CN1211149C - Desulfurizing agent preparing method in circulating fluid dry flue gas desulfurization process - Google Patents
Desulfurizing agent preparing method in circulating fluid dry flue gas desulfurization process Download PDFInfo
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- CN1211149C CN1211149C CN 03125324 CN03125324A CN1211149C CN 1211149 C CN1211149 C CN 1211149C CN 03125324 CN03125324 CN 03125324 CN 03125324 A CN03125324 A CN 03125324A CN 1211149 C CN1211149 C CN 1211149C
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Abstract
The present invention relates to a preparation method of desulfurizing agents in a circulation fluidization dry process flue gas desulfurization technology. The present invention has the characteristic that a two-stage separation device with different separation particle diameter parameters, is adopted, a desulfurizing agent air powder mixture from a digestion reaction tower is separated by a first stage coarse particle separator, and the separated coarse desulfurizing agent particles are put in the digestion reaction tower to continuously and recurrently carry out digestion reaction; the unseparated fine desulfurizing agent particles and off gas are put in a second stage fine particle separator to separate, the separated fine desulfurizing agent particles are put in the desulphurization reaction tower through a warehouse or directly put in the desulphurization reaction tower, and the off gas is directly put in a flue which is near to the inlet position of the desulphurization reaction tower. The method is particularly suitable for the preparation requirements of the large scale dry process flue gas desulfurization system to the desulfurizing agents, and can reduce the volume of the digestion reaction tower in the system, increase the surface activity of the desulfurizing agents and the effect of desulfurization reaction, and improve the utilization rate of desulfurizing agent raw materials, simultaneously the digestive system has the advantages of wide turndown ratio and high reliability.
Description
Technical field
The present invention relates in the flue gas desulfurization technique field digestion of desulfurizing agent is prepared, refer to the desulfurizing agent preparation method in a kind of circulating fluidization dry flue gas desulphurization technology particularly.
Background technology
The improvement of the sulfur dioxide gas body pollution in the combustion apparatus institute smoke discharging is the emphasis of world's most countries environmental protection always; its produced pollution thing causes the greatest contamination source of China's environmental destruction especially, has become the task of top priority of China's air pollution treatment.Improvement to sulfur dioxide in flue gas, the external wet type lime stone-gypsum method (W-FGD) that adopts is usually come desulfurization, though its removal effect is better, investment is huge, water consumption is big but exist, floor space is big, system complex, big, the complex structure of resistance, and need a series of problem such as handle again to water.Therefore the high-efficiency flue gas desulfurization technology of dry type or half dry type becomes the emphasis of domestic and international research and development.Be the flue gas desulfurization market demand of 600MW substantially particularly at China's thermal power generation separate unit installed capacity, simultaneously, more will become the main flow in domestic and international power environment protection market applicable to the maximization dry flue gas desulphurization technology of the above thermal power generation unit of 600MW according to the objective law in flue gas desulfurization technique development and market in the world.
For the dry flue gas desulphurization technology, the size of sorbent particle particle diameter and surface-active height have directly determined the utilization rate of threshing agent in its desulphurization system and the height of desulfuration efficiency.Will be issued to the high desulfurization efficiency more than 90% in the low calcium-sulphur ratio condition of Ca/S=1.1～1.3, the particle diameter of sorbent particle just must be controlled at below the 10 μ m.And the desulfurization by dry method of the flue gas circulating fluidized bed method of using at present, one-tenth slurries after mostly utilizing the non-fluidization mode lime slaking are as desulfurizing agent, perhaps adopt method such as stirring to prepare the dry desulfurizer particle, and these sorbent particles are sprayed in the desulfurization reaction tower carry out desulphurization reaction with sulfur-containing smoke gas.As publication number is sulfur removal technology and the system that the Chinese invention patent prospectus of CN86108755A and CN1307926A is introduced.Because the dry desulfurizer grain diameter is bigger, surface-active is not high, and defective such as have that desulfurizing agent preparation system complexity, water consumption are big, floor space is big, pipeline is perishable, fouling and obstruction, nozzle are easy to wear, thereby the utilization rate of sorbent particle is very low, the reliability of desulphurization system is relatively poor, and smoke desulfurization efficiency is also lower.Simultaneously, desulfurizing agent preparation method in this type of dry flue gas desulphurization technology, mostly only adopt the secondary separation device of one-level separator or same type that the sorbent particle that comes out in the digestion reaction tower is carried out the separating cycle processing, like this in the maximization unit, because air quantity, grain amount is all quite big, the external recirculation grain amount is very big simultaneously, the load of separator has often exceeded its designed capacity, if adopt similar separator parallel connection, also will cause the structure of digestive system too complicated huge, therefore be difficult to guarantee effective separation of sorbent particle, and the activity of the particle size of sorbent particle and particle surface.In addition, adopt the one-level separator to realize digesting the recirculation of particle and during the sorbent particle that obtains preparing, considerable little sorbent particle can not effectively be collected, and carries out desulphurization reaction efficiently in the desulfurizing tower thereby can not in an organized way spray into.
