CN102160960A - Soda wet desulphurization process and system for sintering flue gas - Google Patents
Soda wet desulphurization process and system for sintering flue gas Download PDFInfo
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- CN102160960A CN102160960A CN2011100459112A CN201110045911A CN102160960A CN 102160960 A CN102160960 A CN 102160960A CN 2011100459112 A CN2011100459112 A CN 2011100459112A CN 201110045911 A CN201110045911 A CN 201110045911A CN 102160960 A CN102160960 A CN 102160960A
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Abstract
The invention discloses a soda wet desulphurization process and a soda wet desulphurization system for sintering flue gas, and solves the problems of severe pollution and the like in the prior art. Sodium carbonate serves as a desulfurizing agent, and a desulfurization by-product is sodium sulfite; and the process comprises the following steps of: (1) cooling and introducing sulfur-containing flue gas into a desulfurizing tower; and (2) purifying the sulfur-containing flue gas in the step (1) in the desulfurizing tower by taking solution of sodium carbonate or sodium hydroxide as an absorbent, demisting the purified flue gas through a demister and discharging. The process is simple in procedures, high in desulphurization efficiency, high in response speed and high in value of the desulfurization by-product, and saves energy and land.
Description
Technical field
The present invention relates to a kind of wet desulfurizing process of industrial smelting industry smoke treatment, relate in particular to a kind of wet desulfurizing process at the high-temperature flue gas that produces in the agglomerates of sintered pellets production process.
Background technology
At present, China's steel industry sintering (pelletizing) smoke components complexity, fluctuation is bigger, has following characteristics: the one, exhaust gas volumn is big, and one ton of sintering deposit produces flue gas at 4000-6000m3; The 2nd, sulfur dioxide concentration changes greatly, and scope is between 400-5000mg/Nm3; The 3rd, variations in temperature is big, is generally 80 ℃ to 180 ℃; The 4th, changes in flow rate is big, and amplitude of variation is up to more than 40%; The 5th, moisture is big and unstable, is generally 10-13%; The 6th, the oxygen content height is generally 15～18%; The 7th, contain multiple pollution composition, except that containing sulfur dioxide, dust, also contain heavy metal, dioxin, nitrogen oxide etc.These characteristics have all increased the difficulty that the steel sintering SO 2 from fume is administered to a certain extent.Main problem is at present: the first, lack ripe sintering desulfuration technology.The sulfur removal technology that the sintered flue gas desulfurization device that has put into operation at present adopts mainly contains recirculating fluidized bed method, ammonia-ammonium sulfate method, dense-phase tower method, limestone-gypsum method etc., these technologies are in research and development and trial period in China, the practical sulphur removal effect remains further to be verified and assessment.The second, accessory substance utilizes approach few.Thoroughly solve the sinter fume pollution problem, not only will realize the flue gas high-efficiency desulfurization, what also will solve accessory substance effectively utilizes problem.Because the accessory substance complicated component that sintering flue gas desulfurization produces also lacks the approach that effectively utilizes at present.Three, the desulfurizer investment is big, operating cost is high.The sintering desulfuration plant investment accounts for 20%～50% of sintering machine investment, 5～14 yuan of ton sintering deposit desulfurization operation costs.Investment is big, the operating cost height is the key factor that desulfurizer is installed in restriction.
Summary of the invention
In order to overcome above-mentioned defective, it is high to the object of the present invention is to provide a kind of reduced investment, desulfurizing byproduct to be worth, the soda wet desulfurizing process and the system of the sinter fume that operating cost is low, desulfuration efficiency is high.
In order to achieve the above object, soda method sulfur removal technology of the present invention may further comprise the steps:
1. sulfur-containing smoke gas enters desulfurizing tower 1 after lowering the temperature through dedusting;
2. in desulfurizing tower 1 inner absorbent sodium carbonate liquor (initial absorption), sodium sulfite solution (end and absorb) reaction, flue gas after being purified is discharged after demister 2 demists;
3. absorb the solution of sodium bisulfite obtain in and still 6 adds caustic soda or soda ash solution reacts, make sodium hydrogensulfite all be converted into sodium sulfite; Remove heavy metal simultaneously.
