CN101879404B - Recycled flue gas desulfurization and denitration method - Google Patents
Recycled flue gas desulfurization and denitration method Download PDFInfo
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- CN101879404B CN101879404B CN2010102242191A CN201010224219A CN101879404B CN 101879404 B CN101879404 B CN 101879404B CN 2010102242191 A CN2010102242191 A CN 2010102242191A CN 201010224219 A CN201010224219 A CN 201010224219A CN 101879404 B CN101879404 B CN 101879404B
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Abstract
The invention relates to a recycled flue gas desulfurization and denitration method, which sequentially comprises the following steps of: introducing flue gas of SO2 and NOx into a desulfurizing tower, and absorbing the SO2 with a desulfurizing agent (barren liquor) in the desulfurizing tower; desorbing the desulfurizing agent (rich liquor) which absorbs the SO2 through a multi-effect evaporator, releasing the SO2 gas, and concentrating the SO2 gas into liquid SO2 through condensation drying; making the desulfurized flue gas enter a denitration tower, injecting gaseous ozone from an ozone generator, oxidizing the NO in the flue gas, absorbing the oxidized NO by using a denitrifier to form nitrate; crystallizing and separating out the nitrate in the solution after the nitrate reaches certain concentration, and filtering and drying to obtain the nitrate product. The method turns the wastes into wealth, and the SO2 and NOx in the flue gas are recycled by higher-additional value liquid SO2 and nitrate products, so that the recycling and value maximization in the desulfurization and denitration process is realized. Due to the adoption of the technical scheme, the high desulfurization and denitration rate can be achieved, the desulfurization rate is over 96 percent, the denitration rate is more than 90 percent, and the purity of the nitrate product is over 96 percent. The method has the advantages of simple desulfurization and denitration process, low investment, and low operation cost for desulfurization and denitration, and solves the problems that the conventional desulfurization and denitration process has high cost, generates a side product of a mixture of sulfuric acid (sulfate) and nitric acid (nitrate), and has low additional value.
Description
Technical field
The present invention relates to a kind of flue gas desulfurization and denitration method of resource, specifically, relate to NO and SO in the flue gas
2The method that removes and realize respectively resource.
Background technology
China is coal-fired big country, and coal accounts for 75% of primary energy total quantity consumed.A large amount of consumption of the energy have caused serious air environmental pollution, and wherein that the most outstanding is SO
2And NO
xThe acid rain harm that discharging causes, and NO
xThe depletion of the ozone layer that causes and photochemical fog." for the first time national Pollutant source investigation communique " announced on February 6th, 2010 according to national environmental protection section shows, in 2007 years, China's SO2 emissions are 2320.00 ten thousand tons, 1166.64 ten thousand tons of flue dust, 1797.70 ten thousand tons of nitrogen oxide, the air contaminant treatment task is very arduous.At present, China's sulfur dioxide (SO2) emissions total amount occupies first place in the world, and acid rain and sulfur dioxide pollution cause economic loss every year is more than 1,000 hundred million yuan.In recent years, country successively puts into effect the multinomial powerful SO of propelling that is intended to
2The policies and regulations of sulfur dioxide (SO2) emissions growth are alleviated in the measure that reduces discharging, and thermal power plant takes active action, or builds the FGD device, or changes clean fuel, or adopts the clean burning technology, or close, stop old, little unit, make the SO that soars for many years
2Total emission volumn is contained tentatively to some extent.Yet nitrogen oxide but highlights day by day, and well-known, the extent of injury of nitrogen oxide goes even farther than sulfur dioxide, even more deep and broad, and the Acid Rain Pollution of Future in China will be by sulfuric acid type to the compound development of sulfuric acid/nitric acid.Control SO
2With the discharging of nitrogen oxide be extremely urgent.
At present; be placed in status of equal importance in China's desulfurization and denitration; existing mainstream technology has many advantages; can satisfy the requirement of environmental protection; but weak point is that investment and operating cost are high; it is low that desulfurizing byproduct such as calcium sulfate etc. are worth, even also to bring secondary pollution problem, denitration then be unworthy accessory substance N
2, but consume a large amount of reducing agent ammonia and expensive catalyst.Therefore, investment is hanged down in exploitation, the combined desulfurization and denitration technology is the developing direction of pollution that caused by coal burning thing control new technology cheaply.
