CN1224445C - Dry-process flue gas desulfurizing method using combined gas jet - Google Patents
Dry-process flue gas desulfurizing method using combined gas jet Download PDFInfo
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- CN1224445C CN1224445C CN 03125276 CN03125276A CN1224445C CN 1224445 C CN1224445 C CN 1224445C CN 03125276 CN03125276 CN 03125276 CN 03125276 A CN03125276 A CN 03125276A CN 1224445 C CN1224445 C CN 1224445C
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Abstract
The present invention provides a process for desulphurizing fume in a dry process with the adoption of the combined jet streams of the fume, which is characterized in that a jet stream nozzle for the fume is additionally arranged above an atomized water spraying nozzle and a desulphurizing agent nozzle in a desulphurization reaction tower; thereby, a gas phase, a solid phase and a liquid phase in the desulphurization reaction tower can be effectively organized to be thoroughly mixed, desulphurization efficiency is raised, and the flow resistance of the fume is reduced. With the adoption of the technique of the present invention and by combining the recirculation technique of the fume in the desulphurization reaction tower, high desulphurization efficiency can be achieved under the condition that low calcium sulfur ratio is guaranteed, and water consumption is reduced; simultaneously, the wide regulating ratio property of a desulphurization system is realized, and the requirement of the desulphurization in high efficiency with the load variation of combustion equipment from 20% to 110% can be satisfied; particularly, aiming at a large fume desulphurization system in the dry process, the significance of the technique of the present invention is shown in the aspect of the effective organization of the internal flow field of the desulphurization reaction tower.
Description
Technical field
The present invention relates to a kind of dry flue gas desulphurization method that adopts the combination smoke jet, 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.
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, 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 from 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 etc.Especially at the heavy in section tower body design after maximizing, in desulfurization reaction tower, the mixing of material, water droplets and flue gas only depends on the polymorphic structure of desulfurization reaction tower and the flue gas injection of Venturi tube, form the different of interior gas-solid liquid velocity of desulfurization reaction tower and density, about causing in the tower, the heterogeneous of all around flow, this hybrid mode is very high to the structural requirement of the speed of Venturi tube exhanst gas outlet and tower, has increased the power of blower fan like this.In addition, have very big deficiency aspect maximization, after the desulphurization reaction tower structure increased, this hybrid mode was difficult to satisfy the strong mixing requirement of reaction zone, does not reach effective desulfurized effect.
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.Particularly desulfurization by dry method all exists when unit capacity is big, can not satisfy the fluidization requirement of maximization flue gas desulfurization reaction.
Summary of the invention
The problem that in present engineering, exists at existing technology, with deficiency and defective in existence aspect the maximization, the present invention proposes a kind of in the desulfurization reaction tower reaction zone, a kind of dry flue gas desulphurization technology that adopts the combination smoke jet that the gas-solid liquid phase is mixed fully, desulfuration efficiency is high, the flue gas circulating resistance is low.Adopt this kind technology, 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.
The present invention is achieved by the following technical solutions: the dry flue gas desulphurization method of combination smoke jet comprises the separation and the recirculation of desulphurization reaction, sorbent particle in desulfurizing agent preparation digestion, the desulfurization reaction tower, middle part or top at desulfurization reaction tower are provided with nozzle, spray into the combination smoke jet, thereby change the flow behavior in zone, desulfurizing tower middle and upper part, strengthen turbulence intensity, form new vortex, reach abundant mixing and the velocity-slip of effectively organizing gas, solid, liquid three-phase in the desulfurization reaction tower.
The dry flue gas desulphurization method of described employing combination smoke jet, downward 0～60 ° of its flue gas injection stream emission direction along continuous straight runs.
The dry flue gas desulphurization method of described employing combination smoke jet, the installation site of flue gas jet nozzle are above water jet or feedback outlet 1,000mm～35,000mm.
The dry flue gas desulphurization method of described employing combination smoke jet, the speed of jet flue gas can be regulated according to its position on desulfurization reaction tower is different, and its scope is 30～180m/s.
The dry flue gas desulphurization method of described employing combination smoke jet, multiple jet flow nozzle are along 1～4 layer of desulfurization reaction tower main body upper and lower settings, and every number of plies amount can be one or more.