Summary of the invention
Purpose of the present invention will overcome existing defective in the above-mentioned prior art exactly, desulfurizing agent preparation method in a kind of circulating fluidization dry flue gas desulphurization technology is provided, the sorbent particle particle diameter that adopts this method to obtain is even, the surface-active height, can guarantee to be issued to higher desulfuration efficiency in situation than low calcium-sulphur ratio, realize wider load adjusting ratio, can reduce the volume of digestion reaction system simultaneously, reduce equipment investment and operating cost.
For realizing this purpose, desulfurizing agent preparation method in the designed circulating fluidization dry flue gas desulphurization technology of the present invention, comprise raw material with the preparation desulfurizing agent, the digestion reaction water, fluidizing gas sprays into the digestion reaction that mixes in the digestion reaction tower and carry out, and therefrom isolate the sorbent particle that satisfies desulfurization needs particle size range, its special character is: adopt the different two-stage separator of particle separation diameter parameter, the desulfurizing agent wind powder mixture that will come out from the digestion reaction tower, the first order coarse separator that elder generation's process is arranged in behind the digestion reaction tower is separated, and the thick sorbent particle of being separated is sent the interior continuation circulation of digestion reaction tower again back to and carried out digestion reaction; The thin sorbent particle that is not separated is then sent into second level fine grained separator with weary gas and is separated, the thin sorbent particle of being separated is sent in the desulfurization reaction tower by the desulfurizing agent storage warehouse or is directly sent in the desulfurization reaction tower, and weary gas is then directly sent near the flue in desulfurization reaction tower entry position.
In the said method, first order coarse separator can be separated the sorbent particle greater than 7 μ m more than 90%, and second level fine grained separator can be separated the not isolated sorbent particle more than 98% of first order coarse separator.
In the said method, first order coarse separator adopts cyclone separator, and second level fine grained separator adopts electrostatic separator or cloth bag separator or their combination.
In the said method, the particle separation efficient of first order coarse separator is regulated within 30～90% scope, satisfies the particle circulating ratio of digestion reaction tower with the grain diameter according to the desulphurization reaction needs.
In the said method, spray into the fluidizing gas in the digestion reaction tower, directly adopt the clean flue gas after this sulfur removal technology is handled.
Compared with prior art, the invention has the advantages that:
First, the present invention carries out ciculation fluidized processing by the different two-stage combination separator of particle separation diameter parameter to sorbent particle, solved the low defective of separator overload operation separative efficiency that adopts single character in the past, can reduce the volume of digestion reaction tower, increase the circulating ratio of sorbent particle, improve the desulfurizing agent utilization ratio of raw materials, particularly its advantage is more remarkable in the desulfurizing agent preparation system of maximization equipment.
Second, the present invention can effectively be collected in total amount together at 1～6 μ m sorbent particle that digestion is good more than 99% by second level fine grained separator such as electrostatic separator and/or cloth bag separator, and in an organized way spray in the desulfurizing tower, thereby can significantly improve the utilization rate of sorbent particle, realize higher desulfuration efficiency.
The 3rd, the present invention has realized that by thick, thin two-stage separator the narrow-size distribution of sorbent particle distributes, and it is carried out the digestion process of circulating fluidization, can make the prepared sorbent particle particle diameter that goes out even, reach desired particle size range, thereby can significantly improve the surface-active of desulfurizing agent and the effect of desulphurization reaction, guarantee to be issued to high desulfurization efficiency more than 90～92% than the low calcium-sulphur ratio condition in Ca/S=1.1～1.3.
The 4th, the air quantity size that circulating fluidization digestion process mode of the present invention can enter first order coarse separator by the fluidizing gas air quantity and the adjusting of adjusting digestion reaction tower bottom, satisfy needed doctor solution consumption of various load variations and sorbent particle grain through size, thereby also have characteristics such as wide regulating ratio, reliability height.
Description of drawings
Accompanying drawing is the structural representation of employing desulfurizing agent preparation method's of the present invention circulating fluidization dry flue gas desulphurization system.
Among the figure: quick lime storehouse 1, mechanical charging gear 2, digestion atomized water nozzle 3; digestion reaction fluidizing gas inlet 4, digestion reaction tower 5, first order separator inlet pipe 6; first order cyclone separator 7, second level separator inlet pipe 8, digestion reaction recirculation particle inlet tube 9; second level static or cloth bag separator 10; desulfurizing agent storage warehouse inlet tube 11, desulfurizing agent storage warehouse 12, desulfurizing agent inlet tube 13; blast pipe 14; flue gas inlet tube 15, desulfurization reaction tower 16, deduster inlet tube 17; outside deduster 18; external recirculation particle feed back inlet tube 19, cinder tank 20, main induced draft fan 21; chimney 22, desulfurization reaction tower atomized water nozzle 23.
