CN1491739A - Smoke desulfurizing process by circulation fluid state dry method of layered feed back - Google Patents
Smoke desulfurizing process by circulation fluid state dry method of layered feed back Download PDFInfo
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- CN1491739A CN1491739A CNA031253040A CN03125304A CN1491739A CN 1491739 A CN1491739 A CN 1491739A CN A031253040 A CNA031253040 A CN A031253040A CN 03125304 A CN03125304 A CN 03125304A CN 1491739 A CN1491739 A CN 1491739A
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- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 18
- 230000008569 process Effects 0.000 title claims abstract description 5
- 239000000779 smoke Substances 0.000 title description 8
- 239000012530 fluid Substances 0.000 title description 3
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 238000005516 engineering process Methods 0.000 claims abstract description 26
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 239000002245 particle Substances 0.000 claims description 129
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 78
- 239000003546 flue gas Substances 0.000 claims description 78
- 239000002594 sorbent Substances 0.000 claims description 72
- 238000006477 desulfuration reaction Methods 0.000 claims description 44
- 230000023556 desulfurization Effects 0.000 claims description 36
- 238000005243 fluidization Methods 0.000 claims description 21
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 230000029087 digestion Effects 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 2
- 239000003517 fume Substances 0.000 abstract description 3
- 230000000903 blocking effect Effects 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract 1
- 239000000428 dust Substances 0.000 description 10
- 239000008187 granular material Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 5
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- 238000005453 pelletization Methods 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
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- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 239000003818 cinder Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
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Abstract
The present invention relates to external grain re-circulating technology in large circular fluidizing dry fume desulfurizing system. The desulfurizing process includes preparing desulfurizing agent, desulfurizing reaction inside the desulfurizing reaction tower and external desulfurizing agent grain separation and re-circulation. In the external grain re-circulation, the returned material is two-stage separated and re-circulated, the grains separated by the first stage and the second stage desulfurizing agent grain separator are fed to the fluidizing region in the lower part of the desulfurizing reaction tower separately through different re-circulation inlets, resulting in raised desulfurizing agent grain utilization and desulfurizing reaction efficiency. Compared with available technology, the present invention has much higher fume dedusting efficiency, high desulfurizing efficiency up to 92 % at Ca/S of 1.1-1.3, less adhesion and blocking in the lower desulfurizing tower part and lowered load of the desulfurizing agent grain separator.
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 a kind of circulating fluidization dry flue gas desulphurization technology that adopts the layering feed back 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 etc. that responds.
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.
Publication number is that what introduced in the Chinese invention patent prospectus of CN1307926A is the circulating fluidization dry flue gas desulphurization technology that adopts a flue gas ash removal and feeding back device.The reverse-flow type circulating fluid bed flue-gas desulfurizing technology that and for example German Wulff company adopts is that the feedback outlet by a fume dust remover and a recirculation carries out the recirculation of sorbent particle.But, adopt the dry flue gas desulphurization technology of above-mentioned single feed back mode still to have following defective: at first, owing to adopt single deduster and feedback outlet, make that recirculation particle grain size excursion is bigger, cause collision and solid particle between the interior solid particle of desulfurizing tower insufficient with contacting of flue gas, the mixing of flue gas and sorbent particle weakens, and then has influenced the utilization rate and the desulfuration efficiency of desulfurizing agent.Secondly, because the less sorbent particle of particle diameter is more, and its caking property of the sorbent particle of small particle diameter is very strong, is formed on easily to form on desulfurizing tower bottom and the inclined-plane, bottom to bond and phenomenon of blocking on desulfurizing tower bottom and the inclined-plane, bottom.In addition, after the dry flue gas desulphurization unit maximizes, its feed back amount increases morely, adopt single feed back mode can increase the burden of dust pelletizing system and feed back pipeline greatly, not only can influence the dust removing effects of dust pelletizing system, it is up to standard to make that the discharging of dust is difficult to, and can be because the security decline of dust pelletizing system and feed back pipeline influence the normal operation of whole unit.
