CN1239232C - Multiple reaction integrated process for desulfuizing from fume by dry method and its system - Google Patents
Multiple reaction integrated process for desulfuizing from fume by dry method and its system Download PDFInfo
- Publication number
- CN1239232C CN1239232C CN 200310111260 CN200310111260A CN1239232C CN 1239232 C CN1239232 C CN 1239232C CN 200310111260 CN200310111260 CN 200310111260 CN 200310111260 A CN200310111260 A CN 200310111260A CN 1239232 C CN1239232 C CN 1239232C
- Authority
- CN
- China
- Prior art keywords
- flue
- humidification
- flue gas
- calcium
- desulfurizing tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title abstract description 26
- 230000008569 process Effects 0.000 title abstract description 8
- 239000003517 fume Substances 0.000 title abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 59
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 52
- 239000000292 calcium oxide Substances 0.000 claims abstract description 46
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 46
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims abstract description 41
- 230000023556 desulfurization Effects 0.000 claims abstract description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 35
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 35
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 35
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 35
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000005516 engineering process Methods 0.000 claims abstract description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 10
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims abstract description 8
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims abstract description 7
- 235000010261 calcium sulphite Nutrition 0.000 claims abstract description 7
- 229910000019 calcium carbonate Inorganic materials 0.000 claims abstract description 6
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 105
- 239000003546 flue gas Substances 0.000 claims description 105
- 239000002245 particle Substances 0.000 claims description 68
- 239000007789 gas Substances 0.000 claims description 25
- 229910052717 sulfur Inorganic materials 0.000 claims description 23
- 239000011593 sulfur Substances 0.000 claims description 23
- 239000003245 coal Substances 0.000 claims description 22
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 21
- 239000000779 smoke Substances 0.000 claims description 21
- 238000005243 fluidization Methods 0.000 claims description 17
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 11
- 238000009692 water atomization Methods 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 10
- 238000000889 atomisation Methods 0.000 claims description 9
- 238000002347 injection Methods 0.000 claims description 8
- 239000007924 injection Substances 0.000 claims description 8
- 230000004913 activation Effects 0.000 claims description 6
- 238000013459 approach Methods 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 5
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 abstract description 8
- 239000000843 powder Substances 0.000 abstract description 8
- 235000019738 Limestone Nutrition 0.000 abstract description 6
- 239000006028 limestone Substances 0.000 abstract description 6
- 238000005507 spraying Methods 0.000 abstract description 5
- 239000012716 precipitator Substances 0.000 abstract 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 26
- 239000011575 calcium Substances 0.000 description 19
- 239000002594 sorbent Substances 0.000 description 17
- 239000007787 solid Substances 0.000 description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 7
- 229910052791 calcium Inorganic materials 0.000 description 7
- 239000000047 product Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 230000003068 static effect Effects 0.000 description 4
- 241000282326 Felis catus Species 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 239000003818 cinder Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 210000002249 digestive system Anatomy 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000004570 mortar (masonry) Substances 0.000 description 2
- 150000003463 sulfur Chemical class 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000002716 delivery method Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 230000037452 priming Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The present invention discloses a multiple reaction integrated technology for fume desulfurization by a dry method and a system thereof. The technology comprises the following steps: firstly, limestone powder is sprayed through the top of a high-temperature furnace chamber to decompose calcium carbonate into calcium oxide and carbon dioxide, and partial calcium oxide absorbs sulfur dioxide in fumes to generate calcium sulfate; secondly, the calcium oxide is activated by spraying water in a humidifying flue to transform partial calcium oxide to calcium hydroxide which absorbs the sulfur dioxide in the fumes to generate calcium sulfite; finally, the third desulfurization is completed in a circulating fluidising desulfurizing tower, using the residual calcium hydroxide and calcium oxide. The system is composed of a limestone powder sprayer arranged on the top of the furnace chamber of coal-burning equipment, the humidifying flue connecting coal-burning equipment and the desulfurizing tower, the desulfurizing tower, an external electric precipitator, a draught fan, a chimney, etc. The present invention has the advantages of increased utilization rate of desulfurizing agent, satisfactory desulfurization efficiency, simple technological process, less water consumption, simple system structure, low initial investment and low operation cost.
Description
Technical field
The present invention relates to the flue gas desulfurization technique of coal fired power plant, refer to a kind of integrated dry flue gas desulphurization technology and system thereof of repeatedly reacting particularly.
Background technology
China is that a few is one of country of main energy sources with coal in the world, coal in the production of China's primary energy and consumption ratio always more than 70%, the coal-fired sulfur dioxide (SO2) emissions that produce have formed huge environmental pollution, and the pollution of fundamentally administering sulfur dioxide (SO2) emissions and being caused is imperative.
