CN2913345Y - Vertical expanded bed micro-electrolytic catalytic oxidizing reactor - Google Patents
Vertical expanded bed micro-electrolytic catalytic oxidizing reactor Download PDFInfo
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- CN2913345Y CN2913345Y CN 200620070012 CN200620070012U CN2913345Y CN 2913345 Y CN2913345 Y CN 2913345Y CN 200620070012 CN200620070012 CN 200620070012 CN 200620070012 U CN200620070012 U CN 200620070012U CN 2913345 Y CN2913345 Y CN 2913345Y
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Abstract
A micro-electrolysis catalytic oxidation reactor of vertical type expanded bed comprises a vertical cylinder as the reaction vessel, a water inlet pipe disposed at the bottom of the reaction vessel and communicated with the cylinder, and a water outlet pipe disposed at the top of the reaction vessel and communicated with the cylinder. The utility model is characterized in that the inner chamber of the vertical cylinder is divided into two or more iron-carbon mixed beds by a perforated sieve plate in an up-down direction, each mixed bed is filled with high carbon-iron mixture, a flushing pump is disposed outside the cylinder, the outlet of the flushing pump is communicated with the inner chamber at the bottom of the cylinder via a flushing pipe, the inlet of the flushing pump is communicated with the inner chamber at the top of the cylinder via the flushing pipe, and the communication part of the inlet of the flushing pump and the inner chamber at the top of the cylinder is disposed below the water outlet pipe and above the uppermost layer of iron-carbon mixed bed. The utility mode utilizes the principle of multistage expanded bed connected in series to prevent the high carbon-iron filling material from being hardened, laminated and inactivated, and improves the uniformly dispersing effect of the iron-carbon mixture and the wastewater to be treated in the reactor, thereby improving the COD treatment efficiency.
Description
Technical field
The utility model relates to a kind of wastewater treatment equipment, is specifically related to the physical chemistry wastewater treatment equipment that a kind of little electrolysis combines with catalyzed oxidation.
Background technology
Iron carbon method is that multiple physics, chemical actions such as a kind of current collection is separated, coagulation, electricity flocculation, absorption are in the method for wastewater treatment of one.Its ultimate principle is to form the electrochemical techniques that countless small galvanic cells are handled waste water through corrosion effect in electrolyte solution.
Handle in the waste water process in iron carbon method, with organic waste water by the bed of high-carbon iron is housed, owing to contain tart waste water and high-carbon iron has produced various small galvanic cells, in slant acidity solution, the nascent state H that electrode reaction produced has higher activity, can carry out DeR with the tensio-active agent that contains in the waste water.On the lower anode of electropotential, iron loses electronics and generates Fe
2+Enter in the solution, make stream of electrons to carbon cathode.Consequent nascent state Fe
2+Also have very high activity,, thereby promote the galvanic corrosion of iron, make a large amount of Fe on the one hand in order to overcoming the anodic polarized action
2+Enter solution and form flocculation agent, these flocculation agent have higher absorption coagulation activity, can remove the organism and the colloidalmaterial of the change structure that produces in electric field effectively, thereby reach the removal effect to waste water COD.In the iron carbon reactor, add oxygenant on the other hand, utilize the oxidizing reaction of the ferrous ion catalysis peroxidation agent that produces in the iron carbon reaction process.The synergistic effect of little electrolysis and catalyzed oxidation want high more than the stack of each individual effect, and the consumption of oxygenant reduces greatly.Simultaneously, the clearance of COD can reach 60～90%.It is relevant with original concentration and the wastewater property of COD that this removes efficient.
Existing iron carbon reactor form has vertical and horizontal two kinds.The characteristics of vertical reactor are: in the work, current flow from bottom to top, current are even, the processing efficiency height, but shortcoming is the iron carbon filler easily to harden, the easy passivation of particle surface, and processing efficiency obviously descends, the whole bed laminate is formed one when serious, and processing efficiency sharply descends and finally causes equipment normally not move.Though can overcome the problem that hardens of filler behind the horizontal reactor installation whipping appts, current short circuit, low, the serious phenomenon of sealing leak of plant factor have appearred, and processing efficiency is not high yet.In a word, little catalytic and oxidative electrolysis technology method itself has very high efficient to handling high concentrated organic wastewater, and because the defective of existing two kinds of iron carbon reactors self has caused this treatment process to be subjected to considerable restraint in actual applications.Therefore, how to overcome the defective of existing iron carbon reactor, design a kind of rational in infrastructurely, the processing efficiency height can prevent that the iron carbon reactor that filler hardens from being the problem that the utility model presses for solution.
