CN100358612C - Removal of gasified harmful substance from airflow - Google Patents
Removal of gasified harmful substance from airflow Download PDFInfo
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- CN100358612C CN100358612C CNB200410084443XA CN200410084443A CN100358612C CN 100358612 C CN100358612 C CN 100358612C CN B200410084443X A CNB200410084443X A CN B200410084443XA CN 200410084443 A CN200410084443 A CN 200410084443A CN 100358612 C CN100358612 C CN 100358612C
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Abstract
The present invention relates to a method for removing gaseous harmful substances from airflow, which is used for removing harmful gaseous contaminants such as toluene, xylol, etc. from airflow. The method comprises the treating processes that the gas to be treated is led into an electrolytic reactor formed by a plurality of mesh electrodes are superposed, and active carbon granules with the capacity of adsorbing the gaseous harmful substances are filled among electrode plates as a third electrode. Redox reaction happens in the reactor after direct current or pulse electricity is switched on a plate electrode, finally, the harmful substances in the airflow are converted and absorbed by liquid phase, and thus, the aim of purifying gas is achieved.
Description
Technical field
The present invention relates to a kind of purification method technical field of removing the gasified harmful substance that contains in the air-flow that belongs to.
Background technology
Various organic solvents such as toluene and dimethylbenzene are widely used in industrial processes such as chemical industry, pharmacy and application, and these volatile organic matters are poisonous mostly, enter atmosphere after, can influence ecological environment, be detrimental to health.But,, bring very big difficulty to environment protection treating because these organic matters have steady chemical structure, are difficult for degraded.
Usually, the main means of handling these organic exhaust gas and foul gas have absorption process, firing method (comprising Production by Catalytic Combustion Process) and absorption method etc.But said method all has unavoidable separately shortcoming, and absorption process (generally with water as absorbent) can't absorb the organic pollution of insoluble or slightly solubility; Firing method (comprising Production by Catalytic Combustion Process) is had relatively high expectations to service condition, generally requires at operation more than 200 ℃, investment and running cost height.Absorption method is higher to the organic pollution removal efficiency of low concentration, but adsorbent need regenerate, and can't reach the purpose of resolving harmful gas, often needs and method logotypes such as firing method.
The basic principle of three-dimensional electrode electrolysis method is to utilize electrolytic process in electrode surface generation electrochemical reaction, produces strong oxidative free radical O, OH and HO
2Deng, these strong oxidizing property materials and nuisance reaction finally are converted into harmless object to nuisance.The three-dimensional electrode electrolysis method generally is used for the wastewater treatment as difficult degradations such as phenol, aniline, at home and abroad obtained extensive studies (LiBing Huan etc., Techniques and Equipment for Environmental Pollution Control, 2002,2:23-26).
In the Chinese patent literature storehouse, 3 D electrode reactor a large amount of technology reports have also been carried out, as the patent No. is that " 3 D electrode reactor ", the number of patent application of 02114740.X is that 03146904.3 " streaming that circulates continuously fixed bed three dimensional electrode photo electrocatalysis reactor and handle the method for organic wastewater ", the patent No. are 02114739.6 " three phase three-diemsnional electrode photoelectric reactor ", and they all concentrate in the processing of waste water and use.
Therefore, we do not see the report that the three-dimensional electrode electrolysis method is applied to the processing of gaseous organic substances such as toluene as yet.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of method of removing gasified harmful substance from air-flow at existing background technology, and it is easy to use, the efficient height, and expense is cheap.
The present invention solves the problems of the technologies described above the technical scheme that is adopted: a kind of method of removing gasified harmful substance from air-flow, it is characterized in that adopting the three-dimensional electrode electrolysis reactor, comprising the activated carbon granule of filling between network structure fixed electrode and pole plate as third electrode, its processing procedure is that processed gas is imported this reactor, make it by mesh electrode and fluidisation attitude grain bed, after adding direct current or Pulse Electric on the plate electrode, redox reaction takes place in the reactor, nuisance in the air-flow is transformed and absorbed, thereby reach gas purification by liquid phase.
Its structure of 3 D electrode reactor of the present invention is generally column structure, is to be that matrix has coating of metal oxides with the titanium as the anode material of fixed electrode material, and this coating can be IrO
2, RuO
2, PbO
2Or SnO
2Deng mesh electrode, the practical effect of these several anode materials is about the same, with RuO
2And PbO
2/ Ti good slightly (relevant metal oxide electrode material can be compiled " application of electrochemical techniques in environmental project ", Chemical Industry Press, 2002 referring to Feng Yuqiang etc.).Cathode material is to make with the wire netting of titanium or steel material.Electrode spacing visual response device size and electric current and decide are generally 1-200mm; Average geometric diameter as the fluidized particles electrode activity charcoal particle of third electrode is generally 0.1-20mm.Waste gas is fed by reactor bottom, behind gas-solid liquid phase reaction district, is discharged by top.Device can also or be composed in series alternation by a plurality of parallel connections of above-mentioned reacting sucting collector, form as a plurality of unitary reactor stacks, positive and negative electrode is provided with from top to down successively at interval, liquid-inlet and gas vent are arranged on the top of reactor, liquid outlet and gas feed are arranged on the bottom of reactor, thereby constitute the reactor of series connection.
