CN101347709A - Purification system of flue gas and method - Google Patents
Purification system of flue gas and method Download PDFInfo
- Publication number
- CN101347709A CN101347709A CNA2008101193701A CN200810119370A CN101347709A CN 101347709 A CN101347709 A CN 101347709A CN A2008101193701 A CNA2008101193701 A CN A2008101193701A CN 200810119370 A CN200810119370 A CN 200810119370A CN 101347709 A CN101347709 A CN 101347709A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- gas
- oxidation
- gaseous
- liquid phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas purification system and a method with high removing efficiency of flue gas pollutants and low cost. The system consists of a gas phase oxidation unit, a liquid phase oxidation and absorption device and a flue gas recirculating pipeline; the gas phase oxidation unit is provided with a flue gas inlet, a flue gas outlet and a gas phase oxidizing agent inlet; the liquid phase oxidation and absorption device is used for containing liquid phase oxidizing agent and liquid phase absorbing agent and is provided with a flue gas inlet and a flue gas outlet, wherein, the flue gas inlet of the liquid phase oxidation and absorption device is in gas communication with the flue gas outlet of the gas phase oxidation unit; the flue gas recirculating pipeline is respectively in gas communication with the flue gas inlet and the flue gas outlet of the gas-phase oxidation unit and is used for sending part of the flue gas, which passes through the flue gas outlet of the gas phase oxidation unit, back to the flue gas inlet of the gas phase oxidation unit so as to carry out gas-phase oxidation to this part of flue gas once more. The method includes the following steps: carrying out gas-phase oxidation to pollutant-containing raw gas; mixing part of flue gas which is treated with gas-phase oxidation with the raw gas and carrying out gas-phase oxidation again; carrying out liquid-phase oxidation to the flue gas which is treated with gas-phase oxidation and liquid-phase absorbing the oxidation products of the flue gas.
Description
Technical field
The present invention relates to flue gas purification system and method, specifically, relate to flue gas recirculation gas-liquid two-phase oxidizing process coordinated desulfurization, denitration and demercuration system and method thereof.
Background technology
Current, adopt oxidizing process for example vapour phase oxidation process (ozone) and the liquid phase oxidation technology that removes sulfur dioxide in the coal-fired flue-gas, nitric oxide and mercury have more report, for example CN1962034A and CN1923337A are disclosed.No matter being any oxidizing process, all is with the SO in the coal-fired flue-gas
2, NO and Hg
0Be oxidized to SO
3, NO
2And Hg
2+Wash and remove.For vapour phase oxidation process, the time of contact of gaseous oxidizing agent and flue gas is limited, and oxidation efficiency is lower; Also need to install additional absorption plant in addition, absorb and remove oxidation product in the flue gas.For liquid phase oxidation, oxidation is carried out with being absorbed in the same device, and oxidation efficiency is higher, and can reach higher pollutant removing efficient, but liquid phase oxidation agent cost is too high.
Summary of the invention
The purpose of this invention is to provide low flue gas purification system of flue gas pollutant removal efficiency height and cost and method.
Flue gas purifying method of the present invention comprises step: the former flue gas that contains pollutant is carried out gaseous oxidation; Will through the partial fume of gaseous oxidation with carry out gaseous oxidation once more after former flue gas mixes; And absorb the flue gas oxidation product to carry out liquid phase oxidation and liquid phase through the flue gas of gaseous oxidation.
Flue gas pollutant generally comprises SO
2, NO and Hg
0
Preferably utilize ozone to carry out gaseous oxidation as gaseous oxidizing agent.
Preferably utilize NaClO
2, KMnO
4Or H
2O
2Carry out liquid phase oxidation as the liquid phase oxidation agent.
Preferably utilize NaOH or CaCO
3Carrying out liquid phase as liquid absorbent absorbs.
When carrying out gaseous oxidation once more, be preferably 20% to 25% through the flue gas of gaseous oxidation and the mixed proportion of former flue gas.
Flue gas purification system of the present invention comprises: the gaseous oxidation device has smoke inlet, exhanst gas outlet and gaseous oxidizing agent inlet; Hold the liquid phase oxidation absorption plant of liquid phase oxidation agent and liquid absorbent, have smoke inlet and exhanst gas outlet, wherein the smoke inlet of liquid phase oxidation absorption plant is communicated with the exhanst gas outlet gas of gaseous oxidation device; With the flue gas recirculation pipeline, be communicated with the smoke inlet and the exhanst gas outlet gas of gaseous oxidation device respectively, be used for partly sending the flue gas of the exhanst gas outlet by the gaseous oxidation device smoke inlet of gaseous oxidation device back to so that this partial fume is carried out gaseous oxidation once more.