At present, the technology that is used for coal fired power plant flue gas desulfurization generally has wet method, semidry method and dry desulfurization.In-furnace calcium spraying is a kind of desulfurization by dry method that grows up the sixties in 20th century, is calcium carbonate CaCO because it uses cheap lime stone
3As desulfurizing agent, have characteristics such as small investment, technology be simple, and be subjected to the attention and the exploitation of Europe, the U.S., Japan and other countries, and on the coal fired power plant of 15～700MW, use in succession in the seventies in 20th century.But the utilization rate of calcium is not high in this sulfur method, and desulfuration efficiency also has only about 30%, so how to recycle in the flue gas unreacted calcium oxide CaO to improve desulfuration efficiency be the focus that the scientific research personnel explores always.Finland Tempella company has researched and developed the LIFAC sulfur method, and this method is also set up a priming reaction device except spraying into the agstone before electric cleaner in stove, makes unreacted calcium oxide CaO meet water and generates calcium hydroxide Ca (OH)
2, calcium hydroxide Ca (OH)
2In activated reactor with sulfur dioxide SO
2React, reach the purpose of flue gas desulfurization.Adopt this sulfur method, smoke desulfurization efficiency is greatly improved, desulfuration efficiency can reach about 70%, but the desulphurization system that it adopted is comparatively complicated.For the desulfuration efficiency of further raising system, Finland Tempella company, U.S. B﹠amp; W company has also developed the LIFAC and the LIDS sulfur method of dry ash and mortar recirculation respectively, and the technical process of above-mentioned two kinds of methods is basic identical, is about to collected flying dust, calcium oxide CaO and calcium hydroxide Ca (OH) in electric cleaner, the activated reactor
2Send activated reactor recirculation back to, with its desulfuration efficiency of further raising and calcium utilization.Though the LIFAC and the LIDS sulfur method of the recirculation of dry ash and mortar can improve system's desulfuration efficiency, desulfuration efficiency also has only about 80%, and calcium utilization is improved a lot, and its desulphurization system bulky complex still.
The circulating fluidization fume desulphurization method is a kind of semi-dry process flue gas desulphurization technology that grows up the eighties in 20th century, because this technology has small investment, characteristics such as floor space is little, equipment is simple, desulfuration efficiency height, become the emphasis of researching and developing and promoting in the power environment protection industry.Yet also there is following deficiency in the circulating fluidization fume desulphurization method: the desulfurizing agent that this method is used is high-quality calcium hydroxide Ca (OH)
2Maybe need be through the calcium oxide CaO of digestive system processing, on the one hand because high-quality calcium hydroxide Ca (OH)
2Or the price of calcium oxide CaO is also high, and the operating cost of whole desulphurization system is significantly increased; Owing to increased digestive system, make the complex structure of whole desulphurization system on the other hand, operating cost is high, and the surface-active of hydrated lime particle is difficult for guaranteeing.In addition, because calcium hydroxide Ca (OH)
2Or calcium oxide CaO has certain harm to health, when therefore adopting it as desulfurizing agent, must guarantee that transportation and desulphurization system have good sealing and safety measure, makes system architecture more complicated, and operating cost can't reduce.
Summary of the invention
Purpose of the present invention will overcome above-mentioned existing in prior technology defective exactly, a kind of integrated dry flue gas desulphurization technology and system thereof of repeatedly reacting is provided, adopt this technology and system can improve the utilization rate of desulfurizing agent, reach satisfied desulfuration efficiency, and its technological process is simple, water consumption is less, and system architecture is simplified, and initial cost and operating cost are cheap.
For realizing this purpose, the present invention is designed go out repeatedly react integrated dry flue gas desulphurization technology, adopt the method that humidification activation, circulating fluidization flue gas desulfurization combine in furnace injection agstone, the flue, desulfurization by different level acts synergistically.Its operating process in turn includes the following steps:
1) sprays agstone in the burner hearth flue gas is carried out the processing of desulfurization for the first time: agstone is ejected in the flue gas of coal combustion equipment burner hearth top, make the calcium carbonate in the agstone in hot environment, be decomposed into calcium oxide particle and carbon dioxide, calcium oxide particle immediately with the sulfur in smoke gas generation calcium sulfate that reacts, its desulfuration efficiency is 20～30%.
2) water spray carries out the processing of desulfurization for the second time to flue gas in the humidification flue: calcium oxide particle, flying dust, once desulfurization product and flue gas that desulphurization reaction does not take place in the step 1) are imported in the humidification flue by the coal combustion equipment back-end ductwork, and in the humidification flue jet atomization water, make the calcium oxide particle in the flue gas meet the water humidification activation, reaction generates calcium hydroxide particle, calcium hydroxide particle immediately with the sulfur in smoke gas generation calcium sulfite that reacts, its desulfuration efficiency is 20～30%.
