CN1513584A - Vertical eddy flow type circulating fluidization dry process stack gas desulfur method - Google Patents
Vertical eddy flow type circulating fluidization dry process stack gas desulfur method Download PDFInfo
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Abstract
A dry-method fume-desulfurizing process using vertical eddy and circulated fluidizing features that the fume to be desulfurized is sprayed into desulfurizing tower from front and back of tower at different heights to generate the vertical eddy flow of fume in tower, which can carry the sprayed desulfurizing agent particles and atomized water drops to form a strong gas-solid-liquid eddy, resulting in strong desulfurizing reaction. Its advantages are high desulfurizing efficiency, and low cost.
Description
Technical field
The invention belongs to the flue gas desulfurization technique field, relate to the dry desulfurization of various combustion apparatus institute smoke discharging, refer to the dry flue gas desulphurization method of a kind of vertical whirlpool type circulating fluidization particularly.
Background technology
The improvement of the sulfur dioxide gas body pollution in the combustion apparatus institute smoke discharging; it is the emphasis of most countries environmental protection in the world 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, have that investment is huge, water consumption big, floor space is big, system complex, resistance are big, complex structure and need a series of problem such as handle again to water.Therefore, the flue gas desulfurization technique of dry method or semidry method becomes the emphasis of domestic and international research and development.
For dry method or semi-dry process flue gas desulphurization technology, the principal element that the influences desulfuration efficiency turbulent mass transfer characteristic of temperature, humidity, sorbent particle surface-active, desulfurizing agent and flue gas haptoreaction time, sorbent particle and flue gas or the like that responds; For whole dry method desulfuration system, also must taking into account system resistance size, the wearing and tearing of system complex degree, device and equipment and burn into system be to the influence of many-sided factors such as the adaptability of load, water consumption size.
Existing dry flue gas desulphurization technology mainly contains spray drying process, in-furnace calcium spraying adds methods such as humidification activation method and circulating fluid bed flue-gas desulfurizing.Sorbent utilization is lower in preceding two kinds of methods, and smoke desulfurization efficiency is not high, and the inwall at desulfurizing tower easily causes corrosion and fouling simultaneously.And circulating fluid bed flue gas desulfurization method is by the repeatedly recycling of sorbent particle, the time of staying of sorbent particle is increased, the utilization rate and the desulfuration efficiency of desulfurizing agent have been improved widely, overcome the deficiency in preceding two kinds of methods, have applied widelyly, can be used for characteristics such as senior middle school's low-sulfur coal.
Because above-mentioned circulating fluid bed flue gas desulfurization method is based on the recirculating fluidized bed principle, therefore different ciculation fluidized modes has very big influence to utilization rate, SR and whole dry flue gas desulphurization technological system and the device of desulfuration efficiency, desulfurizing agent.At present, this sulfur method adopts the mode of bottom cycle fluidisation mostly, promptly sprays into flue gas by flue gas ejection accelerating apparatus such as Venturi nozzle from the desulfurizing tower bottom.Dash at a high speed at the flue gas ejection accelerating apparatus and to penetrate down, the sorbent particle fluidization also fully mixes with flue gas, and flue gas is by reduction of speed behind the flue gas ejection accelerating apparatus, and sorbent particle still dashes with high speed inertia and penetrates, gas-solid exists speed poor, strengthens mass transfer, and flue gas and sorbent particle fully react.Be that what introduced in the Chinese invention patent prospectus of CN1401415A is exactly this bottom fluidization mode as publication number, it is made of venturi fluidisation section and divergent segment two parts, and wherein venturi fluidisation section is made up of Venturi nozzle.Publication number is the bottom cycle streaming mode of being introduced in the Chinese invention patent prospectus of CN1195573A of being made up of air distribution plate and bellows.The reverse-flow type circulating fluid bed flue-gas desulfurizing technology that and for example German Wulff company adopts also is to realize this bottom cycle fluidisation by the flue gas ejection accelerating apparatus of Venturi nozzle.But, adopt the dry flue gas desulphurization technology of this bottom cycle streaming mode still to have following defective: at first, its flue gas circulation drag overall is bigger, and usually above 2000 handkerchiefs, this has just caused the raising of operating cost and the aggravation of equipment attrition under the normal operation.Secondly, the bottom cycle streaming mode is difficult to consider may cause the normally influence of factor such as fluidisation of fluidized bed reaction system because combustion apparatus load variations, exhaust gas volumn diminish, and Load Regulation is relatively poor.In addition, maximization day by day along with present coal-fired power station boiler, the increase of its desulfurizing tower cross section and height, the desulfurizing tower interior flow field of this bottom cycle streaming mode is tending towards even, be difficult to guarantee contacting of collision between solid particle in the desulfurizing tower and solid particle and flue gas, thereby make the mixing of flue gas and sorbent particle weaken, even cause the tissue failure in flue gas and particle flow field, and then influenced the utilization rate and the desulfuration efficiency of desulfurizing agent.
