CN1513583A - Dry process stack gas desulfur reaction tower with variation structure - Google Patents
Dry process stack gas desulfur reaction tower with variation structure Download PDFInfo
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- CN1513583A CN1513583A CNA03125294XA CN03125294A CN1513583A CN 1513583 A CN1513583 A CN 1513583A CN A03125294X A CNA03125294X A CN A03125294XA CN 03125294 A CN03125294 A CN 03125294A CN 1513583 A CN1513583 A CN 1513583A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 64
- 238000001035 drying Methods 0.000 title 1
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 106
- 239000002245 particle Substances 0.000 claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 107
- 239000003546 flue gas Substances 0.000 claims description 105
- 238000005243 fluidization Methods 0.000 claims description 45
- 239000002594 sorbent Substances 0.000 claims description 31
- 230000008676 import Effects 0.000 claims description 18
- 230000006698 induction Effects 0.000 claims description 8
- 239000000779 smoke Substances 0.000 claims description 6
- 238000000034 method Methods 0.000 abstract description 17
- 238000002156 mixing Methods 0.000 abstract description 10
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- 239000003517 fume Substances 0.000 abstract 3
- 238000006477 desulfuration reaction Methods 0.000 description 27
- 230000023556 desulfurization Effects 0.000 description 24
- 238000013461 design Methods 0.000 description 19
- 238000005516 engineering process Methods 0.000 description 15
- 239000007789 gas Substances 0.000 description 9
- 239000012530 fluid Substances 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 230000001351 cycling effect Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000011575 calcium Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000003134 recirculating effect Effects 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000000505 pernicious effect Effects 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000009692 water atomization Methods 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
A dry-method fume-desulfurizing reaction tower with varied structure is composed of fume mixing chamber at bottom, fume jetting unit, fluidizing region at lower part, main reaction region at middle part, the upper region, fresh desulfurizing agent inlet, external recirculated particles inlet, nozzle for atomizing water, and fume outlet. Said main reaction region is composed of more sub-segments with varied structure, that is, each sub-segment has different inlet cross-section and outlet cross-section to form a multi-direction flowing and eddy region, resulting in high desulfurizing efficiency.
Description
Technical field
The present invention relates to a kind of dry flue gas desulphurization reaction tower of the structure that makes a variation, belong to the flue gas desulfurization technique field, relate to a kind of maximization tower body design of dry flue gas desulphurization technical field, special in the large-scale dry flue gas desulphurization technology of the circulating fluidization of single-tower muiti-bed.
Background technology
The improvement of sulfur dioxide gas body pollution is the emphasis of world's most countries environmental protection always, and its pollutant that produces causes the greatest contamination source of China's environmental destruction especially, has become the task of top priority of China's air pollution treatment at present.
Present improvement to sulfur dioxide, external general main employing wet type lime stone-gypsum method (W-FGD), adopt said method, though removal effect is better, investment is huge, water consumption is big but it exists, floor space is big, system complex, big, the complex structure of resistance, and need handle or the like a series of problems again to water.Therefore the high-efficiency flue gas desulfurization technology of dry type or half dry type becomes the emphasis of domestic and international research and development.
Special is the flue gas desulfurization market demand of 600MW at China's thermal power generation separate unit installed capacity substantially, special specific (special) requirements at area, northwestward power environment protection, and country is to the reinforcement of water resource utilization protection.Simultaneously according to the objective law in flue gas desulfurization technique development and market in the world, advanced person's maximization (applicable to the above thermal power generation unit of 600MW) dry flue gas desulphurization technology will become the main force in domestic and international power environment protection technology and market.
For present all dry method (semidry method) desulfur technology and patented technologies, though they all the flue gas desulfurization course of reaction certain some aspect have oneself technical characteristic, but all do not have to consider after unit maximizes, because the increase of desulphurization reaction tower section and height will cause whole desulphurization reaction owing to the tissue failure in flue gas and particle flow field does not reach the desulfur technology requirement.