The dry flue gas desulphurization method of described employing combination smoke jet, flue gas injection nozzle are telescopic along the dark direction of tower.
The dry flue gas desulphurization method of described employing combination smoke jet, the injection direction of flue gas injection nozzle can be regulated.
The dry flue gas desulphurization method of described employing combination smoke jet, its desulfurization reaction tower main body are the variation structures.
The dry flue gas desulphurization method of described employing combination smoke jet, the extraction location of its jet flue gas is any position at exhaust gases passes, comprise flue gas before desulfurization reaction tower inlet, the forward and backward flue gas of pre-dedusting device, the forward and backward flue gas of desulfurization reaction tower outlet back dust arrester, the perhaps above combination smoke in any position Liang Chu of exhaust gases passes and two places.
Advantage of the present invention: owing to effectively organize the interior heterogeneous reaction pattern of desulfurization reaction tower, adopt the flue gas injection system of combination, strengthened the mixing intensity of gas-liquid solid phase in the tower, strengthened tower inner transmission matter effect, improve the utilization rate of desulfurizing agent, reduced the circulating resistance of flue gas; Desulphurization system is under the Ca/S=1.2 situation, and desulfuration efficiency reaches more than 90%, and the total circulating resistance of tower body is less than 1800Pa; When the injection flue gas draws back behind the desulfurization reaction tower exhanst gas outlet, formed the flue gas recirculation system, spraying exhaust gas volumn 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.
Description of drawings
Fig. 1 is a system architecture schematic diagram of the present invention.
Fig. 2 is arranged on the layout schematic diagram of tower body front side for one deck flue gas jet.
Fig. 3 is the layout schematic diagram that three layers of flue gas jet are arranged on the tower body front side.
Fig. 4 is the interlaced arrangement schematic diagram that four layers of flue gas jet are arranged on both sides.
Fig. 5 is four layers of flue gas jet symmetric arrangement schematic diagram.
Fig. 6 looks schematic diagram for the master that jet nozzle is arranged on the tower body wall.
Fig. 7 is arranged on the cross section schematic top plan view of tower body wall for jet nozzle.
Among the figure: the 1st, between the fluidization regions of desulfurization reaction tower, the 2nd, the flue gas induction apparatus, the 3rd of desulfurization reaction tower, desulfurization reaction tower main body, the 4th, the flue gas mixing-chamber at the bottom of the desulfurization reaction tower, the 5th, desulfurization reaction tower exhanst gas outlet, 6. flue gas pre-dedusting device (static, cloth bag, inertial dust separator etc.), the 7th, digestive system, the 8th, desulfurizing agent spray into pipe, the 9th, external recirculation particle feed back pipe, the 10th, desulfurization is with water atomizing nozzle, the 11st, separator be deduster (static, cloth bag,
Inertial dust separator etc.), the 12nd, main induced draft fan, the 13rd, chimney, the 14th, cinder tank, the 15th, jet flue gas nozzle, the 16th, flue gas recycled inlet tube, the 17th, main flue gas inlet tube, the 18th, ash dropping hopper.
The specific embodiment
Desulfurization reaction tower of the present invention comprises: the flue gas induction apparatus (Venturi nozzle, air-distribution device) in the flue gas mixing-chamber at the bottom of the tower, flue gas mixing-chamber, give separation (static, cloth bag, inertia etc.) device, the desulfurizing tower flue gas recirculation device of water atomizing nozzle, charging gear, feeding back device, flue gas jet nozzle, desulphurization reaction tower body, desulfurization reaction tower outside.The present invention is at the middle part of desulfurization reaction tower or top sprays into the combination smoke jet, thereby change the flow behavior in zone, desulfurizing tower middle and upper part, strengthen turbulence intensity, form new vortex, reach abundant mixing and the velocity-slip of effectively organizing gas, solid, liquid three-phase in the desulfurization reaction tower.
The flue gas jet that the present invention adopts can be drawn at any position of the exhaust gases passes of desulphurization system, and this flue gas jet nozzle is arranged in water jet or feedback outlet top 1, and 000mm～35 are between the scope of 000mm.