Summary of the invention
Purpose of the present invention will overcome existing defective in the above-mentioned prior art exactly, the dry flue gas desulphurization method of a kind of vertical whirlpool type circulating fluidization is provided, adopt this method can guarantee to be issued to higher desulfuration efficiency in situation than low calcium-sulphur ratio, realize wider load adjusting ratio, and further reduce flue gas resistance, the simplification system forms, and reduces equipment investment and operating cost.
For realizing this purpose, the dry flue gas desulphurization method of the vertical whirlpool type circulating fluidization that the present invention proposes through further investigation, comprise the preparation digestion of desulfurizing agent, desulphurization reaction in the desulfurization reaction tower, the separation and the recirculation of outside sorbent particle, its special character is: will need the flue gas of desulfurization to be divided into two-way, one road flue gas is by the flue gas ejection accelerating apparatus, the differing heights position of both sides sprays into the desulfurizing tower respectively before and after the desulfurizing tower lower area, its at the middle and upper levels the jet direction of flue gas be-5 °～-45 ° with the angle of trunnion axis on a vertical plane, the jet direction of lower floor's flue gas is+15 °～-55 ° with the angle of trunnion axis on a vertical plane, the flue gas jet direction is that benchmark is upwards for just with the trunnion axis, for negative, the effluxvelocity of two-layer flue gas is 30～100m/s up and down downwards.Another road flue gas is by the flue gas air-distribution device, upwards in desulfurizing tower, evenly give wind from the bottom of desulfurizing tower lower area with the flow velocity of 0.1～10m/s, make flue gas in the desulfurizing tower lower area, do vertical eddying motion, formation has the interior desulphurization reaction flow field of tower of vertical turbulent structure, thereby makes flue gas and sorbent particle that violent hybrid reaction take place in desulfurizing tower.
In the said method, the difference in height that sprays into the position of two-layer flue gas is preferably before and after the desulfurizing tower 1.0～1.5 times of the both sides degree of depth up and down.
In the said method, the jet direction of upper strata flue gas is-10 °～-20 ° with the preferable angle of trunnion axis on a vertical plane, the jet direction of lower floor's flue gas is+5 °～-5 ° with the preferable angle of trunnion axis on a vertical plane, and the preferable effluxvelocity of two-layer flue gas is 40～80m/s up and down.
In the said method, spray into road exhaust gas volumn in the desulfurizing tower lower area by the flue gas ejection accelerating apparatus and account for 60～95% of the flue gas total amount that needs desulfurization, another road exhaust gas volumn that is blown into desulfurizing tower lower area bottom by the flue gas air-distribution device accounts for 5～40% of the flue gas total amount that needs desulfurization.Regulate the two-way exhaust gas volumn, can make the demand that reaches normal fluidization in the desulfurizing tower, and the non-caked dust in desulfurizing tower bottom, to guarantee the particle proper flow of desulfurizing tower bottom.