4. the sodium sulfite solution of removing impurity by decontamination device 7 carries out evaporation and concentration in concentration kettle 9, is heated to boiling with indirect steam, and temperature is controlled at 95～100 ℃, treats that mass crystallization is separated out just can emit, and the crystal of emitting is through centrifuge 10 dehydrations.Behind centrifuge dewatering, directly contact through the ebullated dryer hot-air again and obtain product.The crystallization water behind the centrifugal drying enters mother liquor tank 11 and sends into choline groove 12 for configuration absorbent solution usefulness.
This technology absorbent is a sodium carbonate, and desulfurizing byproduct is an anhydrous sodium sulfite.Initial Na
2CO
3The solution concentration mass percent is 5%-25%, and the oxygen in the flue gas is Na
2CO
3Be oxidized to Na
2CO
4, add p-phenylenediamine (PPD) as antioxidant.
When the solution after the absorption reaches 4～7.5 when the absorption liquid pH value, send to neutralization.Neutral temperature should be controlled at 38～60 ℃, and the pH=7 of solution adds an amount of caustic soda neutralization then, and temperature can be brought up to 100-110 ℃, and the pH=11 of solution～12 its objective is that the heavy metal of removing part can improve the concentration of sodium sulfite solution simultaneously.Carry out Separation of Solid and Liquid, impurity such as heavy metal are unified to be handled, and liquid enters next step evaporative crystallization.
The sodium sulfite solution of removing impurity concentrates, and is heated to boiling with indirect steam, and temperature should be controlled at 80～120 ℃, treat just can emit after mass crystallization is separated out, the crystal of emitting directly contacts with hot-air through ebullated dryer behind centrifuge dewatering again, obtains the anhydrous sodium sulfite crystallization.
A kind of soda wet desulfurizing process system that is used for sinter fume, comprise the absorption tower that is provided with gas feed and liquid import and export, described absorption tower liquid-inlet is connected with the choline groove, described absorption tower connects demister, liquid outlet connect successively the absorption liquid basin, in and still, press filtration pump, plate and frame filter press, neutralizer basin, concentration kettle, centrifuge, the centrifuge solid outlet connects belt conveyor, feeding machine, packing machine, deduster, sack cleaner and oven dry air-introduced machine successively, and the centrifuge liquid outlet connects mother liquor tank and choline groove successively.
Above-mentioned process and system have the following advantages:
1, operation of the present invention is simple, desulfuration efficiency is high.In the present invention, among the present invention, absorption liquid is a solution state, and absorbent becomes ionic condition, and desulfuration efficiency is easy to reach more than 95%.
2, the present invention can energy efficient.In the present invention, liquid-gas ratio is littler than conventional wet liquid-gas ratio, can reduce the flow of circulating pump, thereby cut down the consumption of energy.The resistance of same reason fume side also is far smaller than conventional wet, thereby reduces the energy consumption of booster fan, not even with increasing booster fan, just can satisfy the pressure loss of desulfurizer substantially by the overbottom pressure of main exhauster in sintering machine or pelletizing desulfurization.
3, the present invention saves occupation of land.In the present invention, absorption process belongs to reaction between ions, and reaction speed is fast, can shorten the reaction time, reduces the desulfurizing tower height, reduces the desulfurizing tower warp, thereby saves the area.
4, desulfurizing byproduct is worth high.Among the present invention, product sodium sulfite purity is sent out in desulfurization can reach 96%, is mainly used in printing and dyeing industry as deoxidier and bleaching agent, is used for the boiling-off of various baftas, and can prevent cotton fiber localization and influence fibre strength, and the whiteness of raising boiling-off thing.Sensitization industry is as developer.Organic industry is as m-phenylene diamine (MPD), 2, and the reducing agent that 5-dichloro pyrazolone, anthraquinone-1-sulfonic acid, 1-amino anthraquinones, paramisan sodium etc. are produced can prevent half-finished oxidation in the course of reaction.Paper industry is as the delignification agent.Textile industry is as the stabilizing agent of staple fibre.Electronics industry is used to make photo resistance.Water treatment industry is used for the processing of electroplating wastewater, drinking water.Purposes is wide, is worth high.
