CN1224446C - large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization - Google Patents
large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization Download PDFInfo
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
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Abstract
The present invention provides a large scale dry process flue gas desulfurization method of single tower multibed circulating fluidization, which aims at the requirements of large scale dry process flue gas desulfurization. A fluidized interval at the bottom of a desulphurization reaction tower is divided into two or more than two small fluidized intervals (fluidized secondary beds) which are relatively independent, and the small fluidized secondary beds which are relatively independent, are organically combined to form a desulfurizing reaction tower which has the constructional characteristics of the single tower at the upper part of the fluidized secondary beds of the lower part of the desulfurizing tower. The method solves the problems of the desulfurizing agent particle fluidization after single tower large scale, the flow field organization during the heterogeneous chemical reaction process, and the core technology of single tower large scale of circulating fluidization dry process flue gas desulfurization, and simultaneously can reduce the height of large desulfurizing towers, realize the requirements of single tower large scale of dry process flue gas desulfurization technology, reduce the unit cost of the dry process flue gas desulfurization, and realize the desulfurization technical requirements of high desulfurization efficiency, wide turndown ratio, low investment, low operation cost and low water consumption.
Description
Technical field
The present invention relates to a kind of maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization, particularly proposed the circulating fluidization dry flue gas desulphurization technology that large-scale single tower divides bed in the dry flue gas desulphurization field.Belong to the flue gas desulfurization technique field, maximization dry method desulfuration system and technology in the particularly various large-scale combustion apparatus discharging flue gases.
Background technology
The improvement of sulfur dioxide gas body pollution is the emphasis of world's most countries environmental protection always, and its pollutant that produces causes the greatest contamination source of China's environmental destruction especially, has become the task of top priority of China's air pollution treatment at present.
Present improvement to sulfur dioxide, external general main employing wet type lime stone-gypsum method (W-FGD), adopt said method, though removal effect is better, investment is huge, water consumption is big but it exists, floor space is big, system complex, big, the complex structure of resistance, and need handle or the like a series of problems again to water.Therefore the high-efficiency flue gas desulfurization technology of dry type or half dry type becomes the emphasis of domestic and international research and development.
Special is the flue gas desulfurization market demand of 600MW at China's thermal power generation separate unit installed capacity substantially, special specific (special) requirements at area, northwestward power environment protection, and country is to the reinforcement of water resource utilization protection.Simultaneously according to the objective law in flue gas desulfurization technique development and market in the world, advanced person's maximization (applicable to the above thermal power generation unit of 600MW) dry flue gas desulphurization technology will become the main force in domestic and international power environment protection technology and market.
For present all dry method (semidry method) desulfur technology and patented technologies, though they all the flue gas desulfurization course of reaction certain some aspect have oneself technical characteristic, but all do not have to consider after unit maximizes, because the increase of desulphurization reaction tower section and height will cause whole desulphurization reaction owing to the tissue failure in flue gas and particle flow field does not reach the desulfur technology requirement.
Especially for the desulfurization by dry method of the flue gas circulating fluidized bed method of present application, 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.As patent CN86108755A, CN1307926 or the like, " reverse-flow type circulating fluid bed flue-gas desulfurizing technology " of and for example German Wulff company etc., all be to adopt a desulfurization reaction tower that is similar to fluid bed, realize the desulfurization purpose by haptoreactions in tower such as flue gas, sorbent particle and water sprays, and all be single design of single tower, the single tower design in the heavy in section after it maximizes can not be satisfied the basic fundamental requirement of circulating fluidization.
As seen, in ciculation fluidized flue gas desulphurization system, the fluidisation requirement that can the heterogeneous flow field tissue in the tower satisfy design is the key factor that can desulphurization reaction carry out smoothly from the above-mentioned background technology introduction.And all at present fluidization desulfurization by dry method all exist when unit capacity is big, can not satisfy the fluidization requirement of maximization flue gas desulfurization reaction.
Summary of the invention
Deficiency and defective at the prior art existence, purpose of the present invention and task provide a kind of novel maximization dry flue gas desulphurization systems technology, adopt a kind of circulating fluidization reaction tower for stack gas desulfurization, system and technology of single-tower muiti-bed, make its can guarantee under higher boiler unit load (＞=600MW), satisfy the balanced fluid mapper process of heavy in section desulfurizing tower, desulfuration efficiency and every performance indications can be better than the dry flue gas desulphurization performance of conventional unit (300MW is following).