Flue gas purification system of the present invention can also comprise clean fume emission device, is communicated with the exhanst gas outlet gas of liquid phase oxidation absorption plant.
Flue gas purification system of the present invention can also comprise the gaseous oxidation agent feeding device, is communicated with the gaseous oxidizing agent inlet gas of gaseous oxidation device.
In flue gas purification system of the present invention, the gaseous oxidizing agent of preferred gaseous oxidation device inlet is located at the downstream position of the smoke inlet of gaseous oxidation device.
According to the present invention, coal-fired flue-gas at first carries out the pre-oxidation of flue gas recirculation gas phase, with the part SO in the flue gas
2, NO and Hg
0Be oxidized to SO
3, NO
2And Hg
2+, flue gas enters the liquid phase oxidation absorption plant subsequently, carries out deep oxidation and washing absorption in the liquid phase oxidation device, thereby can efficiently remove the pollutant in the flue gas.
Description of drawings
Fig. 1 is the schematic diagram according to flue gas recirculation gas-liquid two-phase oxidizing process coordinated desulfurization of the present invention, denitration and demercuration system and method thereof.
The specific embodiment
Below present invention will be described in detail with reference to the accompanying.
Fig. 1 schematically shows flue gas recirculation gas-liquid two-phase oxidizing process coordinated desulfurization of the present invention, denitration and demercuration system (flue gas purification system), and it comprises that the gaseous oxidation device is gaseous oxidation flue 1 and liquid phase oxidation absorption plant 2.Gaseous oxidation flue 1 has smoke inlet, gaseous oxidizing agent inlet and exhanst gas outlet (all not specifically illustrating in the drawings).Liquid phase oxidation absorption plant 2 is used to hold liquid phase oxidation agent and liquid absorbent, has smoke inlet and exhanst gas outlet (also all not specifically illustrating in the drawings) equally.The smoke inlet of liquid phase oxidation absorption plant 2 is communicated with the exhanst gas outlet gas of gaseous oxidation flue 1.System of the present invention also comprises the flue gas recirculation pipeline, be communicated with the smoke inlet and the exhanst gas outlet gas of gaseous oxidation flue 1 respectively, be used for partly sending the flue gas of the exhanst gas outlet by gaseous oxidation flue 1 smoke inlet of gaseous oxidation flue 1 back to so that this partial fume is carried out gaseous oxidation once more.
In addition, system of the present invention can comprise gaseous oxidation agent feeding device (not specifically illustrating in the drawings), is communicated with the gaseous oxidizing agent inlet gas of gaseous oxidation flue 1.The gaseous oxidizing agent inlet of preferred gaseous oxidation flue 1 is located at the downstream position (at the flow of flue gas direction) of the smoke inlet of gaseous oxidation flue.In addition, system of the present invention can also comprise clean fume emission device (not specifically illustrating in the drawings), is communicated with the exhanst gas outlet gas of liquid phase oxidation absorption plant 2.
Followingly flue gas recirculation gas-liquid two-phase oxidizing process coordinated desulfurization of the present invention, denitration and demercuration method (flue gas purifying method) are described with reference to Fig. 1.
Coal fire discharged flue gas (former flue gas) contains SO
2, NO and Hg
0Deng pollutant, feed in the gaseous oxidation flue 1 from smoke inlet, react the part SO in the flue gas with the gaseous oxidizing agent (for example ozone) that enters gaseous oxidation flue 1 from the gaseous oxidizing agent inlet
2, NO and Hg
0Be oxidized to SO
3, NO
2And Hg
2+Be effectively to improve gas phase pre-oxidation efficient, the present invention utilizes the flue gas of the exhanst gas outlet that the flue gas recirculation pipeline will be by gaseous oxidation flue 1 partly to send the smoke inlet of gaseous oxidation flue 1 back to so that this partial fume is carried out gaseous oxidation once more.The mode of this employing flue gas recirculation has prolonged the time of contact of flue gas and gaseous oxidizing agent, thereby has effectively improved oxidation efficiency.Preferably with the proportion control of amount of circulating gas and former exhaust gas volumn in 20%～25% scope.After the gas phase pre-oxidation, flue gas enters in the liquid phase oxidation absorption plant 2 from the smoke inlet of the exhanst gas outlet process liquid phase oxidation absorption plant 2 of gaseous oxidation flue 1.In liquid phase oxidation absorption plant 2, unoxidized pollutant SO
2, NO and Hg
0By deep oxidation, alkaline absorbent solution and the oxidation product generation absorption reaction in the device realized removing of pollutant simultaneously.The liquid phase oxidation agent can be NaClO
2, also can be KMnO
4, H
2O
2Or other suitable strong oxidizer.Liquid absorbent can be NaOH, CaCO
3Deng alkaline matter.At last, flue gas after being purified can enter clean fume emission device from the exhanst gas outlet of liquid phase oxidation absorption plant 2.