Description of drawings
Fig. 1 is the concrete arrangement schematic diagram of sintering soda method sulfur removal technology of the present invention.
The specific embodiment
The present invention is described in more detail below in conjunction with drawings and Examples.
As shown in Figure 1, soda method sulfur removal technology of the present invention may further comprise the steps:
1. sulfur-containing smoke gas enters desulfurizing tower 1 after lowering the temperature through dedusting;
2. in desulfurizing tower 1 inner absorbent sodium carbonate liquor (initial absorption), sodium sulfite solution (end and absorb) reaction, flue gas after being purified is discharged after demister 2 demists;
3. absorb that the solution of sodium bisulfite obtain adds caustic soda or soda ash solution reacts, make sodium hydrogensulfite all be converted into sodium sulfite; Remove heavy metal simultaneously.
4. the sodium sulfite solution of removing impurity carries out evaporation and concentration, is heated to boiling with indirect steam, and temperature is controlled at 95～100 ℃, treats that mass crystallization is separated out just can emit, and the crystal of emitting is through centrifuge dewatering.Behind centrifuge dewatering, directly contact through the ebullated dryer hot-air again and obtain product.
Absorbent is a sodium carbonate, and desulfurizing byproduct is an anhydrous sodium sulfite.Initial Na2CO3 solution concentration mass percent is 5%-25%, and the oxygen in flue gas is oxidized to Na2CO4 to Na2CO3, adds p-phenylenediamine (PPD) as antioxidant.When the solution after the absorption reaches 4～7.5 when the absorption liquid pH value. send to neutralization.Neutral temperature should be controlled at 38～60 ℃, and the pH=7 of solution adds an amount of caustic soda neutralization then, and temperature can be brought up to 100-110 ℃, the pH=11 of solution～12, and what it was sweet is to remove the concentration that heavy metal partly can improve simultaneously sodium sulfite solution.Carry out Separation of Solid and Liquid, impurity such as heavy metal are unified to be handled, and liquid enters next step evaporative crystallization.The sodium sulfite solution of removing impurity concentrates, be heated to boiling with indirect steam, temperature should be controlled at 80～120 ℃. treats just can emit after mass crystallization is separated out, the crystal of emitting is after centrifuge 10 dehydrations, directly contact with hot-air through ebullated dryer again, obtain the sodium sulfite product, this product is packed through belt conveyor 13 and feeding machine 14, deduster, sack cleaner 16, oven dry air-introduced machine 17 and packing machine 15.The crystallization water behind the centrifugal drying enters mother liquor tank 11 and sends into choline groove 12 for configuration absorbent solution usefulness.
A kind of soda wet desulfurizing process system that is used for sinter fume, comprise the absorption tower 1 that is provided with gas feed and liquid import and export, described absorption tower liquid-inlet is connected with choline groove 12, described absorption tower connects demister 2, liquid outlet connect successively the absorption liquid basin, in and still, press filtration pump, plate and frame filter press, neutralizer basin, concentration kettle, centrifuge, the centrifuge solid outlet connects belt conveyor, feeding machine, packing machine, deduster, sack cleaner and oven dry air-introduced machine successively, and the centrifuge liquid outlet connects mother liquor tank and choline groove successively.
Embodiment 1, produce 300000 tons of pelletizing plants per year at certain, raw flue gas parameter such as following table:
| Project | Unit | Data |
| The exhaust gas volumn that enters | ||
| Mark condition flue gas flow | Nm3/h | 77446 |
| The operating mode exhaust gas volumn | m3/h | 120000 |
| SO2 concentration | mg/Nm3 | 1500～2000 |
| Flue-gas temperature | ℃ | 120-200 |
| Dust concentration | mg/Nm3 | ≤100 |
| Exhaust gas temperature | ℃ | 55 |
After adopting the present invention, about 4,000,000 yuan of gross investment can be produced the about 2000t of sodium sulfite per year, by 3000 yuan of calculating per ton, deducts the fee, and a year profit can reach 4,000,000 yuan.
