CN108069501A - A kind of technique for handling organic wastewater - Google Patents
A kind of technique for handling organic wastewater Download PDFInfo
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- CN108069501A CN108069501A CN201610991500.5A CN201610991500A CN108069501A CN 108069501 A CN108069501 A CN 108069501A CN 201610991500 A CN201610991500 A CN 201610991500A CN 108069501 A CN108069501 A CN 108069501A
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- 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
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
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- Hydrology & Water Resources (AREA)
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- Environmental & Geological Engineering (AREA)
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
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Abstract
The present invention relates to technical field of waste water processing, specifically disclose a kind of technique for handling organic wastewater, and the technique includes herein below：Using rotary drill reactor as consersion unit, include interior revolving bed and outer revolving bed in the rotary drill reactor housing, using organic wastewater as raw material, oxidation reaction is carried out under the conditions of existing for ozone, the interior revolving bed is made of corrosion-resistant frame and catalyst A, and the outer revolving bed is made of corrosion-resistant frame and catalyst B.Present invention process is simple, and stability is good, and not only COD removes ability height, and can solve the problems, such as metal loss.
Description
Technical field
The present invention relates to field of Environment Protection, particularly a kind for the treatment of process of organic wastewater.
Background technology
A large amount of organic polluting waters caused by industrial production have seriously affected the survival condition and ecological environment of the mankind,
Through becoming society and the economic problems of getting worse, be especially difficult to biodegradable treatment of Organic Wastewater get up it is more tired
It is difficult；Further, since water resource is increasingly in short supply, national, the formulation of new standard further stringent to water pollutant prediction emission
The preventing and controlling of China's Petrochemical Enterprises water pollution are proposed with new challenge, Petrochemical Enterprises use existing secondary biochemical process
Afterwards, efflux wastewater sewage majority cannot still reach the emission request of new standard.It is therefore desirable to carry out depth to externally discharged waste water
Reason with realize qualified discharge in addition can reuse, this to reduce waste water the discharge capacity to discharge pollutants, cut down enterprise blowdown
Consumption of expense and reduction water resource etc. is of great significance.
High-level oxidation technology（AOP）It is more than that all common oxidants or oxidizing potential are close to or up to hydroxyl to refer to oxidability
Base free radical OH is horizontal, and serial radical chain reaction can be carried out with organic pollution, so as to destroy its structure, it is made progressively to drop
It solves as the organic matter of harmless low molecular weight, is finally degraded to CO2、H2The technology of O and other mineral salts.Hydrogen peroxide and ozone are
Common AOP oxidants.Hydrogen peroxide generates hydroxyl radical free radical by Fenton methods, but used homogeneous catalyst has use
The problems such as medicament is more, and recycling is difficult, easily cause secondary pollution.There is ozone molecule and organic matters for the independent oxidation technology of ozone
Direct reaction selectivity is strong, reaction rate constant is low and Recalcitrant chemicals cannot it is quick and complete by oxidation removal the shortcomings of.
Ozone catalytic Wet Oxidation Process generates great amount of hydroxy group free radical during the reaction by adding in catalyst ozone（Hydroxyl
Rate constant is 10 when free radical is reacted with most of organic matters6~109M-1s-1, with ozone and the organic matter reaction rate constant
Compared to being at least higher by 7 orders of magnitude）, can those be difficult to the organic matter oxygen for individually being aoxidized or being degraded with ozone at normal temperatures and pressures
Change to purify water.Catalytic wet oxidation can overcome the shortcomings that independent ozone oxidation, so as to become more with practical value new
Type high-level oxidation technology.