In the said method, the degree of depth of desulfurizing tower lower area is 1.0～2.0 times of the desulfurizing tower upper area degree of depth, the variation structure that the desulfurizing tower upper area adopts cross sectional shape to change arbitrarily.Its cross sectional shape can be circle, polygon, ellipse or other combination of shapes, owing to make a variation mutually between its cross section and the cross section, can further increase the turbulence intensity of flue gas.
In the said method, fresh sorbent particle, recirculation sorbent particle and atomized water can be sprayed into the desulfurizing tower from the desulfurizing tower lower area.
In the said method, can adopt segmentation water spray mode, middle hypomere at desulfurizing tower lower area and upper area, the water atomizing nozzle of 1～4 layer of segmentation decreasing temperature and increasing humidity is set in one-sided or both sides along radial direction, wherein: the distance at the position of the orlop nozzle of hypomere and desulfurizing tower lower area top is 300～2000mm in the upper area, and the distance between each layer nozzle is 800～1500mm.Water atomizing nozzle can adopt fixed or scalable shuttle-type structure, and the atomizing particle size of the particle water of ejection can be regulated as required at any time.
In the said method, can adopt the combination smoke mode of jet, arrange flue gas jet nozzle under 1～4 course at the middle hypomere of desulfurizing tower upper area in one-sided or both sides along radial direction, 10～30% the cleaning after outside deduster separates is contained wet flue gas as medium, flow velocity with 30～180m/s sprays in the desulfurizing tower, to strengthen the flue gas turbulence intensity of desulfurization middle and later periods.
In the said method, the flue gas ejection accelerating apparatus can adopt the Rafael nozzle and the combination thereof of lower resistance, and its nozzle can adopt flexible in tower and the adjustable form of direction, with the speed that improves its injection and the efficient of injection.
Compared with prior art, the invention has the advantages that: at first, owing to adopted the flue gas recirculation streaming mode of vertical whirlpool type, most flue gas is at the front and back of desulfurizing tower lower area two side positions, spray into difference in height, the angle of inclination of setting and the flow velocity of setting of setting, produce vertical eddying motion, the inevitable flue gas flow field that forms vertical vortex flow at the desulfurizing tower lower area.Remaining flue gas is upwards evenly given wind from the bottom of desulfurizing tower lower area with the flow velocity of setting simultaneously, add the sorbent particle and the atomizing cooling water that spray into from the desulfurizing tower lower area, can be in the desulfurizing tower strong hybrid reaction of three-phase material, form fluidization preferably and granule interior recirculation characteristic, thereby greatly improved the ability of its desulphurization reaction, strengthen the activation characteristic of sorbent particle, also significantly improved the utilization rate of desulfurizing agent.
Secondly, in the maximization flue gas desulfurization device, adopt the desulfurizing tower in this vertical vortex flow field, its fluidization characteristics can obtain by the extension on the desulfurizing tower width well satisfying, and it is very violent that the ciculation fluidized mode in vertical vortex flow field makes that effect is entrainmented in the mixing of the air-flow of desulfurizing tower bottom and sorbent particle, when having reduced the sorbent particle normal fluidization to the degree of dependence of exhaust gas volumn demand, thereby be easy to realize the wide control characteristic of desulphurization system load variations.Therefore, it has speciality and the wide regulating ratio characteristic that maximization units gas desulfurization technology is used, and can satisfy the high-efficiency desulfurization requirement of 300MW～1000MW thermal power generation unit from 20% to 110% load variations.
The 3rd, because the flue gas flow field structure of this vertical vortex flow is to entrainment sorbent particle to realize that it is fluidised, the fluidised method of its mechanism and bottom cycle is completely different, and it has reduced the resistance of flue gas ejection accelerating apparatus greatly, has reduced the SR of desulfurizing tower.Therefore, the present invention can realize higher desulfuration efficiency, can reach the desulfuration efficiency more than 90～92% between calcium sulfur ratio Ca/S=1.1～1.3; The adjusting ratio of broad satisfies the high-efficiency desulfurization requirement of combustion apparatus 20～110% load variations; And the desulfur technology requirement of lower drag, make equipment be tending towards simplifying, reduce operating cost.