The present invention is not limited to above-mentioned embodiment, no matter do any variation on its shape or structure, every to utilize above-mentioned sintering soda method sulfur removal technology all be a kind of distortion of the present invention, all should think and drop within the protection domain of the present invention.
Claims (10)
1. the soda wet desulfurizing process of a sinter fume is characterized in that: adopt sodium carbonate as desulfurizing agent, desulfurizing byproduct is the sodium sulfite powder, and this technology may further comprise the steps:
1. sulfur-containing smoke gas enters desulfurizing tower (1) after lowering the temperature;
2. the sulfur-containing smoke gas of step in 1. purified as absorbent with sodium carbonate liquor or sodium hydroxide solution in desulfurizing tower (1), flue gas after being purified is discharged after demister (2) demist.
2. the soda wet desulfurizing process of sinter fume according to claim 1 is characterized in that: adopt Na
2CO
3Solution or sodium hydroxide solution are done initial absorption liquid, and initial absorption liquid absorbs the SO in the flue gas
2After, change Na into
2SO
3Solution uses as absorbent.
3. the soda wet desulfurizing process of sinter fume according to claim 2 is characterized in that: described Na
2CO
3The solution concentration mass percent is 5%-40%, adds p-phenylenediamine (PPD) as antioxidant.
4. the soda wet desulfurizing process of sinter fume according to claim 3, it is characterized in that: described step in 2. sodium carbonate liquor and the sulfur-containing smoke gas reaction after the solution of sodium bisulfite that obtains in and add caustic soda in the still (6) or soda ash solution carries out neutralization reaction, make sodium hydrogensulfite all be converted into sodium sulfite; Remove beavy metal impurity simultaneously.
5. the soda wet desulfurizing process of sinter fume according to claim 4, it is characterized in that: solution of sodium bisulfite pH value reaches at 4～7.5 o'clock and carries out neutralization reaction; The temperature of neutralization reaction is controlled at 38～60 ℃, and pH value of solution=7 o'clock add an amount of caustic soda neutralization, and temperature is brought up to 100-110 ℃, and the concentration that heavy metal improves sodium sulfite solution is simultaneously removed in pH value of solution=11～12 o'clock; Carry out Separation of Solid and Liquid, this beavy metal impurity is unified to handle, liquid enters next step evaporative crystallization.
6. the soda wet desulfurizing process of sinter fume according to claim 5, it is characterized in that: the sodium sulfite solution of removing impurity concentrates, be heated to boiling with indirect steam, temperature should be controlled at 80～120 ℃. treats just to emit after mass crystallization is separated out, the crystal of emitting is behind centrifuge dewatering, directly contact with hot-air through ebullated dryer again, obtain the anhydrous sodium sulfite crystallization.
7. the soda method sulfur removal technology of sinter fume according to claim 6, it is characterized in that: the sodium sulfite solution of removing impurity by decontamination device (7) enters concentration kettle (9) and carries out evaporation and concentration, be heated to boiling with indirect steam, temperature is controlled at 95～100 ℃, treat to emit after mass crystallization is separated out, the crystal of emitting is after centrifuge (10) dehydration, and directly contacting the desulfurizing byproduct that obtains through the ebullated dryer hot-air again is the anhydrous sodium sulfite crystallization.
8. the soda method sulfur removal technology of sinter fume according to claim 7 is characterized in that: the crystallization water behind the centrifugal drying enters mother liquor tank (11) and sends into choline groove (12) and use for configuration absorbent solution.
9. according to the soda method sulfur removal technology of the arbitrary described sinter fume of claim 1-8, it is characterized in that: liquid-gas ratio is controlled between the 0.25-6 in the absorption tower, and desulfuration efficiency is greater than 99%.