Summary of the invention
The utility model provides a kind of vertical expanded bed catalyst oxidation reactor, its objective is that the iron carbon filler easily hardens and passivation during will solve existing vertical iron carbon reactor uses, and causes the low problem of processing efficiency.
For achieving the above object, the technical solution adopted in the utility model is: the little catalytic and oxidative electrolysis technology reactor of a kind of vertical expanded bed, with vertical cylindrical shell as reaction vessel, reaction container bottom is provided with water inlet pipe and is communicated with cylindrical shell, the top is provided with rising pipe and is communicated with cylindrical shell, vertical inner barrel above-below direction is divided into two or more iron carbon mixed beds with porous sieve plate, be filled with the high-carbon iron mixture in each mixed bed, flushing pump is established in the cylindrical shell outside, the flushing pump outlet is communicated with cylindrical shell bottom inner chamber through washpipe, the flushing pump import is communicated with cylindrical shell top inner chamber through washpipe, and the flushing pump import is located on the position that rising pipe is following and the superiors' iron carbon mixed bed is above with the position that is communicated with of cylindrical shell top inner chamber.
Related content in the technique scheme is explained as follows:
1, in the such scheme, in order to improve the homogeneity of wastewater treatment, can be provided with a stir shaft from top to bottom in inner barrel central authorities, corresponding every layer of iron carbon mixed bed is equipped with agitating vane on the stir shaft, agitating vane is positioned at the superjacent air space of every floor height carbon iron mixture, and stir shaft is connected with electric motor through speed reduction unit.For the ease of installing and maintenance, stir shaft can be formed by connecting by many minor axises, and stir shaft is provided with the wearing and tearing that removable wearing bush is avoided stir shaft outward again.
2, in the such scheme, flow out reactor for fear of the high-carbon iron particle with water, make the reactor water outlet even simultaneously, avoid the current short circuit, can be provided with triphase separator at the cylindrical shell top, triphase separator is made of an awl bucket and one group of blow-down pipe, awl bucket outer rim is connected with the sealing of cylindrical shell top inner wall, bores the bucket bottom and is provided with through hole, and one group of blow-down pipe vertically is located on awl bucket and the extreme higher position, cylindrical shell junction, and along circumferentially uniform, the outlet of blow-down pipe is higher than liquid level in the cylindrical shell., gas solid in order further to increase, water three phase separation effect can be provided with expanding reach at the cylindrical shell top, and the awl bucket outer rim in the triphase separator is sealed with the expanding reach inwall and is connected.Also can be provided with overflow weir at the cylindrical shell top, the overflow port of overflow weir is higher than the awl bucket, and liquid is communicated with rising pipe through overflow weir in the cylindrical shell.Like this in the bed by current take out of high-carbon iron filling settlement and be back to bed, handle the gas that produces in the waste water process and discharge by blow-down pipe, water outlet is flowed out from rising pipe through overflow weir by the through hole of awl bucket bottom, realizes solid, gas, water three phase separation with this.
3, in the such scheme,, can be connected with compressed air pipe, utilize compressed-air actuated effect that the high-carbon iron filler is washed away at cylindrical shell bottom inner chamber in order further to improve the effect that prevents to harden with purifying.Evenly upwards flow in reactor in order to ensure waste water and pressurized air, water inlet pipe, washpipe and compressed air pipe all are communicated with inner barrel by even distribution device after entering cylindrical shell, make water gentle in bed even upper reaches, lifting processing efficiency and developing result.
4, in the such scheme, steadily efficient in order to make the reactor oxidation, according to the concentration of waste water, so should be provided with doser outside the cylindrical shell, doser feeds in the cylindrical shell by the road.Can be to applying oxygenant in the reactor by doser, oxygenant adds mode can be divided into two kinds: first kind is waste strength when not too high, adds hydrogen peroxide to reactor bottom; Second kind is waste strength when very high, adds hydrogen peroxide simultaneously to reactor bottom and middle part.
