CN104028101A - Flue gas desulfurization and demercuration integrated system and process - Google Patents
Flue gas desulfurization and demercuration integrated system and process Download PDFInfo
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- CN104028101A CN104028101A CN201410281032.3A CN201410281032A CN104028101A CN 104028101 A CN104028101 A CN 104028101A CN 201410281032 A CN201410281032 A CN 201410281032A CN 104028101 A CN104028101 A CN 104028101A
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- flue gas
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Abstract
The invention relates to a flue gas desulfurization and demercuration integrated system and process. The flue gas desulfurization and demercuration integrated process comprises the following steps: combusted hot smoke firstly contacts sprayed adsorbing agent slurry containing compressed air in a high-speed absorbing region for adsorbing and/or oxidizing elementary mercury in the smoke into particular mercury and oxidation state mercury and then particular mercury and oxidation state mercury enters a tower bottom oxidation groove; then the adsorbing agent slurry and sulfur dioxide in the smoke in a low-speed adsorbing region react to generate calcium sulfate hemihydrate and calcium sulfite, and calcium sulfate hemihydrate and calcium sulfite enter the tower bottom oxidation groove. The flue gas desulfurization and demercuration integrated system provided by the invention is simple in structure, low in investment and operation cost, high in demercuration and desulphurization efficiencies, wide in application range of the smoke, stable to operate, high in adaptability, free from blockage design, less prone to scaling, simple to operate, and small in occupation area; the demercuration and desulphurization efficiencies are both not less than 90 percent.
Description
Technical field
The present invention relates to the technical field that flue gas separates and purifies, the present invention relates to specifically a kind of for coal-burning boiler, flue gas of sintering machine demercuration integral system and technique.
Background technology
China is that big country is produced and used to Industrial Boiler, and China is exceeding more than 50 ten thousand with Industrial Boiler at present, and quantity is large, distribute wide, and wherein more than 80% be coal-burning boiler.At present, China's coal-burned industrial boiler has following features: (1) separate unit boiler average size is little, and overall energy consumption level is high, and energy-saving and emission-reduction managerial skills are low, and energy waste and environmental pollution are serious; (2) steam coal kind is changeable, combustion system backward, and taking grate firing boiler as main, efficiency of combustion is lower, and pollutants emission intensity is high; (3) short, the high fume temperature of boiler chimney, pollution are large; (4) active boiler has a large capacity and a wide range, and layout is quite disperseed, and it is large that pollution control reduces discharging difficulty.At present the coal fire discharged sulfur dioxide of China's coal-burned industrial boiler surpasses 1,000 ten thousand tons, approximately 2,000,000 tons of oxynitrides, approximately 1,000,000 tons, dust, is the second largest coal-smoke pollution source that China is only second to coal fired power generation.
Mercury is one of at present main global contaminant, and atmospheric residence time is long, toxicity is large, and has bioaccumulation, and health is formed to very large threat.The existence form of mercury in coal-fired plant flue gas, mainly comprises gaseous elemental mercury (Hg
0), oxidation state mercury (Hg
2+) and solid phase particles state mercury (Hg
p), three is collectively referred to as total mercury (HgT).That is: HgT=Hg
0+ Hg
2++ Hg
p.Hg
0-gaseous elemental mercury, is present in flue gas. and be insoluble in water, other composition generation homogeneous reaction in it and flue gas generates Hg
2+, formed particle mercury Hg by fly ash granule absorption
p.Agstone can adsorb and promote Hg
0oxidation.Mercury in coal-fired plant flue gas more than 80% is with Hg
0form exists.Hg
2+-oxidation state mercury, soluble in water.HgP-particle mercury, it is by solid phase HgCl
2, Hg
0, HgSO
4, HgS composition.Available electric cleaner or sack cleaner, pricker dimensional filter device remove.In the prior art, demercuration technology mainly concentrates on three aspects: flue gas demercuration after demercuration and burning in the front fuel demercuration of burning, burning.Fuel demercuration before burning: stokehold adds Bromide additive to make it generate mercuric bromide, then is removed with desulfuring and denitrifying apparatus, can reach the object of demercuration.Demercuration in burning: by control combustion operating mode, add certain catalyst or additive can reduce the discharge of mercury when burning.Flue gas demercuration after burning: after burning there be the main method of flue gas demercuration: the object of reinjecting, inject acticarbon, calcium adsorbent and other adsorbents etc. and can reach demercuration with electrostatic precipitator, sack cleaner, desulphurization denitration facility, flying dust.But above-mentioned three kinds of methods, demercuration efficiency is all lower, generally the highest 80% left and right that also can only reach.