Summary of the invention
Purpose of the present invention will overcome existing defective in the above-mentioned prior art exactly, a kind of circulating fluidization dry flue gas desulphurization technology of layering feed back is provided, adopt this technology can guarantee that heterogeneous flow field is organized more rationally in the desulfurizing tower, and the particle recirculating technique requirement in the dry flue gas desulphurization system that is specially adapted to maximize, realize very high flue gas ash removal efficient, simultaneously be issued to higher desulfuration efficiency, and alleviate the bonding of desulfurization reaction tower bottom and the burden of obstruction and sorbent particle separator in situation than low calcium-sulphur ratio.
For realizing this purpose, technical scheme of the present invention is the circulating fluidization dry flue gas desulphurization technology of layering feed back, comprises the separation and the recirculation of desulphurization reaction, outside sorbent particle in desulfurizing agent preparation digestion, the desulfurization reaction tower.
The present invention is in the external particle process recycling of desulfurization reaction tower, feed back has adopted two-stage particle separation and recirculation, and the first order and the isolated particle of second level sorbent particle separator are sent into desulfurization reaction tower bottom fluidisation area by the first order and second level sorbent particle recirculation inlet respectively and carried out particle recirculation.
The circulating fluidization dry flue gas desulphurization technology of described layering feed back is characterized in that: the flue gas that comes out from desulfurization reaction tower passes through first order sorbent particle separator and second level sorbent particle separator successively.
The circulating fluidization dry flue gas desulphurization technology of described layering feed back; it is characterized in that: first order sorbent particle recirculation inlet is above second level recirculation particle feed back inlet; with the highly about 500～1000mm of its distance; second level recirculation particle feed back inlet is above sorbent particle feed inlet opposite side, with the highly about 500～1000mm of its distance.
The circulating fluidization dry flue gas desulphurization technology of described layering feed back, it is characterized in that: the separative efficiency of first order sorbent particle separator is 20%～80%, wherein the separative efficiency for the above particle of＞8 μ m is more than 80%, and the particle that this grade sorbent particle separator is separated is all sent desulfurizing tower back to, continues to participate in desulphurization reaction as the recirculation particle.
The circulating fluidization dry flue gas desulphurization technology of described layering feed back, it is characterized in that: the separative efficiency of second level sorbent particle separator is more than 99%, 50%～99% particle of wherein separating is sent desulfurizing tower back to, continue to participate in desulphurization reaction as the recirculation particle, and the following particle of most 2 μ m will directly be delivered to grey storehouse, no longer participate in recirculation.
Compared with prior art, the invention has the advantages that:
At first, owing to adopted layering feed back technology, make to the control of the recirculation grain diameter of feed back more accurate, because the position that the feedback outlet of the recirculation particle of greater particle size leans in the desulfurizing tower bottom, than the feedback outlet of the recirculation particle of small particle diameter the desulfurizing tower bottom by under the position, because granule moves upward, bulky grain moves downward, so not only increased the oarse-grained stop reaction time, and strengthened the building that bumps between granule and the bulky grain, improve the flow field structure in the desulfurizing tower, thereby improved the utilization rate and the desulfuration efficiency of desulfurizing agent, between calcium sulfur ratio Ca/S=1.1～1.3, can reach the desulfuration efficiency more than 92%.
Second; the bulky grain feed back inlet that the present invention separates the first order is arranged in the top of second level recirculation particle feed back inlet; because oarse-grained momentum is bigger; flow downward comparatively strongly in this entrance area formation; and can fully drive the recirculation granule of separating (or pushing down) second level and also move downward; avoiding granule one to enter desulfurizing tower is promptly taken away by flue gas; strengthened simultaneously between the size particles collision frequency; help to break the surface reaction product of sorbent particle; improve the utilization rate of sorbent particle, improved the utilization rate and the desulphurization reaction efficient of desulfurizing agent.
The 3rd; because the recirculation bulky grain is arranged in the top of all particle inlets; and major part is complete reaction not; in the time of in it enters desulfurization reaction tower; because the particle momentum very big (very big) that refluxes mainly due to backflow particle gross mass; sedimentation downwards earlier; mixed flow then again makes progress under the fluidisation wind action; and participation desulphurization reaction; if feedback outlet pastes the desulfurization reaction tower wall and arranges; then the feed back particle can be along under the desulfurization reaction tower internal face sticking wall flow; help washing away the desulfurizing tower internal face like this; thereby alleviated should the zone the wall bonding and the obstruction of desulfurizing tower bottom because tower interior gas-solid liquid phase turbulent flow and mixing intensity are strengthened in the sedimentation meeting of feed back, also help improving desulphurization reaction efficient.