5, in the such scheme, the shape of described cylindrical shell can have following two kinds of forms:
(1), cylindrical shell is up big and down small conically shaped, the porous sieve plate external diameter of below is less than the internal diameter of top porous sieve plate support.The advantage of this structure is: the first, and the cylindrical shell side need not be provided with and add discharge opening, reinforced can in cylindrical shell, carrying out layer by layer from bottom to top, discharging can be carried out in cylindrical shell from top to bottom layer by layer.The second, when the filler of each layer iron carbon mixed bed hardens, handle also more convenient.
(2), cylindrical shell is straight tube, its corresponding each layer iron carbon mixed bed is provided with at sidepiece and adds discharge opening.
Therefore 6, in the such scheme, in reactor, fully contact, when design, will consider this problem aspect two of the path length that waste water flows through and the residence time with the iron carbon mixture in order to make processed waste water.In order to realize such effect, be divided into two or more iron carbon mixed beds with porous sieve plate from bottom to top in the reactor, can avoid channel and wall stream like this.The purpose that agitating vane is installed in the reactor is that the water of iron carbon mixed bed underflow to the upper strata is mixed, from whole bed, because stirring action on the water screw, can promote waste water treatment efficiency like this.
7, in the such scheme, the height of reactor or the iron carbon mixed bed number of plies can design according to waste strength, and reactor diameter can design according to wastewater flow.
The utility model technical conceive and principle are: utilize plural serial stage expanded bed principle, the bed of being made up of the high-carbon iron filler in the vertical iron carbon reactor is in expand the state that rolls, the filler of avoiding vertical iron carbon reactor to occur usually to harden under the flushing pump effect and the difficult problem of particle passivation.
Because the technique scheme utilization, the utility model compared with prior art has following advantage:
1, because the utility model utilizes the vertical expanded bed principle of plural serial stage, single slage fixed bed with original vertical iron carbon reactor, be improved to the plural serial stage expanded bed that band stirs, make the bed of forming by the high-carbon iron filler in the vertical iron carbon reactor when flushing, be in the state that rolls that expands, in this process, the ironing surface oxide compound of high-carbon is washed away removal, make the high-carbon iron filler really accomplish not lump, not passivation, and the structure of plural serial stage has improved the homodisperse effect of interior high-carbon iron of reactor and processed waste water greatly, inside reactor is installed whipping appts also can effectively avoid the current short circuit, has therefore improved the COD processing efficiency of reactor greatly.
Problems such as 2, the expanded bed form because the vertical multi-stage that the utility model adopts band to stir is connected has overcome the easy short circuit of horizontal iron carbon reactor current, and equipment efficiency of usage is low.In vertical expanded bed reactor, waste water is the upper reaches after reactor bottom is by uniform distribution, in the overflow weir outflow of top triphase separator periphery, can guarantee that waste water evenly passes bed in bed, avoid short circuit, and in operational process, waste water has been full of reactor all the time, and plant factor is higher.
3, because the utility model adopts the gap backwashing manner to make the high-carbon iron bed be in swelling state when flushing, during normal the operation still is fixed bed, not only improved the homodisperse effect of iron carbon filler in the reactor, and avoid reactor to be in the back mixing state for a long time, energy-saving effect is obvious, and improves reactor for treatment efficient.
4, because the utility model reactor is installed whipping appts, therefore reactor waste water in operational process flows through reaction bed with spiral path, prolong the residence time of waste water in reactor so greatly, under the similarity condition, the flow process of waste water is longer, more duration of contact with the high-carbon iron bed, improved processing efficiency.
5,, a small amount of gas with foreign flavor that reactor produces at operational process can be drawn the back and concentrate discharging because the utility model reactor design has blow-down pipe.
Description of drawings
Accompanying drawing 1 is the utility model embodiment one structural representation;
Accompanying drawing 2 is the utility model embodiment two structural representations.
