CN1513582A - Dry process stack gas desulfur technology using circulating fluidization mode to proceed desulfurizer preparation - Google Patents
Dry process stack gas desulfur technology using circulating fluidization mode to proceed desulfurizer preparation Download PDFInfo
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- CN1513582A CN1513582A CNA031252931A CN03125293A CN1513582A CN 1513582 A CN1513582 A CN 1513582A CN A031252931 A CNA031252931 A CN A031252931A CN 03125293 A CN03125293 A CN 03125293A CN 1513582 A CN1513582 A CN 1513582A
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Abstract
A dry-method fume desulfurizing process using cyclic fluidized mode to prepare desulfurizing agent features that the gas is used to fluidize the solid material in digestion tower to form a fluidized phase with high concentration at lower position and low concentration at higher position, the water is sprayed and atomized in tower to generate fine desulfurizing agent particles, the part of particles is separated in duster for recirculation, and the rest of particles comes in desulfurizing tower or hydrated lime carbon. Its advantages are high digestion efficiency, high activity of desulfurizing agent, small size and high system reliability.
Description
Technical field
The present invention relates to a kind of dry flue gas desulphurization technology that adopts the circulating fluidization mode to carry out the desulfurizing agent preparation, belong to the dry flue gas desulphurization technical field, maximization dry method desulfuration system and technology in the particularly various large-scale combustion apparatus discharging flue gases.
Background technology
The improvement of sulfur dioxide gas body pollution is the emphasis of world's most countries environmental protection always, and its pollutant that produces causes the greatest contamination source of China's environmental destruction especially, has become the task of top priority of China's air pollution treatment at present.
Present improvement to sulfur dioxide, external general main employing wet type lime stone-gypsum method (W-FGD), adopt said method, though removal effect is better, investment is huge, water consumption is big but it exists, floor space is big, system complex, big, the complex structure of resistance, and need handle or the like a series of problems 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.
Special is the flue gas desulfurization market demand of 600MW at China's thermal power generation separate unit installed capacity substantially, special specific (special) requirements at area, northwestward power environment protection, and country is to the reinforcement of water resource utilization protection.Simultaneously according to the objective law in flue gas desulfurization technique development and market in the world, advanced person's maximization (applicable to the above thermal power generation unit of 600MW) dry flue gas desulphurization technology will become the main force in domestic and international power environment protection technology and market.
For present all dry method and semi-dry desulphurization technology and patented technologies, though they all the flue gas desulfurization course of reaction certain some aspect have oneself technical characteristic, but all do not have to consider after unit maximizes, because the increase of desulphurization reaction tower section and height will cause whole desulphurization reaction owing to the tissue failure in flue gas and particle flow field does not reach the desulfur technology requirement.
Especially for the desulfurization by dry method of the flue gas circulating fluidized bed method of present application, one-tenth slurries after mostly utilizing the non-fluidization mode lime slaking are as absorbent, perhaps adopt method such as stirring to prepare the dry desulfurizer particle, and such absorbent granules sprayed in the reactor carry out desulphurization reaction with sulfur-containing smoke gas.As patent CN86108755A, CN1307926 or the like.Because the dry desulfurizer grain diameter is bigger, surface-active is relatively poor, has desulfurizing agent preparation system complexity simultaneously, and water consumption is big, and floor space is bigger, and pipeline is perishable, fouling and obstruction, and nozzle is easy to wear, and the utilization rate of sorbent particle is very low.Therefore the reliability of this type systematic is relatively poor, and smoke desulfurization efficiency is lower.
Summary of the invention
Deficiency and defective at the prior art existence, purpose of the present invention and task provide a kind of dry flue gas desulphurization technology that adopts novel desulfurizing agent preparation system, employing in the desulfurizing agent preparation system mode of circulating fluidization carry out the desulfurizing agent preparation, at calcium water mol ratio Ca/H
2In the scope of O=1.0～1.3, reach higher digestive efficiency (more than 95%), under the prerequisite of the system of assurance reliability service, for the desulphurization reaction Tower System provides colory dry powder attitude desulfurizing agent, thereby guarantee the efficient running of whole desulphurization system, promptly the situation in Ca/S=1.1～1.3 is issued to higher desulfuration efficiency (more than 90%～92%).Realize the wide regulating ratio characteristic of desulphurization system, can satisfy the high-efficiency desulfurization requirement of combustion apparatus from 20% to 110% load variations.