3) water spray carries out desulfurization for the third time to flue gas and handles in the circulating fluidization desulfurizing tower: with step 2) in the calcium hydroxide particle and the remaining calcium oxide particle of desulphurization reaction do not take place, flying dust, once import in the circulating fluidization desulfurizing tower from the outlet of humidification flue rear portion with secondary desulfurization product and flue gas, and in desulfurizing tower jet atomization water once more, calcium hydroxide particle is fully contacted in wet environment with sulfur in smoke gas, and make the reaction of remaining calcium oxide particle and water be converted into calcium hydroxide particle, final calcium hydroxide particle and sulfur in smoke gas reaction generate calcium sulfite; Send the unreacted calcium hydroxide particle of part back in desulfurizing tower circulation absorption sulfur dioxide gas once more by external electric cleaner simultaneously, owing to carried out twice desulphurization reaction before this, this desulfuration efficiency only is 50～60%, and obtain clean flue gas final the separation.
In the step 1) of above-mentioned technology, preferably agstone is ejected into coal combustion equipment burner hearth top temperature range and is in 950～1150 ℃ the flue gas, the easiest calcium oxide particle and the carbon dioxide of being decomposed into of calcium carbonate in this temperature range sodalime stone flour helps improving the utilization rate of agstone.
The step 2 of above-mentioned technology) in, preferably by in the humidification flue, spraying an amount of water droplets, wherein flue-gas temperature is remained in 85～95 ℃ the scope, calcium oxide particle is met the rapid activation of water and is generated calcium hydroxide particle under this temperature conditions, calcium hydroxide particle and sulfur in smoke gas have very high reaction rate, thereby sulfur dioxide gas can be absorbed rapidly.
In the step 3) of above-mentioned technology, preferably by jet atomization water in desulfurizing tower, wherein flue-gas temperature is controlled in 60～75 ℃ the scope, humidity of flue gas is controlled in 11～15% the scope, this moment, the reaction environment condition of calcium hydroxide sorbent particle and sulfur in smoke gas reached optimum state, can effectively improve the utilization rate of smoke desulfurization efficiency and sorbent particle.
Repeatedly react integrated dry flue gas desulphurization system for realizing that above-mentioned technology is custom-designed, comprising links together by smoke conveying duct and recycle stock pipeline forms desulfurizing tower, external electric deduster, air-introduced machine and the chimney of circulating fluidization desulfurization system, also comprises the agstone injection apparatus and the humidification flue that increase newly.The agstone arrangement of nozzles of agstone injection apparatus can be to wherein spraying agstone above the burner hearth of coal combustion equipment.Be provided with the humidification water atomizing nozzle in the humidification flue, can be in the humidification flue even jet atomization water droplet.The anterior import of humidification flue links to each other with the back-end ductwork of coal combustion equipment, and the rear portion outlet of humidification flue links to each other with the gas approach flue of above-mentioned desulfurizing tower.The sulfur-containing smoke gas that gives off from coal combustion equipment carries out the desulfurization first time above the burner hearth of coal combustion equipment, carry out the desulfurization second time in the humidification flue, carries out desulfurization for the third time in the circulating fluidization desulfurizing tower.
Compared with prior art, the invention has the advantages that:
At first, the present invention adopts cheap agstone as desulfurizing agent, and utilize it to generate calcium oxide at furnace injection with certain activity, and calcium oxide and flying dust are through after work of water sprinkling for better material moisture activates in humidification flue and the circulating fluidization desulfurizing tower, can form sorbent particle, increase reaction rate with sulfur dioxide with very high surface activity.So it not only can reduce the desulphurization cost of flue gas, and can improve the desulfuration efficiency of flue gas.
Secondly, the present invention designs the flue gas humidification system behind the coal combustion equipment back-end ductwork, can make the calcium oxide particle in the flue gas meet the rapid activation of water and generate calcium hydroxide sorbent particle efficiently on the one hand, and the part sulfur dioxide gas in the flue gas is absorbed rapidly; Cooling rapidly behind the flue gas humidification on the other hand, the temperature when having reduced it and entering desulfurizing tower has prolonged reaction compartment and reaction time between flue gas and the calcium hydroxide sorbent particle, has significantly improved the utilization rate of sorbent particle.
The 3rd, the present invention carries out desulfurization by different level above the burner hearth of coal combustion equipment, in afterbody humidification flue and the circulating fluidization desulfurizing tower, and each several part equipment is only born a part of desulfurization work.Thereby under the prerequisite that reaches the total system high desulfurization efficiency, the desulfuration efficiency in this desulfurizing tower only need reach 50～60% and get final product.In this case, can suitably reduce the mass flow that recycle stock returns desulfurizing tower, make the interior material concentration of desulfurizing tower remain on 400～600g/m
3Level in, so not only reduced the flow resistance in the desulfurizing tower, and alleviated the operating load of exterior static deduster, thereby also significantly reduced the operating load of whole desulphurization system, further simplified the structure of whole process system.
