CN101862589A - Desulfurization process for sintering flue gas - Google Patents
Desulfurization process for sintering flue gas Download PDFInfo
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- CN101862589A CN101862589A CN 201010215508 CN201010215508A CN101862589A CN 101862589 A CN101862589 A CN 101862589A CN 201010215508 CN201010215508 CN 201010215508 CN 201010215508 A CN201010215508 A CN 201010215508A CN 101862589 A CN101862589 A CN 101862589A
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- desulfurizing agent
- sodium carbonate
- flue gas
- desulfurizing
- desulfurization
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Abstract
The invention discloses a desulfurization process for sintering flue gas, which comprises a desulfurizing agent preparation system, a desulfurization system and a recycling and processing system; and the desulfurizing agent is of sodium carbonate fine powder with the passing rate not less than 75 percent of the 0.045mm standard sieve. Compared with the prior art, the invention has the advantages that the processing cost is lower tan the cost of slaked lime by more than 30 percent; the prepared solid desulfurizing agent is not easy to metamorphosize, and has longer storage life than calvital; the efficiency of desulfurization is improved and the operating cost is reduced; the operating procedure is simplified; the by-product of the desulfurization can be convenient to process and recycle, the produced mixture of calcium sulfate, calcium sulfite and calcium carbonate can be conveniently used for producing the environment-friendly building materials such as light building blocks and the like, and the by-product is easier to recycle and use than the currently-produced desulphurizing by-product, thus reducing the discharge of the solid waste and the follow-up handling cost at maximum, and meeting the current environmental protection policy.
Description
Technical field
The invention belongs to the desulfurization worker technology of sinter fume, belong to the sulfur removal technology of sintering flue gas of semidry-method recirculating fluidized bed especially.
Background technology
The main character of steel works sintering flue gas and composition are SO
2600-4800mg/m
3, a spot of sulfur trioxide, dust-laden 100-450mg/m
3, water capacity 7%-15%, 85 ℃-190 ℃ of temperature, exhaust gas volumn is greater than 20 * 10
4m
3/ hour.Even at same emission point, SO in the flue gas
2Content also might have than great fluctuation process in the different time periods.Circulating fluid bed semi-drying method technology is more advanced sulfur removal technology, system introduces projects from VAI, mainly form by desulfurizing agent preparation system, desulphurization system, dust collecting system, use the calcium hydroxide micro mist of high-ratio surface to make desulfurizing agent, in the digestion process of lime, in order to increase the specific area of calcium hydroxide micro mist, used triethanolamine, the diethylene glycol class chemicals of some.According to former design parameter, under present market condition, calcium hydroxide is made the production cost of desulfurizing agent above 1000 yuan/ton.In service, the reactivity of desulfurizing agent is lower, only is about 50%; And the accessory substance complex chemical composition after the desulfurization: classical group becomes calcium sulfite 20-31%, calcium sulfate 8-15%, and calcium hydroxide 15-30% reclaims difficulty, and as doing landfill disposal by trade waste, cost is very high, both land occupation, secondary pollution environment again.
Summary of the invention
Technical problem to be solved by this invention provides the sulfur removal technology of the sinter fume that a kind of cost is low, accessory substance is easy to reclaim.
The technical scheme of technical solution problem of the present invention is: the sulfur removal technology of sinter fume, comprise desulfurizing agent preparation system, desulphurization system, recovery and processing system, described desulfurizing agent is that the percent of pass of 0.045mm standard screen is not less than 75% sodium carbonate, dust following in the desulfurizing tower of sodium carbonate micro mist in desulphurization system, powdered granule fully contacts with flue gas, sodium carbonate and acidic gas in flue gas generation neutralization reaction reduce flue gas sulphur oxide concentration.
After the content (weight) of sodium carbonate residual in the desulfurizing agent was less than 15%, desulfurizing byproduct was mainly sodium sulphate, sodium sulfite, sodium carbonate, desulfurizing byproduct is discharged desulphurization system entered recovery and processing system this moment.
Described recovery and processing system is: saturated solution (room temperature 25 ℃ time, solution concentration 30%-35%) made in desulfurizing byproduct water dissolving, carried out the gypsification reaction, generate soda bath with excessive milk of lime, and the isolated by filtration post precipitation, filtrate is NaOH; The sodium hydroxide solution that generates is put into sieve-plate tower, regenerate the NaHCO of generation with the carbon dioxide in the flue gas
3Because solubility is little at normal temperatures, precipitated crystal is separated out, and separates after filtration, and drying obtains the sodium acid carbonate of solid powdery; Sodium acid carbonate is being heated more than 270 ℃, decomposition reaction will take place, obtaining sodium carbonate, with the sodium carbonate that recovery and processing system generated, be transported to carry out in the desulfurizing agent preparation system recycling.
Described milk of lime can use the screenings (chemical composition and metallurgical three classes are in full accord, and less because of particle, smelting procedure can't effectively utilize, and the overwhelming majority is done other purposes or discarded) of gained in the metallurgy lime production, thereby this cost is cheaper.
