CN1169604C - Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower - Google Patents
Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower Download PDFInfo
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- CN1169604C CN1169604C CNB02147821XA CN02147821A CN1169604C CN 1169604 C CN1169604 C CN 1169604C CN B02147821X A CNB02147821X A CN B02147821XA CN 02147821 A CN02147821 A CN 02147821A CN 1169604 C CN1169604 C CN 1169604C
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Abstract
The present invention provides a combined cycle type fluidization dry flue gas desulfurization process and a desulfurization reaction tower. The process has characteristics that quicklime is used as raw material of desulfurizing agents, and processed by a simple digestion system used for fluidizing clean dampish flue gas to form high surface active lime hydrate as desulfurizing agents; the system adopts three recirculation arrangement methods, namely the designs of desulfurizing agent particle inner circulation, desulfurizing agent particle outer circulation, and recirculation of clean dampish flue gas. Compared with the prior art, firstly, the desulfurization efficiency of the present invention can reach more than 90 to 92% under the condition of lower calcium sulfur ratio (Ca/S = 1.1 to 1.3); secondly, the present invention has the characteristic of wide turndown ratio and can meet the requirement that combustion equipment high efficiency desulphurization under the condition of 20% to 110% load variation; thirdly, the water consumption and the carrying water quantity of the clean flue gas are reduced; fourthly, the quicklime is used as raw material of desulphurization, and a simplified digestive system is adopted so as to reduce the investment and the operation cost.
Description
Technical field
The present invention relates to a kind of combined-circulation formula fluidization dry flue gas desulphurization technology, belong to the flue gas desulfurization technique field, dry method desulfuration system and technology in the particularly various 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.
For dry method (semidry method) desulfur 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; 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 etching problem, system be to the influence of many-sided factors such as the adaptability problem of load, water consumption size.
Flue gas circulating fluidized bed desulfurization by dry method for present application, mostly utilize postdigestive lime (slurry) as absorbent, the material of separating with absorbent and external separator is as the circulation fluidized bed material, is used for pernicious gas in the flue gas by strong gas-solid liquid three-phase in fluid bed reacting tower.This is on the one hand owing to adopt the lime white system, not only technological process complexity, and floor space is big, and mortar transports easy fouling of pipeline and obstruction, and the operation and maintenance cost that has increased system is used.For adopting the calcium hydroxide system, as patent CN86108755A, its operating cost costliness, and hydrated lime particle (Ca (OH)
2) surface-active be difficult for to guarantee, only be applicable to the desulfurization requirement of heavy duty boiler unit from the sexual valence.
At these problems, many new dry method desulfuration systems and technology were proposed again over past ten years, as Chinese invention patent CN1307926, it mixes the material of formation as desulfurizing agent by a certain percentage with dry lime (CaO) and flue gas flying dust and water, send in the fluid bed reacting tower, the interior separator that has increased simultaneously a similar boiler furnace arch, furnace nose in fluid bed reacting tower increases the interior internal circulating load of sorbent particle, and has arranged the gas-solid separating device of an impacting type outside desulfurizing tower." the reverse-flow type circulating fluid bed flue-gas desulfurizing technology " of and for example German Wulff company adopts the comparatively complicated digestive system of a cover that dry lime is digested to calcium hydroxide as desulfurizing agent, and interior separator is set in reaction tower equally.These two technology all adopt the flue gas induction apparatus of venturi type in order to reduce the flue gas resistance of reaction tower.Because the temperature range of desulphurization reaction is narrower, the desulfurization reaction tower of these two technology all adopts water spray that flue-gas temperature is dropped to suitable scope.Because interior separator (adopting the patent CN1195573 in addition of same facility) is set, has increased flue gas resistance and caused corrosion easily simultaneously.