The present invention realizes by following technical method:
Flue gas desulfurization technique of the present invention, comprise that mainly desulfurizing agent prepares the separation and the recirculating system of digestive system, desulphurization reaction system and desulfurization reaction tower, outside sorbent particle, desulfurizing agent prepares digestive system and adopts the circulating fluidization mode to carry out the highly active desulfurization agent preparation of granules, feed the recycle stock of desulfurizing agent raw material and digestive system in digestion reaction tower bottom, the tower body bottom is sent into gas and is carried out fluidisation, and spray into an amount of digestion reaction water at the tower body certain altitude, making digestion reaction is to finish under the condition of gas, liquid, solid three-phase fluidization.
The void tower fluidizing velocity of digestion reaction tower is at 0.2～10m/s.
Described employing circulating fluidization mode is carried out the flue gas desulfurization technique of desulfurizing agent preparation, and the most of particle that once digests separator is sent the digestion reaction tower back to and recycled reaction;
The fluidization air feed of digestive system adopts the fluidizing gas of recirculation;
Or the fluidization air feed of digestive system adopts compressed air;
Or the fluidization air feed of digestive system adopts clean flue gas recycled.
The separation equipment that adopts the circulating fluidization mode to carry out the digestive system of desulfurizing agent preparation is one or more levels layout.
Adopting the circulating fluidization mode to carry out the desulfurizing agent preparation, is in digestion reaction tower body bottom, and the scope of 1～5m feeds the recycle stock of desulfurizing agent raw material and digestive system at the bottom of the tower.
Adopting the circulating fluidization mode to carry out the desulfurizing agent preparation, be to send into gas from the tower body bottom to carry out fluidisation, and the position of 3～10m sprays into an amount of digestion reaction water at the bottom of the distance tower, and keeping calcium water mol ratio is Ca/H
2The scope of O=1.0-1.3.
Advantage of the present invention:
At first, the present invention is owing to adopted the circulating fluidization mode to carry out the desulfurizing agent preparation, and system is more terse, does not have problems such as pipeline scale obstruction, nozzle wear, has improved the reliability of system.
The second, because the circulating fluidization mode is carried out the desulfurizing agent preparation, the raw material availability height of desulfurizing agent, water consumption is low, and the desulfurizing agent finished product grain size is little, surface-active is high.
The 3rd, because the desulfurizing agent finished product is the dry powder attitude, be convenient to store, therefore can adopt the mode of directly blowing or middle warehouse mode that desulfurizing agent is sent into the desulphurization reaction Tower System, so system's modulability is good.
The 4th, owing to can adopt gas egr mode or clean flue gas egr mode to provide fluidizing gas simultaneously to the digestion tower, so water consumption is low, load adaptability is good
Description of drawings
Fig. 1 carries out the dry flue gas desulphurization system of desulfurizing agent preparation for adopting the circulating fluidization mode.
Fig. 2 carries out the dry flue gas desulphurization system of desulfurizing agent preparation for the circulating fluidization mode that adopts the digestive system flue gas recirculation.
Fig. 3 carries out the dry flue gas desulphurization system of desulfurizing agent preparation for the circulating fluidization mode that adopts the desulphurization system flue gas recirculation.
Among the figure: quick lime storehouse 1; Digestion reaction tower 2; Digestive system primary dust removing device 3; Digestive system secondary ash collector 4; Desulfurizing tower 5; Deduster 6; Cinder tank 7; Main induced draft fan 8; Chimney 9; Desulfurizing agent material inlet 10; Digestion tower atomizing spray mouth 11; Digestion tower fluidisation air inlet 12; Digestive system material recirculation pipe 13; Digestion tower blast pipe 14; Digestive system primary dust removing device blast pipe 15; Digestive system secondary ash collector blast pipe 16; Desulfurizing agent transports pipe 17; Digestion water atomizing spray mouth 18; Desulfurizing tower gas approach 19; Desulfurizing tower blast pipe 20; Desulfurizing tower material recirculation pipe 21; Deduster smoke outlet tube 22; Lime-ash pipe 23; Recirculation blower 24.
The specific embodiment
The present invention is that example describes with quick lime, is the desulfurizing agent raw material but be not limited to quick lime.Comprise lower resistance flue gas injection process in the digestion reaction tower in this method, desulphurization reaction process design with the strong interior cycle characteristics digestion reaction process of particle, and the feeding back device and the system pipeline of external recirculation particle, and set up the adjustable water spraying atomization nozzle in position in the middle and lower part of digestion reaction tower and desulfurization reaction tower, to be suitable for the water spraying atomization requirement that different flue gas loads change and reactive flowfield changes.
Specify embodiments of the present invention, technical process and system layout structure below in conjunction with accompanying drawing 1.