Especially for the desulfurization by dry method of the flue gas circulating fluidized bed method of present application, mostly utilize postdigestive lime (slurry) as absorbent, the material of separating with absorbent and external separator is as the circulation fluidized bed material, is used for pernicious gas in the flue gas by strong gas-solid liquid three-phase in fluid bed reacting tower.As patent CN86108755A, CN1307926 or the like, " reverse-flow type circulating fluid bed flue-gas desulfurizing technology " of and for example German Wulff company etc., all be to adopt a desulfurization reaction tower that is similar to fluid bed, realize the desulfurization purpose by haptoreactions in tower such as flue gas, sorbent particle and water sprays, and all be single design of single tower, all exist the heavy in section list tower after maximizing to design the basic fundamental requirement that to satisfy circulating fluidization.
As seen, in ciculation fluidized flue gas desulphurization system, the fluidisation requirement that can the heterogeneous flow field tissue in the tower satisfy design is the key factor that can desulphurization reaction carry out smoothly from the above-mentioned background technology introduction.And all at present fluidization desulfurization by dry method all exist when unit capacity is big, can not satisfy the fluidization requirement of maximization flue gas desulfurization reaction.
Summary of the invention
At deficiency and the defective that prior art exists, purpose of the present invention and task provide the desulfurizing tower in a kind of novel circulating fluidization dry flue gas desulphurization technology.The structural design of the circulating fluidization reaction tower for stack gas desulfurization by a kind of many complicated variation structures, make its can guarantee under higher boiler unit load (＞=600MW) satisfy the balanced fluid mapper process of heavy in section desulfurizing tower.And complexity variation structure by the tower body cross section, change the flow regime of flue gas each sectional position in tower body, make flue gas any one sectional position in tower all present the combination liquid form of a plurality of vortexes of all directions, strengthen the mixing intensity of flue gas and sorbent particle, along the flue gas ascent direction, ladder reduces the empty cross section speed of flue gas in the tower, and because the existence of the vortex of each position, improve the interior internal circulating load of sorbent particle in tower body greatly, alleviate the sorbent particle ratio of external recirculation, alleviated the operation burden of separator.The present invention has not only improved flue gas desulfurization reaction efficiency in the tower, has more solved technical problems such as the external particle separation equipment that influences the maximization flue gas desulfurization technique and face (as electrostatic precipitator etc.) particle separation load is excessive.
Technical scheme of the present invention:
The dry flue gas desulphurization reaction tower of variation structure of the present invention comprises between the fluidization regions of flue gas mixing-chamber, flue gas induction apparatus, desulfurizing tower bottom of desulfurizing tower bottom, between the main reaction region at desulfurizing tower middle part and the upper interval of desulfurizing tower and inlet, the inlet of external recirculation particle, atomized water nozzle, the exhanst gas outlet of the fresh sorbent particle on the tower body, between the main reaction region at its desulfurizing tower middle part and/or the desulfurizing tower upper interval adopt the variation structure.
The dry flue gas desulphurization reaction tower of described many complicated variation structures, desulfurizing tower section by a plurality of variation structures between the main reaction region at its desulfurizing tower middle part constitutes, the outlet shape of each desulfurizing tower section is different with the import cross sectional shape, and the outlet of next section is exactly the inlet of the preceding paragraph.
The cross-sectional area in the outlet of each desulfurizing tower section and import cross section becomes big from the bottom up gradually between the main reaction region at its desulfurizing tower middle part, and discharge area is 1.1～1.5 times of its import sectional area.
The import and export cross section of the desulfurizing tower of its variation section is X along the width of equipment is long, is Y along the depth direction of equipment is long, and when a cross section is microscler when being X 〉=1.5Y, then another cross section is X=0.8～1.2Y for approximate conformality.
Between the import of the desulfurizing tower section of its variation and the outlet is the excessive face of nature.
Cross section, import and export cross section of the desulfurizing tower section of variation is microscler, promptly replaces the combined shaped of two minor faces by two long limits of rectangle with circular arc, and then another cross section is that approximate conformality is polygon-shaped or round-shaped the best.