The 4th, for the dry flue gas desulphurization technology that maximizes, its feed back amount is bigger, the present invention is owing to adopted layering feed back technology, the recirculation particle is separated by the two-stage dust pelletizing system, rather than adopt single-stage dust pelletizing system and recirculation to enter the mouth, first order inertial separator of the present invention like this can be isolated the recirculation particle of considerable part, thereby adopt the unit burden alleviated the sorbent particle separator greatly, solved to a certain extent that maximization dry flue gas desulphurization equipment faced important technological problems.
Description of drawings
Fig. 1 desulphurization system structural representation of the present invention;
Fig. 2 the present invention adopts the desulphurization system structural representation of combination smoke jet.
Among the figure: flue gas pre-dedusting device 1, flue gas mixing-chamber 2, flue gas ejection accelerating apparatus 3, desulfurization reaction tower 4, desulfurizing tower bottom fluidisation area 4-1, desulfurizing tower exhanst gas outlet 5, water atomizing nozzle 6, the digestive system 7 of desulfurizing agent preparation, sorbent particle entrance 8, first order sorbent particle separator 9 (inertia separator), first order sorbent particle recirculation inlet 10, second level sorbent particle separator 11 (electrostatic separation or cloth bag separator), second level sorbent particle recirculation inlet 12, cinder tank 13, main induced draft fan 14, chimney 15, clean flue gas recirculation conduit 16, combination smoke jet nozzle 17.
The specific embodiment
Circulating fluidization dry flue gas desulphurization technology when below in conjunction with accompanying drawing the present invention being adopted two-layer feed back is described in further detail:
At first, the flue gas of discharging from combustion apparatus is through a flue gas pre-dedusting device 1 (as electrostatic precipitator, sack cleaner, inertial separation deduster or their combining form), remove in the flue gas about 85% flying dust, send in the flue gas mixing-chamber 2 through the flue gas after the pre-dedusting, upwards spray the bottom that enters desulfurization reaction tower 4 by flue gas ejection accelerating apparatus 3 (for example Venturi nozzle), the muzzle velocity scope of keeping the flue gas jet is 30～55m/s.
Simultaneously, desulfurizing agent raw material (as the CaO powder) being sent in the digestive system 7 of desulfurizing agent preparation, generated highly active sorbent particle through digestion reaction, is that the desulfurizing agent of 1～10 μ m is (as Ca (OH) with digestion back particle size range
2) particle, spray into the bottom fluidisation area 4-1 of desulfurization reaction tower by sorbent particle entrance 8.The same side on the top, sorbent particle entrance 8 position of desulfurization reaction tower lower area 4-1 is furnished with water atomizing nozzle 6, and the opposite side on top, sorbent particle entrance 8 position is furnished with second level sorbent particle recirculation inlet 12.The same side on second level sorbent particle recirculation inlet top, 12 position is furnished with second level sorbent particle recirculation inlet 10.Lower area 4-1 that flue gas enters desulfurization reaction tower and the atomizing cooling water that sprays into from the highly active desulfurization agent particle of sorbent particle entrance 8 spirts, by water atomizing nozzle 6; with the particle of separating from first order sorbent particle separator 9 and second level sorbent particle separator 11; promptly recycle the recirculation sorbent particles mixing that inlet 12 is come in from first order sorbent particle recirculation inlet 10 and second level sorbent particle, strong three-phase turbulent heat transfer mass transfer exchange takes place in the three.Cigarette temperature drop (be higher than the interior flue gas dew point temperature of tower 5-15 ℃ between) between 55-70 ℃ in the above-mentioned tower also can be in about 80 ℃ operations of cigarette temperature under some situation, and big 12 partial desulfurization agent particle grain size are between 1-5 μ m.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.
Wherein, from first order sorbent particle recirculation inlet 10 particle grain size that enter desulfurization reaction tower lower area 4-1 is 8～30 μ m, because grain diameter is bigger, make the momentum of its momentum greater than flue gas, so near the flue gas reaching under the percussion of particle flows downward herein, the recirculation particle is directly fallen the bottom of desulfurization reaction tower 4 or is flowed downward along the inclined-plane, bottom of desulfurization reaction tower 4, get back to the bottom of desulfurization reaction tower 4, the part recirculation particle that flows downward along the inclined-plane, bottom of desulfurization reaction tower 4 has certain effect for the bonding and the obstruction that alleviate inclined-plane, desulfurizing tower bottom.