At present, ozone wet raw noodles processing waste water is mostly using metal oxide supported type catalyst and ozone one
It reacts, Cu-series catalyst has preferable catalytic effect, but easy metal loss causes secondary pollution, country's limit in waste water
It is fixed（GB8978-1996）The content of total copper will be less than 500 μ g/L in sewage discharge primary standard, and secondary standard requirement is less than
1000 μg/L。
Patent CN01135047.4 discloses a kind of copper-based catalysts for catalytic wet oxidation processing industrial wastewater
It prepares and applies.The main component of catalyst is the oxide of copper, zinc, nickel, magnesium, aluminium, chromium, iron and a part of rare earth metal.It should
Catalyst is co-precipitated to obtain the catalyst of hydrotalcite-like compound by the salt for containing various metals, is controlled the loss of copper ion
System.But the method for preparing catalyst is complicated, and only has positive effect in phenol, neopelex and bigcatkin willow acid system,
It is very limited in the application.
The content of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of work using catalytic wet ozone Oxidation Treatment organic wastewater
Skill, this is simple for process, and stability is good, and not only COD removes ability height, and can solve the problems, such as metal loss.
The present invention provides a kind of technique for handling organic wastewater, and the technique includes herein below：With rotary drill reactor
As consersion unit, interior revolving bed and outer revolving bed are included in the rotary drill reactor housing, using organic wastewater as raw material,
Oxidation reaction is carried out under the conditions of ozone is existing, the interior revolving bed is made of corrosion-resistant frame and catalyst A, the outer rotation
Bed is made of corrosion-resistant frame and catalyst B, and the catalyst A is noble metal carrier catalyst, and catalyst B loads for copper system
Type catalyst.
In organic wastewater treatment process of the present invention, the rotary drill reactor include revolving bed, end socket, reactor shell,
Feed pipe and charging distributor pipe, the reactor shell and end socket form closing housing, during revolving bed is vertically set in housing
Portion, the revolving bed center are empty barrel structure, and charging distributor pipe is arranged in the empty barrel structure at revolving bed center, feeds distributor pipe
It is connected with feed pipe, discharge port is arranged on reactor shell lower part, by sealing structure between revolving bed top and reactor shell
Part is fixedly connected, and to be rotatably connected between revolving bed top and containment member, revolving bed is filled by rotation axis and lower part driving
Connection is put, the revolving bed includes interior revolving bed and outer revolving bed, and outer revolving bed is arranged at the radial outside of interior revolving bed.
In above-mentioned rotary drill reactor, the reactor shell is cylindrical tube, and the end socket includes upper cover under
End socket, cylindrical reactor are vertically arranged.
In above-mentioned rotary drill reactor, revolving bed shape is cylinder barrel shaped, is set between revolving bed and reactor shell suitable
Suitable gap forms annulus；Revolving bed center is cylindrical empty cylinder, and charging distributor pipe is arranged in the cylindrical empty cylinder, into
Expect to have between distributor pipe and revolving bed suitable for gap, form annulus；On charging distributor pipe suitable material is set to be distributed
Hole, the length for feeding distributor pipe are corresponding with the axial length of revolving bed；Rotation axis is fixedly connected with the fixed plate of revolving bed lower end,
Rotation axis is vertically arranged；Rotation axis is connected by end socket with the driving device that top outside reactor or lower part are set.
In above-mentioned rotary drill reactor, gap is with or without between interior revolving bed and outer revolving bed, when there is gap, inward turning
Clearance distance between rotated bed and outer revolving bed is 5mm~300mm, preferably 10mm~50mm.
In organic wastewater treatment process of the present invention, the organic wastewater enters rotary drill reactor with ozone and is reacted
When, organic wastewater contacts first with interior revolving bed to be reacted, and is then contacted and is reacted with outer revolving bed again.
In organic wastewater treatment process of the present invention, the catalyst A is noble metal carrier catalyst, including carrier and is born
The active metal component being loaded on carrier, wherein with one or more of activated carbon, molecular sieve or oxide for carrier；It is described
Molecular sieve is one or more of A types, Y types, Beta, ZSM-5, TS-1, MCM-41 molecular sieve, and the oxide is oxidation
One or more of aluminium, ceria, zirconium dioxide, titanium dioxide, silica；With in precious metals pt, Pd, Rh, Ru, Ir
One or several kinds for active metal component, on the basis of the weight of catalyst, the content of noble metal is 0.01% based on the element
~5.0%.Adjuvant component is further included in the active metal component of the catalyst A, the adjuvant component is rare earth metal, and rare earth is golden
The content of category is based on the element 0.1% ~ 20.0%, and the rare earth metal is lanthanum, the one or more in cerium, praseodymium, neodymium.