The dry flue gas desulphurization reaction tower of described many complicated variation structures, the inlet of the upper interval of its desulfurizing tower adopts circular cross-section, it upwards makes a variation into the tower body cross section of a rectangular edges and arc section combination, constitute the variation section of upper interval, the discharge area of this variation section is 1.1～2.0 times of its entrance section.
The dry flue gas desulphurization reaction tower of described many complicated variation structures is divided into more than 2 or 2 independently fluidisation bed between the fluidization regions of its desulfurizing tower bottom, independently fluidisation bed has two kinds of arrangements, and one is evenly to arrange along the unit width; Another kind of for evenly to arrange along the circumferencial direction of tower body, and bed constituted between the fluidization regions of desulfurizing tower by these fluidisations.In the flue gas mixing-chamber of desulfurizing tower bottom, be furnished with smoke deflector, the mist of flue gas or flue gas and flue gas recycled be evenly distributed in the flue gas induction apparatus of each fluidisation bed.
The dry flue gas desulphurization reaction tower of described many complicated variation structures, the multiple jet flow that is furnished with the recirculation clean flue gas at desulfurizing tower tower body middle part enters the mouth, and forms the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthens the intensity of general headquarters' desulphurization reaction.
Advantage of the present invention:
At first, the present invention can adopt the fluidization technology of single-tower muiti-bed equally, has solved the fluidisation problem of the sorbent particle after single tower maximizes, problem is organized in the flow field of heterogeneous chemical reaction process.The present invention is applicable to the 200-1000MW fired power generating unit, be specially adapted to the single-tower muiti-bed flue gas desulfurization technique and the performance requirement of the fired power generating unit about 600MW, cycling rate can guarantee that between 30%-75% system is issued to higher desulfuration efficiency (more than the 90%-92%) in the situation of Ca/S=1.1-1.3 in the particle in the desulfurizing tower; Desulfurizing tower flow of flue gas resistance is less than 1800Pa.
The second, the present invention adopts complicated variation structure in main reaction region and desulfurizing tower upper area, has strengthened heterogeneous mixing and turbulence intensity that desulphurization reaction needs, has improved desulphurization reaction efficient.
The 3rd, complicated variation tower body of the present invention design has formed the multi-direction of inner each position of tower body and has flowed and the vortex, greatly improved the interior cycle efficieny of particle of desulfurizing tower, cycling rate reaches as high as about 75% of whole particle recirculation in the particle, this has not only improved desulphurization reaction efficient, has more solved the burden of the excessive particle sorting apparatus that causes of external particle recirculation volume (as electrostatic precipitator, sack cleaner, inertia separator or their combining form).Special flue gas dry desulfurizing equipment at maximization 600MW and above unit, solved the dust collection capacity restricted problem of organizing problem and crucial deduster subsidiary engine in particle recirculating technique problem, the three-phase turbulent flow flow field of the key that influences maximization desulphurization system design and running.
The 4th, the present invention not only has above-mentioned advantage, the flue gas desulphurization system design of adopting the present invention to carry out, high desulfurization efficiency (between calcium sulfur ratio 1.1～1.3, can reach the desulfuration efficiency more than 90～92%), wide regulating ratio (high-efficiency desulfurization that satisfies combustion apparatus 20%～110% load variations requires) have been realized equally, the desulfur technology requirement of low investment and operating cost, low water consumption.
Description of drawings
Fig. 1 looks schematic diagram for the master of special-shaped desulfurizing tower of the present invention;
Fig. 2 is the schematic side view of special-shaped desulfurizing tower;
Fig. 3 is a desulfurizing tower upper interval variation section outlet schematic diagram;
Fig. 4～8th, the import and export schematic cross-section of abnormity section between the main reaction region at desulfurizing tower middle part.
Fig. 9 is the front view of flow of flue gas signal in the desulfurizing tower;
Figure 10 is the side view of flow of flue gas signal in the desulfurizing tower;
Figure 11 is the flow of flue gas schematic diagram of the positive tee section of desulfurizing tower;
Figure 12 is the flow of flue gas schematic diagram in the microscler cross section of desulfurizing tower.