Because first order sorbent particle recirculation inlet 10 is positioned at the desulfurizing tower bottom by last position; and the recirculation grain diameter that enters is bigger; and second level sorbent particle recirculation inlet 12 be positioned at the desulfurizing tower bottom by under the position; from second level sorbent particle recirculation inlet 12 particle grain size that enter desulfurization reaction tower 4 is 2～10 μ m; because grain diameter is less; though the flue gas flow rate in empty cross section is higher herein; but under the effect of the oarse-grained downward momentum of recirculation on top; certain trend that flows downward can be pushed down and also become to granule by bulky grain; or direct and bulky grain collision; and collision frequency is higher; so not only increased the oarse-grained stop reaction time; and strengthened collision between granule and the bulky grain; help to break the surface reaction product of sorbent particle; improve the flow field structure in the desulfurizing tower, thereby improved the utilization rate and the desulfuration efficiency of desulfurizing agent.In addition, regulate the ratio of the feed back amount of first order sorbent particle recirculation inlet 10 and second level sorbent particle recirculation inlet 12, also can reasonably regulate the flow field structure in the desulfurization reaction tower 4, and the load that can reasonably distribute first order sorbent particle separator 9 and second level sorbent particle separator 11 is to reach the ruuning situation of highly effective and safe.
Middle and upper part at desulfurizing tower; the tower endoparticle presents bigger falling trend substantially; most of particle moves downward along near the sidewall; arrive behind the bottom of desulfurizing tower because the flue gas flow rate of desulfurizing tower bottom is higher; particle is driven by flue gas again and moves 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.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.
Again, flue gas is drawn by the exhanst gas outlet 5 at desulfurization reaction tower 4 tops, enter first order sorbent particle separator 9 (inertial separation deduster), its separative efficiency is 60%, wherein the separative efficiency for the above particle of＞8 μ m is more than 80%, be that bulky grain major part in the flue gas is separated, owing to wherein also contain some unreacted sorbent particle, in order to improve sorbent utilization, by first order sorbent particle recirculation inlet 10 particle of separating is all sent back to and to carry out particle recirculation in the desulfurizing tower.The flue gas of deviating from behind most of bulky grain by first order sorbent particle separator 9 top discharges enters second level sorbent particle separator 11 (as electrostatic precipitator, sack cleaner or their combining form), the entrained remainder particulate overwhelming majority of flue gas is separated, its separative efficiency is more than 99%, wherein yet contain some unreacted sorbent particle, in order to improve sorbent utilization, by second level sorbent particle recirculation inlet 12 wherein isolated about 90% particle send back in the desulfurizing tower again, no longer participate in recirculation and reacted most of granule (less than 2 μ m) of finishing, promptly desulfuration byproduct and flying dust are then sent into cinder tank 13 storages, transhipment is walked.From the clean flue gas up to standard that second level sorbent particle separator 11 comes out, send into chimney 15 through main induced draft fan 14, enter atmosphere at last.
Method as shown in Figure 2, also basic identical with said method, just it has increased the flue gas mode of jet.The feature of flue gas mode of jet is to arrange the combination smoke jet nozzle of introducing through clean flue gas recirculating system 16 17 at the middle part of desulfurization reaction tower 4, cleaning after the desulfurization is contained wet flue gas to be sent into and carries out flue gas recirculation in the fluidization desulfurizing tower, to form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the intensity of total desulphurization reaction.Take away by clean flue gas recirculating system 16 from the clean flue gas up to standard that second level sorbent particle separator 11 comes out, carry out flue gas recirculation, all the other then send into chimney 15 through main induced draft fan 14, enter atmosphere at last.The recirculation cleaning of being taken away by clean flue gas recirculating system 16 contains wet flue gas, pass through downwards at combination smoke jet nozzle 17 one-sided or that both sides are arranged at the middle part of desulfurization reaction tower 4, flow velocity with 90～120m/s sprays in the desulfurizing tower, to guarantee that strong three-phase turbulent heat transfer mass transfer exchange takes place between sorbent particle, atomizing cooling water and this three of jet flue gas to be mixed.Simultaneously, because the water capacity of flue gas recycled itself is higher than normal dry air, reduced required injection flow rate in the desulfurization reaction tower to a certain extent.Clean flue gas up to standard is extracted point out in the outlet and the pipeline between the chimney 15 of second level sorbent particle separator 11, the clean wet flue gas amount that contains of recirculation is 10～30% of total discharging exhaust gas volumn, can regulate, reach the requirement of 5～20 ℃ of desulfurizing tower inlet flue gas coolings.