From as seen last, all there are various problems in above-mentioned all desulfurization by dry method, as clean flue gas to carry the water yield more, or digestive system complexity or the sorbent particle surface-active is relatively poor or resistance is bigger, perishable obstruction or the like, simultaneously since the smoke inlet temperature generally all greater than 120 ℃, and only adopt spray cooling in the tower, reduced the utilization rate of the reaction tower useful space.And all technology all do not have to consider because the combustion apparatus load variations, and exhaust gas volumn diminishes and may cause the normally influence of factor such as fluidisation of fluidized bed reaction system, and Load Regulation is relatively poor.Generally, normally when having solved a problem, caused the generation of other problems.
Summary of the invention
Deficiency and defective at the prior art existence, purpose of the present invention and task provide a kind of novel dry flue gas desulphurization system and technology, adopt fluidization flue gas desulfurization technique, system and the technology of combined-circulation formula, make it be issued to higher desulfuration efficiency (more than 90%～92%) in the situation that guarantees lower calcium sulfur ratio (Ca/S=1.1～1.3), reduce the water yield of carrying of water consumption and clean flue gas simultaneously, guarantee the sorbent particle higher surface activity.Realize the wide regulating ratio characteristic of desulphurization system simultaneously, can satisfy the high-efficiency desulfurization requirement of combustion apparatus from 20% to 110% load variations.State in realization under the purpose prerequisite, and further simplify system, reduce equipment investment and operating cost, reduce flue gas resistance, thus the real purpose that realizes the dry flue gas desulphurization of efficient, wide regulating ratio, low cost, low water consumption.
Technical solution of the present invention:
Combined-circulation formula fluidization dry flue gas desulphurization technology comprises that mainly inner sorbent particle circulation that separates of desulfurization reaction tower and the isolated sorbent particle of outside deduster recycle, and particularly cleaning is contained flue gas that wet flue gas discharges and send into recirculation in the circulating fluidization desulfurization reaction tower in combustion apparatus.Recirculation is clean to contain the 10%-50% that the wet flue gas amount is total burning and exhausting exhaust gas volumn, can regulate.
Described cleaning contains the recirculation of wet flue gas, its recirculation cleaning contains the wet flue gas amount and regulates according to service requirement, reduce the smoke inlet temperature of desulfurization reaction tower on the one hand, make the flue-gas temperature that enters desulfurization reaction tower reduce by 5～20 ℃, on the other hand, because the flue gas recycled amount can regulate easily according to service requirement, widened the load variations adaptive capacity of desulphurization system, can satisfy the high-efficiency desulfurization requirement of combustion apparatus (as boiler etc.) from the 20%-110% load variations.
Described combined-circulation formula fluidization dry flue gas desulphurization technology, the external circulating system that wherein adopts sorbent particle is to adopt gas-solid separating device to send isolated sorbent particle back to desulfurization reaction tower again by the feed back pipeline outside tower, circulation in the particle in tower is up to the sorbent utilization requirement of satisfying design.
Described combined-circulation formula fluidization dry flue gas desulphurization technology, cleaning contain the flue gas of discharging in wet flue gas and the combustion apparatus and upwards inject the reaction tower from the reaction tower bottom by lower resistance flue gas induction apparatus at the flue gas of mixing chamber hybrid cooling.
Described combined-circulation formula fluidization dry flue gas desulphurization technology, spray into the highly active desulfurization agent particle that obtains through digestive system, a part of sorbent particle that sprays into the atomizing cooling water and separate from outside deduster in the desulfurization reaction tower bottom, making needs desulfurization flue gas and sorbent particle, atomized water particle that strong three-phase turbulent heat transfer mass transfer exchange takes place.
Described cleaning contains the flue gas of wet flue gas recirculation and extracts the pipeline any place of point between desulfurization reaction tower exhanst gas outlet and chimney 12 out, and the clean wet flue gas amount that contains of recirculation is as the criterion with requirement that reaches 5-20 ℃ of desulfurization reaction tower inlet flue gas cooling and the exhaust gas volumn demand that satisfies the desulfurization reaction tower normal fluidization.
