CN101116795B - Graded water separation type circulating fluidized bed dry-type flue gas desulfurization technics and the special absorptive tower thereof - Google Patents
Graded water separation type circulating fluidized bed dry-type flue gas desulfurization technics and the special absorptive tower thereof Download PDFInfo
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- CN101116795B CN101116795B CN2006100297032A CN200610029703A CN101116795B CN 101116795 B CN101116795 B CN 101116795B CN 2006100297032 A CN2006100297032 A CN 2006100297032A CN 200610029703 A CN200610029703 A CN 200610029703A CN 101116795 B CN101116795 B CN 101116795B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 61
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- 239000003546 flue gas Substances 0.000 title claims description 92
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 90
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- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 10
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 10
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- 229910001861 calcium hydroxide Inorganic materials 0.000 description 10
- 239000003245 coal Substances 0.000 description 9
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Abstract
The invention discloses a dry fume desulfurization process of classified water distribution circulating fluidized bed, which comprises that a circulating fluidized bed formed through the circulating process of an absorption agent in tower can be absorbed, a desulfurization side product, ash, separated from the dust remover can be recirculated, a desuperheating water is added into the absorption tower by the classified water distribution method, a primary process desuperheating water and a secondary process desuperheating water are respectively transported into two inlets in the different location on the absorption tower through a pipe; furthermore, the invention also discloses a special absorption tower for the above process; the invention can reach a higher desulfurization efficiency under the lower Ca/S ratio condition, meanwhile, the reacting temperature inside the absorption tower can be increased, the consumption of the process desuperheating water can be decreased, the operation cost is saved.
Description
Technical field
The present invention relates to a kind of dry flue gas desulphurization technology, relate in particular to a kind of grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology; In addition, the invention still further relates to the absorption tower of above-mentioned technology special use.
Background technology
Acid deposition and SO
2Pollute is the great environmental problem that international scientific circle and national governments are concerned about always.China is production of energy big country, also is energy-consuming big country, acid deposition and SO
2Pollution has caused very big destruction to the ecological environment of China, administers acid deposition and SO at present
2Pollute and become the emphasis that China administers environment.
At present for acid deposition and SO
2The improvement of polluting, general popular employing " wet desulphurization-lime lime-gypsum method " is both at home and abroad adopted this technology, though desulfurized effect is better, but since its exist " initial investment is big; the fresh water (FW) consumption is big, and floor space is bigger, system, complex structure; equipment corrodes easily; electrisity consumption is big and need handle waste water " etc. problem, therefore, the high-efficiency desulfurization technology of dry method and semidry method is just becoming domestic and international research trend.
For dry method, semi-dry desulphurization technology, the principal element that influences desulfuration efficiency has: effective time of contact of moisture distribution, absorbent activity, granularity, absorbent and former flue gas and contact probability etc. in reaction temperature, the absorption tower.Judge whether a kind of dry method desulfuration system is advanced, also should consider the desulfuration efficiency of system, the resistance of system, power consumption, operating cost, equipment attrition, corrosion, service life, to the adaptability of load variations, and the fresh water (FW) consumption etc.
At present, at home and abroad, the dry method, the semidry method engineering construction precedent that are applicable to burning low-sulfur coal unit of existing many relatively successes, but, when host computer system used sulphur coal, existing dry method, semidry process just many deficiencies can occur: desulfuration efficiency is low, running temperature is low, the fresh water (FW) consumption is big etc.
In recent years, along with domestic surge to the power requirement amount, the low-sulfur coal resources engender in short supply, and the coal that power plant used has obviously the trend to the high sulfur content development, so dry method, semi-dry desulfurizing process that research and development are adapted to use the sulphur coal unit will become inevitable trend.
In dry method, semi-dry desulfurizing process, build good gas (SO
2), solid (absorbent) reaction atmosphere is the key that obtains high desulfuration efficiency, this good reaction atmosphere is: the gas, liquid, solid three-phase coexistence and with strong turbulent flow with guarantee to conduct heat, the carrying out smoothly of mass transfer.