In the above accompanying drawing: 1, doser; 2, transferpump; 3, pipeline; 4, stopping valve; 5, under meter; 6, wastewater disposal basin; 7, cylindrical shell; 8, water inlet pipe; 9, the equal stringing of intaking; 10, add discharge opening; 11, compressed air pipe; 12, high-carbon iron filler; 13, rising pipe; 14, porous sieve plate; 15, triphase separator; 16, expanding reach; 17, overflow weir; 18, electric motor; 19, speed reduction unit; 20, stir shaft; 21, agitating vane; 22, flushing pump; 23, washpipe; 24, blow-down pipe; 25, retaining plate.
Embodiment
Below in conjunction with drawings and Examples the utility model is further described:
Embodiment one: referring to shown in Figure 1, the physical chemistry wastewater treatment equipment that a kind of little electrolysis combines with catalyzed oxidation is made up of the little catalytic and oxidative electrolysis technology reactor of vertical expanded bed, doser 1, transferpump 2, pipeline 3, stopping valve 4 and under meter 5 etc.Doser 1 feeds in the cylindrical shell 7 by the road.
Processed waste water in the wastewater disposal basin 6 is sent into the little catalytic and oxidative electrolysis technology reactor of vertical expanded bed by transferpump 2 by pipeline 3 and is handled.Doser 1 (being administration device), stopping valve 4 and under meter 5 are separately positioned on the corresponding pipeline 3.
The little catalytic and oxidative electrolysis technology reactor of vertical expanded bed, as reaction vessel, reaction container bottom is provided with water inlet pipe 8 and is communicated with cylindrical shell 7 with vertical cylindrical shell 7, and the top is provided with rising pipe 13 and is communicated with cylindrical shell 7.Vertical cylindrical shell 7 main bodys are straight tube, straight tube sidepiece is provided with and adds discharge opening 10 (being access opening), cylindrical shell 7 inner above-below directions are divided into four iron carbon mixed beds (seeing shown in Figure 1) with porous sieve plate 14, be filled with high-carbon iron filler 12 in each mixed bed, flushing pump 22 is established in cylindrical shell 7 outsides, flushing pump 22 outlets are communicated with cylindrical shell 7 bottom inner chambers through washpipe 23, and flushing pump 22 imports are communicated with cylindrical shell 7 top inner chambers through washpipe 23.Cylindrical shell 7 bottom inner chambers are connected with compressed air pipe 11.Water inlet pipe 8 is by equal stringing 9 of water inlet and cylindrical shell 7 internal communication, washpipe 23 and compressed air pipe 11 after entering cylindrical shell 7 all by even distribution device and cylindrical shell 7 internal communication.Cylindrical shell 7 bottoms are retaining plate 25, and are fixing with bolt and basis, do not load material in the reactor bottom chamber.
During normal the operation, waste water enters in the reactor from water inlet pipe 8, through upper reaches, water inlet equal stringing 9 back, in cavity, mix the back little catalytic and oxidative electrolysis technology reaction takes place in bed with oxygenant, flow to reactor head expanding reach 16 in the continuation, processed waste water, flows out from rising pipe 13 again through overflow weir 17 at last by the awl bucket bottom through-hole in the triphase separator 15.Small amount of exhaust gas flows out from top blow-down pipe 24.The waste water at expanding reach 16 places turns back to cylindrical shell 7 bottoms through washpipe 23 and flushing pump 22 again.Every certain interval of time post-flush pump 22 and compressed air electromagnetic valve were opened several minutes, make the interior bed of reactor interval some cycles after once, avoid bed to harden and the high-carbon iron surface passivation, reactor waste water lift velocity is enough to make the high-carbon iron bed to be in swelling state during flushing, feeding pressurized air simultaneously makes the high-carbon iron particle roll in sharp impacts, effectively remove the oxide compound of high-carbon iron particle surface, can prevent effectively that the high-carbon iron bed from hardening and passivation (flow velocity that waste water makes progress in the bed during flushing depends on high-carbon iron particulate density and particle diameter).When reactor normally moved, the pressurized air low discharge entered reactor, can improve oxidation efficiency, saved oxygenant.
After each flushing, particle layering trend must appear in the bed, and the time is long more, and demixing phenomenon is obvious more.And vertical plural serial stage expanded bed, though demixing phenomenon occurs in each bed, whole reactor, size distribution are still uniformly.