Advantage of the present invention:
At first, the present invention is owing to adopted the clean recirculating system that contains wet flue gas, the flue gas humidification has also reduced the temperature that enters desulfurization reaction tower, improved the reaction tower space availability ratio, prolonged the smoke reaction room and time, improve sorbent utilization, reduced the water consumption demand to a certain extent relatively, realized the wide control characteristic of desulphurization system load variations simultaneously.The present invention is a raw material with the quick lime of cheapness; adopt a kind of easy digestive system design; the digestion reaction tower has adopted the structural design that is similar to desulfurization reaction tower; three-phase material is strong hybrid reaction in tower; form fluidization preferably and granule interior recirculation characteristic, improved the digestion reaction ability and strengthened postdigestive sorbent particle activity.Digestive system of the present invention, desulfurization reaction tower all adopt the carbon steel manufacturing, and each blower fan does not have special abrasionproof requirement in the system.Therefore the present invention has realized high desulfurization efficiency (can reach the desulfuration efficiency more than 90～92% between calcium sulfur ratio 1.1～1.3), wide regulating ratio (high-efficiency desulfurization that satisfies combustion apparatus 20%～110% load variations requires), the desulfur technology requirement of low investment and operating cost, low water consumption.
Description of drawings
Accompanying drawing 1 is a technological process machine system architecture schematic diagram of the present invention.
Among the figure: 1. quick lime storehouse; 2. mechanical charging gear; 3. digestion reaction tower; 4. cyclone separator; 5. scum pipe; 6. flue gas mixing-chamber; 7. lower resistance flue gas induction apparatus; 8. desulfurization reaction tower, 9. reaction tower smoke outlet tube; 10. deduster (electrostatic precipitator or sack cleaner); 11. main induced draft fan; 12. chimney; 13. flue gas recycled air-introduced machine; 14. cinder tank; 15. digestion tower outlet; 16. the weary gas fairlead of cyclone separator; 17. desulfurizing agent transports pipe; 18. digestion water atomizing nozzle; 19. the decreasing temperature and increasing humidity water atomizing nozzle of desulphurization reaction; 20. advance the flue gas recycled pipe of mixing chamber; 21. advance the flue gas recycled pipe of digestion reaction tower; 22. the particle feed back pipe of external recirculation; 23. lime-ash pipe; 24. main flue gas inlet tube; 25. flue gas recycled fairlead.
The specific embodiment
The first, the present invention has adopted three kinds of egr modes to constitute combined-circulation formula fluidization desulphurization system simultaneously:
1) adopted the interior sorbent particle recirculating technique of desulfurization reaction tower.
Cycle characteristics in the particle of these technology reinforcing desulfuration reaction tower 8 inside.Spray into the highly active desulfurization agent particle that obtains through digestive system, a part of sorbent particle that sprays into the atomizing cooling water and separate from outside deduster in the desulfurization reaction tower bottom, making needs desulfurization flue gas and sorbent particle, atomized water particle that strong three-phase turbulent heat transfer mass transfer exchange takes place.Internal circulating load can reach between 40%～80% in the interior internal circulating load of reinforcing desulfuration agent particle in tower, particle.Under situation about having reduced, prolong the haptoreaction time of sorbent particle to outside gas solid separation reflux wearing and tearing.
2) the external recirculation system of employing sorbent particle.
Return desulfurization reaction tower and adopt gas-solid separating device 10 (electrostatic precipitator or sack cleaner) outward, again send isolated sorbent particle back to desulfurization reaction tower by feed back pipeline 22, circulation in the particle in tower is up to the sorbent utilization requirement of satisfying design (higher).
3) adopt the clean flue gas recirculation system that contains wet flue gas.
