CN104028101B - Flue gas desulfurizing and hydrargyrum-removing integral system and technique - Google Patents

Flue gas desulfurizing and hydrargyrum-removing integral system and technique Download PDF

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CN104028101B
CN104028101B CN201410281032.3A CN201410281032A CN104028101B CN 104028101 B CN104028101 B CN 104028101B CN 201410281032 A CN201410281032 A CN 201410281032A CN 104028101 B CN104028101 B CN 104028101B
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tower
slurry
flue gas
absorbent
integral
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CN104028101A (en
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李玢
周琪
黄茂开
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李玢
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Abstract

The present invention relates to flue gas desulfurizing and hydrargyrum-removing integral system and technique, the heat smoke after burning is first in high speed uptake zone and adsorbing the Elemental Mercury in described flue gas containing compressed-air actuated adsorbent slurry liquid contacts of spraying into and/or be oxidized to particle mercury and oxidation state mercury enters in oxidation trough at the bottom of tower; Then, the sulfur dioxide in low speed uptake zone absorbent slurry and flue gas reacts and generates calcium sulfate and calcium sulfite and enter in oxidation trough at the bottom of tower.System architecture of the present invention is simple, investment and operating cost low; Demercuration desulfuration efficiency is high; To the wide accommodation of flue gas; Stable, strong adaptability; Without blocking design, less scaling; Simple to operate, floor space is little; And desulfurization and demercuration efficiency are all not less than 90%.