The 4th, the integrated repeatedly desulphurization reaction of the present invention all carries out under the dry method state, thereby reduces the water consumption of whole desulphurization system greatly.
In sum, the present invention has succinct technological process, simple system structure, cheap operating cost, and higher desulfuration efficiency can reach the desulfuration efficiency more than 93～95% at the low calcium current of Ca/S=1.1～1.2 than under the condition.
Description of drawings
Fig. 1 is a kind of structural representation that repeatedly reacts integrated dry flue gas desulphurization system;
Fig. 2 is installed in structural representation on the humidification flue center line for the humidification water atomizing nozzle;
Fig. 3 is installed in structural representation on the humidification flue sidewall for the humidification water atomizing nozzle;
Fig. 4 is installed in structural representation in the humidification flue for the ring-type turbulator.
The specific embodiment
Below at a coal-fired power station boiler, in conjunction with the accompanying drawings dry flue gas desulphurization technology and system thereof of repeatedly reacting integrated of the present invention is described in further detail:
Repeatedly react integrated dry flue gas desulphurization system shown in the figure, mainly constitute by agstone injection apparatus, humidification flue 9, desulfurizing tower 28, external electric deduster 24, air-introduced machine 25 and the chimney 26 etc. that are connected to become a complete desulfurization system by smoke conveying duct and recycle stock pipeline.
The agstone injection apparatus by limestone powder bin 3, be installed in limestone powder bin 3 lower ends rotation machine supplying powder 2, form with the rotation compressor 1 that links to each other of machine supplying powder 2 and the agstone nozzle 5 that is installed in pulverized coal feed pipe 4 ends by pulverized coal feed pipe 4.Agstone nozzle 5 is arranged in the burner hearth top of coal-fired power station boiler 6.
Desulfurizing tower 28 comprises ash-storing bin 11 at the bottom of the tower, flue gas mixing-chamber 13, Venturi tube fluidisation section 14, flaring cone segments 15, intermediate reaction section 19, cat head changeover portion 20 and tower top section 21 successively.Gas approach flue 12 is arranged on the flue gas mixing-chamber 13.The recycle stock inlet 17 of external electric deduster 24 is arranged on the flaring cone segments 15.The atomized water nozzle 16 of desulfurizing tower 28 is arranged in the bottom of intermediate reaction section 19.Intermediate reaction section 19 inwalls of desulfurizing tower 28 are provided with the essentially identical ring-type turbulent flow generator 18 of ring-type turbulator 8 structures in 1～3 road and the humidification flue 9.The setting of ring-type turbulent flow generator 18, the turbulence level of each the phase material in the desulfurizing tower 28 is significantly increased, heat and mass transfer exchange between reinforcing desulfuration agent particle, flue gas and the water droplets three, increase the time of contact of flue gas and sorbent particle, thereby significantly improve the efficient of desulfurization for the third time.The cat head that connects intermediate reaction section 19 and tower top section 21 excessively section 20 can adopt by polylith plane triangle plate and the splicing of cambered surface triangular plate and surrounds upwards gradually wealthy variation structure of the intracavity section that forms, with the turbulence level and the interior internal circulating load of further increase flue gas, improve the utilization rate and the desulfuration efficiency of sorbent particle.The structure difference with the prior art of this desulfurizing tower 28 is: the sorbent particle nozzle is not set on the body of the tower, and sorbent particle directly enters in the flue gas mixing-chamber 13 of desulfurizing tower 28 from gas approach flue 12 by humidification flue 9.
Sulfur removal technology process of repeatedly reacting integrated dry flue gas desulphurization system of the present invention is such:
At first, the coal dust of coal-fired power station boiler 6 burner hearth internal combustion generates high-temperature flue gas and sulfur dioxide SO
2, and mobile to upper furnace, at the high-temperature area of 950～1150 ℃ of upper furnace formation.At this moment, agstone is sent in the pulverized coal feed pipe 4 through rotation machine supplying powder 2 by limestone powder bin 3, compressor 1 work, compressed air is ejected into agstone in the flue gas of 950～1150 ℃ of burner hearth tops by agstone nozzle 5.The change in flow scope of agstone nozzle 5 is between 35～50 meter per seconds.Spray into agstone and high-temperature flue gas rapid mixing in the burner hearth top, rapid diffusion makes the calcium carbonate CaCO in the agstone
3Be decomposed into calcium oxide CaO and carbon dioxide CO
2, calcium oxide CaO particle immediately with sulfur in smoke SO
2Reaction generates calcium sulfate CaSO
4, finish desulfurization for the first time, can remove 20～30% of total sulfur content in the flue gas approximately.