Embodiment two: referring to shown in Figure 2, the little catalytic and oxidative electrolysis technology reactor of a kind of vertical expanded bed, be with embodiment one difference: the first, cylindrical shell 7 is up big and down small conically shaped, porous sieve plate 14 external diameters of below are less than the internal diameter of top porous sieve plate 14 supports.The second, cylindrical shell 7 sides are not established and are added discharge opening.Other is identical with embodiment one, no longer is repeated in this description here.
The foregoing description only is explanation technical conceive of the present utility model and characteristics, and its purpose is to allow the personage who is familiar with this technology can understand content of the present utility model and enforcement according to this, can not limit protection domain of the present utility model with this.All equivalences of being done according to the utility model spirit change or modify, and all should be encompassed within the protection domain of the present utility model.
Claims (10)
1, the little catalytic and oxidative electrolysis technology reactor of a kind of vertical expanded bed, with vertical cylindrical shell as reaction vessel, reaction container bottom is provided with water inlet pipe and is communicated with cylindrical shell, the top is provided with rising pipe and is communicated with cylindrical shell, it is characterized in that: vertical inner barrel above-below direction is divided into two or more iron carbon mixed beds with porous sieve plate, be filled with the high-carbon iron mixture in each mixed bed, flushing pump is established in the cylindrical shell outside, the flushing pump outlet is communicated with cylindrical shell bottom inner chamber through washpipe, the flushing pump import is communicated with cylindrical shell top inner chamber through washpipe, and the flushing pump import is located on the position that rising pipe is following and the superiors' iron carbon mixed bed is above with the position that is communicated with of cylindrical shell top inner chamber.
2, reactor according to claim 1, it is characterized in that: described inner barrel central authorities are provided with a stir shaft from top to bottom, corresponding every layer of iron carbon mixed bed is equipped with agitating vane on the stir shaft, agitating vane is positioned at the superjacent air space of every floor height carbon iron mixture, and stir shaft is connected with electric motor through speed reduction unit.
3, reactor according to claim 2 is characterized in that: stir shaft is formed by connecting stir shaft peripheral hardware wearing bush in the described cylindrical shell by many minor axises.
4, reactor according to claim 1, it is characterized in that: described cylindrical shell top is provided with triphase separator, triphase separator is made of an awl bucket and one group of blow-down pipe, awl bucket outer rim is connected with the sealing of cylindrical shell top inner wall, awl bucket bottom is provided with through hole, one group of blow-down pipe vertically is located on awl bucket and the extreme higher position, cylindrical shell junction, and along circumferentially uniform, the outlet of blow-down pipe is higher than liquid level in the cylindrical shell.
5, reactor according to claim 3 is characterized in that: described cylindrical shell top is provided with expanding reach, and the awl bucket outer rim in the triphase separator is connected with the sealing of expanding reach inwall.
6, reactor according to claim 3 is characterized in that: described cylindrical shell top is provided with overflow weir, and the overflow port of overflow weir is higher than the awl bucket, and liquid is communicated with rising pipe through overflow weir in the cylindrical shell.
7, reactor according to claim 1 is characterized in that: described cylindrical shell bottom inner chamber is connected with compressed air pipe, and described water inlet pipe, washpipe and compressed air pipe all are communicated with inner barrel by even distribution device after entering cylindrical shell.
8, reactor according to claim 1 is characterized in that: described cylindrical shell is up big and down small conically shaped, and the porous sieve plate external diameter of below is less than the internal diameter of top porous sieve plate support.
9, reactor according to claim 1 is characterized in that: described cylindrical shell is provided with doser outward, and doser feeds in the cylindrical shell by the road.