The present invention has following advantage at least:
1, the present invention adopts flue gas recirculation gas-liquid two-phase oxidizing process coordinated desulfurization, denitration and hydrargyrum-removing technology, can be issued to higher pollutant removing efficient in lower operating cost.
2, the present invention adopts the multiple flue gas pollutant removing process that gaseous oxidation and liquid phase oxidation combine, and gaseous oxidation absorption and liquid phase oxidation are absorbed organically combination, and system's floor space is little.
3, the present invention utilizes the flue gas recirculation gaseous oxidation, has effectively improved gaseous oxidation efficient.
It will be appreciated by those skilled in the art that above-mentioned embodiment just is used for description and interpretation the present invention, is any restriction that the present invention is made and be not to be construed as.
Claims (10)
1. flue gas purifying method comprises step:
The former flue gas that contains pollutant is carried out gaseous oxidation;
Will through the partial fume of gaseous oxidation with carry out gaseous oxidation once more after former flue gas mixes; And
Flue gas through gaseous oxidation is carried out liquid phase oxidation and liquid phase absorption flue gas oxidation product.
2. according to the process of claim 1 wherein that flue gas pollutant comprises SO
2, NO and Hg
0
3. utilize ozone to carry out gaseous oxidation according to the process of claim 1 wherein as gaseous oxidizing agent.
4. utilize NaClO according to the process of claim 1 wherein
2, KMnO
4Or H
2O
2Carry out liquid phase oxidation as the liquid phase oxidation agent.
5. according to the method for claim 4, wherein utilize NaOH or CaCO
3Carrying out liquid phase as liquid absorbent absorbs.
6. according to the method for one of claim 1-4, when wherein carrying out gaseous oxidation once more, be 20% to 25% through the flue gas of gaseous oxidation and the mixed proportion of former flue gas.
7, a kind of flue gas purification system comprises:
The gaseous oxidation device has smoke inlet, exhanst gas outlet and gaseous oxidizing agent inlet;
Hold the liquid phase oxidation absorption plant of liquid phase oxidation agent and liquid absorbent, have smoke inlet and exhanst gas outlet, wherein the smoke inlet of liquid phase oxidation absorption plant is communicated with the exhanst gas outlet gas of gaseous oxidation device; With
The flue gas recirculation pipeline, be communicated with the smoke inlet and the exhanst gas outlet gas of gaseous oxidation device respectively, be used for partly sending the flue gas of the exhanst gas outlet by the gaseous oxidation device smoke inlet of gaseous oxidation device back to so that this partial fume is carried out gaseous oxidation once more.
8. according to the flue gas purification system of claim 7, also comprise clean fume emission device, be communicated with the exhanst gas outlet gas of liquid phase oxidation absorption plant.
9. according to the flue gas purification system of claim 7 or 8, also comprise the gaseous oxidation agent feeding device, be communicated with the gaseous oxidizing agent inlet gas of gaseous oxidation device.
10. according to the flue gas purification system of claim 7 or 8, wherein the gaseous oxidizing agent of gaseous oxidation device inlet is located at the downstream position of the smoke inlet of gaseous oxidation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101193701A CN101347709A (en) | 2008-09-04 | 2008-09-04 | Purification system of flue gas and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101193701A CN101347709A (en) | 2008-09-04 | 2008-09-04 | Purification system of flue gas and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101347709A true CN101347709A (en) | 2009-01-21 |
Family
ID=40266772
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008101193701A Pending CN101347709A (en) | 2008-09-04 | 2008-09-04 | Purification system of flue gas and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101347709A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102228779A (en) * | 2011-06-30 | 2011-11-02 | 华北电力大学（保定） | Absorbent for simultaneously desulfurizing and denitrifying liquid-phase flue gas |
| CN102233230A (en) * | 2011-07-18 | 2011-11-09 | 创冠环保(中国)有限公司 | Waste burning smoke purification process and purification system |
| CN104971594A (en) * | 2014-04-08 | 2015-10-14 | 上海三卿环保科技有限公司 | Gas phase oxidization-liquid phase oxidization-absorption three-section type dry-wet-process flue gas denitration process |
| CN106369625A (en) * | 2016-10-25 | 2017-02-01 | 福建龙净环保股份有限公司 | Dry type smoke purification system and smoke heating method thereof |
| CN109865415A (en) * | 2019-04-08 | 2019-06-11 | 福建省特种设备检验研究院 | CFB boiler, which is mixed, burns anthracite and sawdust sludge gas mercury oxidation control technique |
| CN112915778A (en) * | 2019-12-06 | 2021-06-08 | 中国科学院大连化学物理研究所 | Catalytic oxidation absorption denitration method and device thereof |
-
2008
- 2008-09-04 CN CNA2008101193701A patent/CN101347709A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102228779A (en) * | 2011-06-30 | 2011-11-02 | 华北电力大学（保定） | Absorbent for simultaneously desulfurizing and denitrifying liquid-phase flue gas |
| CN102233230A (en) * | 2011-07-18 | 2011-11-09 | 创冠环保(中国)有限公司 | Waste burning smoke purification process and purification system |
| CN104971594A (en) * | 2014-04-08 | 2015-10-14 | 上海三卿环保科技有限公司 | Gas phase oxidization-liquid phase oxidization-absorption three-section type dry-wet-process flue gas denitration process |
| CN106369625A (en) * | 2016-10-25 | 2017-02-01 | 福建龙净环保股份有限公司 | Dry type smoke purification system and smoke heating method thereof |
| CN106369625B (en) * | 2016-10-25 | 2018-10-19 | 福建龙净环保股份有限公司 | A kind of dry type flue gas purification system and its flue gas method |
| CN109865415A (en) * | 2019-04-08 | 2019-06-11 | 福建省特种设备检验研究院 | CFB boiler, which is mixed, burns anthracite and sawdust sludge gas mercury oxidation control technique |
| CN112915778A (en) * | 2019-12-06 | 2021-06-08 | 中国科学院大连化学物理研究所 | Catalytic oxidation absorption denitration method and device thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6171096B2 (en) | Semi-dry simultaneous desulfurization / denitration / demercury equipment and method using circulating fluidized bed | |
| US7048899B2 (en) | Removing NOx, SO2, and Hg from a gas stream using limestone regeneration | |
| TWI432253B (en) | Ozone production processes and its use in industrial processes | |
| AU2004220725B8 (en) | Improved process for the removal of contaminants from gas | |
| CN104474857B (en) | NO in the preposition oxidative absorption coal-fired flue-gas of bioactive moleculexAnd SO2Method and apparatus | |
| CN101352646B (en) | Flue gas denitration method using ultraviolet light double action | |
| CN103990362A (en) | Method and device for removing sulfur, nitre and mercury in smoke | |
| CA2924319C (en) | Treatment of nitrogen oxides in flue gas streams | |
| JP2013529545A (en) | Combustion exhaust gas purification and recycling system and method | |
| WO2009093574A1 (en) | System and method for treating discharge gas from coal-fired boiler | |
| CN1923337A (en) | Boiler smoke gas multipollutant ozonization and simultaneous elimination device and method therefor | |
| CN1923341A (en) | Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification | |
| JP5675364B2 (en) | Method for promoting mercury retention in wet flue gas desulfurization systems | |
| JP4719228B2 (en) | Exhaust gas treatment system for coal fired boiler | |
| CN101347709A (en) | Purification system of flue gas and method | |
| CN103736373A (en) | Flue gas treatment method and flue gas treatment device capable of simultaneous desulfurization, de-nitration and mercury removal through magnesium oxide | |
| CN103752151A (en) | Technology for flue gas denitration by magnesium sulfite | |
| CN104941410A (en) | Flue gas desulfurization and denitrification integrated method and device based on two-step oxidation process of active molecules O3 at low temperature | |
| CN113941238A (en) | Integrated control method for low-temperature smoke pollutants | |
| JP5144967B2 (en) | Exhaust gas treatment system | |
| CN204619713U (en) | A kind of system and boiler removing various pollutants in fume | |
| CN107638792B (en) | Composite flue gas denitration oxidant and application method thereof | |
| CN203829899U (en) | Smoke desulfurization denitration and demercuration device | |
| CN114768509B (en) | Method and device for removing multi-component pollutants in flue gas based on supergravity technology | |
| CN106512611A (en) | Method for desulfurizing and treating flue gas from boiler of thermal power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Open date: 20090121 |