21 century, the world has entered the epoch of kownledge economy and sustainable development, requires to set up the unity of opposites of development and environment.Along with the mankind's development, many resources are faced with and reduce even depleted stage.Fully make rational use of resources or even waste resource has become contemporary science and technology worker's social responsibility.In theory, any production process does not all have discarded object, only has the resource that is not fully utilized.Also be so aspect atmosphere pollution, be called as at present the SO of one of Air Pollutant Discharge
2And NO
x, but be two important and be badly in need of resources in China.SO
2Be the necessary raw material of producing sulfuric acid, and sulfuric acid is the necessary raw material of producing chemical fertilizer, the title of " father of the female and agricultural of industry " is arranged.Equally, NO
xAlso be the necessary raw material of producing nitric acid, nitric acid is again the important source material of producing NpK complex fertilizer, also is the important source material of the industries such as chemical industry, military project, the people be quick-fried.Therefore, carry out SO
2And NO
xPollution control and recovery technology research are to alleviating acid rain harm, promoting that rationally utilizing of resource is significant!
The desulphurization and denitration technology mainly contains three kinds in the prior art:
(I) desulfur technology (the removal of nitrogen oxide rate is lower in this technology): such as lime-gypsum method (CN1281747), wet ammonia process desulfurizing technology (CN1226459), seawater desulfurizing process (CN1262145), double alkali method desulfurizing technology (CN1475298), semi-dry desulphurization technology (CN101249380), circulating fluidized bed desulfur technology (CN1401411), Electron Beam FGD Technology (environmental protection, 2004 (9): 15-18) etc.
(II) denitration technology: comprise selective catalytic reduction (SCR), such as US 4221768, US4101238, US4048112; With SNCR method (NCSR), such as CN1817415, CN101244361.
(III) while desulphurization denitration technology: such as CN1454700, CN1147416, CN1843574, CN1923341, CN101053747, CN101337152, CN101485957, CN101352648, CN101306308, CN1311052, CN101053750 etc.
In the technology (I), mainly take desulfurization as main, the denitration rate is generally lower.Lime-gypsum method is maximum a kind of technology of using in the present state inner desulfurization technology, desulfuration efficiency is higher, the energy by-product gypsum, but because China is a plaster of paris resource-rich country, and the gypsum of desulfurization by-product is being compared in addition nuance qualitatively with the plaster of paris, such as color and luster, content of beary metal etc., going back that therefore domestic desulfurated plaster really uses is few, and most of desulfurated plasters are among the stacking.A large amount of constructions along with the power plants desulfurizing item, the desulfurated plaster discharge capacity increases severely, how handling this a part of gypsum well also will be a very important problem, store up if take to abandon, need to build special slag field, not only invest hugely, take a large amount of soils, also easily cause dust, underground water to the pollution of surrounding environment, the operating cost of processing simultaneously gypsum is also very high.The ammonia process of desulfurization, belong to the resource desulfur technology, sulfur dioxide recovery in the flue gas is produced ammonium sulfate fertilizer, but ammonium sulfate has certain limitation as fertilizer application, and long-term use can make soil compaction, and under flooding condition, soil meeting severe depletion of oxygen, after ammonium sulfate was used, sulfate ion wherein can be reduced into sulfide, and the too high root system of plant that makes of sulfide concentration accumulation is injured and death.Ammonium sulfate fertilizer uses better in the salt-soda soil.Therefore, if a large amount of desulfurizing items adopts ammonia process, might cause the market problem of thiamine fertilizer.Other desulfur technology is used also relatively less at present in industry.
In the technology (II), the denitration efficiency of SCR is higher than NCSR, and the denitration efficiency of SCR can reach more than 80%, and most of technology of using in the denitrification apparatus at present are SCR.But the major defect of SCR method is that catalyst is easily poisoned, and exists ammonia leakage and investment cost, operating cost to cross the problems such as high.According to (China Power, 2006,39 (3): 86～89) measuring and calculating, utilize the SCR method remove-ton NOx expense reached more than 9800 yuan! High operating cost will hinder the enthusiasm of enterprise's denitration, and the researcher is exploring new denitration technology both at home and abroad.