Claims (5)
1. the circulating fluidization dry flue gas desulphurization technology of a layering feed back, comprise the separation and the recirculation of desulphurization reaction, outside sorbent particle in desulfurizing agent preparation digestion, the desulfurization reaction tower, it is characterized in that: in the external particle process recycling of desulfurization reaction tower, feed back has adopted two-stage particle separation and recirculation, and the first order and the isolated particle of second level sorbent particle separator are sent into desulfurization reaction tower bottom fluidisation area by the first order and second level sorbent particle recirculation inlet respectively and carried out particle recirculation.
2. the circulating fluidization dry flue gas desulphurization technology of layering feed back according to claim 1 is characterized in that: the flue gas that comes out from desulfurization reaction tower passes through first order sorbent particle separator and second level sorbent particle separator successively.
3. the circulating fluidization dry flue gas desulphurization technology of layering feed back according to claim 1; it is characterized in that: first order sorbent particle recirculation inlet is above second level recirculation particle feed back inlet; with the highly about 500～1000mm of its distance; second level recirculation particle feed back inlet is above sorbent particle feed inlet opposite side, with the highly about 500～1000mm of its distance.
4. the circulating fluidization dry flue gas desulphurization technology of layering feed back according to claim 1, it is characterized in that: the separative efficiency of first order sorbent particle separator is 20%～80%, wherein the separative efficiency for the above particle of＞8 μ m is more than 80%, and the particle that this grade sorbent particle separator is separated is all sent desulfurizing tower back to, continues to participate in desulphurization reaction as the recirculation particle.
5. the circulating fluidization dry flue gas desulphurization technology of layering feed back according to claim 1, it is characterized in that: the separative efficiency of second level sorbent particle separator is more than 99%, 50%～99% particle of wherein separating is sent desulfurizing tower back to, continue to participate in desulphurization reaction as the recirculation particle, and the following particle of most 2 μ m will directly be delivered to grey storehouse, no longer participate in recirculation.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125304 CN1225304C (en) | 2003-08-21 | 2003-08-21 | Smoke desulfurizing process by circulation fluid state dry method of layered feed back |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 03125304 CN1225304C (en) | 2003-08-21 | 2003-08-21 | Smoke desulfurizing process by circulation fluid state dry method of layered feed back |
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| Publication Number | Publication Date |
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| CN1491739A true CN1491739A (en) | 2004-04-28 |
| CN1225304C CN1225304C (en) | 2005-11-02 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103041693A (en) * | 2012-12-24 | 2013-04-17 | 攀钢集团攀枝花钢钒有限公司 | Desulfurization process for rapidly building stable circulating fluidized bed and device |
| CN103084058A (en) * | 2013-01-31 | 2013-05-08 | 浙江浙大海元环境科技有限公司 | Flue gas dry desulfurization device |
| CN109731457A (en) * | 2019-02-20 | 2019-05-10 | 南京金瀚环保科技有限公司 | A kind of flue gas step desulfurizer and its sulfur method |
-
2003
- 2003-08-21 CN CN 03125304 patent/CN1225304C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103041693A (en) * | 2012-12-24 | 2013-04-17 | 攀钢集团攀枝花钢钒有限公司 | Desulfurization process for rapidly building stable circulating fluidized bed and device |
| CN103084058A (en) * | 2013-01-31 | 2013-05-08 | 浙江浙大海元环境科技有限公司 | Flue gas dry desulfurization device |
| CN103084058B (en) * | 2013-01-31 | 2014-01-29 | 浙江浙大海元环境科技有限公司 | Flue gas dry desulfurization device |
| CN109731457A (en) * | 2019-02-20 | 2019-05-10 | 南京金瀚环保科技有限公司 | A kind of flue gas step desulfurizer and its sulfur method |
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| CN1225304C (en) | 2005-11-02 |
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