CN1217728C - Dry process stack gas desulfur system using malti tower in parallel structure - Google Patents
Dry process stack gas desulfur system using malti tower in parallel structure Download PDFInfo
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- CN1217728C CN1217728C CN 03125296 CN03125296A CN1217728C CN 1217728 C CN1217728 C CN 1217728C CN 03125296 CN03125296 CN 03125296 CN 03125296 A CN03125296 A CN 03125296A CN 1217728 C CN1217728 C CN 1217728C
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Abstract
The present invention relates to a flue gas desulphurization system in a dry process with the adoption of the parallel structure of multiple towers, which belongs to the technical field of flue gas desulphurization, and particularly relates to a desulphurization system in a dry process for the flue gas exhausted from various large-sized combustion equipment, and a technique thereof. The present invention mainly solves problems in the fluidization of the granules of a desulphurizing agent after a flue gas desulphurization technique in the dry process is enlarged, and the organization of a flow field in the process of a heterogeneous chemical reaction; the present invention is characterized in that a desulphurization reaction tower of the system is composed of more than two desulphurization reaction sub-towers, and fume mixing chambers at the bottoms of the desulphurization reaction sub-towers are connected in parallel to form the large-sized desulphurization reaction system with the property of broad regulation ratio; fume flow deflectors which are arranged in the fume mixing chambers at the bottoms of the multiple desulphurization reaction sub-towers are used for uniformly distributing the fume to the fume injection accelerating unit of each of the desulphurization reaction sub-towers; combined jet flows of the fume are formed in the middle parts of the tower bodies of the desulphurization reaction sub-towers, so a high-strength turbulent mixing zone is formed in the middle part of the desulphurization reaction tower.
Description
Technical field
The present invention relates to a kind of maximization dry flue gas desulphurization method, 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.
At China's thermal power generation separate unit installed capacity is the flue gas desulfurization market demand of 600MW substantially; the special reinforcement of the water resource utilization being protected at the specific (special) requirements and the country of some regional power environment protections; 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, for example spray drying process, in-furnace calcium spraying add humidification activation method and flue gas circulating fluidized bed method etc., 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 the Chinese patent publication number CN86108755A, CN1307926A and German Wulff company " reverse-flow type circulating fluid bed flue-gas desulfurizing technology " 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.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, the purpose of this invention is to provide a kind of dry flue gas desulphurization system that adopts the multitower parallel-connection structure, make it can guarantee under higher boiler unit load (400～1000MW), 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).Another object of the present invention is to 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 realize the purpose of flue gas desulfurization of efficient, wide regulating ratio, low cost, the low water consumption of maximization dry flue gas desulphurization.
Realize technical scheme of the present invention:
The large-scale circulating fluidization dry flue gas desulphurization system of multitower parallel-connection structure of the present invention, the digestion preparation system, desulfurization reaction tower and the outside sorbent particle that comprise desulfurizing agent separate and recirculating system, the desulfurization reaction tower of this system adopts the sub-desulfurization reaction tower more than 2 or 2 to form, and this a little desulfurization reaction tower bottom flue gas mixing-chamber is together in parallel, form the desulphurization reaction system of the wide regulating ratio characteristic that maximizes and have.
The dry flue gas desulphurization system of described multitower parallel-connection structure is furnished with smoke deflector in the flue gas mixing-chamber of a plurality of sub-desulphurization reaction tower bottoms, flue gas is evenly distributed in the flue gas ejection accelerating apparatus of each sub-desulfurization reaction tower.
The dry flue gas desulphurization system of described multitower parallel-connection structure is furnished with the combination smoke jet nozzle at the tower body middle part of each sub-desulfurization reaction tower, sprays into the combination smoke jet, so that form the high intensity turbulent mixed zone at each sub-desulfurization reaction tower middle part.