In the technology (III), refer in a process, use the same method with the SO in the flue gas
2Technology with NOx removes simultaneously that is to say, no matter the product behind the desulphurization denitration has or not use, contains simultaneously SO in the product
3 -/ SO
4 -Or NO
2 -/ NO
3 -, be a kind of mixture.CN1454700 adopts microwave in the absorption sensitizer layer that is comprised of Ni, Fe, Co, Mn metal or metal oxide, the SO in the flue gas
2Be reduced into sulphur, NOx is reduced into N
2, but this process unit is complicated, has microwave from leakage problem etc.CN1147416 discloses and has used TiO
2SO in the absorption flue gas
2With the technology of NOx, adsorb saturated TiO
2Realize regeneration in the dilute sulfuric acid by being immersed in, but the method is not illustrated TiO
2The SO of middle absorption
2With the place to go of NOx in its regenerative process, well-known, dilution heat of sulfuric acid be not can and SO
2With NOx reaction.CN1843574 discloses and has utilized sodium chlorite and additive to form absorbent solution, with SO in the flue gas
2Be oxidized to SO
4 -, NO is oxidized to NO
3 -, then generate the mixture of ammonium sulfate and ammonium nitrate with the ammoniacal liquor effect; But the consumption of sodium chlorite is large in this technology, and absorbent pH value is lower, and is large to the corrosivity of equipment.CN1923341 discloses and has utilized ozone simultaneous oxidation SO
2With the method for NO, utilize the oxidisability of ozone with SO
2Be oxidized to SO
3, NO is oxidized to NO
2Or NO
3, then use alkali liquor absorption, crystallization, form the mixture of sulfate and nitrite, nitrate, if but this mixture without separation, be without much use.CN101053747 by hydrogen peroxide or ozone with the SO in the flue gas
2With the NO oxidation, then use ammonia absorption, form at last ammonium sulfate and ammonium nitrate mixture, as fertilizer application.Although desulphurization denitration accessory substance last in this technology can be used as fertilizer application, added value is relatively low.CN101337152 is then by the ozone SO in the flue gas just
2With the NO oxidation, then water absorbs, and forms at last sulfuric acid and nitric acid weak solution, and separates the single product that forms sulfuric acid and nitric acid by chemical method.But how this technology also unspecifiedly separates the nitration mixture of sulfuric acid and nitric acid, the worker of chemical field knows, very large with the mixed solution separating difficulty of sulfuric acid and nitric acid, and in desulphurization plant, form dilute acid soln, corrosivity to equipment is very large, and equipment investment and maintenance cost will be very large.CN101485957 then discloses desulfurization and denitration has been carried out in two equipment, uses alkali lye the SO in the flue gas
2Absorption is got off, and with ozone sulfite oxidation is become sulfate again in liquid phase; In denitration device, use ozone the NO oxidation, then form the mixture of nitrite/nitrate with alkali liquor absorption.Although this technology is carried out desulphurization and denitration respectively in two equipment, realized separating of sulphur resource and nitrogen resource, high more a lot of than the cost with air oxidation with ozone deoxidation sulphite.CN101352648 then absorbs NO, bivalent metal oxide or carbonate alkalescence desulfurizing agent with cobalt amine complex solution and absorbs SO
2Method realize simultaneously desulphurization denitration.This is a kind of pure SO that removes
2With the method for NOx, do not have to realize resource.CN101306308 and CN101352648 are similar, and knowledge has replaced to the ferrous ammonium complex solution to cobalt amine complex solution.CN1311052 then discloses the complex compound that forms with divalence cobalt and ammonia NO has been oxidized to NO
2, then generate ammonium nilrite, the SO in the flue gas with the ammoniacal liquor reaction
2Generate ammonium sulfite with ammonia react, in liquid phase, be oxidized to ammonium sulfate, formed the mixture of ammonium sulfate and ammonium nilrite/ammonium nitrate, reach the purpose of desulphurization denitration.The same with CN101053747, the accessory substance of desulphurization denitration can only be as fertilizer application, and added value is lower.CN101053750 then discloses at photochemical catalyst TiO
2Effect under, by UV-irradiation, the NO in the flue gas is oxidized to NO
2, NO
2Be reduced into N by sodium sulfite
2NO
2Be reduced into N
2This saying is worth discussion, because in the file of this patent, does not have NO in the relevant reaction equation
2Generate N with the sodium sulfite reaction
2Reaction, in aforesaid each desulphurization denitration patent, mostly be NO
2By alkali liquor absorption, form nitrite/nitrate, with SO
2The sulphite that generates after absorbing mixes.