Power supply mode that the present invention adopts comprises direct current or pulse, and direct current supply voltage is generally 1-30V, and pulse power supply voltage is O-40V, and pulse recurrence frequency is generally 20Hz-5KHz.Current density is generally 50-500A/m
2Adopt the clearance of pulse power supply will be higher than direct current supply.
Liquid phase among the present invention adopts handling the little various electrolyte solutions of influence, and generally adopting mass concentration is the sodium chloride solution of 0.1-10%, and to reduce running cost, simultaneously, this sodium chloride solution is also smaller to handling influence.
Compared with prior art, the invention has the advantages that: the mode that adopts charcoal absorption and electrode reaction to combine, be decomposed when making pernicious gas and absorbed by solution after the oxidation by 3 D electrode reactor, can be used for handling the various gases that organic matter pollutes that contain, be specially adapted to the processing of water-soluble bad organic exhaust gas such as triphen class, and treatment effeciency height, operating cost are low, simple and practical.
Description of drawings
Fig. 1 is the cellular construction schematic diagram of 3 D electrode reactor;
Fig. 2 is the A-A schematic cross-section of Fig. 1;
Fig. 3 is the 3 D electrode reactor structural representation (series connection) that a plurality of cellular construction stacks are formed.
The specific embodiment
Embodiment describes in further detail the present invention below in conjunction with accompanying drawing.
The cellular construction schematic diagram of 3 D electrode reactor of the present invention as shown in Figure 1.Its parts label is: 1 processed gas feed, 2 filling openings, 3 purified gas outlet, 4 meshed anode plates, 5 mosaic electrode packed beds, 6 mesh cathode plates, 7 leakage fluid drams.
Reactor can be made up of a plurality of stacks of above-mentioned cell electrode during real work, and Fig. 3 is 6 groups of structural representations that the unit stack is formed.Its parts label is: 1 processed gas feed, 2 filling openings, 3 purified gas outlet, 4 mesh cathode plates, 5 mosaic electrode packed beds, 6 meshed anode plates, 7 leakage fluid drams.
Embodiment 1: experimental provision adopts the reactor of being made up of 6 groups of electrode units stacks shown in Figure 3, is column structure, is of a size of 120mm * 120mm * 800mm, and polar plate spacing is from being 50mm.The meshed anode material is PbO
2/ Ti, mesh cathode material are stainless steel material, and thickness is 2mm, and mesh is 5mm * 5mm.Fluidized particles as third electrode is an activated carbon granule, and the average geometric diameter is about 1mm.Electrolyte is 1% sodium chloride solution, and liquid level can all battery lead plates of submergence.Simulated exhaust is fed by reactor bottom, behind gas-solid liquid phase reaction district, is discharged by top.
Experiment condition is: power parameter: DC voltage 20V, and electric current 5A,
Gas flow: 2000ml/min, gas temperature: 25 ℃
Carrier gas: air
Experimental result: as shown in table 1
Table 1
| Nuisance | Inlet concentration (mg/m 3) | Exit concentration (mg/m 3) | Clearance (%) |
| Toluene | 324 | 35 | 89 |
| Toluene | 845 | 237 | 72 |
| Toluene | 1350 | 663 | 51 |
| Dimethylbenzene | 316 | 29 | 91 |
| Dimethylbenzene | 937 | 295 | 69 |
| Dimethylbenzene | 1470 | 721 | 50 |
| Trichloro-ethylene | 356 | 27 | 92 |
| Trichloro-ethylene | 863 | 248 | 71 |
| Trichloro-ethylene | 1286 | 597 | 54 |
Embodiment 2: experimental provision removes the meshed anode material and changes RuO into embodiment 1
2/ Ti, other are constant.
Experiment condition is: power parameter: the pulse power, voltage peak 30V, pulse frequency 200Hz.
Gas flow: 2000ml/min, gas temperature: 25 ℃
Carrier gas: air
Experimental result: as shown in table 2
Table 2
| Nuisance | Inlet concentration (mg/m 3) | Exit concentration (mg/m 3) | Clearance (%) |
| Toluene | 324 | 23 | 93 |
| Toluene | 845 | 205 | 76 |
| Toluene | 1350 | 593 | 56 |
| Dimethylbenzene | 316 | 17 | 95 |
| Dimethylbenzene | 937 | 265 | 72 |
| Dimethylbenzene | 1470 | 631 | 57 |
| Trichloro-ethylene | 376 | 15 | 96 |
| Trichloro-ethylene | 843 | 198 | 76 |
| Trichloro-ethylene | 1286 | 463 | 64 |
Through to the gas chromatograph analysis of reacted solution composition, the liquid product after finding toluene and dimethylbenzene transformed is the benzoic acids material, is hydrogen chloride and binary acid to the primary product of the degraded of trichloro-ethylene.