In organic wastewater treatment process of the present invention, the catalyst B is copper system support catalysts, including carrier and load
Active metal component on carrier, wherein with one or more of activated carbon, molecular sieve, oxide for carrier；Described point
Son sieve is A types, Y types, one or more of Beta, ZSM-5, TS-1, MCM-41 molecular sieve, the oxide is aluminium oxide,
One or more of ceria, zirconium dioxide, titanium dioxide, silica；Using copper as active metal component, rare earth metal
For auxiliary agent, on the basis of the weight of catalyst, active metal component is calculated with the content of oxide：CuO is 1 ~ 30wt%；It is dilute
Soil metal oxide is 0.1 ~ 25wt%.It can also include iron, nickel or vanadium in the copper system support catalysts active metal component
One or more of.
In organic wastewater treatment process of the present invention, the rare earth metal is lanthanum, the one or more in cerium, praseodymium, neodymium.
In organic wastewater treatment process of the present invention, the reaction temperature in reactor is 0~50 DEG C, is preferably 20~30 DEG C；
Reaction pressure is normal pressure.
In organic wastewater treatment process of the present invention, the volume ratio of the catalyst A and catalyst B is 20%~80%：20%~
80%, it is preferably 40%~70%：30%~60%.
In organic wastewater treatment process of the present invention, the rotating speed of revolving bed is 0~5000 rev/min, is preferably 150~2000
Rev/min.
In organic wastewater treatment process of the present invention, the ozone usage is smelly as needed for calculating original organic wastewater COD value
0.3~2.0 times of oxygen dosage.
In organic wastewater treatment process of the present invention, the COD of the organic wastewater is 10 ~ 10000 mg/L, and the waste water can
Think any one of waste water from dyestuff, petrochemical wastewater and coal chemical industrial waste water or several.
Organic wastewater treatment process of the present invention, waste water under the conditions of existing for ozone first with noble metal catalyst
Contact, the ozone of high concentration convert a part of organic pollution under the action of noble metal catalyst, downstream ozone concentration drop
It is low, it is contacted again with the stronger Cu-series catalyst of catalytic capability at this time, gives full play to the catalytic action of Cu-series catalyst；Your gold passed through
The synergistic effect of metal catalyst and Cu-series catalyst, not only treatment of Organic Wastewater effect is good, but also can also effectively reduce metallic copper
Loss, solve the problems, such as in the prior art use existing for Cu-series catalyst copper metal be lost in it is serious.With prior art phase
Than, the present invention in higher organic wastewater COD removal effects are maintained by using grading method of catalyst, reduce metal from
The discharge of son, and with higher reactivity and stability in use, especially suitable for catalytic wet ozone oxidation reaction.This hair
Bright procedure is simply, conveniently, easily operated, is suitble to commercial Application.
Organic wastewater treatment process of the present invention, using rotary drill reactor as consersion unit, and will catalysis
Agent is packed into the bed of revolving bed in the form of filler, and the contacting efficiency of waste water, ozone and catalyst greatly improved, contract significantly
The short reaction time, and efficiency is improved, consersion unit scale can substantially reduce, and then reduce equipment cost and operating cost
With.
Description of the drawings
Fig. 1 is a kind of rotary drill reactor structure diagram in the treatment process of organic wastewater of the present invention.Wherein：1 is upper
End socket, 2 be low head, and 3 be reactor shell, and 4 be outer revolving bed, and 5 be interior revolving bed, and 6 be revolving bed, and 7 be charging distributor pipe,
8 be feed pipe, and 9 be rotation axis, and 10 be low head mechanical seal, and 11 be shaft coupling, and 12 be motor, and 13 be discharge port, and 14 be to have
Machine waste water, 15 be ozone, and 16 be containment member, and 17 be fixed plate.