China is the country of an a lack of sulfur, the annual need from external a large amount of imported sulphur with preparation SO
2Or sulfuric acid, and China is a SO
2Discharging big country in the existing desulfur technology, is SO mostly
2Absorb and form the solid waste gypsum, the ammonium sulfate of the low fertilizer efficiency of a small amount of desulfur technology generation.In the desulfurizing and denitrifying process, also be the SO in the flue gas mostly simultaneously
2Absorb the mixture of formation sulfate and nitrate with NOx, be difficult to form the resource product of high added value.
In sum, in the existing desulfurizing and denitrifying process, the part that still has some deficits, desulphurization denitration technology remain further to be improved.
Summary of the invention
The object of the invention is, overcomes the defective that prior art exists, and provides a kind of and can remove SO from flue gas
2With NOx, can reclaim SO again
2, NOx resource desulphurization denitration technology.
Realize the technical scheme of the object of the invention:
The inventor thinks, in order to reclaim SO
2Can adopt the method for absorbent absorption, desorb, from flue gas, remove SO
2And prepare liquid SO
2, realize the SO in the resource type treating flue gas
2Problem, and realized value maximization.SO with the sodium sulfite solution absorption
2Method claim again the Wellman-Lord method, its principle is:
Absorption process: Na
2SO
3+ SO
2+ H
2O → 2NaHSO
3
Desorption process:
Side reaction: Na
2SO
3+ 1/2 O
2→ Na
2SO
4
But, the main cause that sodium sulfite absorption and desorption method is difficult to promote is: (1) alkaline consumption is high: lost absorbability owing to some sodium sulfite is oxidized to sodium sulphate, oxygenation efficiency is about 10%, so the sodium sulfite that needs additional alkali such as soda ash to fall with replenish lost:
Na
2CO
3+SO
2→Na
2SO
3+CO
2
Like this, 1 ton of SO of every recovery
2Replenish 0.3 ton of soda ash.(2) steam consumption is high.Desorption process need to be used Steam Heating, 1 ton of SO of every desorb
2Approximately need the water of about 10 tons of evaporations, if adopt single effect evaporator, need to consume 11 tons of steam, if adopt double effect evaporator, also will consume the steam about 7 tons.Desulphurization cost is high, has just limited applying of this method.
For some oxygen in the flue gas, the situation of the easy oxidation of sodium sulfite, the inventor finds to add the oxidation that high-efficiency anti-oxidant can suppress to press sodium sulphate effectively by great many of experiments, the oxygenation efficiency of sodium sulfite can drop to below 1.5%, thereby greatly reduces alkaline consumption.For former Arbiso process desorb SO
2The time steam consumption high problem, adopted the secondary steam high pressure that 2nd effect evaporator is steamed to heat rear reuse, make the live steam consumption be down to 3 tons of/ton SO
2Below.
Owing to be NO more than the NOx95% in the flue gas, and NO is insoluble in water, is difficult to absorb with absorbent, therefore adopts NO is oxidized to NO
2After use again alkali liquor absorption, thereby reach the purpose of denitration.Utilize ozone O
3The reaction mechanism of oxidation NO is very complicated, still lacks at present further investigation.Key reaction has:
O
3+NO→NO
2+O
2
NO
2+O
3→NO
3+O
2
NO
3+NO
2→2N
2O
5
Use alkali liquor absorption, just can form nitrate.Therefore, remove SO
2After flue gas enter denitrating tower, pass into O in the tower bottom
3Gas, tower top sprays into alkali liquor absorption, and the denitration rate can reach more than 90%.Nitrate crystallizable separating out after being accumulated to finite concentration in the solution after filtration, drying obtains the higher nitrate product of purity, thereby realized the resource of denitrification process.