Existing dry method, in the semi-dry desulfurizing process, because the adding of technology desuperheating water all is the modes that adopt disposable fixed point to add, therefore, adding zone at the technology desuperheating water, good gas is arranged, admittedly react atmosphere, but, because the rapid evaporation of moisture, make gas, liquid, Gu the scope of three-phase coexistence is limited in the very little height space, in the desulfurization island of reality is arranged, in order to satisfy the normal operation of each equipment, the ratio that the absorption tower is generally all designed is higher, only the bottom, absorption tower very among a small circle in, just good gas can appear, liquid, Gu three-phase coexistence, and in the bigger upper space of scope, only having gas phase and solid phase, desulphurization reaction is difficult to carry out in this scope.This just has been equivalent to limit absorbent in the absorption tower and effective time of contact of former flue gas, has also wasted the upper space on absorption tower simultaneously.When unit uses sulphur coal, in order to obtain higher desulfuration efficiency, general way is that the addition that strengthens the technology desuperheating water enlarges " gas, liquid, solid three-phase coexistence district " coverage in the absorption tower indirectly at present, though this raising to desulfuration efficiency has certain effect, but this way is also brought many more serious negative effects: the absorption tower outlet temperature is low excessively, and the flue gas dew point temperature raises; The mobile reduction of desulfurization product ash causes grey induction system to be easy to stop up; Overcurrent equipment hardens; The danger increasing of equipment corrosion etc.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology, this technology can reach higher desulfuration efficiency under than the situation of low calcium-sulphur ratio (Ca/S), improve the reaction temperature in the absorption tower simultaneously, reduced the consumption of technology desuperheating water.For this reason, the present invention also will provide a kind of special-purpose absorption tower of above-mentioned technology.
For solving the problems of the technologies described above, the invention provides a kind of grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology, this technology comprises in the absorption tower recirculation of the recirculating fluidized bed that formed by the absorbent circulation, desulfurization product ash that deduster is separated, the mode of this process using classification water distribution adds desuperheating water to the absorption tower, first order technology desuperheating water and second level technology desuperheating water respectively by pipeline be delivered to the absorption tower two diverse locations add inlet.
The inlet that adds of described first order technology desuperheating water is positioned at bottom, absorption tower diffuser, described second level technology desuperheating water add the recirculating fluidized bed transition zone that inlet is positioned at the absorption tower.
This technology also comprises clean flue gas recirculation, and described clean flue gas recirculation is the clean flue gas of part after deduster purifies to be caused the upstream, absorption tower send into from the bottom, absorption tower with former flue gas and recycle.
Described clean flue gas is to be drawn by the horizontal flue collector that air-introduced machine is exported to chimney inlet, and the connecting system place then is chosen on the horizontal flue before the inlet of absorption tower, clean flue gas recirculation amount be under the main frame operating mode flue gas flow 0～40%.
This technology comprises that also clean flue gas send water system, on clean flue gas recirculation flue, the clean flue gas of extension is delivered to the absorption tower by sending water with the adding pipeline of the clean flue gas that refluxes, the inlet that adds of described second level technology desuperheating water is arranged in this adding pipeline that send the clean flue gas of water usefulness backflow, is used for improving the horizontal penetrability of second level water distribution in the absorption tower.
The recirculation of described desulfurization product ash is to be carried again by outside material circulating system by the desulfurization product ash that deduster is separated to get back in the absorption tower, and the absorbent in tower participates in desulphurization reaction.
The absorbent and the circulation desulfurization product ash that are added by the bottom, absorption tower fully mix with the technology desuperheating water that classification adds, after quickening, the Venturi tube that is located at the bottom, absorption tower enters the absorption tower, and at the bottom on absorption tower diffuser formation recirculating fluidized bed, fully mix with the technology desuperheating water that the first order adds at recirculating fluidized bed inner absorbent, circulation desulfurization product ash, form strong turbulent flow, thereby make recirculating fluidized bed have splendid heat transfer and mass transfer characteristic.