Specific embodiment
The preparation method further illustrated the present invention with reference to specific embodiment, but the scope of the present invention is not only
It is limited to the scope of these embodiments.
Existing rotation in this field may be employed in rotary drill reactor used in the treatment process of organic wastewater of the present invention
Rotated bed reactor can also be prepared according to method disclosed in the prior art, specifically be used in the embodiment of the present invention such as Fig. 1 institutes
The rotary drill reactor shown.
As shown in Figure 1, the present invention provides a kind of rotary drill reactor, the rotary drill reactor includes upper cover 1, lower envelope
First 2, reactor shell 3, feed pipe 8, charging distributor pipe 7, revolving bed 6, the reactor shell 3, upper cover 1,2 structure of low head
Into closing housing, the reactor shell 3 is cylindrical tube, and revolving bed 6 is vertically set on middle part in housing, outside revolving bed 6
Shape is cylinder barrel shaped, is set between revolving bed 6 and reactor shell suitable for gap, forms annulus, feeds and is set on distributor pipe 7
Suitable material distribution hole is put, the length for feeding distributor pipe 7 is corresponding with the axial length of revolving bed 6；6 center of revolving bed is
Cylindrical empty barrel structure, charging distributor pipe 7 are arranged in the cylindrical empty barrel structure at 6 center of revolving bed, charging distributor pipe 7 and rotation
Have between rotated bed 6 suitable for gap, form annulus；Charging distributor pipe 7 is connected with feed pipe 8, and discharge port 13 is arranged on instead
Answer device lower housing portion, be fixedly connected between 6 top of revolving bed and reactor shell by containment member 16,6 top of revolving bed with
To be rotatably connected between containment member 16, rotation axis 9 is fixedly connected with the fixed plate 17 of 6 lower end of revolving bed, and revolving bed 6 passes through
Rotation axis 9 is connected with lower part driving device 12, and the revolving bed 6 includes interior revolving bed 5 and outer revolving bed 4, and outer revolving bed 4 is set
In the radial outside of interior revolving bed 5.
When carrying out treatment of Organic Wastewater using rotary drill reactor of the present invention, organic wastewater 14 and ozone 15 into
Into revolving bed 6 after being distributed after expects pipe 8 by feeding distributor pipe 7, successively with the catalyst A in interior revolving bed 5 and outer revolving bed 4
It is reacted with catalyst B contact contacts, the purified water obtained after reaction is discharged by discharge port 13.
The preparation of catalyst A1（Ru/AC）
By diameter 2.0mm, specific surface area 704m2/ g, pore volume 0.7cm3The commercial column-shaped active carbon item of/g, 2.0 nm of average pore size
It is dried for standby at 120 DEG C.The active sketching charcoal of 500g drying is weighed, according to its water absorption rate RuCl3Total catalyst weight is accounted for by Ru
2% ratio wiring solution-forming.With Ru solution incipient impregnation activity sketching charcoal 24 it is small when, 100 DEG C drying after be put into tube furnace,
400 DEG C with containing 10%H2N2Reduce 4 it is small when, then with containing 1%O2N2Be passivated 4 it is small when, temperature is taken out after dropping to room temperature, is urged
Agent A1.