Secondly, responseless calcium oxide CaO, flying dust, once desulfurization product and flue gas enter in thereafter the humidification flue 9 through economizer, air preheater and the back-end ductwork 7 of coal-fired power station boiler 6.After flue gas enters humidification flue 9, be subjected on the one hand from the cooling of the water droplets of humidification water atomizing nozzle 10 ejections, make flue-gas temperature be reduced to 85～95 ℃ rapidly, flue gas is maintained in this temperature range all the time by the straying quatity of regulating water droplets from 120～150 ℃ of humidification flue 9 anterior imports; Be subjected to the squeezing action of ring-type turbulator 8 on the other hand, be that the part solid particle in the flue gas stream is turned to, flowing in center to humidification flue 9, has strengthened the turbulence level of humidification flue 9 interior flue gas streams with solid particle, prolonged the time of contact of flue gas and solid desulfurating agent particle.At this moment, partial oxidation calcium CaO in the flue gas and atomized water H
2O reacts and generates calcium hydroxide Ca (OH)
2, because calcium hydroxide Ca (OH)
2With sulfur in smoke SO
2Has very high reaction rate, at once just with sulfur dioxide SO
2Absorb and generation calcium sulfite CaSO
3, finish desulfurization for the second time, can remove 20～30% of total sulfur content in the flue gas approximately once more.
Once more, the flue gas that flows out from humidification flue 9 rear portions outlets, flying dust, once with the secondary desulfurization product and the calcium hydroxide particle of desulphurization reaction does not take place and the gas approach flue 12 of remaining calcium oxide particle by desulfurizing tower 28 both sides enters the flue gas mixing-chamber 13, the both sides flue gas enters Venturi tube fluidisation section 14 after mixing.Venturi tube fluidisation section 14 can adopt single tube or multitube to form, the load variations situation that is in operation according to desulfurizing tower 28, flue gas remains in the scope of 25～60 meter per seconds in the speed of Venturi tube fluidisation section 14 throats, and the speed that exports in Venturi tube fluidisation section 14 is controlled in the scope of 8～20 meter per seconds.After smoke mixture enters the bottom reaction zone flaring cone segments 15, intermediate reaction section 19 bottoms of desulfurizing tower 28 from Venturi tube fluidisation section 14, be subjected to the cooling of the atomized water of atomized water nozzle 16 ejections immediately, the recycle stock of separating from exterior static deduster 24 also enters into flaring cone segments 15 through fluid-bed 22 from recycle stock inlet 17, the temperature of flue gas is reduced rapidly and remain in 60～75 ℃ the scope, humidity of flue gas is controlled in 11～15% the scope.Before the remaining calcium oxide CaO of secondary desulphurization reaction particle once more with atomized water H
2O reacts and generates Ca (OH)
2Particle, the solid particle average diameter in the desulfurizing tower 28 are in the scope of 10～80 μ m, and flue gas drive solid particle moves upward and is suspended state.
When smoke mixture rises the cat head changeover portion 20 enter desulfurizing tower 28 tops and tower top section 21, because desulfurizing tower 28 inner chamber cross section in this section increases from bottom to top gradually, flue gas flow rate reduces, there is local eddy currents to produce simultaneously, solid particle bigger in the flue gas is flowed downward, circulation in desulfurizing tower 28, forming along tower side wall.Strengthen collision, particle surface wearing and tearing between flying dust, sorbent particle and the desulfurization product like this, increased the reaction table area of sorbent particle effectively.Sulfur in smoke SO
2With sorbent particle Ca (OH)
2Circulation repeatedly contact in fully reaction generate calcium sulfite CaSO
3, finish desulfurization for the third time, can remove approximately 50～60% of total sulfur content in the flue gas.Meanwhile, a spot of sulfur trioxide SO in the flue gas
3And pernicious gases such as the hydrochloric acid HCl that may exist, hydrogen fluoride HF also are absorbed in the lump and remove.After flue gas is handled through three desulfurization, can be up to 93～95% at the low calcium current of Ca/S=1.1～1.2 than desulfuration efficiency total under the condition.