The present invention also provides a kind of special-purpose absorption tower of above-mentioned technology, and tower body is a kind of structure of variable cross-section, and it comprises from top to bottom: bottom rectangle section (T1) is used for guaranteeing to dock with the main system flue; Below round knot (T2), this section be provided with fresh absorbent the desulfurization product ash that adds inlet (T8) and recycle add inlet (T9); Venturi tube (T3) in this section, is accelerated after flue gas, absorbent and desulfurization product ash mix; Diffuser (T4), in the continuous reduction of this section owing to flue gas flow rate, its entrained material particles is partly separated and is formed recirculating fluidized bed, and the inlet (T10) that adds of first order technology desuperheating water is positioned at this diffuser (T4); Straight section (T5), this section be exactly the transition zone of recirculating fluidized bed than lower part, its top is the dilute-phase zone of recirculating fluidized bed, what the transition zone of this recirculating fluidized bed was provided with second level technology desuperheating water adds inlet (T11), and the inlet (T11) that adds of this second level technology desuperheating water is arranged on and send in the adding pipeline (T12) of water with the clean flue gas that refluxes; Top round knot (T6); Outlet section (T7).
The outlet of flue gas is positioned at the side of outlet section (T7), and flue gas leaves the absorption tower rear-inclined and enters deduster downwards.
Compared with prior art, beneficial effect of the present invention is: can make system be issued to higher desulfuration efficiency (more than 90%～92.5%) in the situation than low calcium-sulphur ratio (Ca/S=1.1～1.25), especially more can manifest the high efficiency superiority of its desulfurization when unit uses sulphur coal.Improved the reaction temperature in the absorption tower simultaneously, reduced the consumption of technology desuperheating water,, can make system have better load performance by the recirculation of clean flue gas.Be specially:
1, owing to adopted the technology desuperheating water of classification water distribution to add mode, the coverage of " gas, liquid, solid " three-phase coexistence district in the absorption tower obviously enlarges, improved the desulphurization reaction environment in the absorption tower to a great extent, prolonged effective time of contact of absorption tower inner absorbent and former flue gas relatively, just can obtain higher desulfuration efficiency under less technology desuperheating water addition, the raising of the reaction temperature that simultaneity factor is required makes system works safer.
2, desulfuration efficiency height, operating cost is low.Select best CFB (recirculating fluidized bed) operation air velocity easily, Dual-Phrase Distribution of Gas olid is landing speed maximum in CFB, desulfurization reaction zone layer density height, and particle is long in the absorption tower time of staying, makes SO
2Can be mixed fully with desulfurizing agent, guarantee to reach than high desulfurization efficiency.
3, owing to the utilization rate height of desulfurizing agent, the desulfurizing byproduct discharging that it produced is few.The desulfurizing byproduct good fluidity is easy to handle.The ash content overwhelming majority that deduster is collected recycles, and has only on a small quantity to efflux, and grey integrated treatment cost is low.
4, rotatable parts are few, whole device availability height.Be void tower in the absorption tower, do not have moving component, it is little to wear and tear, long service life.
5, control is simple, and because of desulfurizing agent is a dry state, what of injection flow rate bed temperature only depend on, is not subjected to SO in the import flue gas
2The restriction of concentration.
6, load adaptability is good.Owing to adopted the cleaning flue gases recirculating technique, and measure such as desulfurization ash recirculation, can satisfy different boiler load requirements.Boiler load is in 40%～110% scope, and desulphurization system can normally be moved.
7, has good operating flexibility.When the sulfur content increase of coal maybe will improve desulfuration efficiency, need not to increase any equipment, only need regulate the Ca/S mol ratio just.
Description of drawings
The present invention is further detailed explanation below in conjunction with the drawings and specific embodiments:
Fig. 1 is a grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur process flow diagram of the present invention;
The front view on Fig. 2 absorption tower of the present invention;
Fig. 3 is the A-A cutaway view of Fig. 2.