The preparation of catalyst A2（Ru-Ce/ZSM-5）
By diameter 2.0mm, specific surface area 320m2/ g, 0.3 cm of pore volume3The commercial ZSM-5 molecular sieve of/g, average pore size 2.4nm
Bar shaped carrier is dried for standby at 120 DEG C.The ZSM-5 carriers of 500g drying are weighed, it is a certain amount of to account for the measurement of 1.0% ratio according to Ru
RuCl3Solution, when incipient impregnation carrier 24 is small.It is put into after 120 DEG C of drying in tube furnace, at 400 DEG C with containing 10%H2N2Also
When original 4 is small, then with containing 1%O2N2Be passivated 4 it is small when.5.0% ratio, which is accounted for, according still further to Ce weighs a certain amount of Ce (NO3)3·6H2O is made into molten
Liquid, when incipient impregnation carrier 24 is small again by sample made from previous step.120 DEG C drying after be put into tube furnace, 800 DEG C with
When nitrogen roasting 4 is small, then with containing 1%O2N2Be passivated 4 it is small when.Temperature is taken out after dropping to room temperature, obtains catalyst A2.
The preparation of catalyst A3（Pt/TiO2）
By diameter 2.0mm, 100 m of specific surface area2/ g, 0.4 cm of pore volume3The bar shaped TiO of/g, average pore size 3.4nm2Carrier exists
120 DEG C are dried for standby.Weigh TiO2Carrier 500g, according to its water absorption rate chloroplatinic acid（H2PtCl6·6H2O）Catalyst is accounted for by Pt
The ratio wiring solution-forming of total weight 2%.With Pt solution incipient impregnations TiO2When carrier 24 is small, tube furnace is put into after 100 DEG C of drying
In, at 400 DEG C with containing 10%H2N2Reduce 4 it is small when, then with containing 1%O2N2Be passivated 4 it is small when, temperature is taken out after dropping to room temperature, obtains
To catalyst A3.
The preparation of catalyst B1（Cu-Ce/AC）
By diameter 2.0mm, specific surface area 583m2/ g, pore volume 0.6cm3The commercial column-shaped active carbon item of/g, 2.0 nm of average pore size
It is dried for standby at 120 DEG C.The active sketching charcoal of 500g drying is weighed, according to its water absorption rate Cu (NO3)2·3H2O and Ce (NO3)3·
6H2O presses CuO and CeO2The ratio wiring solution-forming of total catalyst weight 5% and 1.5% is accounted for respectively.With Cu-Ce solution incipient impregnations
When active sketching charcoal 2 is small, 80 DEG C of drying, when roasting 4 is small under 550 DEG C of nitrogen atmospheres, temperature is taken out after dropping to room temperature, obtains catalyst
B1。
The preparation of catalyst B2（Cu-La/TS-1）
By diameter 2.0mm, specific surface area 432m2/ g, 0.2 cm of pore volume3The TS-1 molecular sieves bar shaped of/g, average pore size 3.3nm carry
Body is dried for standby at 120 DEG C.TS-1 molecular sieve carrier 500g are weighed, with Cu (NO3)2·3H2O and La (NO3)3·6H2O by CuO and
La2O3The ratio for accounting for total catalyst weight 6% and 1.5% respectively is made into 1000 mL solution.With Cu-La solution dipping TS-1 carriers 3
Hour, stand in air 24 it is small when after with 80 DEG C of evaporated in vacuo of rotary evaporator, dried in 100 DEG C of drying boxes of obtained sample
It is dry.Then when 550 DEG C of roastings 4 are small in Muffle furnace, temperature is taken out after dropping to room temperature, obtains catalyst A2.
The preparation of catalyst B3（Cu-Ce/SiO2）
By diameter 2.0mm, specific surface area 207m2/ g, 0.8 cm of pore volume3The bar shaped SiO of/g, average pore size 5.8nm2Carrier is 120
It DEG C is dried for standby.Weigh SiO2Carrier 500g, with Cu (NO3)2·3H2O and Ce (NO3)3·6H2O presses CuO and CeO2Catalysis is accounted for respectively
The ratio wiring solution-forming of agent total weight 5% and 1.5%.With Cu-Ce solution incipient impregnations SiO2When carrier 2 is small, 80 DEG C of drying,
When roasting 4 is small under 550 DEG C of nitrogen atmospheres, temperature is taken out after dropping to room temperature, obtains catalyst B3.