The specific embodiment
Below in conjunction with accompanying drawing desulfurizing agent preparation method of the present invention and applied circulating fluidization dry flue gas desulphurization technology thereof are described in further detail:
The present invention is with the quick lime of cheapness and to be not limited to quick lime be the desulfurizing agent raw material, and it mainly by digestion reaction system, prepares the high surface sorbent particle that meets the high desulfurization rate requirement.As shown in drawings:
The desulfurizing agent raw material quick lime of sending here from quick lime storehouse 1 sprays into from digestion reaction tower 5 bottoms by mechanical charging gear 2, and its mode of spraying into can be multiple: both sides spray into but can one-sidedly spray into also, can adopt the combination of single or multiple lift nozzle to spray into simultaneously.Digestion also is arranged on digestion reaction tower 5 bottoms with atomized water nozzle 3, and than the high 500～3000mm of desulfurizing agent raw material nozzles, digestion is scalable oscillation adjustment with atomized water nozzle 3 to its particular location on vertical height, also can arrange by single or multiple lift.The digestion reaction water is ejected in the digestion reaction tower 5 with atomized water nozzle 3 by digestion.
Adopt the fluidization reactive mode, the fluidizing gas that sprays into the flow velocity of 0.1～10m/s by digestion reaction fluidizing gas inlet 4 from the bottom of digestion reaction tower 5, this fluidizing gas can directly adopt the clean flue gas after this sulfur removal technology is handled, and forms energy savings with simplified apparatus.Can certainly adopt other compressed air.
In digestion reaction tower 5, fluidizing gas is with the desulfurizing agent raw material, the digestion reaction water dripization that spray into, and gas, solid, liquid three-phase material mix in tower strongly like this, can form fluidization preferably and digestion reaction condition, guarantee carrying out fast of digestion reaction.Not the bulky grain desulfurizing agent raw material of catapepsis reaction at digestion reaction tower 5 tops because the airflow drops of fluidizing gas, be subjected to the influence of digestion reaction tower 5 internal structures simultaneously, flow downward again, continue to take place digestion reaction, and the desulfurizing agent feed particles of less not catapepsis and digestion reaction sorbent particle completely, then be fluidized gas and carry, and enter in the first order cyclone separator 7 that is arranged in digestion reaction tower 5 outsides by first order separator inlet pipe 6 from the discharge of digestion reaction tower 5 tops.Then, inertial separation effect by first order cyclone separator 7, the sorbent particle greater than the not catapepsis of 7 μ m more than 90% is separated, and send into digestion reaction tower 5 bottoms by digestion reaction recirculation particle inlet tube 9, in digestion reaction tower 5, mix again, fluidisation and digestion reaction.Sorbent particle that the digestion of separating from first order cyclone separator 7 is good and weary gas, then enter in second level static or the cloth bag separator 10 by second level separator inlet pipe 8, the thin sorbent particle that digestion more than 98% is finished separates with weary gas, sends into desulfurizing agent storage warehouse 12 by desulfurizing agent storage warehouse inlet tube 11 and stores.The not isolated weary gas of second level static or cloth bag separator 10 and a small amount of thin especially desulfurizing agent dust are then directly sent near the air inlet flue of desulfurization reaction tower 16 inlets by blast pipe 14.According to the grain diameter of practical sulphur removal reaction needed, the particle separation efficient of first order cyclone separator 7 can be regulated within 40～90% scope, satisfies the sorbent particle circulating ratio in the needed digestion reaction tower 5.
Need desulfurization flue gas from other combustion apparatus discharges such as boilers; send into the tower from the bottom of desulfurization reaction tower 16 by flue gas inlet tube 15; the thin sorbent particle that comes out from desulfurizing agent storage warehouse 12 is injected to desulfurization reaction tower 16 bottoms by desulfurizing agent inlet tube 13; add the atomizing cooling water that sprays into from desulfurization reaction tower atomized water nozzle 23; and be back to the recirculation particle of desulfurization reaction tower 16 bottoms through external recirculation particle feed back inlet tube 19 from what outside deduster 18 was separated; strong three-phase turbulent heat transfer mass transfer exchange takes place in desulfurization reaction tower 16, carries out desulphurization reaction.Between the cigarette temperature drop to 55 in the above-mentioned tower～70 ℃, be higher than in the tower 5～15 ℃ of flue gas dew point temperature, also can be under some situation in about 80 ℃ operations of cigarette temperature.Flue gas, particle water, sorbent particle and recirculation particle move upward under the drive of flue gas jet like this, are the fluidized suspension attitude in the whole desulfurizing tower.