Reaction principle of the present invention is as follows:
The reaction of sodium carbonate and sulfur dioxide in flue gas is:
Na
2CO
3+SO
2+H
2O→NaHSO
3+NaHCO
3
NaHSO
3+Na
2CO
3→Na
2SO
3+NaHCO
3
The reaction of sulfur trioxide is in sodium carbonate and the flue gas:
Na
2CO
3+SO
3→NaHSO
4+NaHCO
3
NaHS?O
4+Na
2CO
3→Na
2S?O
4+NaHCO
3
The principle that reclaims reaction is as follows:
Na
2SO
4+Ca(OH)
2→CaSO
4↓+NaOH
Na
2SO
3+Ca(OH)
2→CaSO
3↓+NaOH
Na
2CO
3+Ca(OH)
2→CaCO
3↓+NaOH
2NaOH+CO
2→Na
2CO
3+H
2O
Na
2CO
3+H
2O+CO
2→2NaHCO
3↓
2NaHCO
3→Na
2CO
3+H
2O+CO
2
Among the present invention, sodium carbonate is as alkaline matter, and after sulfur dioxide in flue gas and sulfur trioxide reaction, product is sodium sulfite and sodium sulphate, and when the concentration of sulfur dioxide or sulfur trioxide is low (less than 500ppm time), the reaction speed of sodium carbonate is fast;
At about 100 ℃ and have under the condition that water vapour exists, the speed of above-mentioned reaction is very fast, and in reaction process, gas CO
2During effusion, the particulate of desulfurizing agent sodium carbonate there is pulverization, its specific surface is increased, help the carrying out that reacts.
Because sodium carbonate
The crystalline hydrate molecular formulaBe Na
2CO
310H
2O is with ten crystallizations water, so the sodium carbonate hygroscopicity of powdered form is strong, is easy to slough the steam in the flue gas.
Compare with two alkali doctor treatments of routine, two alkali doctor treatments absorb operations and are to use the alkali lye desulfurization, and this law is use the powdered sodium carbonate powder injection desulphurization, and the advantage of this law is that floor space is little, and is low to the corrosivity of equipment, be not easy leakage.
This law is compared with lime-gypsum method, and outstanding feature is, directly lime-gypsum method is in operation, and equipment easily stops up, corrodes, and the reaction rate of this law is faster than lime-gypsum method.And sodium carbonate is no consumption in reaction, just does recycled material and uses.
The present invention compared with prior art, the cost that processing cost is made calcium hydroxide than quick lime is low more than 30%; The solid desulfurating agent of making is not perishable, and the storage life is longer than calcium hydroxide; Improve the circulating fluid bed semi-drying method desulfuration efficiency, reduce operating cost; Operation simplifies the operation; Accessory substance after the desulfurization can be processed expediently and handle and utilization, the mixture of the calcium sulfate that is produced, calcium sulfite and calcium carbonate, owing to do not contain calcium hydroxide, can be advantageously used in producing environmental-friendly construction materials such as light block, stable and utilize more than present desulfurizing byproduct than being easier to, reduce the discharging and the subsequent treatment expense of solid waste to greatest extent, met current environmental protection policy.
The specific embodiment
Below in conjunction with embodiment the present invention is done detailed explanation.
Embodiment 1:
The sulfur removal technology of sinter fume comprises desulfurizing agent preparation system, desulphurization system, recovery and processing system, and described desulfurizing agent is that the percent of pass of 0.045mm standard screen is not less than 75% sodium carbonate micro mist; Dust following in the desulfurizing tower of sodium carbonate micro mist in desulphurization system, powdered granule fully contacts with flue gas, sodium carbonate and acidic gas in flue gas SO
2And SO
3Neutralization reaction takes place, and flue gas sulphur oxide concentration is reduced.After the content (weight) of sodium carbonate residual in the desulfurizing agent is 15%, this moment, desulfurizing byproduct was mainly sodium sulphate, sodium sulfite, sodium carbonate, sodium sulphate: sodium sulfite: the sodium carbonate weight ratio is 1: 4: 0.8, desulfurizing byproduct is discharged desulphurization system enter recovery and processing system.
Technological parameter is: 134 ℃ of input gas temperatures, flow 12m
3/ min, amount of sulfur contenting in smoke 500ppm, 25 kilograms of the circulation amounts of dusting, 116 ℃ of exit gas temperatures, cycle-index 6 times, outlet flue gas sulfur-bearing 24ppm, desulfurization degree is big by 95%.
Described recovery and processing system is: full solution (room temperature 25 ℃ time, solution concentration 30%-35%) made in desulfurizing byproduct water dissolving, carried out the gypsification reaction, generate soda bath with excessive milk of lime, and the isolated by filtration post precipitation, filtrate is NaOH; The sodium hydroxide solution that generates is put into sieve-plate tower, regenerate the NaHCO of generation with the carbon dioxide in the flue gas
3Because solubility is little at normal temperatures, precipitated crystal is separated out, and separates after filtration, and drying obtains the sodium acid carbonate of solid powdery; 25 kilograms of sodium acid carbonates are being added thermal decomposition more than 270 ℃, decomposition reaction will take place, obtaining 15 kilograms of sodium carbonate, with sodium carbonate that recovery and processing system generated, be transported to carry out in the desulfurizing agent preparation system recycling.