Embodiment 1
Catalyst A1 and B1 is loaded into the interior rotation of reactor respectively according to the ratio that percent by volume is respectively 65% and 35%
In bed and outer revolving bed, distance 5mm between inside and outside revolving bed.Catalyst total volume is 100cm3.Reaction condition：Acid scarlet mould
Intend the COD of waste water from dyestuff as 286.3 mg/L, feed rate is 200 mL/h, and ozone concentration is 9.0 g/m3, gas flow rate is
400 mL/min, 600 revs/min of revolving bed rotating speed, reaction carry out at normal temperatures and pressures.Its COD of liquid testing after reaction, according to
The removal rate of COD weighs catalyst activity.Liquid inductivity coupled plasma mass spectrometry after reaction（ICP-MS）Copper test from
The content of son, to investigate the wastage of metal.The results are shown in tables 1.
Embodiment 2
It is respectively that 20% and 80% ratio is loaded into reactor according to percent by volume by catalyst A2 and B1, revolving bed rotating speed
200 revs/min, very close to each other between inside and outside revolving bed, other reaction conditions are same as Example 1.The results are shown in tables 1.
Embodiment 3
It is respectively that 80% and 20% ratio is loaded into reactor according to percent by volume by catalyst A3 and B1, revolving bed rotating speed
1200 revs/min, very close to each other between inside and outside revolving bed, other reaction conditions are same as Example 1.The results are shown in tables 1.
Embodiment 4
Be respectively that 65% and 35% ratio is loaded into reactor according to percent by volume by catalyst A1 and B2, reaction condition with
Embodiment 1 is identical.The results are shown in tables 1.
Embodiment 5
Be respectively that 65% and 35% ratio is loaded into reactor according to percent by volume by catalyst A3 and B2, reaction condition with
Embodiment 1 is identical.The results are shown in tables 1.
Embodiment 6
Be respectively that 65% and 35% ratio is loaded into reactor according to percent by volume by catalyst A2 and B3, reaction condition with
Embodiment 1 is identical.The results are shown in tables 1.
1 embodiment 1-6 Comparative results of table
Embodiment 7
Reaction condition is with embodiment 1, and using coal chemical industry brine waste, original solution COD is 449.3 mg/L.Inlet gas ozone concentration changes
For 14.5 g/m3.The results are shown in tables 2.
Embodiment 8
For reaction condition with embodiment 4, the waste water used is the secondary bio-chemical effluent of Nanjing petrochemical industry, and original solution COD is 67.6 mg/L.
Inlet gas ozone concentration is changed to 2.8 g/m3.The results are shown in tables 2.
Embodiment 9
For reaction condition with embodiment 6, the waste water model compound used is phenol, and original solution COD is 324.7 mg/L.Air inlet is smelly
Oxygen concentration is changed to 12.0 g/m3.The results are shown in tables 2.
2 embodiment 7-9 Comparative results of table
Comparative example 1
Catalyst A1 is used alone, reaction condition is same as Example 1.The results are shown in tables 3.
Comparative example 2
Catalyst B1 is used alone, reaction condition is same as Example 1.The results are shown in tables 3.
Comparative example 3
Catalyst B2 is used alone, reaction condition is same as Example 1.The results are shown in tables 3.
Comparative example 4
Catalyst B3 is used alone, reaction condition is same as Example 1.The results are shown in tables 3.
3 comparative example 1-4 Comparative results of table
It can be learnt by above example and comparative example：The catalyst grade of the present invention can significantly reduce the stream of copper ion with mode
It loses, while keeps higher COD removal rates.
Claims (17)
1. a kind of technique for handling organic wastewater, the technique include herein below：Using rotary drill reactor as consersion unit,
Include interior revolving bed and outer revolving bed in the rotary drill reactor housing, using organic wastewater as raw material, in item existing for ozone
Oxidation reaction is carried out under part, the interior revolving bed is made of corrosion-resistant frame and catalyst A, and the outer revolving bed is by corrosion-resistant frame
Frame and catalyst B are formed, and the catalyst A is noble metal carrier catalyst, and catalyst B is copper system support catalysts.
2. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The rotary drill reactor includes rotation
Rotated bed, end socket, reactor shell, feed pipe and charging distributor pipe, the reactor shell and end socket form closing housing, rotation
Bed is vertically set on middle part in housing, and the revolving bed center is empty barrel structure, and charging distributor pipe is arranged on revolving bed center
In empty barrel structure, charging distributor pipe is connected with feed pipe, and discharge port is arranged on reactor shell lower part, revolving bed top and reaction
It is fixedly connected between device housing by containment member, to be rotatably connected between revolving bed top and containment member, revolving bed leads to
It crosses rotation axis to be connected with lower part driving device, the revolving bed includes interior revolving bed and outer revolving bed, and outer revolving bed is arranged at interior
The radial outside of revolving bed.
3. the technique of processing organic wastewater described in accordance with the claim 2, it is characterised in that：The reactor shell is cylinder
Cylinder, the end socket include upper cover and low head, and cylindrical reactor is vertically arranged.
4. the technique of processing organic wastewater described in accordance with the claim 2, it is characterised in that：Revolving bed shape is cylinder barrel shaped,
It is set between revolving bed and reactor shell suitable for gap, forms annulus；Revolving bed center is cylindrical empty cylinder, and charging divides
Stringing is arranged in the cylindrical empty cylinder, and feeding between distributor pipe and revolving bed has suitable for gap, forms annulus；Charging
Suitable material distribution hole is set on distributor pipe, and the length for feeding distributor pipe is corresponding with the axial length of revolving bed；Rotation axis with
The fixed plate of revolving bed lower end is fixedly connected, and rotation axis is vertically arranged；Rotation axis passes through top or lower part outside end socket and reactor
The driving device connection of setting.
5. the technique of processing organic wastewater described in accordance with the claim 2, it is characterised in that：Between interior revolving bed and outer revolving bed
It is with or without gap.
6. according to the technique of the processing organic wastewater described in claim 5, it is characterised in that：Between interior revolving bed and outer revolving bed
Clearance distance be 5mm~300mm, preferably 10mm~50mm.
7. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The catalyst A and catalyst B's
Volume ratio is 20%~80%：20%~80%.
8. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The catalyst A and catalyst B's
Volume ratio is 40%~70%：30%~60%.
9. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The catalyst A bears for noble metal
Supported catalyst, including carrier and the active metal component being supported on carrier, wherein in activated carbon, molecular sieve, oxide
One or more be carrier；The molecular sieve for A types, Y types, one kind in Beta, ZSM-5, TS-1, MCM-41 molecular sieve or
Several, the oxide is one or more of aluminium oxide, ceria, zirconium dioxide, titanium dioxide, silica；With
One or several kinds in precious metals pt, Pd, Rh, Ru, Ir are active metal component, on the basis of the weight of catalyst, your gold
The content of category is 0.01% ~ 5.0% based on the element.
10. according to the technique of the processing organic wastewater described in claim 9, it is characterised in that：The catalyst A includes helping
Agent, the auxiliary agent is lanthanum, the one or more in cerium, praseodymium, neodymium, and the auxiliary agent content is 0.1 ~ 20wt%.
11. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The catalyst B include carrier and
The active metal component being supported on carrier, wherein with one or more of activated carbon, molecular sieve, oxide for carrier；Institute
Molecular sieve is stated as one or more of A types, Y types, Beta, ZSM-5, TS-1, MCM-41 molecular sieve, the oxide is oxidation
One or more of aluminium, ceria, zirconium dioxide, titanium dioxide, silica；Active metal component is contained with oxide
It measures to calculate：CuO is 1 ~ 30wt%；Rare-earth oxide is 0.1 ~ 25wt%.