The exhuast gas desulfurization method of denitration of the said resource of the present invention, it comprises the steps:
(1) flue gas from boiler enters desulfurizing tower from the bottom, and absorbent sprays into from the top of desulfurizing tower, in desulfurizing tower, and absorbent sodium sulfite and SO
2Reaction generates sodium hydrogensulfite.
(2) enter 1st effective evaporator after the rich solution of desulfurizing tower bottom and the lean solution heat exchange from multi-effect evaporator in the step (1), after the heating vaporization, contain SO
2Gas phase enter 2nd effect evaporator heating; After the compressed machine supercharging of the gas phase of 2nd effect evaporator, enter 1st effective evaporator with fresh steam.
(3) evaporimeter steam condensate (SC) and the SO in the step (2)
2Mixture enters knockout drum, and gas phase can make liquid SO with compressor compresses after condenser condenses
2Product enters storage tank.Liquid then with mix from the lean solution of the second effect by with the rich solution heat exchange after enter desulfurizing tower and recycle.
(4) the cat head flue gas out in the step (1) enters in the denitrating tower, from the O of ozone generator
3Also enter in the denitrating tower, NO is by O in desulfurizing tower
3Be oxidized to NO
2, the denitrfying agent that is sprayed into from denitrating tower top absorbs, and forms nitrate.
When (5) nitrate reached finite concentration in step (4) absorption liquid, the meeting crystallization can obtain the higher nitrate of purity by filtering.
(6) step (5) is filtered the filtrate that obtains and is turned back to denitrating tower top with the denitrfying agent that replenishes.
Wherein, in said desulfurization absorbent sodium sulfite solution, add high-efficiency anti-oxidant, said antioxidant is that said antioxidant concentration is 0.001%～0.5% by a kind of in hydroquinones soluble in water, catechol, resorcinol, tert-butyl catechol, alpha-Naphthol, betanaphthol, p-phenylenediamine (PPD), dimethyl-p-phenylenediamine, sodium thiosulfate, vulcanized sodium, sodium dithionate, the thiourea dioxide or two or more compositions of mixtures.
Said denitrfying agent is a kind of in sodium carbonate, potash, ammonium carbonate, carbonic hydroammonium, sodium acid carbonate, saleratus, NaOH, potassium hydroxide, liquefied ammonia or the ammoniacal liquor.
Said desulfurizing tower is spray column, plate column or packed tower.
Said denitrating tower is spray column, plate column or packed tower.
Adopt technique scheme can obtain liquid SO
2, desulfurization degree can reach more than 96%, and the denitration rate can reach more than 90%, and nitrate content is more than 96%.
Description of drawings
Fig. 1 is the exhuast gas desulfurization method of denitration schematic flow sheet from resource.
The part symbol description is as follows among Fig. 1:
The 3-desulfurizing tower, the 5-ozone generator, the 7-denitrating tower, 11-filter, 17-poor rich liquid heat exchanger, 23-the first single-effect evaporator, 26-the first effect gas-liquid separator, 30-the second single-effect evaporator, 36-the second effect gas-liquid separator, 40-condensate liquid gas-liquid separator, 44-SO
2Gas condenser, 48-liquid SO
2Storage tank.