Among Fig. 1: the 1st, the quick lime storehouse; The 2nd, the multi-stag digester; The 3rd, second level technology desuperheating water pipeline; The 4th, first order technology desuperheating water pipeline; The 5th, the calcium hydroxide storehouse; The 6th, calcium hydroxide feed control valve; The 7th, calcium hydroxide feed measuring instrument; The 8th, calcium hydroxide is carried skewed slot; The 9th, clean flue gas recirculation controllable register door; The 10th, send water to regulate butterfly valve with the clean flue gas of recirculation; The 11st, the absorption tower; T10 is the inlet that adds of first order technology desuperheating water; T11 is the inlet that adds of second level technology desuperheating water; The 12nd, deduster; The 13rd, desulfurization product ash recirculating line; The 14th, the desulfurization product ash effluxes pipeline; The 15th, skewed slot is carried in the recirculation of desulfurization product ash; The 16th, the desulfurization product ash effluxes baffle-box; The 17th, air-introduced machine; The 18th, chimney.
Among Fig. 2: T1 is the bottom rectangle section on absorption tower; T2 is the below round knot; T3 is a Venturi tube; T4 is the diffuser on absorption tower; T5 is the straight section on absorption tower; T6 is the top round knot on absorption tower; T7 is an outlet section; T8 is the inlet that adds of fresh absorbent; T9 be recirculation the desulfurization product ash add inlet; T10 is the inlet that adds of first order technology desuperheating water; T11 is the inlet that adds of second level technology desuperheating water; T12 send the adding pipeline of water with the clean flue gas that refluxes.
The specific embodiment
The first, grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur process using of the present invention three kinds of egr modes:
1, the recirculation of the solid particle in the absorption tower has formed the recirculating fluidized bed in the tower:
As shown in Figure 2, be provided with a flue gas accelerator one Venturi tube T3 in the bottom on absorption tower, flue gas and the solid particle that carries thereof are accelerated to very high flow velocity at this, and then the downstream is the diffuser T4 on absorption tower, at this, because the expansion gradually of passage, the flow velocity of flue gas descends fast, its entrained solid particle major part is separated and landing downwards, is formed the recirculating fluidized bed in the tower then again by follow-up high speed flue gas picking-up.Recirculating fluidized bed has splendid heat and material transmission characteristic, is in fierce turbulence state at this regional inner fluid, and the Ca/S value in the recirculating fluidized bed can reach 40-50, and this determines because of fast greatly difference between fine particle and the flue gas.The particle reaction interface constantly rubs, and collision is upgraded, and has greatly strengthened the heat and mass transport of desulphurization reaction.
2, the recirculation of desulfurization product ash:
As shown in Figure 1, carry skewed slot 15 to carry again and get back in the absorption tower 11 by desulfurization product ash recirculating line 13, the recirculation of desulfurization product ash by the desulfurization product ash particle that deduster 12 is separated, absorbent granules in tower participates in desulphurization reaction, the recirculation of desulfurization product ash has improved the utilization rate of absorbent, further reduce Ca/S, save operating cost.
3, clean flue gas recirculation:
As shown in Figure 1, clean flue gas after deduster 12 purifies recycles in the underload lower part, clean flue gas recirculation is the clean flue gas of part to be caused 11 upstreams, absorption tower send into 11 bottoms from the absorption tower with former flue gas, adjust the recirculation volume of clean flue gas according to the situation of change of main unit load, guaranteeing that absorption tower 11 keeps the required exhaust gas volumn of normal fluidization when the main frame underload, thereby can make this system (load accommodation is 40%～110%) under underload have higher desulfuration efficiency and security equally.It comprises a clean flue gas recirculation controllable register door 9 of cover and relevant flue system.
The second, the present invention has adopted the mode of classification water distribution to come to add the desuperheat fresh water (FW) in the absorption tower:
1, as shown in Figure 1, the inlet T10 that adds of first order technology desuperheating water is selected in the concentrated phase area of absorption tower 11 inner loop fluid beds.