The arrangement form of flue gas jet nozzle of the present invention has multiple: jet nozzle is installed in the desulfurization reaction tower wall, along 1～4 layer of nozzle of desulfurization reaction tower main body upper and lower settings.
Fig. 2～Fig. 5 is arranged on the various layout schematic diagrames of tower body for jet nozzle.3 is desulfurization reaction tower main bodys among the figure, the 15th, and jet flue gas nozzle.
Flue gas jet nozzle of the present invention is that fix or adjustable.A kind of stretching promptly telescopic along the dark direction of tower, regulated the lateral attitude; Another kind is that the injection direction of flue gas injection nozzle can be regulated, and promptly nozzle is rotatable, regulates spraying into direction; Perhaps two kinds of combinations.These are regulated as required and are provided with, and these nozzles can adopt the existing nozzle of boiler industry.
The speed of jet flue gas of the present invention can be regulated according to the diverse location at desulfurization reaction tower, and its scope can be 30～180m/s.
Adopt desulfurization reaction tower of the present invention can with various textural associations, combine as technology such as single-tower muiti-bed, complicated variation towers.
Adopt the version that makes a variation in conjunction with tower body, can improve the endocorpuscular nitrate recirculation ratio rate of tower, improve 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.
Jet flue gas used in the present invention can be the recirculation clean flue gas, or needs the flue gas of desulfurization, also can be the flue gas that attracts of air (comprising humid air) or any position of flue or the combination of each position flue gas.The extraction location of general jet flue gas flue gas the best behind the dust arrester of desulfurization reaction tower outlet back.
Specify the design feature and the operation principle of the technology of the present invention below in conjunction with accompanying drawing:
The flue gas mixing-chamber 4 of desulphurization reaction Tower System is connected with main flue gas inlet tube 17 and with flue gas recirculation inlet tube 16, its below connects ash dropping hopper 18, its top connects flue gas induction apparatus 2, be right after on it between the fluidization regions of desulfurizing tower 1, and be equipped with between this fluidization regions to water atomizing nozzle 10, desulfurizing agent and spray into pipe 8 and external recirculation particle feed back inlet tube 9; Up promptly connect desulfurization reaction tower main body 3, combination smoke jet nozzle 15 is installed on the desulfurization reaction tower main body 3, desulfurization reaction tower smoke outlet tube 5 is connected with particle separation (static, cloth bag, the inertia etc.) device 11 of desulfurization reaction tower outside, from separator 11 isolated a part of particles, particle feed back pipe 9 through external recirculation flow back in the desulfurization reaction tower, and another part particle flow into cinder tank 14 by the lime-ash pipe; The flue gas that draws back from any position of desulfurization reaction tower exhanst gas outlet 5 rear pass can by flue gas recycled enter the mouth 16 and flue gas jet nozzle 15 get back in the desulfurization reaction tower.
The combination smoke jet that the present invention proposes, its jet flue gas can be drawn from any position of flue, the also combination of many places flue gas, this jet flue gas with certain speed (according to the difference that is ejected into position in the desulfurization reaction tower, its speed can be ejected in the desulfurization reaction tower from 30～180m/s), can organize the flow field in the desulfurization reaction tower to flow effectively, strengthen the Turbulent Kinetic of gas-solid liquid phase in the desulfurization reaction tower reaction zone, it is mixed fully, accelerate desulphurization reaction speed, improve desulfuration efficiency.In addition, the jet flue gas that sprays into if any position behind the desulfurization reaction tower exhanst gas outlet draw back, it is moving that then the jet flue gas is not only effectively organized the interior multiphase flow field flow of desulfurization reaction tower, also can play the effect of flue gas recirculation in the desulfurization reaction tower simultaneously, reach the purpose that reduces the desulphurization system water consumption thereby reduce the water yield of carrying of discharging flue gas, and realize the wide regulating ratio characteristic of desulphurization system.
Below in conjunction with accompanying drawing,, be described in further detail the dry flue gas desulphurization technology of employing combination smoke jet of the present invention by introduction to technological process.
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 into flue gas mixing-chamber 4 through the flue gas after the pre-dedusting, and the flue gas induction apparatus 2 of process desulfurizing tower bottom, the muzzle velocity scope of keeping the flue gas jet is the 10-55 meter per second, quickens to enter desulfurizing tower bottom fluidization interval 1.