Among the figure: flue gas mixing-chamber 1, gas approach 1-1, lower resistance flue gas induction apparatus 2, between the fluidization regions of desulfurizing tower fluidisation bottom 3, between the middle part main reaction region of desulfurizing tower 4, desulfurizing tower upper interval 5, the exhanst gas outlet 6 of desulfurizing tower, fresh desulfurizing agent entrance 7, water atomization entrance 8, the refluxing opening 9 of external recirculation sorbent particle, smoke deflector 10, fluidisation bed 3-1, son section 4-1 between the middle part main reaction region of desulfurizing tower, the variation section 5-1 of desulfurizing tower upper interval, combination smoke jet inlet 11.
The specific embodiment
The present invention has proposed the complexity variation structure design principle and the art designs scheme of desulfurizing tower in the dry flue gas desulphurization field, the special fluidization technology of the single-tower muiti-bed that adopts at maximization dry flue gas desulphurization system, in the tower body design, by the variation design is adopted in the cross section of each position of tower body, fluidised three-phase (flue gas is satisfied in each space in tower, sorbent particle, the atomized water particle) the strong mixing, and realize that very high turbulence intensity improves desulphurization reaction efficient, and because tower body cross section variation, flow of flue gas forms multidirectional in the tower, each cross section all will have more recirculating zone to exist in the tower, this will greatly improve the interior internal circulating load of sorbent particle in the tower, and improve the velocity-slip of flue gas and particle, thereby realize the specification requirement of cycling rate in high desulfurization efficiency and the high particle.
The present invention is primarily aimed between the middle main reaction region of desulfurizing tower and the desulfurizing tower upper interval.
As depicted in figs. 1 and 2: have between flue gas mixing-chamber 1, lower resistance flue gas induction apparatus 2, desulfurizing tower fluidisation bottom fluidization regions 3 at the bottom of the tower; 3 are furnished with the inlet 7 of fresh sorbent particle and the inlet 9 of external recirculation desulfurization particle between the fluidization regions of desulfurizing tower; initiate sorbent particle and external recirculation sorbent particle feed back all enter 3 bottoms between the desulfurizing tower fluidization regions respectively, and water atomizing nozzle 8 is arranged between each fluidization regions near 3 the exit position.For the large-scale circulating fluidization desulfurizing tower that adopts single-tower muiti-bed, promptly be divided into more than 2 or 2 independently fluidisation bed 3-1 between the fluidization regions of desulfurizing tower bottom, independently fluidisation bed has two kinds of arrangements, and one is evenly to arrange along the unit width; Another kind of for evenly to arrange along the circumferencial direction of tower body, and bed constituted between the fluidization regions of desulfurizing tower by these fluidisations.In the flue gas mixing-chamber of desulfurizing tower bottom, be furnished with smoke deflector 10, the mist of flue gas or flue gas and flue gas recycled be evenly distributed in the flue gas induction apparatus 2 of each fluidisation bed.
