CN204490649U - Circulation speed change fluidized-bed Fenton catalytic oxidizing equipment - Google Patents
Circulation speed change fluidized-bed Fenton catalytic oxidizing equipment Download PDFInfo
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- CN204490649U CN204490649U CN201520098387.9U CN201520098387U CN204490649U CN 204490649 U CN204490649 U CN 204490649U CN 201520098387 U CN201520098387 U CN 201520098387U CN 204490649 U CN204490649 U CN 204490649U
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Abstract
The utility model provides a kind of circulation speed change fluidized-bed Fenton catalytic oxidizing equipment, comprises the Rotary-table and a reacting tank body that are interconnected, and a rising pipe, pyrrhosiderite carrier, a medicine storage pool, enter Teat pipette, a wastewater disposal basin and an intake pump; Described Rotary-table is positioned at the top of reacting tank body, and described rising pipe is communicated in the top of Rotary-table; Described pyrrhosiderite carrier from top to bottom interval is filled in reacting tank body; Described enter one end of Teat pipette be communicated with the bottom of medicine storage pool, the other end is communicated in the bottom of reacting tank body; One end of described intake pump is communicated with the bottom of wastewater disposal basin, and the other end is communicated in the bottom of reacting tank body.The utility model reduces H
2o
2rate of decomposition, adds concentration and the utilising efficiency of hydroxyl radical free radical in mixed solution, improves the mass-transfer efficiency of reactant, improve catalyzing oxidizing degrading pollutent efficiency, recycling of promoting catalyst, reduces catalyzer dosage, thus reduces the sludge yield of reaction system.
Description
Technical field
The utility model is specifically related to a kind of circulation speed change fluidized-bed Fenton catalytic oxidizing equipment.
Background technology
High-level oxidation technology is used to indegradable industrial effluent process because it can produce the hydroxyl radical free radical of high oxidation activity in homogeneous phase or heterophasic system.Fenton fluidized-bed is a kind of Technology that Fenton catalyzed reaction combines with fluidized-bed reactor, cardinal principle is applied in fluidized-bed reactor by Fenton reagent, the mode of fluidization reaction bed is utilized to improve the contact efficiency of catalyzer and reaction solution, utilize the different valence state iron ion produced in Fenton's reaction process, cover from load at fluidized-bed carrier surface in the mode of crystallization or precipitation, enable these ferriferous oxides participate in the supply of a part of iron, reduce adding thus reducing the generation of mud of molysite.
In conventional homogeneous Fenton catalytic oxidation system, oxygenant and ferrous salt usage quantity greatly, generate a large amount of iron containing sludge after process, and its subsequent treatment cost and secondary pollution problem seriously, constrain the industrial application of homogeneous phase Fenton-like system.
Utility model content
The technical problems to be solved in the utility model, is to provide a kind of circulation speed change fluidized-bed Fenton catalytic oxidizing equipment.
The utility model is achieved in that a kind of circulation speed change fluidized-bed Fenton catalytic oxidizing equipment, comprise the Rotary-table and a reacting tank body that are interconnected, and a rising pipe, pyrrhosiderite carrier, a medicine storage pool, enter Teat pipette, a wastewater disposal basin and an intake pump; Described Rotary-table is positioned at the top of reacting tank body, and described rising pipe is communicated in the top of Rotary-table; Described pyrrhosiderite carrier from top to bottom interval is filled in reacting tank body; Described enter one end of Teat pipette be communicated with the bottom of medicine storage pool, the other end is communicated in the bottom of reacting tank body; One end of described intake pump is communicated with the bottom of wastewater disposal basin, and the other end is communicated in the bottom of reacting tank body.
Preferably, also to comprise on one filtering net and once filtering net, described upper filtering net is located between Rotary-table and reacting tank body, and described lower filtering net is located at the bottom of reacting tank body, and is positioned at the below of described pyrrhosiderite carrier; The aperture of described upper filtering net and lower filtering net is 0.6mm.
Preferably, also comprise a recycle pump, one end of described recycle pump is communicated with the bottom of reacting tank body, and the other end is communicated in the bottom of Rotary-table.