Then, flue gas flows out from the exhanst gas outlet 27 on the tower top section 21 of desulfurizing tower 28, enters exterior static deduster 24 by flue.Externally in the electrostatic precipitator 24, the solid particle in the flue gas is separated, and wherein contains some not sorbent particle of complete reaction.A separated solid particle part of getting off is returned the desulfurizing tower 28 from recycle stock inlet 17 by fluid-bed 22, carries out the material circulation once more.Another part solid particle comprises that desulfuration byproduct, flying dust etc. then send into cinder tank 23 by the circulating ash ash-valve and store, transport.Send into chimney 26 from the clean flue gas that exterior static deduster 24 comes out through air-introduced machine 25, enter in the atmosphere at last.Fall into the lime-ash of ash-storing bin 11 at the bottom of the tower of desulfurizing tower 28, send in the cinder tank 23 with gas delivery method.
Claims (10)
1. one kind is repeatedly reacted integrated dry flue gas desulphurization technology, in turn includes the following steps:
1) sprays agstone in the burner hearth flue gas is carried out the processing of desulfurization for the first time: agstone is ejected in the flue gas of coal combustion equipment burner hearth top, make the calcium carbonate in the agstone in hot environment, be decomposed into calcium oxide particle and carbon dioxide, calcium oxide particle immediately with the sulfur in smoke gas generation calcium sulfate that reacts;
2) water spray carries out the processing of desulfurization for the second time to flue gas in the humidification flue: calcium oxide particle, flying dust, once desulfurization product and flue gas that desulphurization reaction does not take place in the step 1) are imported in the humidification flue by the coal combustion equipment back-end ductwork, and in the humidification flue jet atomization water, make the calcium oxide particle in the flue gas meet the water humidification activation, reaction generates calcium hydroxide particle, calcium hydroxide particle immediately with the sulfur in smoke gas generation calcium sulfite that reacts;
3) water spray carries out desulfurization for the third time to flue gas and handles in the circulating fluidization desulfurizing tower: with step 2) in the calcium hydroxide particle and the remaining calcium oxide particle of desulphurization reaction do not take place, flying dust, once import in the circulating fluidization desulfurizing tower from the outlet of humidification flue rear portion with secondary desulfurization product and flue gas, and in desulfurizing tower jet atomization water once more, calcium hydroxide particle is fully contacted in wet environment with sulfur in smoke gas, and make the reaction of remaining calcium oxide particle and water be converted into calcium hydroxide particle, final calcium hydroxide particle and sulfur in smoke gas reaction generate calcium sulfite; Send the unreacted calcium hydroxide particle of part back in desulfurizing tower circulation absorption sulfur dioxide gas once more by external electric cleaner simultaneously, obtain clean flue gas final the separation.
2. according to claim 1ly repeatedly react integrated dry flue gas desulphurization technology, it is characterized in that: in the said step 1), it is in 950～1150 ℃ the flue gas that agstone is ejected into coal combustion equipment burner hearth top temperature range.
3. according to claim 1 and 2ly repeatedly react integrated dry flue gas desulphurization technology, it is characterized in that: said step 2), jet atomization water remains in 85～95 ℃ the scope wherein flue-gas temperature in the humidification flue.
4. according to claim 1 and 2ly repeatedly react integrated dry flue gas desulphurization technology, it is characterized in that: in the said step 3), jet atomization water is controlled in 60～75 ℃ the scope wherein flue-gas temperature in desulfurizing tower, and humidity of flue gas is controlled in 11～15% the scope.
5. according to claim 3ly repeatedly react integrated dry flue gas desulphurization technology, it is characterized in that: in the said step 3), jet atomization water is controlled in 60～75 ℃ the scope wherein flue-gas temperature in desulfurizing tower, and humidity of flue gas is controlled in 11～15% the scope.
6. one kind is adopted the described technology of claim 1 and custom-designedly repeatedly reacts integrated dry flue gas desulphurization system, comprise the desulfurizing tower (28), external electric deduster (24), air-introduced machine (25) and the chimney (26) that link together by smoke conveying duct and recycle stock pipeline, it is characterized in that: it also comprises agstone injection apparatus and humidification flue (9), and the agstone nozzle (5) of agstone injection apparatus is arranged in the burner hearth top of coal combustion equipment (6); Be provided with humidification water atomizing nozzle (10) in the humidification flue (9), the anterior import of humidification flue (9) links to each other with the back-end ductwork (7) of coal combustion equipment (6), and the rear portion outlet of humidification flue (9) links to each other with the gas approach flue (12) of desulfurizing tower (28).
7. according to claim 6ly repeatedly react integrated dry flue gas desulphurization system, it is characterized in that: the inwall of said humidification flue (9) is provided with the ring-type turbulator (8) that some roads axial cross section is triangular form, this ring-type turbulator (8) is positioned at the one side of flue gas upstream and the inwall angle α of humidification flue (9)=25～35 °, be positioned at the one side in flue gas downstream and the inwall angle β of humidification flue (9)=35～45 °, outstanding depth H=0.1～the 0.2D of this ring-type turbulator (8), wherein D is the internal diameter or the equivalent internal diameter of humidification flue (9); Each humidification water atomizing nozzle (10) is arranged in the flue gas upstream position of corresponding each road ring-type turbulator (8).