One. the digestion reaction process to the desulfurizing agent raw material elaborates:
Desulfurizing agent raw materials of Ca O powder is sent into the bottom of digestion reaction tower 2 by quick lime storehouse 1 through material inlet 10, and fluidizing gas is sent into the digestion tower by air inlet 12 from the digestion tower bottom, and material is carried out fluidisation.The digestion reaction water sprays in the tower after atomizing through atomizing spray mouth 11, keeps calcium water mol ratio Ca/H
2O=1.0～1.3, gas, liquid, solid three-phase material are strong hybrid reaction in tower, forms fluidization preferably and digestion reaction condition, and the part particle circulates in the formation tower endoparticle down owing to the tissue characteristics of flow field in tower is separated in the digestion tower.Another part particle is fluidized gas and carries through digestion tower blast pipe 14 and enter digestive system deduster 3.Because digestion reaction is exothermic reaction, under fluidization, reaction will cause quicklime particles to be broken, and become the high activity hydrated lime particle of small particle diameter, high-specific surface area, the most grain diameters that arrive the outlet of digestion top of tower are dry powder attitude material between 1-30 μ m.The primary dust removing device 3 that the dusty gas that the digestion tower is discharged at first enters digestive system carries out gas solid separation, is to improve digestibility, and the sorbent particle that wherein is separated is sent into the digestion tower and circulated through transporting pipe 13; The dusty gas of discharging from the primary dust removing device enters secondary ash collector 4 through blast pipe 15, the separated desulfurizing agent that gets off is through transporting the bottom that pipe 17 sprays into desulfurization reaction tower 5, and remainder is sent in the main flue gas inlet pipeline 19 with cyclone separator top blast pipe 16.
The fluidizing gas of digestive system can have three kinds of sources: the first, and the air after the employing pressurization, sprays into from digestion tower fluidisation air inlet 12 as Fig. 1 as fluidizing agent; Second, employing through the gas of the laggard promoting the circulation of qi body recirculation of digestion reaction tower and dedusting as fluidizing agent, as Fig. 2, will directly guide to digestion tower fluidisation air inlet 12 from the gas that digestive system secondary ash collector blast pipe 16 is discharged, enter fluidisation air inlet 12 by recirculation blower 24; The 3rd, adopt the clean flue gas that carries out flue gas recirculation behind the whole desulphurization system desulfurization and dedusting as fluidizing agent, as Fig. 3, the clean flue gas after the desulphurization system desulfurization is sent into fluidisation air inlet 12 by recirculation blower 24.
The void tower fluidizing velocity of digestion reaction tower is at 0.2～10m/s.
The deduster of digestive system can be not limited to inertial dust separator, electric cleaner, sack cleaner or other forms of deduster and their compound mode.And can arrange for one or more levels.
Two, summary sweetening process:
The flue gas that produces from combustion apparatus enters desulfurizing tower 5 by the flue gas induction apparatus, and desulfurizing agent is through transporting the bottom that pipe 17 sprays into desulfurization reaction tower 5, and the digestion water sprays into desulfurization reaction tower from water atomization water spout 18.Flue gas, particle water, sorbent particle and recirculation particle move upward under the drive of flue gas jet in desulfurizing tower, are the fluidized suspension attitude in the whole desulfurizing tower.In the tower body middle and upper part, 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.SO2 in tower in the flue gas and desulfurizing agent Ca (OH) 2 reactions generate calcium sulfite or calcium sulfate, and can deviate from pernicious gas composition such as a spot of SO3 and the HCl that may exist, HF in the flue gas simultaneously, and desulfuration efficiency can reach more than 90% at least.
Flue gas is drawn by the outlet conduit 20 at desulfurizing tower top, enters by (or sack cleaner) in the electrostatic separator 6, and the particle that carries in the flue gas is separated, and wherein also contains some unreacted sorbent particle.In order to improve sorbent utilization,, their recirculation is sent back in the desulfurizing tower by a recirculation particle feed back pipe 21; Desulfuration byproduct that does not circulate and flying dust are then sent into cinder tank 7 and are stored, and transhipment is walked; Send into chimney 9 through deduster smoke outlet tube 22 by main induced draft fan 8 from the clean flue gas up to standard that deduster 6 comes out, enter atmosphere at last.
Core of the present invention is to adopt the digestion reaction tower fully to digest calcium hydroxide Ca (OH)
2Deng desulfurizing agent, the raw material availability height of desulfurizing agent, water consumption is low, and the desulfurizing agent finished product grain size is little, surface-active is high.To improve the utilization rate of desulfurizing agent, guarantee to be issued to higher desulfuration efficiency in the situation of lower calcium sulfur ratio.Therefore, every employing digestion reaction tower prepares desulfurizing agent and all belongs to protection scope of the present invention.