In the described system, the flue gas ejection accelerating apparatus 3 of each sub-desulfurization reaction tower adopts 5～7 lower resistance Rafael nozzles, and to keep the flue gas jet rigidity of fluidisation demand preferably, resistance is lower simultaneously.
In the described system, initiate sorbent particle, atomized water particle and external recirculation sorbent particle all enter each sub-desulfurization reaction tower bottom respectively.
The present invention introduces the flue gas mixing-chamber of desulfurization reaction tower group bottom with the flue gas that the large electric power plant unit need carry out desulfurization, also enter the flue gas ejection accelerating apparatus of each the sub-desulfurization reaction tower that links to each other with mixing chamber then by the smoke deflector uniform distribution respectively, in each sub-desulfurization reaction tower, spray into calcium-based desulfurizing agent, atomized water particle and external recirculation sorbent particle.
The invention has the advantages that: at first, the present invention is owing to adopted the fluidization technology of multitower parallel-connection structure, solved the fluidisation problem of the sorbent particle after single tower maximizes and the flow field of heterogeneous chemical reaction process and organized problem, this also is the core that solves circulating fluidization dry flue gas desulphurization maximization technology.The second, the present invention is directed to the flue gas desulfurization requirement of actual big capacity fired power generating unit, according to actual needs, can any combining form increase sub-desulfurization reaction tower, solved the maximization problem of dry flue gas desulphurization.The 3rd, the present invention passes through to adopt the multitower parallel-connection structure, 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 can reduce the height of large desulfurization reaction tower preferably, has realized the maximization requirement of dry flue gas desulphurization technology simultaneously, reduces 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 2 is for being that B-B in the accompanying drawing 1 is to generalized section.
Accompanying drawing 3 is the desulfurization reaction tower horizontal layout schematic diagram of three tower parallel-connection structures.
Accompanying drawing 4 is not for the process flow system schematic diagram of the present invention of combination smoke jet.
Accompanying drawing 5 is for having the process flow system schematic diagram of the present invention of combination smoke jet.
Among the figure: sub-desulfurization reaction tower 1, smoke deflector 2, flue gas ejection accelerating apparatus 3, flue gas mixing-chamber 4, desulfurizing tower exhanst gas outlet 5, the pre-dust pelletizing system 6 of flue gas, the digestive system 7 of desulfurizing agent preparation, sorbent particle entrance 8, the refluxing opening 9 of external recirculation sorbent particle, water atomization entrance 10, flue gas dust collecting system 11, main induced draft fan 12, chimney 13, cinder tank 14, combination smoke jet entrance 15.
The specific embodiment
The present invention is to provide the installed capacity of a thermal power generation unit separate unit is the example of 600MW, has adopted a kind of dry flue gas desulphurization reaction system with 2 sub-desulfurization reaction tower features in parallel.
At first, the flue gas of discharging from combustion apparatus through a flue gas pre-dedusting device 6 (as electrostatic precipitator, sack cleaner, inertial separation deduster or their combining form), remove in the flue gas about 90% flying dust, send in the flue gas mixing-chamber 4 through the flue gas after the pre-dedusting, flue gas is assigned to equably in the flue gas ejection accelerating apparatus 3 (for example Venturi nozzle) of each sub-desulfurization reaction tower 1 by the smoke deflector 2 that is arranged in the flue gas mixing-chamber 4, the muzzle velocity scope of keeping the flue gas jet is 10-55m/s, quickens to enter the bottom of each sub-desulfurization reaction tower.
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 of each sub-desulfurization reaction tower 1 by sorbent particle entrance 8; while is on the top, sorbent particle entrance 8 position of each sub-desulfurization reaction tower bottom; be furnished with the refluxing opening 9 of external recirculation desulfurization particle; subsequently; bottom that flue gas enters sub-desulfurization reaction tower 1 and highly active desulfurization agent particle from sorbent particle entrance 8 spirts; the atomizing cooling water that sprays into by water atomization entrance 10; the recirculation sorbent particle of coming in the refluxing opening of separating from flue gas dust collecting system 11 9 from the external recirculation sorbent particle mixes, and strong three-phase turbulent heat transfer mass transfer exchange takes place 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.