Begin to make a variation from 3 outlets between fluidization regions, enter in the middle of the desulfurizing tower between main reaction region 4, the 4 desulfurizing tower section 4-1 by a plurality of variation structures constitute between main reaction region, the outlet shape of each desulfurizing tower section is different with the import cross sectional shape, and the outlet of next section is exactly the inlet of the preceding paragraph.The outlet of each desulfurizing tower section and the cross-sectional area in import cross section become big from the bottom up gradually, and discharge area is 1.1～1.5 times of its import sectional area.Mouthful cross section of advancing, set out of the desulfurizing tower of its variation section is X along the width of equipment is long, is Y along the depth direction of equipment is long, and when a cross section is microscler when being X 〉=1.5Y, then another cross section is X=0.8～1.2Y for approximate conformality.Between the import of the desulfurizing tower section of variation and the outlet is excessive face.The import and export cross section of the desulfurizing tower section of variation, a cross section is microscler, comprise Fig. 6 rectangle, Fig. 7 replace the combined shaped of two minor faces, the ellipse of Fig. 8 etc. by two long limits of rectangle with circular arc; Then another cross section is that approximate conformality is promptly as the circle of polygon-shaped, Fig. 5 of Fig. 4 etc.But replace the combined shaped of two minor faces with a cross section by two long limits of rectangle with circular arc, another cross section be circular the best.So both can satisfy the balanced fluid mapper process of heavy in section desulfurizing tower, pass through the complexity variation structure in tower body cross section again, change the flow regime of flue gas each sectional position in tower body, make flue gas any one sectional position in tower all present the combination liquid form of a plurality of vortexes of all directions, strengthened the mixing intensity of flue gas and sorbent particle, and along the flue gas ascent direction, ladder reduces the empty cross section speed of flue gas in the tower, simultaneously because the existence of the vortex of each position, greatly improve the interior internal circulating load of sorbent particle in tower body, alleviate the sorbent particle ratio of external recirculation.
The inlet of the upper interval 5 of desulfurizing tower adopts circular cross-section, this inlet promptly be in the middle of 4 outlet between main reaction region, upwards then make a variation into the tower body cross section of rectangle three limits and circular arc combination, as Fig. 3, constitute the variation section 5-1 of upper interval, the discharge area of this variation section is 1.1～2.0 times of its entrance section.So both can satisfy the balanced fluid mapper process of heavy in section desulfurizing tower, pass through the complexity variation structure in tower body cross section again, change the flow regime of flue gas each sectional position in tower body, make flue gas any one sectional position in tower all present the combination liquid form of a plurality of vortexes of all directions, strengthened the mixing intensity of flue gas and sorbent particle, and along the flue gas ascent direction, ladder reduces the empty cross section speed of flue gas in the tower.Because the existence of the vortex of each position improves the interior internal circulating load of sorbent particle in tower body greatly, alleviate the sorbent particle ratio of external recirculation simultaneously.The exhanst gas outlet 6 of desulfurizing tower is arranged above the variation section, and desulfurizing tower top cat head shrinks, so that strengthen the backflow of sorbent particle on desulfurizing tower top.
Desulfurizing tower tower body middle part at the requirement of maximization desulfurization chemical reaction, also is furnished with the multiple jet flow inlet 11 of recirculation clean flue gas, so that form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthens the desulphurization reaction intensity of middle part desulfurizing tower,
Specify the technical process of using system of the present invention below in conjunction with accompanying drawing.
At first, the flue gas that the need desulfurization of discharging from combustion apparatus is handled sends into the flue gas mixing-chamber 1 from gas approach 1-1, be assigned to equably in the flue gas induction apparatus 2 of desulfurizing tower bottom by the deflector 10 that is arranged in the mixing chamber, the muzzle velocity scope of keeping the flue gas jet is the 10-55 meter per second, acceleration enters between the desulfurizing tower fluidization regions, perhaps each fluidisation bed bottom of many designs.
Simultaneously, with sorbent particle (as Ca (OH)
2); its particle size range is 1～10 μ m particle; spray into 3 bottoms between each fluidization regions of desulfurizing tower by sorbent particle entrance 7; while top, sorbent particle entrance 7 position of 3 bottoms between fluidization regions is furnished with the refluxing opening 9 of external recirculation sorbent particle; flue gas enter the bottom of desulfurization reaction tower with from the highly active desulfurization agent particle of nozzle 7 spirts, by the 8 atomizing cooling waters that spray into; with separate from deduster come in to recycle sorbent particle from spout 9 and mix, 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 1-6 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.
Between the main reaction region of desulfurizing tower 4, because complicated variation structural design, form the multidirectional of each sectional position and flow in that tower body is inner, and form between multipoint vortex, flow of flue gas is as shown in accompanying drawing 9,10,11,12 in its desulfurizing tower.The great like this three-phase turbulent flow mixing intensity of having strengthened between main reaction region has been strengthened desulphurization reaction speed, has formed the flow field in tower characteristic of high backflow of particles simultaneously, has improved the interior cycle efficieny of sorbent particle.