The specific embodiment
Referring to accompanying drawing 1, the present invention is achieved in that
From the flue gas of boiler fan from managing 1 bottom that enters desulfurizing tower 3, from lean solution-sodium sulfite (containing a small amount of sodium hydrogensulfite) absorption liquid (containing antioxidant) of rich or poor heat exchanger 17 from managing 2 tops that enter desulfurizing tower 3.Rich solution-the solution of sodium bisulfite of desulfurizing tower 3 bottoms (containing a small amount of sodium sulfite) enters heat exchanger 17 from managing 16, by from be from managing 24 live steam and from the indirect steam of compressor 38 from managing 18 thermals source that enter the first single-effect evaporator 23, the first single-effect evaporators 23 through pump 21 after the heating of pipe 19 lean solution.After rich solution is vaporized by 23 heating of the first single-effect evaporator, enter the first effect gas-liquid separator 26, gas phase enters the second single-effect evaporator 30 from managing 27 as thermal source, the liquid major part then enters the first single-effect evaporator 23 from managing 28 through pump 21 circulation, and a part of liquid enters the second single-effect evaporator 30 through pump 32 from managing 29.Condensate liquid in the first single-effect evaporator 23 enters the condensate liquid gas-liquid separator 40 from managing 34.After rich solution in the second single-effect evaporator 30 is vaporized, gas enters the second effect gas-liquid separator 36 from managing 31, after gas-liquid separation, gas phase enters the first single-effect evaporator 23 from managing 37 compressed machines 38, the liquid major part then enters the second single-effect evaporator 30 through pump 32 circulation from managing 42, and a part of liquid is extracted out through pump 20 from managing 39 as lean solution.Condensate liquid in the second single-effect evaporator 30 enters the condensate liquid gas-liquid separator 40 gas phase SO from managing 35
2From manage 43 enter condenser 44 condensers after, be compressed into liquid SO from managing 45 by compressor 46
2, enter the storage tank 48 from managing 47.Liquid in the condensate liquid gas-liquid separator 40 from manage 41 with mix from pipe 39 liquid, extract out through pump 20.
Through removing SO
2Flue gas from the top of desulfurizing tower 3 out, from managing 4 bottoms that enter denitrating tower 7, from the O of ozone generator 5
3Enter pipe 4 from managing 6, the denitrfying agent of circulation enters the top of denitrating tower 7 from managing 15 with being mixed from pipe 9 additional denitrfying agent.Inner at denitrating tower, NO is oxidized to NO
2And N
2O
5, it is soluble in water to be absorbed formation nitrate by denitrfying agent, when nitrate concentration reaches one regularly, can crystallization, enter filter 11 and carry out Separation of Solid and Liquid from the bottom of denitrating tower 7 from managing 10, solid is discharged by pipe 12, and drying can get the nitrate product of purity more than 95%.Filtrate from manage 13 by pump 14 through managing 15 tops that pump into denitrating tower 7, recycle.Through the flue gas after the denitration from the top of denitrating tower from managing 8 chimneys that enter boiler.
Contain like this SO
2Obtain improvement with the flue gas of NOx, reclaimed liquid SO
2, the nitrate product, becoming useless is the mixture of single useful products rather than sulphur and nitrogen, has realized the value maximization of exhuast gas desulfurization denitration resource process, greatly reduces the desulphurization denitration expense.
To originally being further elaborated, its purpose only is better to understand content of the present invention below by embodiment.Therefore, the cited case does not limit protection scope of the present invention:
Embodiment 1
Flue gas condition: 15000Nm
3/ h, SO
2Concentration 2000ppm (5714mg/Nm
3), NO concentration 460ppm (616mg/Nm
3), 150 ℃ of temperature.
Absorption liquid (lean solution) forms: sodium sulfite 16.78%, sodium hydrogensulfite 11.45%, antioxidant hydroquinones 0.03%, vulcanized sodium 0.02%.
Flue gas enters desulfurizing tower (desulfurizing tower is the plate ripple arranged packing tower), and lean solution sprays in the tower from tower top, and flow is 2t/h.Through after the desulfurization, the rich solution at the bottom of the desulfurization Tata consists of: sodium sulfite 8.69%, sodium hydrogensulfite 23.37%.SO in the flue gas of tower top outlet
2Content is 190mg/Nm
3, desulfurization degree is 96.6%.
Rich solution discharges SO after the 2nd effect evaporator desorb
2, after condensation, compression, obtain liquid SO
282.8kg/h.Solution after the desorb is lean solution, forms the same.
Remove SO
2After flue gas enter denitrating tower, denitrating tower is spray column, has produced the O of 14.8kg/h from ozone generator
3Enter in the flue gas, spray into 5% ammonia spirit 500kg/h from the top of denitrating tower.Through after the denitration, NO concentration is 49mg/Nm from the flue gas of denitrating tower tower top discharge
3, the denitration rate is 92%.After the ammonium nitrate that produces is accumulated to finite concentration, dry after filtration from denitrating tower tower reactor crystallization, obtain ammonium nitrate 23.4kg/h, content 96.5%.
Embodiment 2
Flue gas condition: 54200Nm
3/ h, SO
2Concentration 1560ppm (4457mg/Nm
3), NO concentration 650ppm (875mg/Nm
3), 140 ℃ of temperature.
