3, air flow rate 0.6 Nm
3/ h, controlling dissolved ozone concentration in water is 1.3 ± 0.3 mg/L, and tail gas delivers to tail gas breaking plant through gas skirt;
(2) current are in water conservancy diversion inclined-plane uniformly distributing to 4 pipe connecting, then enter from catalyzed oxidation tower bottom, and single tower hydraulic detention time is 16.0 min, working pressure 0.15 MPa; According to the pressure gauge reading of top tail gas discharging pipe, regulate exhaust shutter and ozone air input, to realize pressure-controlling.Pressure combined action controlling diaphragm separation assembly cross-film working pressure 0.15 ~ 0.2 MPa vacuumized by tower internal pressure and rising pipe.Titanium aeration plate diameter 80 mm, mean pore size 5 μm, inlet pipe is connected to a CF-G-2-80g type ozonizer, and the latter take air as source of the gas.Inlet gas ozone concentration 15 g/Nm of single catalyzed oxidation tower
3, air flow rate 0.9 Nm
3/ h, controlling dissolved ozone concentration in water is 0.2 ± 0.1 mg/L, and tail gas delivers to tail gas breaking plant through gas skirt.Solid catalyst adopts hydrous iron oxide particle, particle diameter at 0.08 ~ 0.12 mm, tap density 700 kg/m
3, the dosage of unit tower volume is 350 g/m
3, it is complete fluidized state under air-flow, flow action.Process water, by membrane separation assemblies, enters rising pipe and discharges, namely complete water treatment procedure.
Use the utility model continuous Treating Municipal Sewage treatment plant bio-chemical effluent 10 h, result is as shown in table 2.
The device of table 2 the present embodiment is to the advanced treatment effect of bio-chemical effluent
As seen from the above table, central contact tower is only 10% to the clearance of TOC in bio-chemical effluent, but its process colority of water, UV
254value and CFU all significantly reduce, and this is consistent with the accumulation of dissolved ozone.Follow-up catalyzed oxidation tower can not only mineralising partial organic substances, and makes water outlet aromaticity be down to less than 1.2.This means that the utility model is well suited for and the biochemical process couplings such as BAF, to obtain splendid decontamination effect improving.
Claims (8)
1. for a device for heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: comprise 1 central contact tower, 1 ~ 4 catalyzed oxidation tower, radial-flow pipe connecting and solid catalyst, water inlet manifold; Described central contact tower is connected by radial-flow pipe connecting with catalyzed oxidation tower;
Described central contact tower tower body is cylindrical structural, and aspect ratio is 6 ~ 8: 1;
Described central contact top of tower is provided with gas skirt; This gas skirt is provided with tail gas discharging pipe; Described tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve;
Described water inlet manifold stretches in central contact tower through gas skirt; Described water inlet manifold is positioned at 20 ~ 25% of contact tower tower body height centered by central contact Ta Tanei length partly;
Described central contact tower bottom is provided with titanium aeration head; The aperture of described titanium aeration head is 2 ~ 5 μm; Described titanium aeration head periphery is provided with water conservancy diversion inclined-plane; The upper end on described inclined-plane contacts with the bottom surface of titanium aeration head, and lower end contacts with radial-flow pipe connecting;
Described catalyzed oxidation tower tower body is cylindrical structural, and its virtual height is consistent with the virtual height of central contact tower, and aspect ratio is 4 ~ 6: 1;
Described catalyzed oxidation top of tower is provided with gas skirt; This gas skirt is provided with tail gas discharging pipe; Described tail gas discharging pipe is provided with tensimeter and electromagnetic throttle valve;
Cylindrical membrane separation assembly is provided with in the middle part of described catalyzed oxidation tower; The length of described membrane separation assemblies is 30 ~ 60% of catalyzed oxidation tower tower body height; The diameter of described membrane separation assemblies is 30 ~ 50% of catalyzed oxidation tower tower body diameter; The filtering accuracy of described membrane separation assemblies is 0.1 ~ 1.0 μm;
Described membrane separation assemblies top is provided with rising pipe; Described rising pipe passes catalyzed oxidation tower, and pass part be provided with vacuum meter;
Described catalyzed oxidation tower middle and lower part is provided with circular cylindrical solid catalyst addition tube; Described solid catalyst filling tube is provided with stopping valve;
Described catalyzed oxidation tower bottom is provided with titanium aeration plate; The aperture of described titanium aeration plate is 2 ~ 5 μm; Described titanium aeration plate diameter is 1.0 ~ 1.5 times of membrane separation assemblies diameter; The top of described titanium aeration plate is lower than the bottom of radial-flow pipe connecting;
Described catalyzed oxidation tower bottom is provided with collection bucket; Drain and stopping valve is provided with bottom described collection bucket;
Described solid catalyst is positioned at catalyzed oxidation tower;
Closed dissolved ozone scale tank is equipped with in the middle part of described central contact tower, catalyzed oxidation tower.
2. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: described gas skirt is connected with tower body by flange; Described collection bucket is connected with tower body by flange.
3. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: the gas skirt of described central contact top of tower is frustro-pyramidal; The gas skirt of described catalyzed oxidation top of tower is conical; The collection bucket of described catalyzed oxidation tower bottom is turbination.
4. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: described membrane separation assemblies is fixed on support; Described support is fixed on catalyzed oxidation inner wall of tower.
5. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: described radial-flow pipe connecting is provided with electromagnetic throttle valve and thief hole.
6. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: the tap density of described solid catalyst is 450 ~ 900 kg/m
3; The flaky material that described solid catalyst is particle diameter is the particle of 0.05 ~ 0.30 mm, long limit is 1 ~ 20 mm or length are the filamentary material of 1 ~ 20 mm.
7. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: in described central contact tower, titanium aeration head service area be 1.5 times of tower body sectional area, the inclination angle on water conservancy diversion inclined-plane is 45 degree, and water inlet manifold is positioned at position, gas skirt axis.
8. according to claim 1 for the device of heterogeneous catalysis ozone Oxidation Treatment water, it is characterized in that: in described membrane separation assemblies, film unit is tubular type aluminum oxide ceramic membrane, tubular type zirconium white ceramic membrane, tubular type titanium dioxide ceramic membrane or tubular type titanium metal film.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420452864.2U CN204058048U (en) | 2014-08-12 | 2014-08-12 | For the device of heterogeneous catalysis ozone Oxidation Treatment water |
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| CN201420452864.2U CN204058048U (en) | 2014-08-12 | 2014-08-12 | For the device of heterogeneous catalysis ozone Oxidation Treatment water |
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| CN (1) | CN204058048U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104211160A (en) * | 2014-08-12 | 2014-12-17 | 苏州科技学院 | Heterogeneous catalysis ozone oxidation method for water treatment and device applied to the method |
| CN105731629A (en) * | 2016-02-19 | 2016-07-06 | 博天环境集团股份有限公司 | Catalytic oxidation treatment method of reverse-osmosis strong brine |
| CN106745670A (en) * | 2016-12-09 | 2017-05-31 | 深圳市康源环境纳米科技有限公司 | The water purifying processing system and method for a kind of brominated mineral water |
| CN109928484A (en) * | 2017-12-15 | 2019-06-25 | 中国科学院大连化学物理研究所 | A kind of O3 catalytic oxidation reaction unit |
-
2014
- 2014-08-12 CN CN201420452864.2U patent/CN204058048U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104211160A (en) * | 2014-08-12 | 2014-12-17 | 苏州科技学院 | Heterogeneous catalysis ozone oxidation method for water treatment and device applied to the method |
| CN105731629A (en) * | 2016-02-19 | 2016-07-06 | 博天环境集团股份有限公司 | Catalytic oxidation treatment method of reverse-osmosis strong brine |
| CN106745670A (en) * | 2016-12-09 | 2017-05-31 | 深圳市康源环境纳米科技有限公司 | The water purifying processing system and method for a kind of brominated mineral water |
| CN109928484A (en) * | 2017-12-15 | 2019-06-25 | 中国科学院大连化学物理研究所 | A kind of O3 catalytic oxidation reaction unit |
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