12. according to the technique of the processing organic wastewater described in claim 11, it is characterised in that：The activity gold of the catalyst B
Belonging to component includes one or more of iron, nickel, vanadium.
13. according to the technique of the processing organic wastewater described in claim 11, it is characterised in that：The rare earth metal for lanthanum,
One or more in cerium, praseodymium, neodymium.
14. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：Reaction temperature in reactor is 0
~50 DEG C, be preferably 20~30 DEG C；Reaction pressure is normal pressure.
15. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The rotating speed of the revolving bed for 0~
5000 revs/min, be preferably 150~2000 revs/min.
16. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The ozone usage is by raw material
0.3~2.0 times of ozone usage needed for the calculating of organic wastewater COD value.
17. the technique of processing organic wastewater described in accordance with the claim 1, it is characterised in that：The COD of the organic wastewater is 10
~10000 mg/L。
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|---|---|---|---|
| CN201610991500.5A CN108069501A (en) | 2016-11-11 | 2016-11-11 | A kind of technique for handling organic wastewater |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610991500.5A CN108069501A (en) | 2016-11-11 | 2016-11-11 | A kind of technique for handling organic wastewater |
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| CN109603836A (en) * | 2019-01-09 | 2019-04-12 | 广州桑尼环保科技有限公司 | A kind of recyclable magnetic powdery ozone catalyst and preparation method thereof |
| CN109761337A (en) * | 2019-03-21 | 2019-05-17 | 杭州小橙工业设计有限公司 | A kind of reactor of wet oxidation processing waste water |
| CN111377521A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating organic wastewater by catalytic oxidation of ozone |
| CN111377525A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating wastewater by adopting ozone catalytic wet oxidation |
| CN111377526A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Organic wastewater treatment method |
| CN111377523A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Catalytic wet oxidation treatment method for organic wastewater |
| CN111377519A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating organic wastewater |
| CN111377520A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Organic wastewater treatment process |
| CN111377524A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating wastewater by using ozone catalytic wet oxidation |
| CN111377522A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating wastewater by ozone catalytic wet oxidation |
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| CN111377524A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating wastewater by using ozone catalytic wet oxidation |
| CN111377521A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating organic wastewater by catalytic oxidation of ozone |
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| CN111377520A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Organic wastewater treatment process |
| CN111377526B (en) * | 2018-12-28 | 2021-06-04 | 中国石油化工股份有限公司 | Organic wastewater treatment method |
| CN111377524B (en) * | 2018-12-28 | 2021-06-04 | 中国石油化工股份有限公司 | Method for treating wastewater by using ozone catalytic wet oxidation |
| CN111377525A (en) * | 2018-12-28 | 2020-07-07 | 中国石油化工股份有限公司 | Method for treating wastewater by adopting ozone catalytic wet oxidation |
| CN111377523B (en) * | 2018-12-28 | 2021-05-04 | 中国石油化工股份有限公司 | Catalytic wet oxidation treatment method for organic wastewater |
| CN111377522B (en) * | 2018-12-28 | 2021-05-04 | 中国石油化工股份有限公司 | Method for treating wastewater by ozone catalytic wet oxidation |
| CN111377519B (en) * | 2018-12-28 | 2021-05-04 | 中国石油化工股份有限公司 | Method for treating organic wastewater |
| CN111377520B (en) * | 2018-12-28 | 2021-05-04 | 中国石油化工股份有限公司 | Organic wastewater treatment process |
| CN111377525B (en) * | 2018-12-28 | 2021-05-04 | 中国石油化工股份有限公司 | Method for treating wastewater by adopting ozone catalytic wet oxidation |
| CN109603836A (en) * | 2019-01-09 | 2019-04-12 | 广州桑尼环保科技有限公司 | A kind of recyclable magnetic powdery ozone catalyst and preparation method thereof |
| CN109761337A (en) * | 2019-03-21 | 2019-05-17 | 杭州小橙工业设计有限公司 | A kind of reactor of wet oxidation processing waste water |
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