On the one hand, the part of the clean flue gas that will obtain through desulfurization and deduster is sent back in the flue gas mixing-chamber 6 of desulphurization reaction tower bottom again, this at first can reduce the smoke inlet temperature of desulfurization reaction tower, make the flue-gas temperature that enters desulfurization reaction tower reduce by 5～20 ℃, be equivalent to increase the effective reaction space of desulfurization reaction tower, and reduced the required injection flow rate requirement of flue gas cool-down; Simultaneously, because the flue gas recycled amount can be regulated easily according to service requirement, widened the load variations adaptive capacity of desulphurization system, this invention can be satisfied the high-efficiency desulfurization requirement of combustion apparatus (as boiler etc.) from the 20%-110% load variations, during especially for the combustion apparatus underrun, by regulating the fluidization requirement that the flue gas recirculation amount can guarantee desulfurization reaction tower equally.On the other hand, the sub-fraction flue gas recycled boosted serve as the fluidizing gas of digestive system in the digestion tower 3 of delivering to quick lime, cancelled and adopted dry air to carry out the fluidisation and the digestion reaction demand of quick lime, can not cause the secondary pollution of air, simultaneously, because the water capacity of flue gas recycled itself is higher than normal dry air, has reduced the required injection flow rate of quicklime slaking to a certain extent.
Second, the present invention adopts quick lime CaO as the desulfurizing agent raw material, fluidization digestive system by a cover simplification, quicklime slaking is become the hydrated lime particle of the high surface of desulphurization reaction needs, and adopt recirculation to contain wet flue gas as fluidizing gas, spray into atomized water in the digestion tower, and the digestion tower is arranged same variation and the variable cross-section design that strengthens cycle characteristics in the particle of adopting, or separator in increasing again, making the calcium hydroxide that satisfies the desulfurization performance requirement just can leave the digestion tower enters in the cyclone separator 4 of digestive system, the sorbent particle that enters cyclone separator 4 is a dry state, and the water capacity of gas-solid mixture is between 8%-16%.After entering cyclone separator, desulfurizing agent gas grain mixture is separated into two parts; wherein most sorbent particles of separating enter into desulfurization reaction tower from the separator bottom through feed pipeline 17 and the injection of strength feeding device; sub-fraction is failed isolated thin sorbent particle and is sent into the gas approach pipeline 24 from separator top through conveying pipe 16 with weary gas, enters desulfurization reaction tower 8 with flue gas.
The 3rd, desulfurization reaction tower reactive agent of the present invention comprises flue gas mixing arrangement 6, lower resistance flue gas induction apparatus 7, desulfurization reaction tower 8 with the strong interior cycle characteristics of particle, the feeding back device of external recirculation sorbent particle and pipeline 22 have desulfurizing agent feed nozzle, water spraying atomization nozzle, the import of external recirculation particle in desulfurization reaction tower 8 lower disposed.The flue gas and the flue gas recycled that produce from combustion apparatus fully mix in mixing chamber by flue gas induction apparatus 7 (can adopt the air distribution plate device of venturi nozzle form or fluid bed), the flue gas that has reduced temperature like this enters desulfurization reaction tower, fully and evenly strengthen at desulphurization reaction tower bottom and sorbent particle, water spraying atomization particle and to contact, on the one hand because the evaporation of particle water further drops to suitable reaction temperature (than the high 5-15 of water dew point temperature in the flue gas ℃ with flue gas, usually between 55～70 ℃), and keep suitable surface appropriateness; On the other hand, owing in tower, form the strong three-phase turbulent flow commutativity and the interior cycle characteristics of sorbent particle, realize the high desulfurization efficiency under the low calcium-sulphur ratio.
Specify preferred forms of the present invention, technical process and system layout structure below in conjunction with accompanying drawing.
At first, send into flue gas mixing-chamber 6 by main flue gas inlet tube 24 from the flue gas that combustion apparatus is discharged, and in 6, contain with the recirculation cleaning that wet flue gas fully mixes, cooling, humidification, inject in the desulfurization reaction tower through the flue gas induction apparatus 7 of lower resistance again.Above-mentioned flue gas inlet tube 24 links to each other with the blast pipe road of digestive system cyclone separator 4; Regulate the flue gas recycled amount, flue gas lower the temperature in mixing chamber 5-20 ℃, the flue gas induction apparatus adopts 5-11 root Venturi tube composition, and the muzzle velocity excursion of keeping the flue gas jet is the 10-26 meter per second.