The technology desuperheating water that adds vast scale in this zone is because in this zone, the SO in solid phase particles concentration and the former flue gas
2Concentration is all very high, forms " gas, liquid, solid " three-phase coexistence district of good high concentration easily, and this zone has very violent turbulent-flow conditions heat transfer, mass transfer are carried out fast, and this just makes this zone become main desulfurization reaction zone.
2, as shown in Figure 1, the inlet T11 that adds of second level technology desuperheating water is selected in the transition zone of absorption tower 11 inner loop fluid beds.
Though decrease in this zone solid phase particles concentration, also include a considerable amount of absorbents that finish of reaction that do not have in the remaining solid phase particles, and the SO that escapes out from the concentrated phase area of recirculating fluidized bed
2Also a great deal of in addition in flue gas Deng pollution gas, especially when using sulphur coal, SO
2The quantity of escaping from concentrated phase area Deng pollution gas can be more, but because the rapid evaporation of concentrated phase area moisture, after arriving transition zone, the ratio of liquid phase is very thin, is difficult to keep further desulphurization reaction.Therefore need add part technology desuperheating water in this zone again,, make the SO that escapes by concentrated phase area to recover good " gas, liquid, solid " three-phase coexistence state
2Can be removed smoothly in this zone totally Deng pollution gas, further be improved the desulfuration efficiency of system.
Adding for second level technology desuperheating water, because the water yield is less relatively, therefore limited by the penetrability of droplet bundle in flue gas of nozzle ejection, especially in big unit, because the diameter on absorption tower is excessive, the moisture that secondary adds is difficult to cover the cross section on whole absorption tower.Given this, the present invention proposes to improve the jet rigidity (that is: clean flue gas send water) of droplet bundle in the absorption tower with the backflow of the clean flue gas of part.It comprises that one is sent water to regulate butterfly valve 10 and relevant flue system thereof with the clean flue gas of recirculation.
Specify preferred forms of the present invention and technical process below in conjunction with accompanying drawing:
As depicted in figs. 1 and 2, from the flue gas that boiler combustion system is discharged, the bottom rectangle section T1 by the absorption tower enters by former flue gas system.Round knot T2 part high-temperature flue gas and adding absorbent that inlet T8 adds, fully mix below the absorption tower then by fresh absorbent by the circulation ash content that inlet T9 adds that adds of the desulfurization product ash of recirculation, carry out preliminary desulphurization reaction, Venturi tube T3 by the bottom, absorption tower quickens then, be subjected to the percussion of air-flow and suspend at the diffuser T4 on absorption tower inner absorbent, circulation desulfurization ash, form recirculating fluidized bed, carry out sufficient desulphurization reaction.
Diffuser T4 on the absorption tower is provided with the T10 that enters the mouth that adds of first order technology desuperheating water, by a cover high-pressure sprayer, the technology desuperheating water of the vast scale that sprays into is through atomizing back one side humidification particle surface, make the cigarette temperature drop to being higher than dew-point temperature 20-25 ℃ on the other hand, create good " gas, liquid, solid " three-phase coexistence environment and suitable desulfurization reaction temperature.First order technology desuperheating water enters absorption tower 11 by the inlet T10 that adds of first order technology desuperheating water pipeline 4 and first order technology desuperheating water.Also be provided with the T11 that enters the mouth that adds of second level technology desuperheating water in the transition zone (the latter half of the straight section T5 on absorption tower) of recirculating fluidized bed; the adding of the technology desuperheating water of small scale can continue at the good " gas, liquid, solid of this zone maintenance " the three-phase coexistence state, so that desulphurization reaction continued to carry out, relative prolongation effective time of contact of absorbent and former flue gas.Second level technology desuperheating water enters absorption tower 11 by the inlet T11 that adds of second level technology desuperheating water pipeline 3 and second level technology desuperheating water.