The present invention is applicable to 300～1000MW fired power generating unit, is specially adapted to the single tower flue gas desulfur technology and the performance requirement of the fired power generating unit about 600MW, and promptly the situation in Ca/S=1.1～1.3 is issued to higher desulfuration efficiency (more than 90%～92%); Reduce the water yield of carrying of water consumption and clean flue gas; Realize the wide regulating ratio characteristic of desulphurization system, can satisfy the high-efficiency desulfurization requirement of combustion apparatus from 20% to 110% load variations.State in realization under the purpose prerequisite, and further simplify system, reduce equipment investment and operating cost, reduce flue gas resistance, and the unit equipment cost can drop to about 0.7～0.8 of present dry method flue gas desulfur device, thereby really realizes the purpose of flue gas desulfurization of efficient, wide regulating ratio, low cost, the low water consumption of maximization dry flue gas desulphurization.
Technical scheme of the present invention: the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization comprises the desulphurization reaction in the preparation digestion of desulfurizing agent, the desulfurization reaction tower, the separation and the recirculation of outside sorbent particle, it is characterized in that the relatively independent rill interval that the bottom fluidization interval with desulfurization reaction tower is divided into more than 2 or 2 is a fluidisation bed, and these relatively independent fluidisations bed organic assembling are become a desulfurization reaction zone with single tower structure on the interval top of relatively independent rillization.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization is furnished with smoke deflector in the flue gas mixing-chamber of desulfurizing tower bottom, flue gas or flue gas and flue gas recycled are evenly distributed in the flue gas induction apparatus of each fluidisation bed.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization, the flue gas induction apparatus 2 of each fluidisation bed adopts 5～7 lower resistance Rafael nozzles, and to keep the flue gas jet rigidity of fluidisation demand preferably, resistance is lower simultaneously.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization, the lower section that it is characterized in that the desulfurizing tower that fluidisation bed merging back forms has following several form, and promptly broad ways is similar to plurality of stepped serrations or is similar to the compound section of two semicircles and rectangle or is similar to circular cross-section.
The lower section of described desulfurizing tower is when being similar to circular cross-section, and fluidisation bed is evenly to arrange along the circumferencial direction of tower body.
The lower section of described desulfurizing tower is a broad ways when being similar to plurality of stepped serrations or being similar to the compound section of two semicircles and rectangle, and fluidisation bed is evenly arranged along the unit width.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization; its initiate sorbent particle and external recirculation sorbent particle feed back all enter each fluidisation bed bottom respectively, and water atomizing nozzle is arranged in the exit position of each fluidisation bed.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization, at desulfurizing tower tower body middle part, requirement at the maximization desulfurization chemical reaction, also be furnished with the multiple jet flow nozzle of recirculation clean flue gas, form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the intensity of middle part desulphurization reaction.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization, adopt the recirculating system of clean flue gas, introduce clean flue gas to mixing chamber,, satisfy the service requirement of combustion apparatus from 20%～110% load to improve the wide regulating ratio characteristic of equipment.
The maximization dry flue gas desulphurization method of described single-tower muiti-bed circulating fluidization, its tower body adopt the version of variation to improve the endocorpuscular nitrate recirculation ratio rate of tower, improve desulphurization reaction efficient.
Advantage of the present invention:
At first, the present invention is owing to adopted the single-tower muiti-bed fluidization technology, solved the fluidisation problem of the sorbent particle after single tower maximizes, problem is organized in the flow field of heterogeneous chemical reaction process, this also is the core that solves circulating fluidization dry flue gas desulphurization list tower maximization technology.
The second, the present invention is directed to the flue gas desulfurization requirement of actual big capacity fired power generating unit, but increasing, broad ways arranges fluidisation bed, solved the maximization problem of dry flue gas desulphurization.
The 3rd, the present invention passes through to adopt the single-tower muiti-bed technology, thereby can guarantee every conventional dry flue gas desulphurization technology in the later smooth application of unit maximization, and meets or exceeds the performance parameter index of routine techniques.
The 4th, the present invention adopts many streaming modes according to the design of desulfurizing tower concrete structure, can reduce the desulfurizing tower height under the situation that guarantees various performance parameters, satisfies concrete engineering design needs.Realize single tower maximization requirement of dry flue gas desulphurization technology simultaneously, reduced the unit cost of dry flue gas desulphurization significantly.