Simultaneously, desulfurizing agent raw materials of Ca O powder is sent into the bottom of digestion reaction tower 3 through mechanical charging gear 2 by quick lime storehouse 1, its bottom is introduced part recirculation cleaning and is contained wet flue gas, inject the digestion tower through boosting by pipeline 21, and the bottom sprays into atomized water in tower, keep the tower inner bottom part that suitable humidity and fluidized state are arranged, the digestion tower adopts variation and the variable cross-section design that strengthens cycle characteristics in the particle, or a kind of interior separator is adopted in increase, because digestion reaction is exothermic reaction, under fluidization, reaction will cause quicklime particles to be broken, become small particle diameter, the high activity hydrated lime particle of high-specific surface area, the most grain diameters that arrive the outlet of digestion top of tower are between 10-70 μ m, be the dry state material, the water capacity of gas-solid mixture is between 9%-15%, enter again in the cyclone separator 4 of digestive system, the sorbent particle that wherein is separated is through transporting pipe 17, spray into the bottom of desulfurization reaction tower 8 by the pneumatic transport device, remainder is sent in the main flue gas inlet pipeline 24 with cyclone separator top blast pipe 16.
Subsequently; flue gas enters the bottom of desulfurization reaction tower 8; with by 17 the highly active desulfurization agent particles of sending here, by the 19 atomizing cooling waters that spray into from nozzle 85 spirts; and mix from 86 the come in a part of sorbent particles that enter the mouth through 22 from deduster is isolated, strong three-phase turbulent heat transfer mass transfer exchange takes place in the three.Cigarette temperature drop (be higher than in the tower flue gas dew point temperature 5-15 ℃ between) between 55-70 ℃ in the above-mentioned tower, the interior humidity of flue gas of tower maintains between the 12-15%, and the sorbent particle overwhelming majority is Ca (OH)
2, its most of particle diameter is between 10-70 μ m, and sorbent particle surface water capacity remains between 8～15% in the tower.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 desulfurization reaction tower.
In the tower body middle and upper part, substantially present bigger falling trend, and because the variation of inner wall of tower face and variable cross-section design, 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.
Again; flue gas is drawn by the outlet conduit 9 of desulphurization reaction top of tower; enter by (or sack cleaner) in the electrostatic separator 10; the particle that carries in the flue gas is separated; wherein also contain some unreacted sorbent particle, in order to improve sorbent utilization, by a recirculation particle feed back pipe 22; their recirculation is sent back in the desulfurization reaction tower, and desulfuration byproduct that does not circulate and flying dust are then sent into cinder tank and are stored, transport.Taken away by recirculation air-introduced machine 13 from the clean flue gas part up to standard that deduster 10 comes out, carry out flue gas recirculation, all the other then send into chimney 12 by main induced draft fan 11, enter atmosphere at last.By the flue gas recycled that recirculation blower 13 is taken away, wherein major part is sent in the flue gas mixing-chamber 6, and remainder then as the fluidizing gas of digestion tower, through pipeline 21, and boosts and sprays into the bottom of digestion reaction tower 3.
Claims (6)
1. combined-circulation formula fluidization dry flue gas desulphurization technology, mainly comprise inner sorbent particle circulation that separates of desulfurization reaction tower and the isolated sorbent particle recirculation of outside deduster, it is characterized in that cleaning is contained flue gas that wet flue gas discharges in combustion apparatus send in the fluidization desulfurization reaction tower and recycle, recirculation is clean, and to contain the wet flue gas amount be that 10%～50% of total burning and exhausting exhaust gas volumn is regulated.
2. combined-circulation formula fluidization dry flue gas desulphurization technology according to claim 1, it is characterized in that recycling cleaning contains the wet flue gas amount and regulates according to service requirement, reduce the smoke inlet temperature of desulfurization reaction tower, make the flue-gas temperature that enters desulfurization reaction tower reduce by 5～20 ℃, satisfy the exhaust gas volumn demand of the normal fluidization of desulfurization reaction tower under the varying loading operating mode simultaneously.