For improve technology desuperheating water that secondary adds in the absorption tower horizontal penetrability and improve turbulence intensity in the absorption tower, this technology also disposes " clean flue gas send water system ", on clean flue gas recirculation flue, before the clean flue gas recirculation controllable register door 9, the clean flue gas of extension, after sending water to regulate butterfly valve 10 with the clean flue gas of recirculation by one, 11 the water that send sprays into the absorption tower with the adding pipeline T12 of the clean flue gas of backflow from the absorption tower.The inlet T11 that adds of technology desuperheating water just is arranged among the adding pipeline T12 that send water to use the clean flue gas of backflow for the second time, the fresh water (FW) droplet that it sprayed is wrapped in the stronger clean flue gas stream of rigidity, so, the fresh water (FW) droplet that a plurality of nozzle sprayed just can have good coverage rate (as shown in Figure 3) on the cross section on absorption tower.Fig. 3 has shown adding inlet T11 and sending water with the corresponding relation between the adding pipeline T12 of the clean flue gas of backflow, and their roughly distribution situations after spraying into the absorption tower of second level technology desuperheating water.
As shown in Figure 1, the present invention adopts CaO as original absorbent, Ca (OH)
2As final absorbent, the quick lime of buying outside factory at first is stored in the quick lime storehouse 1, through multi-stag digester 2 quicklime slaking is become calcium hydroxide (final absorbent) then, be transported to by a cover air-transport system calcium hydroxide and carry out buffer memory in the calcium hydroxide storehouse 5, then through accurate metering system---the calcium hydroxide feed control valve 6 of a cover, calcium hydroxide feed measuring instrument 7, carry skewed slot 8 by calcium hydroxide again, it is joined (as shown in Figure 2) before the Venturi tube T3 of 11 bottoms, absorption tower, enter in the absorption tower 11 after being mixed together acceleration with the desulfurization product ash that recycles.
Absorbent and SO
2Fully reaction mainly generates calcium sulfite CaSO
31/2H
2O, calcium sulfate CaSO
41/2H
2O and calcium carbonate CaCO
3, they and flying dust are carried to the outlet section T7 on absorption tower together by cleaning flue gases, be separated in the deduster 12 of back then.The desulfurization product ash of separating is most of to be carried skewed slot 15 to carry again and gets back in the absorption tower 11, with the time of staying of extension of absorbent particle, reduce Ca/S mol ratio in the technical process by desulfurization product ash recirculating line 13, the recirculation of desulfurization product ash.This technology has slightly in the Ca/S mol ratio under the situation of increase, and desulfurization degree is reached more than 95%.For a spot of desulfurization product ash, efflux pipeline 14 by the desulfurization product ash and be discharged into the desulfurization product ash and efflux in the baffle-box 16, enter the ash disposal system of power plant at last.
Clean flue gas after being purified by deduster 12 enters atmosphere by air-introduced machine 17 back of boosting by chimney 18.
Claims (9)
1. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology, it is characterized in that, comprise the recirculating fluidized bed that forms by the absorbent circulation in the absorption tower, the recirculation of the desulfurization product ash that deduster is separated and clean flue gas recirculation, the mode of this process using classification water distribution adds desuperheating water to the absorption tower, first order technology desuperheating water and second level technology desuperheating water respectively by pipeline be delivered to the absorption tower two diverse locations add inlet, described clean flue gas recirculation comprises that clean flue gas send water system, on clean flue gas recirculation flue, the clean flue gas of extension is delivered to the absorption tower by sending water with the adding pipeline of the clean flue gas that refluxes.
2. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology according to claim 1, it is characterized in that, the inlet that adds of described first order technology desuperheating water is positioned at bottom, absorption tower diffuser, described second level technology desuperheating water add the recirculating fluidized bed transition zone that inlet is positioned at the absorption tower.
3. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology according to claim 1, it is characterized in that described clean flue gas recirculation is the clean flue gas of part after deduster purifies to be caused the upstream, absorption tower send into from the bottom, absorption tower with former flue gas and recycle.
4. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology according to claim 3, it is characterized in that, described clean flue gas is to be drawn by the horizontal flue collector that air-introduced machine is exported to chimney inlet, and the connecting system place then is chosen on the horizontal flue before the inlet of absorption tower.