10. soda wet desulfurizing process system that is used for sinter fume, it is characterized in that, comprise and be provided with gas feed and liquid advances, the absorption tower of outlet, described absorption tower liquid-inlet is connected with the choline groove, described absorption tower connects demister, liquid outlet connects the absorption liquid basin successively, in and still, the press filtration pump, plate and frame filter press, the neutralizer basin, concentration kettle, centrifuge, the centrifuge solid outlet connects belt conveyor successively, feeding machine, packing machine, deduster, sack cleaner and oven dry air-introduced machine, the centrifuge liquid outlet connects mother liquor tank and choline groove successively.
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Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102380306A (en) * | 2011-10-18 | 2012-03-21 | 中钢集团天澄环保科技股份有限公司 | Flue gas desulfurization tower adopting sodium-alkaline method |
| CN103877840A (en) * | 2014-03-14 | 2014-06-25 | 成都华西堂投资有限公司 | Integral purification process of pollutants in sintering flue gas |
| CN104402162A (en) * | 2014-12-02 | 2015-03-11 | 成都华西堂投资有限公司 | Heat pump evaporation system for recycling flue gas purification byproducts |
| CN104437046A (en) * | 2014-10-29 | 2015-03-25 | 上海大学 | Catalytic cracking flue gas desulfurization and dust removal process and desulfurization and dust removal device |
| CN104941421A (en) * | 2014-03-28 | 2015-09-30 | 曼恩柴油机涡轮股份公司曼恩柴油机涡轮德国分公司 | Internal combustion engine, and method of removing sulphur oxides from exhaust gas |
| CN103961995B (en) * | 2014-05-22 | 2016-01-13 | 天津理工大学 | A kind of coal-fired flue-gas alkali desulphurization produces the method for high-purity sodium sulfite and sodium sulphate |
| CN106139848A (en) * | 2016-08-02 | 2016-11-23 | 成都华西堂环保科技有限公司 | A kind of flue gas pollutant purifies technique |
| CN106178819A (en) * | 2016-08-22 | 2016-12-07 | 朱双跃 | Activated coke desulfurization denitration by-product reforming unit and system for desulfuration and denitration and method |
| CN106215683A (en) * | 2016-08-29 | 2016-12-14 | 重庆合川盐化工业有限公司 | A kind of sulfur method of burning in circulating fluid bed boiler flue gas |
| CN108557777A (en) * | 2018-03-13 | 2018-09-21 | 杨奕颉 | A kind of production technology of sodium sulfite |
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN109970082A (en) * | 2019-05-06 | 2019-07-05 | 黄石加柯环保科技有限公司 | A method of high-pure anhydrous sodium sulfite is prepared using relieving haperacidity flue gas |
| CN110028085A (en) * | 2019-04-23 | 2019-07-19 | 鞍钢集团工程技术有限公司 | A kind of technique and system for producing anhydrous sodium sulphate using Desulphurization |
| CN110252761A (en) * | 2019-04-10 | 2019-09-20 | 水口山有色金属有限责任公司 | A method of the harmless treatment of waste residue containing beryllium |
| CN110833736A (en) * | 2019-11-26 | 2020-02-25 | 江西晶昊盐化有限公司 | Parallel pretreatment type two-stage wet dust removal method and application thereof |
| CN111777083A (en) * | 2020-07-21 | 2020-10-16 | 中钢集团天澄环保科技股份有限公司 | Reaction crystallization process for extracting sodium sulfite product by sodium desulfurization post-treatment |
| CN112093811A (en) * | 2020-09-27 | 2020-12-18 | 山东兴达化工有限公司 | Sodium sulfite production method |
| CN112939028A (en) * | 2020-11-03 | 2021-06-11 | 宣城市楷昂化工有限公司 | Preparation method of sodium sulfite |