Summary of the invention
In order to solve the above-mentioned technical problem existing in prior art, the object of the present invention is to provide a kind of cigarette flue gas desulfurizing and hydrargyrum-removing integral system and technique.
Realize foregoing invention object in order to solve the problems of the technologies described above, a first aspect of the present invention provides following technical scheme:
A kind of flue gas desulfurizing and hydrargyrum-removing integral process, is characterized in that: the hot flue gas after burning first the Elemental Mercury in described flue gas is adsorbed with contacting containing compressed-air actuated adsorbent slurries of spraying in high speed uptake zone and/or be oxidized to particle mercury and oxidation state mercury and enter tower at the bottom of in oxidation trough; Then, react with the sulfur dioxide in flue gas at low speed uptake zone absorbent slurry generate calcium sulfate and calcium sulfite and enter tower at the bottom of in oxidation trough.
Wherein, described adsorbent slurries are made up of the water of agstone, flyash and surplus; Granularity≤250 order of described agstone and flyash.
Wherein, described absorbent slurry is made up of the water of agstone, activated coke and surplus, and its pH value is 10～13.
Wherein, the ratio of described adsorbent slurries and flue gas is 2-3L/m
3; The ratio of described absorbent slurry and flue gas is 15-20L/m
3.
A second aspect of the present invention, also relate to a kind of flue gas desulfurizing and hydrargyrum-removing integral system, it is characterized in that: described system comprises absorption tower, described absorption tower comprises oxidation trough at the bottom of tower, high speed uptake zone tower body and low speed uptake zone tower body, is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent on described high speed uptake zone tower body; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layers and the demist layer that are made up of absorbent slurry nozzle; At the bottom of absorbent slurry nozzle and tower, between oxidation trough, be connected with circulation line, circulation line is also provided with slurry circulating pump.
Wherein, in described system, also comprise absorbent groove with slurry, absorbent groove with slurry top is provided with fresh water (FW) import, absorbent trench bottom with slurry is provided with absorbent slurry outlet, and slurry feeding pump is delivered to absorbent slurry by this slurries outlet the circulation line on absorption tower.
Wherein, in described system, at the bottom of absorbing tower, oxidation trough is also provided with oxidation air entrance, and oxidation air delivers into oxidation trough at the bottom of tower by oxidation fan.
Wherein, in described system, at the bottom of absorbing tower, the bottom of oxidation trough is provided with slurries floss hole, and at the bottom of tower, the absorbent slurry of oxidation trough is delivered to cyclone by slurries floss hole by slurries emptying pump; Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of absorbing tower in oxidation trough, and denseer underflow slurries flow in sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent groove with slurry.
Wherein, in described system, on the flue of supplied flue gases, be provided with baffle door, so that bypass operation while breaking down.
In described system, also comprise electric meter RACS and fresh water (FW) system.
Compared with prior art, the present invention has following useful technique effect:
(1) device structure is simple, and investment and operating cost are low; Demercuration desulfuration efficiency is high; To the wide accommodation of flue gas; Stable, strong adaptability; Without stopping up design, less scaling; Simple to operate, floor space is little.