8. according to claim 7ly repeatedly react integrated dry flue gas desulphurization system, it is characterized in that: the intracavity section of said humidification flue (9) is for circular, each humidification water atomizing nozzle (10) is arranged on the axle center of humidification flue (9), and its spray direction is consistent with the flow of flue gas direction.
9. according to claim 7ly repeatedly react integrated dry flue gas desulphurization system, it is characterized in that: the intracavity section of said humidification flue (9) is a rectangle, each humidification water atomizing nozzle (10) is distributed on the inwall of humidification flue (9), and its spray direction level is pointed to the axle center of humidification flue (9).
10. describedly repeatedly react integrated dry flue gas desulphurization system according to claim 6 or 7 or 8 or 9, it is characterized in that: intermediate reaction section (19) inwall of said desulfurizing tower is provided with some roads ring-type turbulent flow generator (18) identical with ring-type turbulator (8) structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310111260 CN1239232C (en) | 2003-10-23 | 2003-10-23 | Multiple reaction integrated process for desulfuizing from fume by dry method and its system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310111260 CN1239232C (en) | 2003-10-23 | 2003-10-23 | Multiple reaction integrated process for desulfuizing from fume by dry method and its system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1537668A CN1537668A (en) | 2004-10-20 |
| CN1239232C true CN1239232C (en) | 2006-02-01 |
Family
ID=34335987
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310111260 Expired - Fee Related CN1239232C (en) | 2003-10-23 | 2003-10-23 | Multiple reaction integrated process for desulfuizing from fume by dry method and its system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1239232C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101596398B (en) * | 2009-05-08 | 2012-05-23 | 朱学智 | Re-devulcanization method based on circulating fluidized bed boiler flue |
Families Citing this family (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100449208C (en) * | 2004-11-23 | 2009-01-07 | 河南大学 | Boiler furnace desulfurization and flue gas activation desulfurization and dust removal device |
| CN100357014C (en) * | 2006-01-06 | 2007-12-26 | 易晓辉 | Chimney desulfurizing tower integrated desulfurizing process and apparatus thereof |
| CN100418613C (en) * | 2006-11-17 | 2008-09-17 | 北京科技大学 | A dense-phase circulating fluidized desulfurization equipment |
| CN101177267B (en) * | 2007-10-31 | 2010-10-13 | 武汉凯迪电力环保有限公司 | Method and system for producing food-grade carbon dioxide from power station flue gas |
| 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 |
| CN102233230A (en) * | 2011-07-18 | 2011-11-09 | 创冠环保(中国)有限公司 | Waste burning smoke purification process and purification system |
| ES2602988T3 (en) * | 2012-10-16 | 2017-02-23 | General Electric Technology Gmbh | Desulfurization in a regenerative calcium cycle system |
| CN103285726A (en) * | 2013-06-21 | 2013-09-11 | 山西平朔煤矸石发电有限责任公司 | Circulating fluidized bed boiler desulfurization method |
| CN103861440B (en) * | 2013-12-26 | 2016-01-20 | 张明鑫 | Layer burning stove desulfurization removing nitric flue gas treating process |
| JP6351278B2 (en) | 2014-01-31 | 2018-07-04 | 三菱日立パワーシステムズ株式会社 | Exhaust gas treatment system |
| CN105617851B (en) * | 2016-03-16 | 2018-08-28 | 中国科学院城市环境研究所 | A kind of method and its device of efficient double tower semi-dry desulphurization |
| CN107661693A (en) * | 2016-07-28 | 2018-02-06 | 哈尔滨博深科技发展有限公司 | A kind of method and combined system of the flue gas denitrification system stable operations of SCR in low- load conditions |
| CN106390727B (en) * | 2016-10-27 | 2019-10-18 | 福建龙净脱硫脱硝工程有限公司 | A kind of dry desulfurizing process handling low-temperature flue gas |
| CN107308803B (en) * | 2017-08-16 | 2023-07-21 | 华能白山煤矸石发电有限公司 | A circulating fluidized bed desulfurization tower and its control method |
| CN107661682B (en) * | 2017-11-03 | 2024-02-06 | 中冶赛迪工程技术股份有限公司 | Flue with intensive mixing component and active carbon injection system |
| CN109173694B (en) * | 2018-09-28 | 2024-04-09 | 河南安彩高科股份有限公司 | Desulfurization reaction tube, desulfurization dust removal system based on desulfurization reaction tube and process of desulfurization dust removal system |
| CN110038420A (en) * | 2019-03-14 | 2019-07-23 | 张家港市艾尔环保工程有限公司 | Flue gas full-dry method purifying technique |
| CN111715049A (en) * | 2020-07-02 | 2020-09-29 | 中冶华天工程技术有限公司 | Air flow disturbance device installed on circulating fluidized bed absorption tower |