The 5th, 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) equally, the desulfur technology requirement of low investment and operating cost, low water consumption.
Description of drawings
Accompanying drawing 1 is a process flow system schematic diagram of the present invention.
Accompanying drawing 3 and accompanying drawing 4 are two kinds of single-tower muiti-bed desulfurization reaction tower bottom fluidization bed arrangement schematic top plan view of the present invention.
The specific embodiment
Among the figure: the digestive system 7 of fluidisation bed 1, lower resistance flue gas induction apparatus 2, desulfurization reaction tower tower body 3, flue gas mixing-chamber 4, smoke deflector 4-1, desulfurizing tower exhanst gas outlet 5, the pre-dust pelletizing system 6 of flue gas, desulfurizing agent preparation, the refluxing opening 9 of desulfurizing agent entrance 8, external recirculation sorbent particle, water atomization entrance 10, flue gas dust collecting system (electrostatic precipitator or sack cleaner) 11, main induced draft fan 12, chimney 13, cinder tank 14, combination smoke jet entrance 15, clean flue gas recirculating system 16.
The first, single tower project organization of the present invention is characterised in that the desulfurizing tower bottom is a kind of Y-shaped multiple compartments, the visible accompanying drawing 2 of its structural representation.The desulfurizing tower bottom is divided into the fluidisation bed 1 more than 2 or 2.These fluidisation beds have two kinds of arrangements, and one is evenly to arrange along the unit width, sees accompanying drawing 3; Another kind of for evenly to arrange along the circumferencial direction of tower body, see accompanying drawing 4.
Second, the design fluidisation scope of each fluidisation bed satisfies the grain fluidized mixing demand of combustion apparatus from 100MW～300MW load, this maximization dry flue gas desulphurization technology is applicable to the flue gas desulfurization requirement of the unit load of 400MW～1000MW, and under the situation that adopts the flue gas recycled technology, can satisfy the fluidization requirement of unit combustion apparatus 20%～110% load variations.
The 3rd, the flue gas induction apparatus 2 of each fluidisation bed adopts 5～7 lower resistance Rafael nozzles, and to keep the flue gas jet rigidity of fluidisation demand preferably, resistance is lower simultaneously.
The 4th, in each fluidisation bed exit position, merge desulfurization reaction tower 3 of formation.The lower section of this desulfurizing tower has following several form, and promptly broad ways is similar to plurality of stepped serrations or is similar to the compound section of two semicircles and rectangle or is similar to circular cross-section.Tower body adopts the version of variation, to improve the endocorpuscular nitrate recirculation ratio rate of tower, improves desulphurization reaction efficient.The variation structure comprises that the intersection of the various combinations of shape size in tower body cross section changes, to reach the change purpose to air velocity and direction.As circle on similar down circle top, the below, otherwise perhaps other structure such as side, circle or ellipse or cross section are become than positivity or the various variation structures of the big or combination of little change are arranged by more microscler.
The 5th, initiate sorbent particle and external recirculation sorbent particle feed back all enter respectively in the flue gas mixing-chamber of desulfurizing tower bottom, through smoke deflector 4-1, flue gas is evenly distributed in the flue gas induction apparatus 2 of each fluidisation bed, to each fluidisation bed bottom; Water atomizing nozzle 10 is arranged in the exit position (single tower space segment) of each fluidisation bed 1.
The 6th, desulfurizing tower tower body 3 middle parts at the requirement of maximization desulfurization chemical reaction, also are furnished with the multiple jet flow entrance 15 of recirculation clean flue gas, form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the intensity of middle part desulphurization reaction.
Specify system of the present invention and technical process below in conjunction with accompanying drawing.
As Fig. 1: at first, the flue gas of discharging from combustion apparatus is at first through a flue gas pre-dedusting device 6 (as electrostatic precipitator, sack cleaner, inertial separation deduster), send in the flue gas mixing-chamber 4 through the flue gas after the pre-dedusting, be assigned to equably in the flue gas induction apparatus 2 of each fluidisation bed 1 by the deflector 4-1 that is arranged in the mixing chamber, the muzzle velocity scope of keeping the flue gas jet is the 10-55 meter per second, quickens to enter each fluidisation bed bottom.