(2) desulfuration efficiency is not less than 98%, and demercuration efficiency is not less than 90%, ensures exhanst gas outlet SO
2content≤50mg/m
3, total mercury emission≤0.03mg/m
3, reach discharging standards.
Brief description of the drawings
Fig. 1: flue gas desulfurizing and hydrargyrum-removing integral process flow chart of the present invention.
In figure, the implication of Reference numeral representative is respectively: 1-tail gas; 2-compressed air; 3-oxidation air; 4-fresh water (FW); 5-absorbent groove with slurry; 6-absorption tower; 7-chimney; 8-cyclone; 9-sedimentation basin; 61-high speed uptake zone tower body; 62-low speed uptake zone tower body; Oxidation trough at the bottom of 63-tower; 64-spraying layer, 65-demister, 66-adsorbent.
Detailed description of the invention
Below in conjunction with specific embodiment and accompanying drawing, technical scheme of the present invention is described in detail.
Flue gas desulfurizing and hydrargyrum-removing integral system of the present invention, described system comprises absorption tower, described absorption tower comprises oxidation trough at the bottom of tower, high speed uptake zone tower body and low speed uptake zone tower body, is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent on described high speed uptake zone tower body; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layers and the demist layer that are made up of absorbent slurry nozzle; At the bottom of absorbent slurry nozzle and tower, between oxidation trough, be connected with circulation line, circulation line is also provided with slurry circulating pump.In described system, also comprise absorbent groove with slurry, absorbent groove with slurry top is provided with fresh water (FW) import, and absorbent trench bottom with slurry is provided with absorbent slurry outlet, and slurry feeding pump is delivered to absorbent slurry by this slurries outlet the circulation line on absorption tower.At the bottom of absorbing tower, oxidation trough is also provided with oxidation air entrance, and oxidation air delivers into oxidation trough at the bottom of tower by oxidation fan.At the bottom of absorbing tower, the bottom of oxidation trough is provided with slurries floss hole, and at the bottom of tower, the absorbent slurry of oxidation trough is delivered to cyclone by slurries floss hole by slurries emptying pump; Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of absorbing tower in oxidation trough, and denseer underflow slurries flow in sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent groove with slurry.In addition, in described system, on the flue of supplied flue gases, be provided with baffle door, so that bypass operation while breaking down, but also comprise electric meter RACS and fresh water (FW) system.
Embodiment 1
Now, taking a boiler (10t/h) as example, carry out desulfuration demercuration processing according to flue gas desulfurizing and hydrargyrum-removing integral process of the present invention.Described adsorbent slurries are made up of lime stone, the flyash of 2.5wt% and the water of surplus of 2.0wt%; Described absorption slurries are made up of lime stone, the activated coke of 1.0wt% and the water of surplus of 2.0wt%; The ratio of described adsorbent slurries and flue gas is 3L/m
3; The ratio of described absorbent slurry and flue gas is 20L/m
3.Wherein, described flyash is modified coal ash, it is that the mixed aqueous solution of the boric acid, the oxalic acid of 2.0wt% and the ATMP of 0.1wt% that utilize 1.2wt% stirs and soaks 2.0～2.5h, the modified coal ash that then roasting obtains at 300 DEG C flyash.
Test gained basic data is as follows: flue gas total flow: 10000m
3/ h; SO in flue gas
2content is 3000-4000mg/m
3, exhanst gas outlet is containing SO
2≤ 50mg/m
3, desulfuration efficiency reaches more than 98%.The content of mercury in flue gas is 0.25-0.30mg/m
3, total mercury emission≤0.03mg/m
3.
Comparative example 1
Compared with embodiment 1, difference is only the modified coal ash difference using, the mixed aqueous solution that is specifically the boric acid, the tartaric acid of 2.0wt% and the ATMP of 0.1wt% that utilize 1.2wt% stirs and soaks 2.0～2.5h, the modified coal ash that then roasting obtains at 300 DEG C flyash.