| CN113144772B (en) * | 2021-04-30 | 2022-10-14 | 青铜峡铝业股份有限公司宁东铝业分公司 | Two-section type electrolytic flue gas purification and discharge device, control system and method |
| CN113117472B (en) * | 2021-05-27 | 2022-07-26 | 江苏峰业环境科技集团股份有限公司 | High-efficient SDS dry desulphurization unit |
| CN113680192A (en) * | 2021-08-14 | 2021-11-23 | 江苏神舟灯饰有限公司 | Waste smoke and waste gas treatment process |
| CN113797755A (en) * | 2021-10-26 | 2021-12-17 | 西安热工研究院有限公司 | A device and method for removing SO3 by using SCR denitration device |
| CN114225667A (en) * | 2021-11-26 | 2022-03-25 | 国家能源集团国源电力有限公司 | Desulfurization equipment and method |
| CN115007617A (en) * | 2022-04-21 | 2022-09-06 | 童铨 | A method for reforming solid waste multiphase resources |
| CN115055040B (en) * | 2022-07-20 | 2024-04-30 | 天津水泥工业设计研究院有限公司 | Low-temperature denitration sulfur fixation method and system based on cement clinker production line |
-
2003
- 2003-10-23 CN CN 200310111260 patent/CN1239232C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101596398B (en) * | 2009-05-08 | 2012-05-23 | 朱学智 | Re-devulcanization method based on circulating fluidized bed boiler flue |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1537668A (en) | 2004-10-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1239232C (en) | Multiple reaction integrated process for desulfuizing from fume by dry method and its system | |
| CN1239235C (en) | Dry smoke cleaning process for desulfurizing and denitrating simultaneously and its system | |
| CN101385943A (en) | Simultaneous removal process based on semi-dry method | |
| CN203436995U (en) | Cooperative control device for multi-pollutant in sintering flue gas | |
| CN101653682A (en) | Boiler-rear flue gas desulphurization and synergism device of circulating fluid bed boiler and desulphurization and synergism method | |
| CN106582232A (en) | Synergistic removal tending to zero discharge purification process and equipment for multicomponent pollutants in flue gas | |
| CN104984656B (en) | Multistage internal circulation semi-dry method desulfurization, denitrification and demercuration integrated device | |
| CN101385941B (en) | Efficient circulating fluid bed flue-gas desulfurizing device | |
| CN1172738C (en) | Composite Desulfurization Process of Circulating Fluidized Bed Boiler | |
| CN1896591A (en) | Smoke purifier of domestic refuse incinerator | |
| CN1137759C (en) | Method and device for comprehensive purification of waste incineration tail gas | |
| CN1895748A (en) | Smoke desulfurization and its desulfurizer by semi-drying method and with straight air-flow along wall | |
| CN217220890U (en) | Domestic waste burns flue gas denitration deacidification dust removal integration system of optimization | |
| CN1425491A (en) | Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower | |
| CN101116795B (en) | Graded water separation type circulating fluidized bed dry-type flue gas desulfurization technics and the special absorptive tower thereof | |
| CN201316600Y (en) | Large double-circulating fluidized bed semi-dry flue gas desulfurization tower | |
| CN1226073C (en) | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices | |
| CN101780370B (en) | Desulphurizing device based on internal circulation W type multi-fluid alkali fog generator and desulphurizing method | |
| CN219580220U (en) | SDS desulfurization system suitable for low temperature flue gas | |
| CN1224445C (en) | Dry-process flue gas desulfurizing method using combined gas jet | |
| CN101721907B (en) | Flue gas desulfurizing method for W-shaped multi-fluid alkaline spray generator | |
| CN1293935C (en) | Compound circulating jet fluidized bed smoke desulfurization method and reaction tower | |
| CN206064142U (en) | A kind of spouted fluidized bed desulfuring and denitrifying apparatus | |
| CN114452793A (en) | Optimized domestic garbage incineration flue gas denitration, deacidification and dedusting integrated method | |
| CN1204958C (en) | Dry-process flue gas desulfurizing method with W-type circulating fluidization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20180628 Granted publication date: 20060201 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20210628 Granted publication date: 20060201 |
|
| PD01 | Discharge of preservation of patent | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20210628 Granted publication date: 20060201 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20230628 Granted publication date: 20060201 |
|
| PD01 | Discharge of preservation of patent | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20230628 Granted publication date: 20060201 |
|
| PP01 | Preservation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060201 |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20231023 Granted publication date: 20060201 |
|
| PD01 | Discharge of preservation of patent |