Description

Flue gas desulfurizing and hydrargyrum-removing integral system and technique
Technical field
The present invention relates to the technical field that flue gas is separated and purifies, the present invention relates to a kind of for coal-burning boiler, flue gas of sintering machine demercuration integral system and technique specifically.
Background technology
China is that Industrial Boiler is produced and uses big country, current China with Industrial Boiler more than 50 more than ten thousand, quantity is large, and distribution is 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, energy waste and environmental pollution serious; (2) steam coal kind is changeable, combustion system backward, and based on grate firing boiler, 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.The coal fire discharged sulfur dioxide of current China coal-burned industrial boiler surpass 1,000 ten thousand tons, oxynitrides about 2,000,000 tons, about 1,000,000 tons, dust, be the second largest coal-smoke pollution source that China is only second to coal fired power generation.
Mercury is one of main at present global contaminant, and atmospheric residence time is long, toxicity is large, and has bioaccumulation, forms very large threat to health.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 particulate Hg Hg by fly ash granule absorption p.Agstone can adsorb and promote Hg 0oxidation.In coal-fired plant flue gas, the mercury of 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: demercuration and the rear flue gas demercuration of burning in fuel pre-combustion demercuration, burning.Fuel pre-combustion demercuration: stokehold adds Bromide additive makes 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, adds the discharge that certain catalyst or additive can reduce mercury during burning.Flue gas demercuration after burning: after burning there being the main method of flue gas demercuration: reinjects with electrostatic precipitator, sack cleaner, desulphurization denitration facility, flying dust, inject the object that acticarbon, calcium adsorbent and other adsorbents etc. can reach demercuration.But above-mentioned three kinds of methods, demercuration efficiency is all lower, generally the highlyest also can only reach about 80%.
Summary of the invention
In order to solve the above-mentioned technical problem existed 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 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 heat smoke after burning is first in high speed uptake zone and adsorbing the Elemental Mercury in described flue gas containing compressed-air actuated adsorbent slurry liquid contacts of spraying into and/or be oxidized to particle mercury and oxidation state mercury enters in oxidation trough at the bottom of tower; Then, the sulfur dioxide in low speed uptake zone absorbent slurry and flue gas reacts and generates calcium sulfate and calcium sulfite and enter in oxidation trough at the bottom of tower.
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, described high speed uptake zone tower body is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layer and demist layer that are made up of absorbent slurry nozzle; Be connected with circulation line between oxidation trough at the bottom of absorbent slurry nozzle and tower, circulation line is also provided with slurry circulating pump.
Wherein, in described system, also comprise absorbent groove with slurry, absorbent groove top with slurry is provided with fresh water (FW) import, absorbent trench bottom with slurry is provided with absorbent slurry outlet, and absorbent slurry is delivered to the circulation line on absorption tower by slurry feeding pump by this serum outlet.
Wherein, in described system, oxidation trough at the bottom of absorbing tower 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 the absorbent slurry of oxidation trough at the bottom of tower 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 in oxidation trough at the bottom of absorbing tower, and denseer bottom slurry flows in sedimentation basin, and the clear liquid overflow on sedimentation basin top is in absorbent groove with slurry.
Wherein, in described system, the flue of supplied flue gases is provided with baffle door, so that bypass runs when 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, investment and operating cost low; Demercuration desulfuration efficiency is high; To the wide accommodation of flue gas; Stable, strong adaptability; Without blocking 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.
Accompanying drawing explanation
Fig. 1: flue gas desulfurizing and hydrargyrum-removing integral process flow chart of the present invention.
Implication in figure representated by Reference numeral 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, described high speed uptake zone tower body is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layer and demist layer that are made up of absorbent slurry nozzle; Be connected with circulation line between oxidation trough at the bottom of absorbent slurry nozzle and tower, circulation line is also provided with slurry circulating pump.In described system, also comprise absorbent groove with slurry, absorbent groove top with slurry is provided with fresh water (FW) import, and absorbent trench bottom with slurry is provided with absorbent slurry outlet, and absorbent slurry is delivered to the circulation line on absorption tower by slurry feeding pump by this serum outlet.Oxidation trough at the bottom of absorbing tower 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 the absorbent slurry of oxidation trough at the bottom of tower 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 in oxidation trough at the bottom of absorbing tower, and denseer bottom slurry flows in sedimentation basin, and the clear liquid overflow on sedimentation basin top is in absorbent groove with slurry.In addition, in described system, the flue of supplied flue gases is provided with baffle door, so that bypass runs when breaking down, but also comprises electric meter RACS and fresh water (FW) system.
Embodiment 1
Now for a boiler (10t/h), carry out desulfuration demercuration process according to flue gas desulfurizing and hydrargyrum-removing integral process of the present invention.Described adsorbent slurries are made up of the water of the lime stone of 2.0wt%, the flyash of 2.5wt% and surplus; Described absorption slurries are made up of the water of the lime stone of 2.0wt%, the activated coke of 1.0wt% and surplus; 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 ATMP utilizing the boric acid of 1.2wt%, the oxalic acid of 2.0wt% and 0.1wt% stirs leaching 2.0 ~ 2.5h to flyash, the modified coal ash that then roasting obtains at 300 DEG C.
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 that the modified coal ash used is different, the mixed aqueous solution of the ATMP of the boric acid of 1.2wt%, the tartaric acid of 2.0wt% and 0.1wt% is utilized to stir leaching 2.0 ~ 2.5h to flyash, the modified coal ash that then roasting obtains at 300 DEG C specifically.
Comparative example 2
Compared with embodiment 1, difference is only that the modified coal ash used is different, the mixed aqueous solution of the ATMP of the boric acid of 1.2wt%, the citric acid of 2.0wt% and 0.1wt% is utilized to stir leaching 2.0 ~ 2.5h to flyash, the modified coal ash that then roasting obtains at 300 DEG C specifically.
Comparative example 3
Compared with embodiment 1, difference is that the modified coal ash used is different, utilizes the tartaric mixed aqueous solution of the boric acid of 1.2wt% and 2.0wt% to stir leaching 2.0 ~ 2.5h to flyash, the modified coal ash that roasting obtains at 300 DEG C specifically.
Comparative example 4
Compared with embodiment 1, difference is only that the modified coal ash used is different, the mixed aqueous solution of the ATMP of the boric acid of 1.2wt%, the hydrochloric acid of 2.0wt% and 0.1wt% is utilized to stir leaching 2.0 ~ 2.5h to flyash, the modified coal ash that then roasting obtains at 300 DEG C specifically.
Adopt the technique of comparative example, described total mercury emission is all at 0.12 ~ 0.18mg/m 3between.
Wet method demercuration desulfurizing technology system of the present invention, to the purification of mediumand smallscale industrial boilers flue gas, has great economic and social profit, is worth promoting in China's economic construction process.
For the ordinary skill in the art; specific implementation of the present invention is not subject to the restrictions described above; as long as have employed the improvement of the various unsubstantialities that method of the present invention is conceived and technical scheme is carried out; or design of the present invention and technical scheme directly applied to other occasion, all within protection scope of the present invention without to improve.