Comparative example 2
Compared with embodiment 1, difference is only the modified coal ash difference using, the mixed aqueous solution that is specifically the boric acid, the citric acid of 2.0wt% and the ATMP of 0.1wt% that utilize 1.2wt% stirs and soaks 2.0～2.5h, the modified coal ash that then roasting obtains at 300 DEG C flyash.
Comparative example 3
Compared with embodiment 1, difference is the modified coal ash difference using, and is specifically to utilize the boric acid of 1.2wt% and the tartaric mixed aqueous solution of 2.0wt% to stir and soak 2.0～2.5h, the modified coal ash that roasting obtains at 300 DEG C flyash.
Comparative example 4
Compared with embodiment 1, difference is only the modified coal ash difference using, the mixed aqueous solution that is specifically the boric acid, the hydrochloric acid of 2.0wt% and the ATMP of 0.1wt% that utilize 1.2wt% stirs and soaks 2.0～2.5h, the modified coal ash that then roasting obtains at 300 DEG C flyash.
The technique that adopts comparative example, described total mercury emission is all at 0.12～0.18mg/m
3between.
The purification of wet method demercuration desulfurizing technology system of the present invention to mediumand smallscale industrial boilers flue gas, has great economic and social profit, in China's economic construction process, is worth promoting.
For the ordinary skill in the art; specific implementation of the present invention is not subject to the restrictions described above; as long as adopted the improvement of the various unsubstantialities that method of the present invention design and technical scheme carry out; or without improving, design of the present invention and technical scheme are directly applied to other occasion, all within protection scope of the present invention.
Claims (10)
1. a flue gas desulfurizing and hydrargyrum-removing integral process, is characterized in that: the hot flue gas after burning first Elemental Mercury in described flue gas is adsorbed with contact containing compressed-air actuated adsorbent slurries of spraying in high speed uptake zone and/or be oxidized to particle mercury and oxidation state mercury and enter tower at the bottom of in oxidation trough; Then, react with the sulfur dioxide in flue gas at low speed uptake zone absorbent slurry generate calcium sulfate and calcium sulfite and enter tower at the bottom of in oxidation trough.
2. integral process according to claim 1, is characterized in that: described adsorbent slurries are made up of the water of agstone, flyash and surplus; Granularity≤250 order of described agstone and flyash.
3. integral process according to claim 1, is characterized in that: described absorbent slurry is made up of the water of agstone, activated coke and surplus, and its pH value is 10～13.
4. integral process according to claim 1, is characterized in that: the ratio of described adsorbent slurries and flue gas is 2-3L/m
3; The ratio of described absorbent slurry and flue gas is 15-20L/m
3.
5. a flue gas desulfurizing and hydrargyrum-removing integral system, it is characterized in that: described system comprises absorption tower, described absorption tower comprises oxidation trough at the bottom of tower, high speed uptake zone tower body and low speed uptake zone tower body, is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent on described high speed uptake zone tower body; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layers and the demist layer that are made up of absorbent slurry nozzle; At the bottom of absorbent slurry nozzle and tower, between oxidation trough, be connected with circulation line, circulation line is also provided with slurry circulating pump.
6. integral system according to claim 5, it is characterized in that: also comprise absorbent groove with slurry, absorbent groove with slurry top is provided with fresh water (FW) import, absorbent trench bottom with slurry is provided with absorbent slurry outlet, and slurry feeding pump is delivered to absorbent slurry by this slurries outlet the circulation line on absorption tower.
7. integral system according to claim 5, is characterized in that: at the bottom of absorbing tower, oxidation trough is also provided with oxidation air entrance, and oxidation air delivers into oxidation trough at the bottom of tower by oxidation fan.
8. integral system according to claim 5, is characterized in that: at the bottom of absorbing tower, the bottom of oxidation trough is provided with slurries floss hole, and at the bottom of tower, the absorbent slurry of oxidation trough is delivered to cyclone by slurries floss hole by slurries emptying pump; Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of absorbing tower in oxidation trough, and denseer underflow slurries flow in sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent groove with slurry.