Preferably, the work lift of described recycle pump is 10m H
2o, described in enter Teat pipette and intake pump work lift be 35m H
2o.
Preferably, also comprise relative and spaced a pair waved plate, described two waved plate verticals are located at middle part in reacting tank body, and described pyrrhosiderite carrier is filled in the space that two waved plates are formed.
Preferably, the top of described Rotary-table is provided with a stifle, and this stifle and Rotary-table are fastenedly connected.
Preferably, the sidewall middle and lower part of described Rotary-table is inwardly shunk, and forms a skew wall, and the acute angle between this skew wall and horizontal plane is 60 degree.
Preferably, the admission space of described pyrrhosiderite carrier is 65% of reacting tank body volume.
The utility model has the advantage of: the utility model under stress, makes mixture be tied to form fluidization by recycle pump; By arranging a pair waved plate in reacting tank body, making the circulation velocity sustained mutations of mixed solution in reacting tank body, becoming strong turbulent state; The utility model, by impressed pressure, reduces H
2o
2rate of decomposition, adds concentration and the utilising efficiency of hydroxyl radical free radical in mixed solution; By the strong turbulent fluctuation state of mixed solution, improve the mass-transfer efficiency of reactant, improve catalyzing oxidizing degrading pollutent efficiency, recycling of promoting catalyst, reduce catalyzer dosage, thus reduce the sludge yield of reaction system.
Accompanying drawing explanation
The utility model is further described with reference to the accompanying drawings in conjunction with the embodiments.
Fig. 1 is the structural representation of the utility model circulation speed change fluidized-bed Fenton catalytic oxidizing equipment.
Embodiment
Refer to Fig. 1, a kind of circulation speed change fluidized-bed Fenton catalytic oxidizing equipment, comprise Rotary-table 1 and the reacting tank body 2 be interconnected, and a rising pipe 3, pyrrhosiderite carrier 4, medicine storage pool 5, enter Teat pipette 6, wastewater disposal basin 7, intake pump 8 and relative and spaced a pair waved plate 9; Also comprise filtering net 10 on, once filtering net 11 and a recycle pump 12.
Referring again to Fig. 1, described Rotary-table 1 is positioned at the top of reacting tank body 2, and described rising pipe 3 is communicated in the top of Rotary-table 1; The top of described Rotary-table 1 is provided with a stifle 13, and this stifle 13 is fastenedly connected with Rotary-table 1, realizes being fastenedly connected with Rotary-table 1 by fastener bolt.The sidewall middle and lower part of described Rotary-table 1 is inwardly shunk, and forms a skew wall 11, and the acute angle between this skew wall 11 and horizontal plane is 60 degree, and a small amount of floc sludge be deposited on Rotary-table inwall can be made to enter reacting tank body 2.Rotary-table 1 and reacting tank body 2 adopt carbon steel, and the voltage withstand class of Rotary-table 1 and reacting tank body 2, stifle 13 and fastening piece is 0.6MPa.The length of described reacting tank body 2 is preferably 1500cm, and basal diameter is preferably 60cm.
Referring again to Fig. 1, described medicine storage pool 5 is for storing Fenton reagent and H
2o
2and Fe
2+the liquid mixed mutually.Described pyrrhosiderite carrier 4 from top to bottom interval is filled in reacting tank body 2; Namely described two waved plate 9 verticals are located at middle part in reacting tank body 2, and described pyrrhosiderite carrier 4 is filled in the space that two waved plates 9 are formed.The admission space of described pyrrhosiderite carrier 4 is 65% of reacting tank body 2 volume.The particle diameter of the pyrrhosiderite sand in pyrrhosiderite carrier 4 is 1mm.The setting of two waved plates 9 makes the flowing of mixed solution become the strong turbulent fluctuation state of vertical unsteady flow speed.