Simultaneously, desulfurizing agent raw material (as the CaO powder) being sent in the digestive system 7, generated highly active sorbent particle through digestion reaction, is that the desulfurizing agent of 1～6 μ m is (as Ca (OH) with digestion back particle size range
2) particle; spray into each fluidisation bed 1 bottom of desulfurizing tower by sorbent particle entrance 8; while is on the top, sorbent particle entrance 8 position of each fluidisation bed bottom; be furnished with the refluxing opening 9 of external recirculation desulfurization particle; subsequently; flue gas enter the bottom of desulfurization reaction tower 3 with from the highly active desulfurization agent particle of nozzle 8 spirts, by the 10 atomizing cooling waters that spray into; reach from what deduster was separated and come in to recycle the sorbent particle mixing from spout 9, 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 most of sorbent particle particle diameter is 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.
Tower body middle part at desulfurizing tower 3 at the requirement of maximization desulfurization chemical reaction, also is furnished with the multiple jet flow nozzle 15 of recirculation clean flue gas, forms the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthens the intensity of middle part desulphurization reaction.Again up; the tower endoparticle presents bigger falling trend substantially; 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 5 at desulfurizing tower top; enter flue gas dust collecting system 11 (electrostatic precipitator or sack cleaner; perhaps their combining form); the particle that carries in the flue gas is separated; wherein also contain some unreacted sorbent particle; in order to improve sorbent utilization; send back to them in the desulfurizing tower again by a recirculation particle feed back pipe by 9; no longer participate in circulation and reacted most of granule (1～2 μ m) of finishing, promptly desulfuration byproduct and flying dust are then sent into cinder tank 14 storages, transhipment is walked.The clean flue gas up to standard that comes out from dust pelletizing system 11 is through main induced draft fan 12, and a part enters clean flue gas recirculating system 16, sends in the flue gas mixing-chamber 6, carries out flue gas recirculation, and all the other then send into chimney 13, enter atmosphere at last.Adopt the recirculating system of clean flue gas, introduce clean flue gas,, satisfy the service requirement of combustion apparatus from 20%～110% load so that improve the wide regulating ratio characteristic of equipment to mixing chamber.
The technology of large-scale circulating fluidization dry flue gas desulphurization technology can comprise following process system: the recirculating system of the external recirculation of the pre-dust pelletizing system of coal-fired flue-gas, the digestion preparation system of desulfurizing agent, desulphurization reaction system, sorbent particle and flue gas dust collecting system, clean flue gas.Core of the present invention is the desulphurization reaction system of single-tower muiti-bed fluidisation, it can with the main several system in combination in above-mentioned.But combination in any case as long as adopt the bottom fluidization interval with desulfurization reaction tower to be divided into a plurality of relatively independent rill intervals, all belongs to protection scope of the present invention.
Claims (10)
1. the maximization dry flue gas desulphurization method of a single-tower muiti-bed circulating fluidization, comprise the interior desulphurization reaction of preparation digestion, desulfurization reaction tower of desulfurizing agent, the separation and the recirculation of outside sorbent particle, it is characterized in that the relatively independent rill interval that the bottom fluidization interval with desulfurization reaction tower is divided into more than 2 or 2 is a fluidisation bed, and these relatively independent fluidisations bed organic assembling are become a desulfurization reaction zone with single tower structure on the interval top of relatively independent rillization.
2. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 is characterized in that being furnished with smoke deflector in the flue gas mixing-chamber of desulfurizing tower bottom, flue gas is evenly distributed in the flue gas induction apparatus of each fluidisation bed.
3. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2 is characterized in that the flue gas induction apparatus of each fluidisation bed adopts 5～7 lower resistance Rafael nozzles.
4. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2, the lower section that it is characterized in that the desulfurizing tower that fluidisation bed merging back forms has following several form, and promptly broad ways is similar to plurality of stepped serrations or is similar to the compound section of two semicircles and rectangle or is similar to circular cross-section.
5. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 4 is characterized in that the lower section when desulfurizing tower is when being similar to circular cross-section, and fluidisation bed is evenly to arrange along the circumferencial direction of tower body.
6. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 4, it is characterized in that lower section when desulfurizing tower is a broad ways when being similar to plurality of stepped serrations or being similar to the compound section of two semicircles and rectangle, fluidisation bed is evenly to arrange along long width.
7. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2; it is characterized in that initiate sorbent particle and external recirculation sorbent particle feed back all enter each fluidisation bed bottom respectively, water atomizing nozzle is arranged in the exit position of each fluidisation bed.
8. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2, it is characterized in that at desulfurizing tower tower body middle part, be furnished with the multiple jet flow nozzle of recirculation clean flue gas, form the high intensity turbulent mixed zone at desulfurizing tower middle part.
9. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2 is characterized in that adopting the recirculating system of clean flue gas, introduces clean flue gas to mixing chamber.
10. the maximization dry flue gas desulphurization method of single-tower muiti-bed circulating fluidization according to claim 1 and 2 is characterized in that tower body adopts the version with the variation that improves the endocorpuscular nitrate recirculation ratio rate of tower.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125277 CN1224446C (en) | 2003-08-15 | 2003-08-15 | large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization |
| PCT/CN2004/000949 WO2005030368A1 (en) | 2003-08-15 | 2004-08-16 | One tower-multibeds circulating fluidization large-scale dry desulfurizating process for flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125277 CN1224446C (en) | 2003-08-15 | 2003-08-15 | large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization |
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| CN1488427A CN1488427A (en) | 2004-04-14 |
| CN1224446C true CN1224446C (en) | 2005-10-26 |
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| CN 03125277 Expired - Fee Related CN1224446C (en) | 2003-08-15 | 2003-08-15 | large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization |
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| CN (1) | CN1224446C (en) |
| WO (1) | WO2005030368A1 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100436941C (en) * | 2005-07-05 | 2008-11-26 | 中国石油大学(北京) | Coal-tar powder combustion method and apparatus |
| CN100425329C (en) * | 2005-11-25 | 2008-10-15 | 山东大学 | Tech. for desulphuni zation of flue-gas by using integrated internal circulation and two-speed fluidized bed |
| CN101417207B (en) * | 2008-11-06 | 2011-02-09 | 武汉凯迪电力环保有限公司 | Large double-cycle fluidized bed semi-dry process flue gas desulphurization tower |
| DE102011052788B4 (en) * | 2011-08-17 | 2014-03-20 | Harald Sauer | Process and apparatus for purifying exhaust gases |
| KR101729460B1 (en) | 2014-01-31 | 2017-04-21 | 아멕 포스터 휠러 에너지아 오와이 | A method of and a scrubber for removing pollutant compounds from a gas stream |
| WO2015113627A1 (en) | 2014-01-31 | 2015-08-06 | Amec Foster Wheeler Energia Oy | A method of and a scrubber for removing pollutant compounds from a gas stream |
| CN104492248B (en) * | 2014-12-24 | 2016-05-25 | 西昌市蓝鼎环保科技有限公司 | For the dry method desulfuration system of high sulphur concentration flue gas |
| CN109833748A (en) * | 2017-11-29 | 2019-06-04 | 中科天龙（厦门）环保股份有限公司 | A kind of near-zero release flue gas coordinated desulfurization denitration dust collecting group technology |
| EP3620227A1 (en) * | 2018-09-05 | 2020-03-11 | Fujian Lonjing Environment Technology Co., Ltd. | Apparatus and process for removal of sulfur dioxide from flue gas |
| CN110404398B (en) * | 2019-06-05 | 2023-09-19 | 国能(山东)能源环境有限公司 | Circulating fluidized bed semi-dry desulfurization and dust removal double-tower switching system, method and application |
| CN110538566A (en) * | 2019-08-22 | 2019-12-06 | 黄震 | dry desulphurization energy-saving hybrid full-load adjustable system and control 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 |
| CN112812857A (en) * | 2021-03-10 | 2021-05-18 | 中冶华天南京工程技术有限公司 | Novel horizontal desulfurizing tower of blast furnace gas dry process |
| CN117138548B (en) * | 2023-09-12 | 2024-05-14 | 山东康源环保科技有限公司 | Vertical fixed bed desulfurization, denitrification and dust removal equipment and application method thereof |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CZ293501B6 (en) * | 1994-05-11 | 2004-05-12 | Babcock@Hitachiákabushikiákaisha | Wet-type flue gas desulfurization method and apparatus for making the same |
| CN1087643C (en) * | 1997-04-04 | 2002-07-17 | 清华大学 | Flue gas desulfurization process and device of dry desulfurizing agent bed material internal circutation |
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| CN1488427A (en) | 2004-04-14 |
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