Claims (7)

1. a flue gas desulfurizing and hydrargyrum-removing integral process, described technique adopts flue gas desulfurizing and hydrargyrum-removing integral system, 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, described high speed uptake zone tower body is provided with smoke inlet and the injection entrance for horizontal-jet adsorbent; The middle and upper part of described low speed uptake zone tower body is provided with the multiple spraying layer and demist layer that are made up of absorbent slurry nozzle; Circulation line is connected with between oxidation trough at the bottom of absorbent slurry nozzle and tower, circulation line is also provided with slurry circulating pump, it is characterized in that: the heat smoke after burning is first in the high speed uptake zone on absorption tower and adsorbing the Elemental Mercury in described flue gas containing compressed-air actuated adsorbent slurry liquid contacts of spraying into and/or be oxidized to particle mercury and oxidation state mercury enters in oxidation trough at the bottom of tower; Then, the sulfur dioxide in the low speed uptake zone absorbent slurry and flue gas on absorption tower reacts and generates calcium sulfate and calcium sulfite and enter in oxidation trough at the bottom of tower; Described adsorbent slurries are made up of the water of agstone, flyash and surplus; Granularity≤250 order of described agstone and flyash; Described absorbent slurry is made up of the water of agstone, activated coke and surplus, and its pH value is 10 ~ 13.
2. 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.
3. integral process according to claim 1, it is characterized in that: also comprise absorbent groove with slurry, absorbent groove top with slurry is provided with fresh water (FW) import, absorbent trench bottom with slurry is provided with absorbent slurry outlet, and absorbent slurry is delivered to the circulation line on absorption tower by slurry feeding pump by this serum outlet.
4. integral process according to claim 1, is characterized in that: oxidation trough at the bottom of absorbing tower is also provided with oxidation air entrance, and oxidation air delivers into oxidation trough at the bottom of tower by oxidation fan.
5. integral process according to claim 1, is characterized in that: at the bottom of absorbing tower, the bottom of oxidation trough is provided with slurries floss hole, and the absorbent slurry of oxidation trough at the bottom of tower 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 in oxidation trough at the bottom of absorbing tower, and denseer bottom slurry flows in sedimentation basin, and the clear liquid overflow on sedimentation basin top is in absorbent groove with slurry.
6. integral process according to claim 1, is characterized in that: on the flue of supplied flue gases, be provided with baffle door.
7. integral process according to claim 1, is characterized in that: also comprise electric meter RACS and fresh water (FW) system.
CN201410281032.3A 2014-06-23 2014-06-23 Flue gas desulfurizing and hydrargyrum-removing integral system and technique Expired - Fee Related CN104028101B (en)

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AU2016200890A1 (en) * 2015-02-13 2016-09-01 The Babcock & Wilcox Company Method and apparatus for removing mercury from a flue gas stream
DE102015211326A1 (en) * 2015-06-19 2016-12-22 Rwe Power Aktiengesellschaft Process for the separation of mercury from flue gases of incinerators

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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

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EP1932579A1 (en) * 2006-12-07 2008-06-18 Mitsubishi Heavy Industries, Ltd. Method and device for removing mercury
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
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