Claims (9)
1. one kind is adopted the circulating fluidization mode to carry out the flue gas desulfurization technique that desulfurizing agent prepares, comprise that mainly desulfurizing agent prepares digestive system, desulphurization reaction system and desulfurization reaction tower, the separation and the recirculating system of outside sorbent particle, it is characterized in that desulfurizing agent prepares digestive system and adopts the circulating fluidization mode to carry out the highly active desulfurization agent preparation of granules, feed the recycle stock of desulfurizing agent raw material and digestive system in digestion reaction tower bottom, the tower body bottom is sent into gas and is carried out fluidisation, and spray into an amount of digestion reaction water at the tower body certain altitude, making digestion reaction is at gas, liquid, Gu finish under the condition of three-phase fluidization.
2. employing circulating fluidization mode according to claim 1 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, and the void tower fluidizing velocity that it is characterized in that the digestion reaction tower is at 0.2～10m/s.
3, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, and the most of particle that it is characterized in that once digesting separator is sent the digestion reaction tower back to and recycled reaction.
4, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, it is characterized in that the fluidization air feed of digestive system adopts the fluidizing gas that recycles.
6, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, it is characterized in that the fluidization air feed of digestive system adopts compressed air.
7, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, it is characterized in that the fluidization air feed of digestive system adopts clean flue gas recycled.
8, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, and the separation equipment that it is characterized in that digestive system is multistage layout.
9, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, it is characterized in that in digestion reaction tower body bottom, and the scope of 1～5m feeds the recycle stock of desulfurizing agent raw material and digestive system at the bottom of the tower.
10, employing circulating fluidization mode according to claim 1 and 2 is carried out the flue gas desulfurization technique of desulfurizing agent preparation, it is characterized in that tower body bottom sends into gas and carry out fluidisation, and the position of 3～10m sprays into an amount of digestion reaction water at the bottom of the distance tower, and keeping calcium water mol ratio is Ca/H
2The scope of O=1.0～1.3.
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| Application Number | Priority Date | Filing Date | Title |
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| CNA031252931A CN1513582A (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur technology using circulating fluidization mode to proceed desulfurizer preparation |
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| CNA031252931A CN1513582A (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur technology using circulating fluidization mode to proceed desulfurizer preparation |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102363095A (en) * | 2011-09-16 | 2012-02-29 | 莫沙纱 | Dry flue gas desulfurization process method and dry flue gas desulfurization system thereof |
| CN105645113A (en) * | 2016-01-27 | 2016-06-08 | 西安航天源动力工程有限公司 | Sodium bicarbonate gathering, transporting and injecting method |
| CN105645112A (en) * | 2016-01-27 | 2016-06-08 | 西安航天源动力工程有限公司 | Sodium bicarbonate gathering, transporting and jetting complete technology system |
| CN111642733A (en) * | 2020-06-18 | 2020-09-11 | 瞿瀚鹏 | Increasing vitamin D in mushrooms2Content method and method for preparing edible mushroom powder |
| CN114618291A (en) * | 2020-12-10 | 2022-06-14 | 西南科技大学 | Dry digestion and flue gas desulfurization integrated process of quicklime |
-
2003
- 2003-08-19 CN CNA031252931A patent/CN1513582A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102363095A (en) * | 2011-09-16 | 2012-02-29 | 莫沙纱 | Dry flue gas desulfurization process method and dry flue gas desulfurization system thereof |
| CN105645113A (en) * | 2016-01-27 | 2016-06-08 | 西安航天源动力工程有限公司 | Sodium bicarbonate gathering, transporting and injecting method |
| CN105645112A (en) * | 2016-01-27 | 2016-06-08 | 西安航天源动力工程有限公司 | Sodium bicarbonate gathering, transporting and jetting complete technology system |
| CN105645113B (en) * | 2016-01-27 | 2018-05-11 | 西安航天源动力工程有限公司 | A kind of sodium acid carbonate collection is defeated and injection method |
| CN105645112B (en) * | 2016-01-27 | 2018-05-11 | 西安航天源动力工程有限公司 | A kind of sodium acid carbonate collection is defeated and sprays complete process system |
| CN111642733A (en) * | 2020-06-18 | 2020-09-11 | 瞿瀚鹏 | Increasing vitamin D in mushrooms2Content method and method for preparing edible mushroom powder |
| CN114618291A (en) * | 2020-12-10 | 2022-06-14 | 西南科技大学 | Dry digestion and flue gas desulfurization integrated process of quicklime |
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