After the present invention used 1 year, its extent of corrosion to equipment was quite little, because the alkalescence of sodium carbonate is stronger, steel surface was had passivation, so its corrosion is little.
Desulfurizing agent of the present invention is compared with the calcium hydroxide of the high-ratio surface that uses at present, and its rate of sulphur expulsion is fast, and the utilization rate height need not can be used present desulphurization plant transformation.
The present invention has two distinguishing features: the one, the powdered lime of iron and steel enterprise's inside low value is fully utilized, and make desulfurizing agent obtain regeneration by reaction and use, can effectively reduce operating cost; The 2nd, the byproduct stability that step for regeneration produces better can easily can be avoided the stocking and storing of trade waste for the production of wall materials such as light blocks, economizes on resources protection of the environment.
Claims (2)
1. the sulfur removal technology of sinter fume comprises desulfurizing agent preparation system, desulphurization system, recovery and processing system, it is characterized in that: described desulfurizing agent is that the percent of pass of 0.045mm standard screen is not less than 75% sodium carbonate micro mist; Dust following in the desulfurizing tower of sodium carbonate micro mist in desulphurization system, powdered granule fully contacts with flue gas, after the content (weight) of sodium carbonate residual in the desulfurizing agent is less than 15%, form the desulfurizing agent accessory substance, desulfurizing byproduct is discharged desulphurization system enter recovery and processing system.
2. the sulfur removal technology of sinter fume according to claim 1, it is characterized in that: described recovery and processing system is: saturated solution is made in desulfurizing byproduct water dissolving, carried out the gypsification reaction with excessive milk of lime, generate soda bath, isolated by filtration post precipitation, filtrate are NaOH;
The sodium hydroxide solution that generates is put into sieve-plate tower, react the NaHCO of generation with the carbon dioxide in the flue gas
3Precipitation is separated sedimentation and filtration, and drying obtains the sodium acid carbonate of solid powdery, and mother liquor liquid recycles;
Sodium acid carbonate heating more than 270 ℃, is obtained sodium carbonate, with the sodium carbonate that recovery and processing system generated, be transported to carry out in the desulfurizing agent preparation system recycling.
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| CN 201010215508 CN101862589A (en) | 2010-06-30 | 2010-06-30 | Desulfurization process for sintering flue gas |
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|---|---|---|---|
| CN 201010215508 CN101862589A (en) | 2010-06-30 | 2010-06-30 | Desulfurization process for sintering flue gas |
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Family
ID=42954629
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104324605A (en) * | 2014-11-13 | 2015-02-04 | 安徽同兴环保工程股份有限公司 | Dry desulfurization agent pretreatment system and pretreatment method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4247525A (en) * | 1978-05-10 | 1981-01-27 | Metallgesellschaft Aktiengesellschaft | Method of and apparatus for removing sulfur oxides from exhaust gases formed by combustion |
| GB2106488A (en) * | 1981-09-18 | 1983-04-13 | Environmental Elements Corp | Process for removal of sulphur oxides from waste gases |
| JPS5884024A (en) * | 1981-11-14 | 1983-05-20 | Ishikawajima Harima Heavy Ind Co Ltd | Method for regenerating soda ash used for soda ash dry type desulfurization method |
| US4481172A (en) * | 1981-09-18 | 1984-11-06 | Environmental Elements Corp. | Process for removal of sulfur oxides from waste gases |
| CN101262930A (en) * | 2005-09-15 | 2008-09-10 | 索尔维化学有限公司 | Method of removing sulfur trioxide from a flue gas stream |
-
2010
- 2010-06-30 CN CN 201010215508 patent/CN101862589A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4247525A (en) * | 1978-05-10 | 1981-01-27 | Metallgesellschaft Aktiengesellschaft | Method of and apparatus for removing sulfur oxides from exhaust gases formed by combustion |
| GB2106488A (en) * | 1981-09-18 | 1983-04-13 | Environmental Elements Corp | Process for removal of sulphur oxides from waste gases |
| US4481172A (en) * | 1981-09-18 | 1984-11-06 | Environmental Elements Corp. | Process for removal of sulfur oxides from waste gases |
| JPS5884024A (en) * | 1981-11-14 | 1983-05-20 | Ishikawajima Harima Heavy Ind Co Ltd | Method for regenerating soda ash used for soda ash dry type desulfurization method |
| CN101262930A (en) * | 2005-09-15 | 2008-09-10 | 索尔维化学有限公司 | Method of removing sulfur trioxide from a flue gas stream |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104324605A (en) * | 2014-11-13 | 2015-02-04 | 安徽同兴环保工程股份有限公司 | Dry desulfurization agent pretreatment system and pretreatment method |
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Application publication date: 20101020 |