10, reactor according to claim 1 is characterized in that: described cylindrical shell is straight tube, and its corresponding each layer iron carbon mixed bed is provided with at sidepiece and adds discharge opening.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620070012 CN2913345Y (en) | 2006-03-06 | 2006-03-06 | Vertical expanded bed micro-electrolytic catalytic oxidizing reactor |
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| CN 200620070012 CN2913345Y (en) | 2006-03-06 | 2006-03-06 | Vertical expanded bed micro-electrolytic catalytic oxidizing reactor |
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| CN 200620070012 Expired - Fee Related CN2913345Y (en) | 2006-03-06 | 2006-03-06 | Vertical expanded bed micro-electrolytic catalytic oxidizing reactor |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040299A (en) * | 2010-11-19 | 2011-05-04 | 中南民族大学 | Integrated laboratory waste water treatment method and device |
| CN103011348A (en) * | 2012-12-12 | 2013-04-03 | 上海交通大学 | Integrated sub-three-phase separated-type internal electrolysis reactor and applications |
| CN103073093A (en) * | 2013-01-24 | 2013-05-01 | 昆明理工大学 | Multistage inclined-plate type electric filter bed and application thereof in purification of heavy metal wastewater |
| CN103663802A (en) * | 2012-08-29 | 2014-03-26 | 安徽南风环境工程技术有限公司 | Microelectrolysis-fenton oxidizing reaction device |
| CN103880225A (en) * | 2014-03-21 | 2014-06-25 | 安徽华骐环保科技股份有限公司 | Multistage ferric-carbon microelectrolysis coupled Fenton oxidation bed reactor |
| CN104229947A (en) * | 2014-09-03 | 2014-12-24 | 广州绿日环保科技有限公司 | Wastewater treatment device and method using multi-element coal and iron carbon |
| CN106554057A (en) * | 2016-11-25 | 2017-04-05 | 江苏鼎弘环境科技有限公司 | A kind of micro-electrolysis reactor of sewage containing tar |
| CN107445290A (en) * | 2017-09-11 | 2017-12-08 | 安庆师范大学 | A kind of wastewater treatment equipment of wind drive |
| CN112320896A (en) * | 2020-09-30 | 2021-02-05 | 山东默锐环境产业股份有限公司 | Little electrolytic reactor of synergism |
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2006
- 2006-03-06 CN CN 200620070012 patent/CN2913345Y/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040299A (en) * | 2010-11-19 | 2011-05-04 | 中南民族大学 | Integrated laboratory waste water treatment method and device |
| CN103663802A (en) * | 2012-08-29 | 2014-03-26 | 安徽南风环境工程技术有限公司 | Microelectrolysis-fenton oxidizing reaction device |
| CN103663802B (en) * | 2012-08-29 | 2015-06-24 | 安徽南风环境工程技术有限公司 | Microelectrolysis-fenton oxidizing reaction device |
| CN103011348A (en) * | 2012-12-12 | 2013-04-03 | 上海交通大学 | Integrated sub-three-phase separated-type internal electrolysis reactor and applications |
| CN103073093A (en) * | 2013-01-24 | 2013-05-01 | 昆明理工大学 | Multistage inclined-plate type electric filter bed and application thereof in purification of heavy metal wastewater |
| CN103880225A (en) * | 2014-03-21 | 2014-06-25 | 安徽华骐环保科技股份有限公司 | Multistage ferric-carbon microelectrolysis coupled Fenton oxidation bed reactor |
| CN103880225B (en) * | 2014-03-21 | 2018-09-25 | 安徽华骐环保科技股份有限公司 | A kind of multistage iron-carbon micro-electrolysis coupling Fenton oxidation bed reactor |
| CN104229947A (en) * | 2014-09-03 | 2014-12-24 | 广州绿日环保科技有限公司 | Wastewater treatment device and method using multi-element coal and iron carbon |
| CN104229947B (en) * | 2014-09-03 | 2016-08-24 | 广州绿日环保科技有限公司 | Use wastewater treatment equipment and the method for polynary coal ferrum carbon |
| CN106554057A (en) * | 2016-11-25 | 2017-04-05 | 江苏鼎弘环境科技有限公司 | A kind of micro-electrolysis reactor of sewage containing tar |
| CN107445290A (en) * | 2017-09-11 | 2017-12-08 | 安庆师范大学 | A kind of wastewater treatment equipment of wind drive |
| CN112320896A (en) * | 2020-09-30 | 2021-02-05 | 山东默锐环境产业股份有限公司 | Little electrolytic reactor of synergism |
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Granted publication date: 20070620 Termination date: 20140306 |