In desulfurization reaction tower 16 middle and upper parts, substantially present bigger falling trend, most of particle moves downward along near the sidewall, and moved upward reciprocal by the flue gas drive again to the tower bottom, in tower, form high-intensity three-phase turbulent flow swap status, the complicated physical and chemical process of strong mixing, heat transfer, mass transfer and chemical reaction takes place.SO in tower in the flue gas
2With desulfurizing agent Ca (OH)
2Reaction generates calcium sulfite or calcium sulfate, and can deviate from a spot of SO in the flue gas simultaneously
3And pernicious gas compositions such as the HCl that may exist, HF, desulfuration efficiency can reach more than 90% at least.
Then; flue gas is discharged by desulfurization reaction tower 16 tops; enter outside deduster 18 by deduster inlet tube 17; the particle that carries in the flue gas is separated; the part particle is sent back to by external recirculation particle feed back inlet tube 19 and is continued to participate in desulphurization reaction in the desulfurization reaction tower 16, and desulfuration byproduct that does not circulate and flying dust are then sent into cinder tank 20 and stored, transport.Send into chimney 22 from the clean flue gas up to standard that outside deduster 18 comes out by main induced draft fan 21, enter atmosphere at last.
Claims (9)
1. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology, comprise raw material with the preparation desulfurizing agent, the digestion reaction water, fluidizing gas sprays into the digestion reaction that mixes in the digestion reaction tower and carry out, and therefrom isolate the sorbent particle that satisfies desulfurization needs particle size range, it is characterized in that: adopt the different two-stage separator of particle separation diameter parameter, the desulfurizing agent wind powder mixture that will come out from the digestion reaction tower, the first order coarse separator that elder generation's process is arranged in behind the digestion reaction tower is separated, and the thick sorbent particle of being separated is sent the interior continuation circulation of digestion reaction tower again back to and carried out digestion reaction; The thin sorbent particle that is not separated is then sent into second level fine grained separator with weary gas and is separated, the thin sorbent particle of being separated is sent in the desulfurization reaction tower by the desulfurizing agent storage warehouse or is directly sent in the desulfurization reaction tower, and weary gas is then directly sent near the flue in desulfurization reaction tower entry position.
2. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 1 is characterized in that: said first order coarse separator can be separated the sorbent particle greater than 7 μ m more than 90%; Said second level fine grained separator can be separated the not isolated sorbent particle smaller or equal to 7 μ m more than 98% of first order coarse separator.
3. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 1 and 2, it is characterized in that: said first order coarse separator adopts cyclone separator, and second level fine grained separator adopts electrostatic separator or cloth bag separator or their combination.
4. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 1 and 2, it is characterized in that: the particle separation efficient of said first order coarse separator is regulated within 30～90% scope, satisfies the particle circulating ratio of digestion reaction tower with the grain diameter according to the desulphurization reaction needs.
5. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 3, it is characterized in that: the particle separation efficient of said first order coarse separator is regulated within 30～90% scope, satisfies the particle circulating ratio of digestion reaction tower with the grain diameter according to the desulphurization reaction needs.
6. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 1 and 2 is characterized in that: the said fluidizing gas that sprays in the digestion reaction tower, directly adopt the clean flue gas after this sulfur removal technology is handled.
7. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 3 is characterized in that: the said fluidizing gas that sprays in the digestion reaction tower, directly adopt the clean flue gas after this sulfur removal technology is handled.
8. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 4 is characterized in that: the said fluidizing gas that sprays in the digestion reaction tower, directly adopt the clean flue gas after this sulfur removal technology is handled.
9. the desulfurizing agent preparation method in the circulating fluidization dry flue gas desulphurization technology according to claim 5 is characterized in that: the said fluidizing gas that sprays in the digestion reaction tower, directly adopt the clean flue gas after this sulfur removal technology is handled.
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|---|---|---|---|
| CN 03125324 CN1211149C (en) | 2003-08-25 | 2003-08-25 | Desulfurizing agent preparing method in circulating fluid dry flue gas desulfurization process |
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| CN 03125324 CN1211149C (en) | 2003-08-25 | 2003-08-25 | Desulfurizing agent preparing method in circulating fluid dry flue gas desulfurization process |
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| CN1211149C true CN1211149C (en) | 2005-07-20 |
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| CN100363091C (en) * | 2004-11-26 | 2008-01-23 | 武汉凯迪电力股份有限公司 | Preparation of integrated desulfurizing agent during the two-stage digestible and separating process and its system thereof |
| CN108126510B (en) * | 2018-01-16 | 2024-01-26 | 邯郸学院 | Flue gas desulfurization and denitrification equipment |
| CN115430272B (en) * | 2022-10-24 | 2023-07-25 | 北京北科环境工程有限公司 | Preparation method of calcium-based SDS desulfurization process raw material |
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