Description of drawings
Fig. 1 is for adopting the desulphurization system structural representation of sulfur method of the present invention;
Fig. 2 be among Fig. 1 the desulfurizing tower main body with and the structural representation of interior flow field;
Fig. 3 is the desulfurizing tower lower area cross section among Fig. 1 and the structural representation of main flue gas import;
Among the figure: flue gas pre-dedusting device 1, main flue gas import 2, desulfurizing tower lower area 3; combination smoke jet nozzle 4, desulfurizing tower upper area 5, bottom gas approach 6; desulfurizing tower exhanst gas outlet 7, fume dust remover 8, external recirculation particle feedback outlet 9; cinder tank 10; main induced draft fan 11, water atomizing nozzle 12, chimney 13; desulfurizing agent prepares digestive system 14, sorbent particle entrance 15.
The specific embodiment
Be described in further detail below in conjunction with the dry flue gas desulphurization method of accompanying drawing vertical whirlpool of the present invention type circulating fluidization:
As shown in the figure, adopt in the desulphurization system of sulfur method of the present invention, active desulfurizing tower is made up of lower area 3 (vertical vortex reaction zone) and upper area 5.The degree of depth of lower area 3 is 1.0～2.0 times of the degree of depth of upper area 5, the variation structure that upper area 5 adopts cross sectional shapes to change arbitrarily.The need desulfurization flue gas of discharging from combustion apparatus carries out preliminary treatment at first through a flue gas pre-dedusting device 1 as electrostatic precipitator, sack cleaner, inertial separation deduster etc.Be divided into two-way through the flue gas after the pre-dust removal process, one tunnel 70～90% flue gas sprays into the desulfurizing tower respectively from differing heights position, both sides, desulfurizing tower lower area 3 front and back by being installed in the flue gas ejection accelerating apparatus at main flue gas import 2 places.The flue gas ejection accelerating apparatus can adopt the Rafael nozzle of 5～35 lower resistance to form.The difference in height of flue gas ejection accelerating apparatus installation site, both sides before and after the desulfurizing tower, promptly the two-layer flue gas difference in height that sprays into the position is 1.0～1.5 times of the both sides degree of depth before and after the desulfurizing tower up and down.Wherein, the jet direction of upper strata flue gas is-10 °～-20 ° with the angle of trunnion axis on a vertical plane, and the jet direction of lower floor's flue gas is+5 °～-5 ° with the angle of trunnion axis on a vertical plane, and the effluxvelocity of two-layer flue gas is 40～80m/s up and down.The flue gas on another road 10～30% is by being installed in the flue gas air-distribution device at gas approach 6 places, bottom, upwards in desulfurizing tower, evenly give wind from the bottom of desulfurizing tower lower area 3 with the flow velocity of 0.5～5m/s, exhaust gas volumn can be regulated as required, make the demand that reaches normal fluidization in the desulfurizing tower, to guarantee desulfurizing tower bottom particle proper flow.Therefore, under the guiding function of main flue gas jet, the desulfurizing tower lower reaction zone has formed desulphurization reaction flow field in the tower with vertical clockwise or counterclockwise vortex flow field structure.The size of tower inside vortex, power can be injected speed and inject angle and regulate by regulating main flue gas.