Referring again to Fig. 1, described in enter Teat pipette 6 one end be communicated with the bottom of medicine storage pool 5, the other end is communicated in the bottom of reacting tank body 2; One end of described intake pump 8 is communicated with the bottom of wastewater disposal basin 7, and the other end is communicated in the bottom of reacting tank body 2.One end of described recycle pump 12 is communicated with the bottom of reacting tank body 2, and the other end is communicated in the bottom of Rotary-table 1.The work lift of described recycle pump 12 is 10m H
2o, described in enter Teat pipette 6 and intake pump 8 work lift be 35m H
2o.
Referring again to Fig. 1, described upper filtering net 10 is located between Rotary-table 1 and reacting tank body 2, and described lower filtering net 11 is located at the bottom of reacting tank body 2, and is positioned at the below of described pyrrhosiderite carrier 4; The aperture of described upper filtering net 10 and lower filtering net 11 is 0.6mm.
Referring again to Fig. 1, when applying utility model works, waste water containing pollutent enters bottom reacting tank body 2 by wastewater disposal basin 7 by intake pump 8, Fenton reagent is passed through to enter bottom reacting tank body 2 into Teat pipette 6 by medicine storage pool 5, enter after lower filtering net 11 filters again in space that two waved plates 9 surround, carry out adsorbing and reacting with pyrrhosiderite carrier 4.Circulation, external power is provided by recycle pump 12, and the water inlet pipe mouth of recycle pump 12 is positioned at the central position of Rotary-table 1, and recycle pump 12 from the bottom suction mixed solution of Rotary-table 1, then puts it into the bottom of reacting tank body 2.Upper filtering net 10 and lower filtering net 11 are all fixedly welded on reacting tank body 2, and lower filtering net 11 is double does water distribution effect, and uniform fluid distribution is entered in reacting tank body 2.Pyrrhosiderite carrier 4 surface has four kinds of Lewis acid position surface hydroxyls, and the part ferrous ion in mixed solution can be adsorbed on ferriferous oxide surface, forms the surface bonding catalystic converter system that ferrous iron-ferriferous oxide coexists.Free state Fe (II) reactive behavior in Fenton reagent is more weak, and the Fe (II) being adsorbed on pyrrhosiderite carrier 4 surface then has quite high reactive behavior.The catalytic carrier surface that ferrous iron-ferriferous oxide coexists, by the transfer transport between Fe (II) and Fe (III), the adsorption site FeIII (OH) on iron mineral surface is with free state FeII (OH)+combining generates the intermediate product FeIIOFeIIIOH of the mixed valence stronger than ionic state Fe (II) ion reduction, surface bonding iron has quite high catalytic reaction activity, facilitate the generation of electronic transfer process, accelerate the organic conversion in waste water.Under circulating fluidization effect, constantly separate out at the ferrous ion on pyrrhosiderite carrier 4 surface, dissolve and deposit, constantly there is redox in the ferriferous oxide on pyrrhosiderite carrier 4 surface, form homogeneous phase to heterogeneous heterogeneous catalytic reaction system, reduction and oxidation are constantly carried out, and make Fe (II) ion be able to recycle, catalyst levels greatly reduces, improve the utilising efficiency of catalyzer and Fenton reagent, the sludge quantity that reaction system is produced reduces.
The utility model is pressurized reactor, and namely pressure type circulation speed change fluidized-bed reaction system, has delayed H
2o
2decompose, increase the dividing potential drop of molecular oxygen in mixed solution, improve the recycle efficiency of oxygenant hydroxyl radical free radical.Waved plate 9 is set in reactor, to form the strong turbulent fluctuation state of variable flow.
Before the utility model and conventional homogeneous catalytic oxidation system and Fenton fluidized-bed, load biphasic catalysis is oxidized two kinds of systems and contrasts, under stress, adopt applied mechanical energy Circulation, to promote in heterogeneous system iron ion at carrier surface from loading process, adopt variable circulation flowing, improve carrier surfactant, carrier surface deposited iron can be dissolved rapidly again simultaneously, form homogeneous phase to heterogeneous heterogeneous catalytic reaction system, improve the quadric catalysis usefulness from load iron; Build pressure environment simultaneously, reduce H
2o
2rate of decomposition, improves oxygen partial pressure, improves the utilising efficiency of hydroxyl radical free radical, reduces oxygenant H
2o
2with ferrous salt consumption, reach the iron sludge yield both reducing reaction system, the object of catalyzing oxidizing degrading pollutent efficiency can be improved again.