9. integral system according to claim 5, is characterized in that: on the flue of supplied flue gases, be provided with baffle door.
10. integral system according to claim 5, is characterized in that: also comprise electric meter RACS and fresh water (FW) system.
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|---|---|---|---|
| CN201410281032.3A CN104028101B (en) | 2014-06-23 | 2014-06-23 | Flue gas desulfurizing and hydrargyrum-removing integral system and technique |
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| CN201410281032.3A CN104028101B (en) | 2014-06-23 | 2014-06-23 | Flue gas desulfurizing and hydrargyrum-removing integral system and technique |
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| CN104028101B CN104028101B (en) | 2016-04-13 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105879609A (en) * | 2015-02-13 | 2016-08-24 | 巴布科克和威尔科克斯能量产生集团公司 | Method and apparatus for removing mercury from flue gas stream |
| CN107787245A (en) * | 2015-06-19 | 2018-03-09 | Rwe动力股份公司 | Method for going the removal of mercury from the flue gas of combustion plant |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020102189A1 (en) * | 1998-12-07 | 2002-08-01 | Madden Deborah A. | Alkaline sorbent injection for mercury control |
| EP1932579A1 (en) * | 2006-12-07 | 2008-06-18 | Mitsubishi Heavy Industries, Ltd. | Method and device for removing mercury |
| WO2010146670A1 (en) * | 2009-06-17 | 2010-12-23 | 三菱重工業株式会社 | System for removing mercury and method of removing mercury from mercury-containing high-temperature discharge gas |
| JP2011031222A (en) * | 2009-08-05 | 2011-02-17 | Mitsubishi Heavy Ind Ltd | Device for treating exhaust gas and method for removing mercury in exhaust gas |
| CN202410505U (en) * | 2012-01-20 | 2012-09-05 | 北京中冶设备研究设计总院有限公司 | Desulfurization, denitration and demercuration integral device |
| CN203220852U (en) * | 2013-03-01 | 2013-10-02 | 广东电网公司电力科学研究院 | Intelligent demercuration additive adding system for coal-fired power plant |
-
2014
- 2014-06-23 CN CN201410281032.3A patent/CN104028101B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020102189A1 (en) * | 1998-12-07 | 2002-08-01 | Madden Deborah A. | Alkaline sorbent injection for mercury control |
| EP1932579A1 (en) * | 2006-12-07 | 2008-06-18 | Mitsubishi Heavy Industries, Ltd. | Method and device for removing mercury |
| WO2010146670A1 (en) * | 2009-06-17 | 2010-12-23 | 三菱重工業株式会社 | System for removing mercury and method of removing mercury from mercury-containing high-temperature discharge gas |
| JP2011031222A (en) * | 2009-08-05 | 2011-02-17 | Mitsubishi Heavy Ind Ltd | Device for treating exhaust gas and method for removing mercury in exhaust gas |
| CN202410505U (en) * | 2012-01-20 | 2012-09-05 | 北京中冶设备研究设计总院有限公司 | Desulfurization, denitration and demercuration integral device |
| CN203220852U (en) * | 2013-03-01 | 2013-10-02 | 广东电网公司电力科学研究院 | Intelligent demercuration additive adding system for coal-fired power plant |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105879609A (en) * | 2015-02-13 | 2016-08-24 | 巴布科克和威尔科克斯能量产生集团公司 | Method and apparatus for removing mercury from flue gas stream |
| CN107787245A (en) * | 2015-06-19 | 2018-03-09 | Rwe动力股份公司 | Method for going the removal of mercury from the flue gas of combustion plant |
| CN107787245B (en) * | 2015-06-19 | 2020-12-15 | Rwe动力股份公司 | Method for removing mercury from flue gas of combustion plant |
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| CN104028101B (en) | 2016-04-13 |
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