Simultaneously, desulfurizing agent raw materials of Ca O powder is sent into desulfurizing agent prepare in the digestive system 14, generate highly active Ca (OH) through digestion reaction
2Sorbent particle.With digestion back particle size range is the sorbent particle of 1～10 μ m, is sprayed in the desulfurizing tower by the sorbent particle entrance 15 on desulfurizing tower lower area 3 front side walls.The position that on the rear wall of desulfurizing tower lower area 3, is higher than sorbent particle entrance 15; be furnished with the external recirculation particle feedback outlet 9 that links to each other with fume dust remover 8, will spray into the desulfurizing tower from here from fume dust remover 8 isolated recirculation sorbent particles.Sidewall at desulfurizing tower lower area 3, be furnished with water atomizing nozzle 12, the atomizing cooling water that it sprayed can make sorbent particle and atomized water particle that strong turbulent heat transfer mass transfer exchange takes place, reduce the temperature in the desulfurization reaction tower on the one hand, form water membrane on the sorbent particle surface on the other hand, keep its surperficial high reaction activity and high.
Like this; enter the need desulfurization flue gas of desulfurizing tower lower area 3; mix with atomizing cooling water that sprays into from the highly active desulfurization agent particle of sorbent particle entrance 15 spirts, from water atomizing nozzle 12 and the recirculation sorbent particle of coming in, strong three-phase turbulent heat transfer mass transfer exchange takes place from external recirculation particle feedback outlet 9.Between cigarette temperature drop to 55～70 in the above-mentioned tower ℃, be higher than 5～15 ℃ of the interior flue gas dew point temperature of tower, also can be under some situation in about 80 ℃ operations of cigarette temperature, most of sorbent particle particle diameter is vertical Scrawl fluidized suspension attitude in the whole desulfurizing tower between 1～5 μ m.Under the effect in vertical type flow field, whirlpool, part large granular materials is separated from flue gas under the effect of inertia force, be deposited to the desulfurizing tower bottom to peripheral the flowing of eddy current, under the effect of desulfurizing tower bottom fluidization flue gas, move upward again, circulate and so forth, not only strengthened the interior internal circulating load of sorbent particle in desulfurizing tower, made the interior internal circulating load of sorbent particle can reach 30～70%.And reduced burden to outside gas-solid separating device.Simultaneously because the flue gas stroke is longer, that is increase sorbent particle and the haptoreaction time of flue gas in desulfurization reaction tower, helped the raising with desulfuration efficiency of making full use of of sorbent particle.
In order further to improve desulfurized effect, the present invention also adopts segmentation water spray mode, at the middle hypomere of desulfurizing tower upper area 5, has set up the water atomizing nozzle 12 of 1～2 layer of segmentation humidification in one-sided or both sides along radial direction.Water atomizing nozzle 12 adopts the nozzle of position adjustable atomizing sprays, its collapsing length, swings up and down angle and the angle that swings all can be regulated.In desulfurizing tower upper area 5 because the moisture on desulfurizing agent surface is evaporated to water vapour basically, make the reactivity on desulfurizing agent surface reduce, adopt above-mentioned segmentation water spray mode after, the reactivity on desulfurizing agent surface is further strengthened.Particularly at sulfur dioxide and desulfurizing agent Ca (OH)
2In the reaction, the reaction between the ion accounts for very big share, sprays water by segmentation and can improve the completeness of desulphurization reaction greatly, and desulfuration efficiency is significantly improved.
In order to strengthen the flue gas turbulence intensity of desulfurization middle and later periods, the present invention also adopts the combination smoke mode of jet, middle hypomere at desulfurizing tower upper area 5, along the combination smoke jet nozzle 4 of radial direction under one-sided or both sides layout 1～4 course, 10～30% the cleaning after fume dust remover 8 separates is contained wet flue gas as medium, flow velocity with 90～120m/s sprays in the desulfurizing tower, the high intensity turbulent that further forms the desulfurizing tower middle part is mixed, strengthen the intensity of total desulphurization reaction, improve the reaction efficiency in desulphurization reaction later stage.Certainly, also can be directly the flue gas without fume dust remover 8 separating treatment uses as medium after the flue gas of desulfurization or the desulfurization with needing.