1, the pyrrhosiderite that the utility model employing particle diameter is tiny is as support of the catalyst, and ferrous in the precipitation of carrier surface deposition, formed in conjunction with iron, catalytic activity is improved, and formation heterogeneous catalytic reaction system, catalyst levels reduces.
2, adopt pressurized reactor, delay H
2o
2rate of decomposition, improve the service efficiency of oxygenant.
3, adopt circulation speed change fluidization reaction system, facilitate mass-transfer efficiency, improve catalytic carrier surfactivity, add speed of reaction.
Claims (8)
1. a circulation speed change fluidized-bed Fenton catalytic oxidizing equipment, is characterized in that: comprise the Rotary-table and a reacting tank body that are interconnected, and a rising pipe, pyrrhosiderite carrier, a medicine storage pool, enter Teat pipette, a wastewater disposal basin and an intake pump; Described Rotary-table is positioned at the top of reacting tank body, and described rising pipe is communicated in the top of Rotary-table; Described pyrrhosiderite carrier from top to bottom interval is filled in reacting tank body; Described enter one end of Teat pipette be communicated with the bottom of medicine storage pool, the other end is communicated in the bottom of reacting tank body; One end of described intake pump is communicated with the bottom of wastewater disposal basin, and the other end is communicated in the bottom of reacting tank body.
2. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, it is characterized in that: also to comprise on one filtering net and once filtering net, described upper filtering net is located between Rotary-table and reacting tank body, described lower filtering net is located at the bottom of reacting tank body, and is positioned at the below of described pyrrhosiderite carrier; The aperture of described upper filtering net and lower filtering net is 0.6mm.
3. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, it is characterized in that: also comprise a recycle pump, one end of described recycle pump is communicated with the bottom of reacting tank body, and the other end is communicated in the bottom of Rotary-table.
4. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 3, is characterized in that: the work lift of described recycle pump is 10m H
2o, described in enter Teat pipette and intake pump work lift be 35m H
2o.
5. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, it is characterized in that: also comprise relative and spaced a pair waved plate, described two waved plate verticals are located at middle part in reacting tank body, and described pyrrhosiderite carrier is filled in the space that two waved plates are formed.
6. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, is characterized in that: the top of described Rotary-table is provided with a stifle, and this stifle and Rotary-table are fastenedly connected.
7. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, it is characterized in that: the sidewall middle and lower part of described Rotary-table is inwardly shunk, and forms a skew wall, and the acute angle between this skew wall and horizontal plane is 60 degree.
8. circulation speed change fluidized-bed Fenton catalytic oxidizing equipment as claimed in claim 1, is characterized in that: the admission space of described pyrrhosiderite carrier is 65% of reacting tank body volume.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520098387.9U CN204490649U (en) | 2015-02-11 | 2015-02-11 | Circulation speed change fluidized-bed Fenton catalytic oxidizing equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520098387.9U CN204490649U (en) | 2015-02-11 | 2015-02-11 | Circulation speed change fluidized-bed Fenton catalytic oxidizing equipment |
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| Publication Number | Publication Date |
|---|---|
| CN204490649U true CN204490649U (en) | 2015-07-22 |
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|---|---|---|---|
| CN201520098387.9U Expired - Fee Related CN204490649U (en) | 2015-02-11 | 2015-02-11 | Circulation speed change fluidized-bed Fenton catalytic oxidizing equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104671500A (en) * | 2015-02-11 | 2015-06-03 | 福建工程学院 | Fenton catalytic oxidation device of circulating variable-speed fluidized bed |
-
2015
- 2015-02-11 CN CN201520098387.9U patent/CN204490649U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104671500A (en) * | 2015-02-11 | 2015-06-03 | 福建工程学院 | Fenton catalytic oxidation device of circulating variable-speed fluidized bed |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150722 Termination date: 20190211 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |