CN102091517A - Integrated absorption solution for simultaneous desulfuration, denitration and mercury removal and preparation method and application thereof - Google Patents

Integrated absorption solution for simultaneous desulfuration, denitration and mercury removal and preparation method and application thereof Download PDF

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Publication number
CN102091517A
CN102091517A CN2010105999292A CN201010599929A CN102091517A CN 102091517 A CN102091517 A CN 102091517A CN 2010105999292 A CN2010105999292 A CN 2010105999292A CN 201010599929 A CN201010599929 A CN 201010599929A CN 102091517 A CN102091517 A CN 102091517A
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China
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absorption liquid
additive
absorption
flue gas
reducing agent
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CN2010105999292A
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Chinese (zh)
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岑超平
方平
唐志雄
陈定盛
陈志航
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环境保护部华南环境科学研究所
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Publication of CN102091517A publication Critical patent/CN102091517A/en

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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The invention discloses integrated absorption solution for simultaneous desulfuration, denitration and mercury removal and application thereof. The conventional wet desulfuration facilities are fully utilized, and an oxidation absorption single-stage treatment mode is adopted, namely the conventional alkali desulfuration absorption solution is improved, SO2, NOX and mercury in the flue gas are washed and removed by adopting mixed absorption solution containing nitrogen reducer and additives, and a nitrogen-containing byproduct serving as a compound fertilizer raw materials is reclaimed; and the absorption solution comprises the following components in percentage by mass: 3 to 20 percent of nitrogen-containing reducer, 1 to 10 percent of alkali additive, 0.05 to 2 percent of oxidation additive, and the balance of water. The invention is simple in process, flexible in selection, low in investment and running cost, high in pollutant removal efficiency and wide in application range; and an industrial boiler provided with the wet desulfuration facilities can be implemented by proper reformation.

Description

Integrated while desulfurization denitration demercuration absorption liquid and its production and application
Technical field
The invention belongs to the air pollution control technique field, be specifically related to the absorption liquid and preparation method thereof and the application in smoke pollution control of integrated while desulfurization denitration demercuration.
Background technology
China's atmosphere polluting problem is outstanding, and main pollutant is SO 2And NO X, also comprise heavy metals such as Hg simultaneously.Wherein the industrial coal process is the main path that above-mentioned atmosphere pollution is discharged in artificial source.China every year is by coal fire discharged SO according to statistics 2Amount just surpasses 1,200 ten thousand tons/year, the NO of discharging XAmount surpasses 4,000,000 tons/year, and the Hg amount of discharging is above 250 tons/year.SO 2, NO XNot only China environmental ecology system is caused serious destruction with a large amount of dischargings of Hg, but also seriously hindered China's economic development and China's people's health is caused a significant threat.Yet the energy resource structure of China present stage has determined that in quite long from now on period China can not change with the consumption general layout based on the energy supply of coal.Therefore carry out the research of coal-fired flue-gas pollutant control technology, the atmospheric environment of improving and administering China is to promoting China's sustained economic development, protecting people healthy significant.
At present, flue dust, the SO that discharging is produced at coal-fired flue-gas 2, NO XPollution control, generally adopt the control mode of building independent dust removal installation (as electrostatic precipitator and sack cleaner), desulfurization facility (as limestone/gypsum wet desulphurization technology) and denitration facility (as SCR and SNCR technology) both at home and abroad, and the control technology of Hg is except that minority enters application in the flue gas, and great majority still are in the research and development.Can effectively control flue dust in the coal-fired flue-gas, SO though build the control mode of independent dedusting, desulfurization, denitration and even demercuration facility 2, NO XPollute with Hg, but there are problems such as complex process, investment operating cost height in this kind control mode, has hindered it and has applied.For this reason, pay attention to day by day coal-fired flue-gas pollutant Collaborative Control Study on Technology exploitation both at home and abroad, as: dust removal combined facility research and development dedusting demercuration jointly controls technology, in conjunction with the catalytic oxidation technology of SCR technical research exploitation mercury, in conjunction with wet desulphurization technical research exploitation while desulphurization denitration technology and while desulfuration demercuration technology etc.Wherein dedusting demercuration technology and the wet method existing at present part engineering application of desulphurization denitration technology simultaneously, but large-scale application still needs further research.And wet method desulfurization denitration demercuration technology research both at home and abroad at present simultaneously is less, and this technology realizes SO simultaneously based on the wet desulphurization technology in a set of equipment 2, NO XWith the removal of Hg, have advantages such as floor space is little, investment operating cost is low, Operation and Maintenance is simple, be a kind of comparatively desirable coal-fired flue-gas pollutant Collaborative Control technology.The present invention just is being based on the fact that present domestic coal-burning boiler generally is equipped with the wet desulphurization facility, by changing existing absorption liquid, adopts the blend absorbent of economic nitrogenous reducing agent+additive to absorb the SO that removes in the flue gas simultaneously efficiently 2, NO XWith the Hg pollutant, realize the flue gas and desulfurizing and denitrifying demercuration, and reclaim nitrogenous byproduct as composite fertilizer material.
Summary of the invention
Primary and foremost purpose of the present invention is to provide the absorption liquid of a kind of integrated while desulfurization, denitration, demercuration, and these absorption liquid raw material sources are extensive, with low cost.
Another object of the present invention provides the preparation method of above-mentioned absorption liquid.
A further object of the present invention is to provide the application of above-mentioned absorption liquid in smoke pollution control, SO in promptly a kind of flue gas 2, NO XWith the integrated method that removes simultaneously of mercury, this method just can be implemented through simple modifications on existing dedusting and wet desulphurization facility, and technology simply, investment and operating cost is low, and the contaminant removal efficiency height is to SO 2Clearance more than 95%, NO XClearance is more than 50%, and the clearance of mercury is more than 80%, simultaneously can also the reclaim sulfuric acid ammonium, nitrogenous byproduct such as ammonium nitrate is as composite fertilizer material.Application implementation of the present invention can effectively reduce SO in China's flue gas 2, NO XWith the pollution of mercury,, promote society, economy, environment harmonious development significant to protection China's atmospheric environment and people's lives and properties health.
Purpose of the present invention realizes by following concrete technical scheme: the absorption liquid of a kind of integrated while desulfurization, denitration, demercuration is made up of nitrogenous reducing agent and additive.
Described nitrogenous reducing agent is one or more in urea, aminoquinoxaline, the ammonium carbonate.
Described additive is bases additive or oxidized form additive or both combinations.
Described bases additive is one or more in NaOH, lime, the lime stone.
Described oxidized form additive is one or more in clorox, calcium hypochlorite, hydrogen peroxide, potassium permanganate, sodium chlorite, the potassium peroxydisulfate.
Each composition of described absorption liquid is as follows by its mass percent:
Nitrogenous reducing agent 3%~20%, bases additive 1%~10%, oxidized form additive 0.5 ‰~2% remains and is water.
For realization the present invention of economical and efficient, its composition of particularly preferred absorption liquid is as follows by mass percentage: urea 10%, and NaOH 1%, hypochlorite oxidation agent 1% remains and is water.
The preparation method of above-mentioned absorption liquid, comprise the steps: to get a certain amount of water, the nitrogenous reducing agent that adds required quality by mass percentage, stir, make nitrogenous reducing agent fully soluble in water, add additive according to mass percent subsequently, stir, promptly obtain the integration desulfurization denitration demercuration absorption liquid.
The application in smoke pollution control of above-mentioned integration desulfurization denitration demercuration absorption liquid, it is the flue gas purifying method of integrated while desulfurization denitration demercuration, temperature is reduced to 130~150 ℃ after comprising the steps: (1) flue gas process economizer and air preheater, enter the deduster dedusting subsequently, the mercury of most of particulate form in dust removal process (<5% total mercury amount) is held back removal with flying dust by deduster.Flue gas is entered by absorption tower bottom subsequently, and from last spray and temperature range down is 40~80 ℃ a circulating absorption solution haptoreaction, and most SO in the flue gas 2, most NO XAnd most mercury is absorbed removal in this process, feeds oxidation air toward the bottom, absorption tower in the running, and the sulfite ion that generates is oxidized to sulfate radical, the flue gas after purifying after the demister demist by the chimney qualified discharge.
(2) absorption liquid absorbs saturated output by the absorption tower afterwards, carry out respective handling according to actual conditions subsequently, when absorption liquid is nitrogenous reducing agent and oxidized form additive, absorption liquid absorbs saturated concentrating and separating, dehydration and the nitrogenous byproduct of dry Processing of Preparation of carrying out afterwards, and final isolated waste water enters Waste Water Treatment and handles qualified discharge; When absorption liquid is nitrogenous reducing agent and bases additive, do not reclaim, directly enter Waste Water Treatment and handle qualified discharge; When absorption liquid is nitrogenous reducing agent, oxidized form additive and bases additive, do not reclaim, directly enter Waste Water Treatment and handle qualified discharge.
Described flue gas produces by coal-burning boiler burning or municipal solid waste incineration.
The pH value of described absorption liquid is controlled in the 5-8 scope.
The temperature of described absorption liquid is 40~80 ℃.
Described absorption tower comprises any one in the absorption tower such as the efficient absorption tower (ZL200420103291.9), packed tower, spray column, rotating stream tray scrubber of existing patented technology preparation.
For realization the present invention of economical and efficient, particularly preferred absorption tower is the efficient absorption tower of existing patented technology preparation.
The flue gas purifying method of integrated while desulfurization denitration demercuration, promptly make full use of existing wet desulphurization facility, " oxidation absorption " the uniprocessing mode of employing by changing existing absorption liquid, promptly adopts the blend absorbent of " nitrogenous reducing agent+additive " to wash the SO that removes in the flue gas 2, NO XAnd mercury.Absorbing saturated slurries can take to reclaim nitrogenous byproduct for treatment according to actual conditions, and the waste water that produces after handling enters Waste Water Treatment and handles qualified discharge; Or do not reclaim and directly enter Waste Water Treatment and handle qualified discharge.
Basic principle of the present invention is: adopt the gas-liquid contact, the principle of diffusion-dissolving is with the Hg in the wet scrubbing removal flue gas 2+Based on oxidation-reduction reaction, utilize the NO in the nitrogenous reducing agent reduction removal flue gases such as urea, aminoquinoxaline X, make its final harmless N of generation 2Discharging, this process also has small amount of N H 4NO 3Generate; Utilize nitrogenous reducing agent or alkaline absorption solution to absorb and remove SO 2, final oxidation generates SO 4 2-Remove; Utilize the simple substance mercury (Hg in the oxidant oxidation flue gas 0) be divalence mercury (Hg 0→ Hg 2+), finally be absorbed by liquid absorption, generate the HgSO of indissoluble 4Precipitation is removed.
Concrete desulphurization reaction equation is (is example with urea, alkali):
SO 2(g)+0.5O 2(g)+(NH 2) 2CO(aq)+2H 2O(l)→(NH 4) 2SO 4(aq)+CO 2(g)
2SO 2(g)+4OH -(aq)+O 2(g)→2H 2O(l)+2SO 4 2-(aq)
Concrete denitration reaction equation is (is example with urea):
NO(g)+NO 2(g)+(NH 2) 2CO(aq)→2N 2(g)+CO 2(g)+2H 2O(l)
Concrete demercuration reaction equation is (hypochlorous sodium is an example):
2Hg(g)+4NaClO(aq)+2H 2O(l)→2HgCl 2(aq)+4NaOH(aq)+O 2(g)
Hg 2+(aq)+SO 4 2-(aq)→2HgSO 4(s)
The present invention compared with prior art has following advantage and beneficial effect:
1) the absorption liquid raw material sources are convenient, and storage and use are simple, and the production use cost is cheap;
2) process choice is flexible, and integrated artistic is simple, and the operation operation is easy, the contaminant removal efficiency height.The present invention is to SO 2Clearance more than 95%, to NO XClearance more than 50%, more than 80%, and can reclaim nitrogenous byproduct to the clearance of Hg as composite fertilizer material.
3) only need carry out appropriate reconstruction to existing coal-burning boiler and can move enforcement, floor space is little, and adaptability is strong, and overall operation is with low cost, no matter is that large-scale coal-burning power plant or small-sized coal-burning boiler can be used.
4) this technology also can be applicable to the improvement of municipal solid waste incineration waste gas such as mud, rubbish, applied range.
Description of drawings
Fig. 1 is the applicating flow chart of absorption liquid of the present invention in smoke pollution control;
The specific embodiment
The present invention is further detailed explanation below in conjunction with specific embodiment and accompanying drawing, but embodiments of the present invention are not limited thereto.
Fig. 1 has provided the applicating flow chart in smoke pollution control of blend absorbent of the present invention.Temperature is reduced to 130~150 ℃ behind flue gas process economizer that burning produces and the air preheater, enters the deduster dedusting subsequently, and the flue gas after the dedusting enters desulfurization denitration demercuration absorption tower simultaneously by the bottom; Nitrogenous reducing agent, additive and fresh water (FW) join and absorb the absorption liquid that liquid pool is mixed with desired concn, and are heated to 40~80 ℃ by adding apparatus, are taken out by water circulating pump then and rise to the top, absorption tower, descend from last spray; Blend absorbent and flue gas be the counter current contacting reaction in the absorption tower, the SO of the overwhelming majority in the flue gas 2, most NO XAnd most mercury is absorbed removal in this process, feeds oxidation air toward the bottom, absorption tower in the running, and the sulfite ion that generates is oxidized to sulfate radical.Flue gas after purifying after the demister demist by the chimney qualified discharge.After the absorption liquid absorption is saturated, export by the absorption tower, enter saturated absorption liquid storage pool, can carry out respective handling according to actual conditions subsequently, when absorption liquid is urea and oxidized form additive, absorb saturated slurries afterwards and can carry out concentrating and separating, dehydration and the nitrogenous byproduct of dry Processing of Preparation, byproduct enters the byproduct apotheca, and isolated waste water enters Waste Water Treatment and handles qualified discharge; When absorption liquid is urea and alkali additive, can not reclaim, directly enter Waste Water Treatment and handle qualified discharge, when absorption liquid is nitrogenous reducing agent, oxidized form additive and bases additive, can not reclaim, directly enter Waste Water Treatment and handle qualified discharge.
Embodiment one
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, sodium chlorite additive, and concrete quality group becomes: urea 5%, sodium chlorite 0.5 ‰ remain and are water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 6~7.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the derivation by pump afterwards and enters nitrogenous byproduct recovery system recovery byproduct, and the waste water of generation enters Waste Water Treatment and handles qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<20mg/m 3, NO XConcentration is<100mg/m 3, Hg concentration is<3 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>84.6%, Hg average removal rate>85%.And whenever remove 1 ton of SO 2And NO XCan reclaim 1.6 tons (NH respectively 4) 2SO 4NH with 0.3 ton 4NO 3Byproduct.
Embodiment two
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, potassium permanganate additive, and concrete quality group becomes: urea 10%, potassium permanganate 2 ‰ remain and are water.Control absorption liquid reaction temperature is 70 ℃ in the use, and pH is 5~6.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the derivation by pump afterwards and enters nitrogenous byproduct recovery system recovery byproduct, and the waste water of generation enters Waste Water Treatment and handles up to standard.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<15mg/m 3, NO XConcentration is<80mg/m 3, Hg concentration is<3 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>88%, Hg average removal rate>85%.And whenever remove 1 ton of SO 2And NO XCan reclaim 1.5 tons (NH respectively 4) 2SO 4NH with 0.25 ton 4NO 3Byproduct.
Embodiment three
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, clorox additive, and concrete quality group becomes: urea 15%, clorox 1% remain and are water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 5~6.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the derivation by pump afterwards and enters nitrogenous byproduct recovery system recovery byproduct, and the waste water of generation enters Waste Water Treatment and handles up to standard.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<20mg/m 3, NO XConcentration is<140mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>78%, Hg average removal rate>80%.And whenever remove 1 ton of SO 2And NO XCan reclaim 1.4 tons (NH respectively 4) 2SO 4NH with 0.2 ton 4NO 3Byproduct.
Embodiment four
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, hydrogen peroxide additive, and concrete quality group becomes: urea 20%, hydrogen peroxide 2% remain and are water.Control absorption liquid reaction temperature is 40 ℃ in the use, and pH is 5~6.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the derivation by pump afterwards and enters nitrogenous byproduct recovery system recovery byproduct, and the waste water of generation enters Waste Water Treatment and handles up to standard.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<35mg/m 3, NO XConcentration is<180mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>98%, NO XAverage removal rate>72%, Hg average removal rate>80%.And whenever remove 1 ton of SO 2And NO XCan reclaim 1.4 tons (NH respectively 4) 2SO 4NH with 0.2 ton 4NO 3Byproduct.
Embodiment five
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, NaOH additive, and concrete quality group becomes: urea 10%, NaOH 5% remain and are water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<10mg/m 3, NO XConcentration is<320mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>50%, Hg average removal rate>80%.
Embodiment six
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, NaOH additive, sodium chlorite additive, and concrete quality group becomes: urea 3%, NaOH 1%, sodium chlorite 1 ‰ remain and are water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, Na 2SO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<20mg/m 3, NO XConcentration is<80mg/m 3, Hg concentration is<3 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>88%, Hg average removal rate>85%.
Embodiment seven
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
The prepared efficient absorption tower of ZL200420103291.9 patented technology is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of carbamide reducing agent, NaOH additive, potassium peroxydisulfate additive, and concrete quality group becomes: urea 5%, NaOH 1%, potassium peroxydisulfate 5 ‰ remain and are water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, Na 2SO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<20mg/m 3, NO XConcentration is<160mg/m 3, Hg concentration is<2 μ g/g, SO 2Average removal rate>99%, NO XAverage removal rate>75%, Hg average removal rate>90%.
Embodiment eight
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
Packed tower is adopted on the absorption tower: tower height 15m, tower diameter are 3m, and ceramic Pall ring packed height is 1m, gas residence time>4s.
Absorption liquid is made up of aminoquinoxaline, NaOH additive, clorox additive, and concrete quality group becomes: aminoquinoxaline 10%, sodium hydrate content 5%, clorox 1% remains and is water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, Na 2SO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<40mg/m 3, NO XConcentration is<200mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>98%, NO XAverage removal rate>69%, Hg average removal rate>80%.
Embodiment nine
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
Spray column is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of ammonium carbonate, lime additive, clorox additive, and concrete quality group becomes: ammonium carbonate 20%, lime content 10%, clorox 2% remains and is water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, CaSO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<80mg/m 3, NO XConcentration is<300mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>96.5%, NO XAverage removal rate>54%, Hg average removal rate>80%.
Embodiment ten
The exhaust gas volumn that certain factory's coal-burning boiler burning produces is 4.5 ten thousand m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 2250~2400mg/m 3, NO XConcentration is 650~800mg/m 3, Hg concentration is 20~25 μ g/g, the cigarette temperature is 130~135 ℃.
Rotating stream tray scrubber is adopted on the absorption tower: tower height 15m, tower diameter are 3m, gas residence time>4s.
Absorption liquid is made up of urea, lime stone additive, clorox additive, and concrete quality group becomes: urea 20%, lime content 10%, calcium hypochlorite 2% remains and is water.Control absorption liquid reaction temperature is 80 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, CaSO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<50mg/m 3, NO XConcentration is<250mg/m 3, Hg concentration is<4 μ g/g, SO 2Average removal rate>97.8%, NO XAverage removal rate>62%, Hg average removal rate>80%.
Embodiment 11
The exhaust gas volumn that certain waste from a factory incinerator burning produces is 80,000 m 3/ h records SO in the flue gas after the deduster dedusting 2Concentration is 400~800mg/m 3, NO XConcentration is 300~400mg/m 3, Hg concentration is 0.5~5mg/g, the cigarette temperature is 190~240 ℃.
The existing prepared efficient absorption tower of patented technology is adopted on the absorption tower: tower height 16m, tower diameter are 3.5m, gas residence time>4s.
Absorption liquid is made up of urea, lime stone additive, clorox additive, and concrete quality group becomes: urea 10%, sodium hydrate content 5%, clorox 2% remains and is water.Control absorption liquid reaction temperature is 60 ℃ in the use, and pH is 7~8.
In the production process, the absorption liquid for preparing is delivered to efficient absorption tower top by circulating pump, and flue gas is then imported by the bottom, absorption tower, and both are the counter current contacting reaction in the absorption tower, the SO in the flue gas 2, NO X, Hg is absorbed by liquid absorption final generation (NH 4) 2SO 4, N 2, NH 4NO 3, HgSO 4Deng, the flue gas after purifying after the demister demist by the chimney qualified discharge.Absorption liquid absorbs saturated the recovery afterwards and directly enters Waste Water Treatment processing qualified discharge.Adopt and to record after the absorption tower SO in the flue gas after the described technical scheme of present embodiment 2Concentration<10mg/m 3, NO XConcentration is<100mg/m 3, Hg concentration is<10 μ g/g, SO 2Average removal rate>97.5%, NO XAverage removal rate>67%, Hg average removal rate>98%.
Above embodiment is a preferred implementation of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other are included within protection scope of the present invention not deviating from change, the modification made under the present invention spirit essence and the principle, substitute, combination, simplifying the substitute mode that all should be equivalent.

Claims (8)

1. the absorption liquid of integrated while desulfurization, denitration, demercuration is characterized in that: be made up of nitrogenous reducing agent and additive;
Described nitrogenous reducing agent is one or more in urea, aminoquinoxaline, the ammonium carbonate;
Described additive is bases additive or oxidized form additive or both combinations;
Described bases additive is one or more in NaOH, lime, the lime stone;
Described oxidized form additive is one or more in clorox, calcium hypochlorite, hydrogen peroxide, potassium permanganate, sodium chlorite, the potassium peroxydisulfate.
2. according to the absorption liquid of the described integrated while desulfurization of claim 1, denitration, demercuration, it is characterized in that: each composition of described absorption liquid is as follows by its mass percent:
Nitrogenous reducing agent 3%~20%, bases additive 1%~10%, oxidized form additive 0.5 ‰~2% remains and is water.
3. according to the absorption liquid of claim 1 or 2 described integrated while desulfurization, denitration, demercuration, it is characterized in that: each composition of described absorption liquid is as follows by its mass percent: urea 10%, and NaOH 1%, hypochlorite oxidation agent 1% remains and is water.
4. the preparation method of the described absorption liquid of each claim of claim 1-3, it is characterized in that comprising the steps: to get a certain amount of water, the nitrogenous reducing agent that adds required quality by mass percentage, stir, make nitrogenous reducing agent fully soluble in water, add additive according to mass percent subsequently, stir, promptly obtain the integration desulfurization denitration demercuration absorption liquid.
5. the application of the described absorption liquid of described each claim of claim 1-3 in smoke pollution control, temperature is reduced to 130~150 ℃ after it is characterized in that comprising the steps: (1) flue gas process economizer and air preheater, enter the deduster dedusting, enter by the bottom, absorption tower subsequently, with from last spray and under temperature range be 40~80 ℃ circulating absorption solution haptoreaction, feed oxidation air toward absorption tower bottom in the running, the flue gas after purifying after the demister demist by the chimney qualified discharge.
(2) after the absorption liquid absorption is saturated, export by the absorption tower, carry out respective handling according to actual conditions subsequently, when absorption liquid is nitrogenous reducing agent and oxidized form additive, absorption liquid absorbs saturated concentrating and separating, dehydration and the nitrogenous byproduct of dry Processing of Preparation of carrying out afterwards, and final isolated waste water enters Waste Water Treatment and handles qualified discharge; When absorption liquid is nitrogenous reducing agent and bases additive, do not reclaim, directly enter Waste Water Treatment and handle qualified discharge; When absorption liquid is nitrogenous reducing agent, oxidized form additive and bases additive, do not reclaim, directly enter Waste Water Treatment and handle qualified discharge.
6. the application of the described absorption liquid of claim 1-3 in smoke pollution control is characterized in that: described flue gas produces by coal-burning boiler burning or municipal solid waste incineration.
7. according to the described application of claim 6, it is characterized in that: the pH value of described absorption liquid is controlled in the 5-8 scope.
8. according to the described application of claim 6, it is characterized in that: the temperature of described absorption liquid is 40~80 ℃.
CN2010105999292A 2010-12-22 2010-12-22 Integrated absorption solution for simultaneous desulfuration, denitration and mercury removal and preparation method and application thereof CN102091517A (en)

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CN102847418A (en) * 2011-07-01 2013-01-02 湖南晟通科技集团有限公司 Additive for limestone-gypsum wet flue gas desulfurization and denitration process
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CN103194296B (en) * 2013-04-25 2015-03-18 兰州新星中性清洗技术有限公司 Coal washing and desulfurizing agent composition and preparation method thereof
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