Claims (10)
1, a kind of method of from air-flow, removing gasified harmful substance, it is characterized in that adopting the three-dimensional electrode electrolysis reactor, comprising the activated carbon granule of filling between network structure fixed electrode and pole plate as third electrode, its processing procedure is that processed gas is imported this reactor, make it by mesh electrode and fluidisation attitude grain bed, after adding direct current or Pulse Electric on the plate electrode, redox reaction takes place in the reactor, nuisance in the air-flow is transformed and absorbed, thereby reach gas purification by liquid phase.
2, method according to claim 1 is characterized in that its fixed electrode of described 3 D electrode reactor adopts mesh electrode, and anode material has coating of metal oxides for the titanium base band, and this coating is: IrO
2, RuO
2, MnO
2, PbO
2Or SnO
2, cathode material is titanium or steel material.
3, method according to claim 2 is characterized in that its mesh electrode mesh of described 3 D electrode reactor adopts 1-100mm
2Specification, electrode spacing are 1-200mm.
4, method according to claim 1, it is characterized in that its power supply mode of described 3 D electrode reactor comprises direct current or pulse, direct current supply voltage is 1-30V, and pulse power supply voltage is 0-40V, pulse recurrence frequency is 20-5KHz, and current density is 50-500A/m
2
5, method according to claim 1 is characterized in that its liquid phase of described 3 D electrode reactor adopts electrolyte solution.
6, method according to claim 5 is characterized in that it is the sodium chloride solution of 0.1-10% that described electrolyte solution adopts mass concentration.
7, method according to claim 1 is characterized in that it is the activated carbon granule of 0.1-20mm that its third electrode of described 3 D electrode reactor adopts average diameter.
8, method according to claim 1, it is characterized in that described 3 D electrode reactor is that a plurality of unitary reactor stacks are formed, positive and negative electrode is provided with from top to down successively at interval, liquid-inlet and gas vent are arranged on the top of reactor, and liquid outlet and gas feed are arranged on the bottom of reactor.
9, method according to claim 1 is characterized in that described processed gas is the gas that contains organic pollutant.
10, method according to claim 1 is characterized in that described processed gas is the gas that contains toluene, dimethylbenzene or trichloro-ethylene organic pollution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410084443XA CN100358612C (en) | 2004-11-24 | 2004-11-24 | Removal of gasified harmful substance from airflow |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200410084443XA CN100358612C (en) | 2004-11-24 | 2004-11-24 | Removal of gasified harmful substance from airflow |
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|---|---|
| CN1778453A CN1778453A (en) | 2006-05-31 |
| CN100358612C true CN100358612C (en) | 2008-01-02 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102654266B (en) * | 2011-03-04 | 2014-11-19 | 吉林师范大学 | Breathing environment-friendly solar street lamp |
| CN102872703A (en) * | 2012-10-03 | 2013-01-16 | 黄立维 | Device and process for purifying harmful gas through combining gas-liquid absorption with micro-electrolysis |
| CN102872701A (en) * | 2012-10-03 | 2013-01-16 | 黄立维 | Ferric-carbon micro-electrolysis gas-solid-liquid three-phase reactor for purifying harmful gas |
| CN103845966A (en) * | 2014-02-19 | 2014-06-11 | 新疆天业（集团）有限公司 | High-temperature chloroethylene gas purification and oil removal process |
| CN110319442A (en) * | 2019-07-05 | 2019-10-11 | 肖林 | A kind of energy-saving and environment-friendly incinerator |
| CN110353801A (en) * | 2019-07-23 | 2019-10-22 | 郑州大学第三附属医院(河南省妇幼保健院) | A kind of Multifunctional electrotome and its fume removal system suitable for performing the operation |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08155461A (en) * | 1994-12-02 | 1996-06-18 | Permelec Electrode Ltd | Method and apparatus for removing nitric-and/or nitrous-nitrogen |
| CN1358672A (en) * | 2002-01-16 | 2002-07-17 | 中山大学 | Three-dimension electrode reactor and use for treating organic waste water |
-
2004
- 2004-11-24 CN CNB200410084443XA patent/CN100358612C/en not_active Withdrawn - After Issue
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08155461A (en) * | 1994-12-02 | 1996-06-18 | Permelec Electrode Ltd | Method and apparatus for removing nitric-and/or nitrous-nitrogen |
| CN1358672A (en) * | 2002-01-16 | 2002-07-17 | 中山大学 | Three-dimension electrode reactor and use for treating organic waste water |
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