Requirement at the maximization desulfurization chemical reaction, one-sided or both sides in the middle part of the tower body of each sub-desulfurization reaction tower 1 also are furnished with the combination smoke jet, spray into the middle part of each sub-desulfurization reaction tower 1 downwards with the outlet jet velocity of 80-120m/s by combination smoke jet entrance 15, form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the intensity of bulk devulcanization reaction.Wherein the combination smoke jet is 1～4 layer, and the distance between each layer flue gas jet entrance is 1000～3000mm, and the number of plies that specifically puts into operation can be regulated according to the needs of ruuning situation.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 each sub-desulfurization reaction tower 1 top, enter flue gas dust collecting system 11 (as electrostatic precipitator, sack cleaner, inertial separation deduster or 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, refluxing opening 9 by an external recirculation sorbent particle is sent back to them in the desulfurizing tower again, 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.From the clean flue gas up to standard that dust pelletizing system 11 is come out, send into chimney 13 through main induced draft fan 12, enter atmosphere at last.
Claims (4)
1. the dry flue gas desulphurization system of a multitower parallel-connection structure, it comprises that digestion preparation system, desulfurization reaction tower and the outside sorbent particle of desulfurizing agent separate and recirculating system, it is characterized in that: the desulfurization reaction tower of this system adopts the sub-desulfurization reaction tower more than 2 or 2 to form, and this a little desulfurization reaction tower bottom flue gas mixing-chamber is together in parallel, form the desulphurization reaction system of the wide regulating ratio characteristic that maximizes and have.
2. the dry flue gas desulphurization system of multitower parallel-connection structure according to claim 1, it is characterized in that in the flue gas mixing-chamber of a plurality of sub-desulphurization reaction tower bottoms, being furnished with smoke deflector, flue gas is evenly distributed in the flue gas ejection accelerating apparatus of each sub-desulfurization reaction tower.
3. the dry flue gas desulphurization system of multitower parallel-connection structure according to claim 1 and 2, it is characterized in that being furnished with the combination smoke jet nozzle at the tower body middle part of each sub-desulfurization reaction tower, spray into the combination smoke jet, so that form the high intensity turbulent mixed zone at each sub-desulfurization reaction tower middle part.
4, the dry flue gas desulphurization system of multitower parallel-connection structure according to claim 1 and 2, the flue gas ejection accelerating apparatus that it is characterized in that each sub-desulfurization reaction tower adopts 5～7 lower resistance Rafael nozzles, to keep the flue gas jet rigidity of fluidisation demand preferably.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125296 CN1217728C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur system using malti tower in parallel structure |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125296 CN1217728C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur system using malti tower in parallel structure |
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| Publication Number | Publication Date |
|---|---|
| CN1513585A CN1513585A (en) | 2004-07-21 |
| CN1217728C true CN1217728C (en) | 2005-09-07 |
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| CN 03125296 Expired - Fee Related CN1217728C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur system using malti tower in parallel structure |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014110883A1 (en) * | 2013-01-18 | 2014-07-24 | 北京神雾环境能源科技集团股份有限公司 | Process system for performing dry desulfurization on fume of pellet fuel boiler |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN104162356B (en) * | 2014-08-27 | 2016-08-17 | 邹海明 | A kind of double multitube combined Pneumatic emulsifying desulfurizing tower |
| 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 |
| 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 |
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2003
- 2003-08-19 CN CN 03125296 patent/CN1217728C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014110883A1 (en) * | 2013-01-18 | 2014-07-24 | 北京神雾环境能源科技集团股份有限公司 | Process system for performing dry desulfurization on fume of pellet fuel boiler |
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| CN1513585A (en) | 2004-07-21 |
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