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 1-10 μ m is (as Ca (OH) with digestion back particle size range
2) particle; spray into the desulfurizing tower bottom by sorbent particle entrance 8; simultaneously on top, sorbent particle entrance 8 position; be furnished with the refluxing opening 9 of external recirculation desulfurization particle; subsequently; the bottom that flue gas enters desulfurization reaction tower 3 with from the highly active desulfurization agent particle of nozzle 8 spirts, come in to recycle sorbent particle from spout 9 and mix by the 10 atomizing cooling waters that spray into from what deduster was separated, 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, requirement at the maximization desulfurization chemical reaction, inject air-flow by jet flue gas nozzle 15 of the present invention, form the high intensity turbulent mixed zone at desulfurizing tower middle part, and the flow of flue gas form of change tower body middle and upper part, strengthen the desulphurization reaction intensity of flue gas middle and upper part, and form the vortex of various forms, size, improve the interior cycle efficieny of particle.
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.
Claims (9)
1. dry flue gas desulphurization method that adopts the combination smoke jet, comprise the separation and the recirculation of desulphurization reaction, sorbent particle in desulfurizing agent preparation digestion, the desulfurization reaction tower, it is characterized in that being provided with jet nozzle on the middle part or the top of desulfurization reaction tower, spray into multiply flue gas jet, form the vortex in zone, desulfurizing tower middle and upper part.
2. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 is characterized in that flue gas jet injection direction is downward 0～60 ° an of along continuous straight runs.
3. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 and 2 is characterized in that position that the flue gas jet sprays into is above water jet or feedback outlet 1,000mm～35,000mm.
4. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 and 2 is characterized in that the speed adjustable range of jet flue gas is 30～180m/s.
5. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 and 2 is characterized in that jet nozzle along 1～4 layer of desulfurization reaction tower main body upper and lower settings, and every number of plies amount is one or more.
6. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 and 2 is characterized in that the flue gas jet nozzle can stretch along the dark direction of tower.
7, the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 and 2 is characterized in that the injection direction of flue gas jet nozzle can be regulated.
8. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1 is characterized in that the desulfurization reaction tower main body is the variation structure.
9. the dry flue gas desulphurization method of employing combination smoke jet according to claim 1, the extraction location that it is characterized in that the jet flue gas is any position at exhaust gases passes, comprise flue gas before desulfurization reaction tower inlet, the forward and backward flue gas of pre-dedusting device, the forward and backward flue gas of desulfurization reaction tower outlet back dust arrester, the perhaps above combination smoke in any position Liang Chu of exhaust gases passes and two places.
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| CN 03125276 CN1224445C (en) | 2003-08-15 | 2003-08-15 | Dry-process flue gas desulfurizing method using combined gas jet |
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| CN 03125276 CN1224445C (en) | 2003-08-15 | 2003-08-15 | Dry-process flue gas desulfurizing method using combined gas jet |
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| CN1224445C true CN1224445C (en) | 2005-10-26 |
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|---|---|---|---|---|
| CN101284207B (en) * | 2008-05-29 | 2011-08-17 | 东北电力大学 | Circulating fluid bed flue gas desulfurization tower |
| 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 |
| CN104190233B (en) * | 2014-09-09 | 2015-12-09 | 东南大学 | A flue gas downdraft jet flow desulfurization device |
| CN106669378A (en) * | 2015-11-06 | 2017-05-17 | 江苏大信环境科技有限公司 | Drying reaction tower |
| CN108939854A (en) * | 2018-07-31 | 2018-12-07 | 苏州科博思设备工程有限公司 | A kind of desulfurizer |
| CN110538566A (en) * | 2019-08-22 | 2019-12-06 | 黄震 | dry desulphurization energy-saving hybrid full-load adjustable system and control method |
| CN110975584B (en) * | 2019-12-23 | 2024-09-24 | 中国能源建设集团湖南省电力设计院有限公司 | Novel flue gas purifying tower |
-
2003
- 2003-08-15 CN CN 03125276 patent/CN1224445C/en not_active Expired - Fee Related
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| Publication number | Publication date |
|---|---|
| CN1488426A (en) | 2004-04-14 |
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