Absorption liquid (lean solution) forms: sodium sulfite 13.58%, sodium hydrogensulfite 5.6%, antioxidant dimethyl-p-phenylenediamine 0.01%, sodium dithionate 0.03%.
Flue gas enters desulfurizing tower (desulfurizing tower spray column), and lean solution sprays in the tower from tower top, and flow is 5.5t/h.Through after the desulfurization, the rich solution at the bottom of the desulfurization Tata consists of: sodium sulfite 5.6%, sodium hydrogensulfite 24.96%.SO in the flue gas of tower top outlet
2Content is 89mg/Nm
3, desulfurization degree is 98.0%.
Rich solution discharges SO after the 2nd effect evaporator desorb
2, after condensation, compression, obtain liquid SO
2236kg/h.Solution after the desorb is lean solution.
Remove SO
2After flue gas enter denitrating tower, denitrating tower is the guide float-valve tower, in-built 3 blocks of column plates have produced the O of 84.7kg/h from ozone generator
3Enter in the flue gas, spray into 5%KOH solution 2600kg/h from the top of denitrating tower.Through after the denitration, NO concentration is 61.2mg/Nm from the flue gas of denitrating tower tower top discharge
3, the denitration rate is 93.0%.After the potassium nitrate that produces is accumulated to finite concentration, dry after filtration from denitrating tower tower reactor crystallization, obtain potassium nitrate product 148.6kg/h, content 97.5%.
Claims (8)
1. the flue gas desulfurization and denitration method of a resource is characterized in that, the method comprises the steps:
(1) will contain SO
2Enter desulfurizing tower with the flue gas of NOx, in desulfurizing tower, contact with desulfurizing agent;
(2) desulfurizing agent that obtains in the step (1) is carried out desorb through multi-effect evaporator, the secondary steam high pressure of 2nd effect evaporator heats rear reuse;
(3) SO that desorb in the step (2) is obtained
2Gas is compressed into liquid SO after the condensation drying
2
(4) flue gas through desulfurization enters denitrating tower in the step (1), sprays into ozone, and flue gas contacts with the denitrfying agent that cat head gets off;
(5) after the nitrate in step (4) solution reaches finite concentration, separate out from the denitrating tower intercrystalline, after filtration, after the drying, obtain the higher nitrate product of purity.
2. the method for claim 1 is characterized in that, wherein said desulfurizing agent is comprised of the aqueous solution of sodium sulfite, niter cake and high-efficiency anti-oxidant.
3. method as claimed in claim 2, it is characterized in that wherein said high-efficiency anti-oxidant is by a kind of in p-phenylenediamine (PPD) soluble in water, dimethyl-p-phenylenediamine, sodium thiosulfate, vulcanized sodium, sodium dithionate, the thiourea dioxide or two or more compositions of mixtures.
4. method as claimed in claim 2 is characterized in that, wherein said antioxidant concentration is 0.001%～0.5%.
5. the method for claim 1 is characterized in that, wherein said ozone amount is 0.5～1.5 times of NO molal quantity.
6. the method for claim 1 is characterized in that, wherein said denitrfying agent is a kind of of sodium carbonate, potash, ammonium carbonate, carbonic hydroammonium, sodium acid carbonate, saleratus.
7. the method for claim 1 is characterized in that, wherein said desulfurizing tower is spray column, plate column or packed tower.
8. the method for claim 1 is characterized in that, wherein said denitrating tower is spray column, plate column or packed tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102242191A CN101879404B (en) | 2010-07-12 | 2010-07-12 | Recycled flue gas desulfurization and denitration method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102242191A CN101879404B (en) | 2010-07-12 | 2010-07-12 | Recycled flue gas desulfurization and denitration method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101879404A CN101879404A (en) | 2010-11-10 |
| CN101879404B true CN101879404B (en) | 2013-01-30 |
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| CN111330426A (en) * | 2020-03-09 | 2020-06-26 | 傅岚 | Medium-low temperature denitration agent and preparation method thereof |
| CN111514694A (en) * | 2020-04-29 | 2020-08-11 | 中国建材国际工程集团有限公司 | Glass flue gas recovery method |
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