3. combined-circulation formula fluidization dry flue gas desulphurization technology according to claim 1 and 2, the recirculation that it is characterized in that sorbent particle is to adopt gas-solid separating device outside tower, again send isolated sorbent particle back to desulfurization reaction tower by the feed back pipeline, circulation in the particle in tower is up to the sorbent utilization requirement of satisfying design.
4. combined-circulation formula fluidization dry flue gas desulphurization technology according to claim 1 and 2, it is characterized in that cleaning contains the flue gas of discharging in wet flue gas and the combustion apparatus and mixes at mixing chamber, the flue gas of hybrid cooling is upwards injected the desulfurization reaction tower from the desulphurization reaction tower bottom by lower resistance flue gas induction apparatus.
5. combined-circulation formula fluidization dry flue gas desulphurization technology according to claim 4, it is characterized in that spraying into the highly active desulfurization agent particle that obtains through digestive system in the desulfurization reaction tower bottom, spray into the atomizing cooling water, and, make desulfurization flue gas and sorbent particle, atomized water particle that strong three-phase turbulent heat transfer mass transfer exchange take place from a part of sorbent particle that outside deduster separates.
6. combined-circulation formula fluidization dry flue gas desulphurization technology according to claim 1 and 2 is characterized in that cleaning contains the pipeline any place of flue gas extraction point between desulfurization reaction tower exhanst gas outlet and chimney of wet flue gas recirculation.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02147821XA CN1169604C (en) | 2002-12-09 | 2002-12-09 | Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB02147821XA CN1169604C (en) | 2002-12-09 | 2002-12-09 | Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower |
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| CN1169604C true CN1169604C (en) | 2004-10-06 |
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100336755C (en) * | 2004-12-29 | 2007-09-12 | 清华大学 | Method for preparing two-stage slaked lime in use for flue gas desulfurization system and equipment |
| CN100418613C (en) * | 2006-11-17 | 2008-09-17 | 北京科技大学 | Circular dense phase fluidizing desulfurization apparatus |
| CN102614761A (en) * | 2012-04-17 | 2012-08-01 | 武汉金源环保科技工程设备有限公司 | Glass coating waste gas treatment dry energy-saving process |
| CN104759192A (en) * | 2015-03-17 | 2015-07-08 | 浙江大学 | Low-cost coal-fired flue gas various pollutant ultralow emission system and low-cost coal-fired flue gas various pollutant ultralow emission method |
| CN105617851B (en) * | 2016-03-16 | 2018-08-28 | 中国科学院城市环境研究所 | A kind of method and its device of efficient double tower semi-dry desulphurization |
| CN106215676B (en) * | 2016-08-30 | 2019-01-29 | 湖南循安环境资源技术有限公司 | A kind of semi-dry desulphurization tower equipped with flue gas self-loopa regulating device |
| CN107952365B (en) * | 2017-12-01 | 2024-05-10 | 中国电建集团河北省电力勘测设计研究院有限公司 | High-temperature flue gas evaporation desulfurization wastewater treatment device and treatment method thereof |
| CN108126510B (en) * | 2018-01-16 | 2024-01-26 | 邯郸学院 | Flue gas desulfurization and denitrification equipment |
| CN110237693A (en) * | 2019-06-14 | 2019-09-17 | 合肥中亚环保科技有限公司 | A kind of cement plant kiln exit gas cooling, desulfurizing synergistic device |
| CN110538566A (en) * | 2019-08-22 | 2019-12-06 | 黄震 | dry desulphurization energy-saving hybrid full-load adjustable system and control method |
| CN113128089B (en) * | 2021-04-07 | 2022-10-21 | 中国辐射防护研究院 | Design method and device of high-density shielding material particle pneumatic conveying device |
| CN113398729B (en) * | 2021-06-11 | 2023-04-28 | 神华神东电力有限责任公司 | Low-load control method of flue gas desulfurization absorption tower and coal combustion system |
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2002
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