After flue gas enters desulfurizing tower upper area 5; sorbent particle presents bigger falling trend substantially; most of particle moves downward along near the sidewall, because upper area 5 adopts complex cross-sectional variation structure, can further strengthen the nitrate recirculation ratio rate of sorbent particle.After the sorbent particle of interior circulation is got back to desulfurizing tower lower area 3; to be driven by flue gas again again and move upward back and forth; 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.Sulfur in smoke SO in tower
2With desulfurizing agent Ca (OH)
2Reaction generates calcium sulfite or calcium sulfate, and can deviate from a spot of sulfur trioxide SO in the flue gas simultaneously
3, and the pernicious gas compositions such as HCl, HF that may exist, desulfuration efficiency can reach more than 90% at least.
Again, flue gas is drawn by the desulfurizing tower exhanst gas outlet 7 at desulfurizing tower upper area 5 tops, enters in the fume dust remover 8.Fume dust remover 8 can be electrostatic precipitator, sack cleaner or their combination; the particle that carries in this flue gas is separated; wherein also contain quite a few not sorbent particle of complete reaction; in order to improve sorbent utilization; by external recirculation particle feedback outlet 9; they are sent back to carry out external particle recirculation in the desulfurizing tower lower area 3; and the granule that has reacted major part 1～2 μ m that finishes no longer participates in circulation, and promptly desulfuration byproduct and flying dust are then sent into cinder tank 10 storages and transported.Send into chimney 13 from the clean flue gas up to standard that fume dust remover 8 comes out through main induced draft fan 11, enter atmosphere at last.
Claims (10)
1. the dry flue gas desulphurization method of a vertical whirlpool type circulating fluidization, comprise the preparation digestion of desulfurizing agent, desulphurization reaction in the desulfurization reaction tower, the separation and the recirculation of outside sorbent particle, it is characterized in that: will need the flue gas of desulfurization to be divided into two-way, one road flue gas is by the flue gas ejection accelerating apparatus, the differing heights position of both sides sprays into the desulfurizing tower respectively before and after the desulfurizing tower lower area, its at the middle and upper levels the jet direction of flue gas be-5 °～-45 ° with the angle of trunnion axis on a vertical plane, the jet direction of lower floor's flue gas is+15 °～-55 ° with the angle of trunnion axis on a vertical plane, and the effluxvelocity of two-layer flue gas is 30～100m/s up and down; Another road flue gas is by the flue gas air-distribution device, upwards in desulfurizing tower, evenly give wind from the bottom of desulfurizing tower lower area with the flow velocity of 0.1～10m/s, make flue gas in the desulfurizing tower lower area, do vertical eddying motion, formation has the interior desulphurization reaction flow field of tower of vertical turbulent structure, thereby makes flue gas and sorbent particle that violent hybrid reaction take place in desulfurizing tower.
2. the dry flue gas desulphurization method of vertical whirlpool according to claim 1 type circulating fluidization is characterized in that: the said difference in height that sprays into the position of two-layer flue gas up and down is 1.0～1.5 times of both sides, the desulfurizing tower front and back degree of depth.
3. the dry flue gas desulphurization method of vertical whirlpool according to claim 1 type circulating fluidization, it is characterized in that: the jet direction of said upper strata flue gas is-10 °～-20 ° with the angle of trunnion axis on a vertical plane, the jet direction of lower floor's flue gas is+5 °～-5 ° with the angle of trunnion axis on a vertical plane, and the effluxvelocity of two-layer flue gas is 40～80m/s up and down.
4. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: saidly spray into road exhaust gas volumn in the desulfurizing tower lower area by the flue gas ejection accelerating apparatus and account for 60～95% of the flue gas total amount that needs desulfurization, said another road exhaust gas volumn that is blown into desulfurizing tower lower area bottom by the flue gas air-distribution device accounts for 5～40% of the flue gas total amount that needs desulfurization.
5. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: the degree of depth of said desulfurizing tower lower area is 1.0～2.0 times of the desulfurizing tower upper area degree of depth, the variation structure that the desulfurizing tower upper area adopts cross sectional shape to change arbitrarily.
6. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: fresh sorbent particle, recirculation sorbent particle and atomized water are sprayed into the desulfurizing tower from the desulfurizing tower lower area.
7. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: adopt segmentation water spray mode, middle hypomere at desulfurizing tower lower area and upper area, the water atomizing nozzle of 1～4 layer of segmentation decreasing temperature and increasing humidity is set in one-sided or both sides along radial direction, wherein: the distance at the position of the orlop nozzle of hypomere and desulfurizing tower lower area top is 300～2000mm in the upper area, and the distance between each layer nozzle is 800～1500mm.
8. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: adopt the combination smoke mode of jet, arrange that along radial direction flue gas jet nozzle under 1～4 course, the cleaning after outside deduster separates with 10～30% contain wet flue gas and spray in the desulfurizing tower with the flow velocity of 30～180m/s at the middle hypomere of desulfurizing tower upper area in one-sided or both sides.
9. according to the dry flue gas desulphurization method of claim 1 or 2 or 3 described vertical whirlpool type circulating fluidizations, it is characterized in that: said flue gas ejection accelerating apparatus adopts the Rafael nozzle and the combination thereof of lower resistance.
10. the dry flue gas desulphurization method of vertical whirlpool according to claim 7 type circulating fluidization, it is characterized in that: adopt the combination smoke mode of jet, arrange that along radial direction flue gas jet nozzle under 1～4 course, the cleaning after outside deduster separates with 10～30% contain wet flue gas and spray in the desulfurizing tower with the flow velocity of 30～180m/s at the middle hypomere of desulfurizing tower upper area in one-sided or both sides.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101721907B (en) * | 2010-02-03 | 2011-09-28 | 上海交通大学 | Flue gas desulfurizing method for W-shaped multi-fluid alkaline spray generator |
| CN102423625A (en) * | 2011-11-29 | 2012-04-25 | 南京龙玖环境工程有限公司 | Circulating fluidized bed flue gas desulfurization tower |
| CN105107366A (en) * | 2015-09-17 | 2015-12-02 | 北京科大朗涤环保工程技术有限公司 | Direct flow spraying semi-dry type flue gas desulfurization method |
| CN111518592A (en) * | 2020-05-11 | 2020-08-11 | 宋青 | Coke oven gas desulfurizing tower |
| CN112675691A (en) * | 2020-12-15 | 2021-04-20 | 中冶京诚工程技术有限公司 | Flue gas semi-dry desulfurization system and desulfurization method |
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2003
- 2003-08-19 CN CN 03125295 patent/CN1239233C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101721907B (en) * | 2010-02-03 | 2011-09-28 | 上海交通大学 | Flue gas desulfurizing method for W-shaped multi-fluid alkaline spray generator |
| CN102423625A (en) * | 2011-11-29 | 2012-04-25 | 南京龙玖环境工程有限公司 | Circulating fluidized bed flue gas desulfurization tower |
| CN105107366A (en) * | 2015-09-17 | 2015-12-02 | 北京科大朗涤环保工程技术有限公司 | Direct flow spraying semi-dry type flue gas desulfurization method |
| CN111518592A (en) * | 2020-05-11 | 2020-08-11 | 宋青 | Coke oven gas desulfurizing tower |
| CN111518592B (en) * | 2020-05-11 | 2021-08-24 | 新疆金晖兆丰焦化有限公司 | Coke oven gas desulfurization method |
| CN112675691A (en) * | 2020-12-15 | 2021-04-20 | 中冶京诚工程技术有限公司 | Flue gas semi-dry desulfurization system and desulfurization method |
| CN112675691B (en) * | 2020-12-15 | 2024-04-26 | 中冶京诚工程技术有限公司 | Flue gas semi-dry desulfurization system and desulfurization method |
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| CN1239233C (en) | 2006-02-01 |
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