5. according to each described grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology of claim 1-4, it is characterized in that, the inlet that adds of described second level technology desuperheating water is arranged in the adding pipeline that send water to use the clean flue gas of backflow on this clean flue gas recirculation flue, is used for improving the horizontal penetrability of second level water distribution in the absorption tower.
6. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology according to claim 1, it is characterized in that, the recirculation of described desulfurization product ash is to be carried again by outside material circulating system by the desulfurization product ash that deduster is separated to get back in the absorption tower, and the absorbent in tower participates in desulphurization reaction.
7. grade separation ability of swimming circulation fluidized bed dry method flue gas desulfur technology according to claim 1, it is characterized in that, the absorbent and the circulation desulfurization product ash that are added by the bottom, absorption tower fully mix, after quickening, the Venturi tube that is located at the bottom, absorption tower enters the absorption tower, and at the bottom on absorption tower diffuser formation recirculating fluidized bed, fully mix with the technology desuperheating water that the first order adds at recirculating fluidized bed inner absorbent, circulation desulfurization product ash, form strong turbulent flow, thereby make recirculating fluidized bed have splendid heat transfer and mass transfer characteristic.
8. the special-purpose absorption tower of the described technology of claim 1, it is characterized in that: tower body is a kind of structure of variable cross-section, and it comprises from top to bottom: bottom rectangle section (T1) is used for guaranteeing to dock with the main system flue; Below round knot (T2), this section be provided with fresh absorbent the desulfurization product ash that adds inlet (T8) and recycle add inlet (T9); Venturi tube (T3) in this section, is accelerated after flue gas, absorbent and desulfurization product ash mix; Diffuser (T4), in the continuous reduction of this section owing to flue gas flow rate, its entrained material particles is partly separated and is formed recirculating fluidized bed, and the inlet (T10) that adds of first order technology desuperheating water is positioned at this diffuser (T4); Straight section (T5), this section be exactly the transition zone of recirculating fluidized bed than lower part, its top is the dilute-phase zone of recirculating fluidized bed, what the transition zone of this recirculating fluidized bed was provided with second level technology desuperheating water adds inlet (T11), and the inlet (T11) that adds of this second level technology desuperheating water is arranged on and send in the adding pipeline (T12) of water with the clean flue gas that refluxes; Top round knot (T6); Outlet section (T7).
9. special-purpose absorption tower according to claim 8 is characterized in that the outlet of flue gas is positioned at the side of outlet section (T7), and flue gas leaves the absorption tower rear-inclined and enters deduster downwards.
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| CN101288825B (en) * | 2008-06-16 | 2012-02-22 | 万若（北京）环境工程技术有限公司 | Semi-dry type fume cleaning method and device |
| WO2016141988A1 (en) * | 2015-03-11 | 2016-09-15 | Hamon Enviroserv Gmbh | Flue gas cleaning installation and method for cleaning flue gas |
| CN105363338A (en) * | 2015-12-07 | 2016-03-02 | 浙江大学 | Analytical method of desulfurization efficiency influence factors in flue gas desulphurization system |
| CN107308803B (en) * | 2017-08-16 | 2023-07-21 | 华能白山煤矸石发电有限公司 | Circulating fluidized bed desulfurizing tower and control method |
| CN107670491A (en) * | 2017-10-24 | 2018-02-09 | 上海电力学院 | Improve the device of fume circulating fluidized bed desulfurization system material return mechanism characteristic using heat smoke |
| CN110975554A (en) * | 2018-10-03 | 2020-04-10 | 新疆宝新昌佳石灰制品有限公司 | Method for flue gas desulfurization of lime rotary kiln by using kiln tail ash |
| CN114618291A (en) * | 2020-12-10 | 2022-06-14 | 西南科技大学 | Dry digestion and flue gas desulfurization integrated process of quicklime |
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| CN1515349A (en) * | 2003-08-25 | 2004-07-28 | 武汉凯迪电力股份有限公司 | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices |
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