| WO2021114563A1 (en) * | 2019-12-13 | 2021-06-17 | 南京杰科丰环保技术装备研究院有限公司 | Flue gas desulfurization system and method |
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| CN102380306A (en) * | 2011-10-18 | 2012-03-21 | 中钢集团天澄环保科技股份有限公司 | Flue gas desulfurization tower adopting sodium-alkaline method |
| CN103877840A (en) * | 2014-03-14 | 2014-06-25 | 成都华西堂投资有限公司 | Integral purification process of pollutants in sintering flue gas |
| CN104941421A (en) * | 2014-03-28 | 2015-09-30 | 曼恩柴油机涡轮股份公司曼恩柴油机涡轮德国分公司 | Internal combustion engine, and method of removing sulphur oxides from exhaust gas |
| CN104941421B (en) * | 2014-03-28 | 2020-01-17 | 曼恩柴油机涡轮股份公司曼恩柴油机涡轮德国分公司 | Internal combustion engine and method for removing sulfur oxides from exhaust gas |
| CN103961995B (en) * | 2014-05-22 | 2016-01-13 | 天津理工大学 | A kind of coal-fired flue-gas alkali desulphurization produces the method for high-purity sodium sulfite and sodium sulphate |
| CN104437046A (en) * | 2014-10-29 | 2015-03-25 | 上海大学 | Catalytic cracking flue gas desulfurization and dust removal process and desulfurization and dust removal device |
| CN104402162B (en) * | 2014-12-02 | 2016-06-08 | 成都华西堂投资有限公司 | A kind of thermo-compression evaporation system of recycling gas cleaning accessory substance |
| CN104402162A (en) * | 2014-12-02 | 2015-03-11 | 成都华西堂投资有限公司 | Heat pump evaporation system for recycling flue gas purification byproducts |
| CN106139848A (en) * | 2016-08-02 | 2016-11-23 | 成都华西堂环保科技有限公司 | A kind of flue gas pollutant purifies technique |
| CN106178819A (en) * | 2016-08-22 | 2016-12-07 | 朱双跃 | Activated coke desulfurization denitration by-product reforming unit and system for desulfuration and denitration and method |
| CN106215683A (en) * | 2016-08-29 | 2016-12-14 | 重庆合川盐化工业有限公司 | A kind of sulfur method of burning in circulating fluid bed boiler flue gas |
| CN108557777A (en) * | 2018-03-13 | 2018-09-21 | 杨奕颉 | A kind of production technology of sodium sulfite |
| CN108744907A (en) * | 2018-06-27 | 2018-11-06 | 湖北鼎创泰裕科技有限公司 | A kind of exhaust gas treating method and processing unit containing sulfur dioxide |
| CN110252761A (en) * | 2019-04-10 | 2019-09-20 | 水口山有色金属有限责任公司 | A method of the harmless treatment of waste residue containing beryllium |
| CN110028085A (en) * | 2019-04-23 | 2019-07-19 | 鞍钢集团工程技术有限公司 | A kind of technique and system for producing anhydrous sodium sulphate using Desulphurization |
| CN109970082A (en) * | 2019-05-06 | 2019-07-05 | 黄石加柯环保科技有限公司 | A method of high-pure anhydrous sodium sulfite is prepared using relieving haperacidity flue gas |
| CN110833736A (en) * | 2019-11-26 | 2020-02-25 | 江西晶昊盐化有限公司 | Parallel pretreatment type two-stage wet dust removal method and application thereof |
| WO2021114563A1 (en) * | 2019-12-13 | 2021-06-17 | 南京杰科丰环保技术装备研究院有限公司 | Flue gas desulfurization system and method |
| CN111777083A (en) * | 2020-07-21 | 2020-10-16 | 中钢集团天澄环保科技股份有限公司 | Reaction crystallization process for extracting sodium sulfite product by sodium desulfurization post-treatment |
| CN112093811A (en) * | 2020-09-27 | 2020-12-18 | 山东兴达化工有限公司 | Sodium sulfite production method |
| CN112939028A (en) * | 2020-11-03 | 2021-06-11 | 宣城市楷昂化工有限公司 | Preparation method of sodium sulfite |
| CN112939028B (en) * | 2020-11-03 | 2023-05-26 | 宣城市楷昂化工有限公司 | Preparation method of sodium sulfite |
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Application publication date: 20110824 |