Between the main reaction region of the tower body of desulfurizing tower middle part 4, at the requirement of maximization desulfurization chemical reaction, be furnished with the multiple jet flow 11 of recirculation clean flue gas, form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the desulphurization reaction intensity at desulfurizing tower middle part.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 through the variation structure of desulfurizing tower top 5-1, because amplify in the cross section, flue gas slows down and is drawn by the outlet conduit 6 at desulfurizing tower top, and quite a few sorbent particle the main reaction region 4 that enters desulfurizing tower recycles because variation and reduction of speed reflux.
Core of the present invention is complexity variation structure design principle and the art designs scheme that has proposed desulfurizing tower in the dry flue gas desulphurization field, the special fluidization technology of the single-tower muiti-bed that adopts at maximization dry flue gas desulphurization system, in the tower body design, by the variation design is adopted in the cross section of each position of tower body, fluidised three-phase (flue gas is satisfied in each space in tower, sorbent particle, the atomized water particle) the strong mixing, and realize that very high turbulence intensity improves desulphurization reaction efficient, and because tower body cross section variation, flow of flue gas forms multidirectional in the tower, each cross section all will have more recirculating zone to exist in the tower, this will greatly improve the interior internal circulating load of sorbent particle in the tower, and improve the velocity-slip of flue gas and particle, thereby realize the specification requirement of cycling rate in high desulfurization efficiency and the high particle.Therefore, the variation structure design principle and the technical scheme of every employing desulfurizing tower all belong to protection scope of the present invention.
Claims (10)
1. the dry flue gas desulphurization reaction tower of the structure that makes a variation, it comprises between the fluidization regions of flue gas mixing-chamber, flue gas induction apparatus, desulfurizing tower bottom of desulfurizing tower bottom, between the main reaction region at desulfurizing tower middle part and the upper interval of desulfurizing tower and inlet, the inlet of external recirculation particle, atomized water nozzle, the smoke entrance of the fresh sorbent particle on the tower body, it is characterized in that between the main reaction region at desulfurizing tower middle part and/or the desulfurizing tower upper interval adopts the variation structure.
2, the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 1, it is characterized in that between the main reaction region at desulfurizing tower middle part constituting by the desulfurizing tower section of a plurality of variation structures, the outlet shape of each desulfurizing tower section is different with the import cross sectional shape, and the outlet of next section is exactly the inlet of the preceding paragraph.
3, the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 1 and 2, the outlet that it is characterized in that each desulfurizing tower section between the main reaction region at desulfurizing tower middle part becomes greatly from the bottom up gradually with the cross-sectional area in import cross section, and discharge area is 1.1～1.5 times of its import sectional area.
4. the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 2, the import and export cross section that it is characterized in that sub section of the desulfurizing tower that makes a variation is along the long X of being of the width of equipment, long along the depth direction of equipment is Y, when a cross section is microscler when being X 〉=1.5Y, then another cross section is X=0.8～1.2Y for approximate conformality.
5. between the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 2, the import that it is characterized in that the desulfurizing tower section that makes a variation and outlet is the excessive face of nature.
6. the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 4, it is characterized in that in the import and export cross section of desulfurizing tower section, a cross section is microscler, promptly replace the combined shaped of two minor faces by two long limits of rectangle with circular arc, then another cross section is that approximate conformality is polygon-shaped or round-shaped.
7, the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 1 and 2, the inlet that it is characterized in that the upper interval of desulfurizing tower adopts circular cross-section, it upwards makes a variation into the tower body cross section of rectangle three limits and arc section combination, it between two mouthfuls the excessive face of nature, constitute the variation section of upper interval, the discharge area of this variation section is 1.1～2.0 times of its entrance section.
8. the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 1 and 2, it is characterized in that being divided between the fluidization regions of desulfurizing tower bottom more than 2 or 2 independently fluidisation bed, these fluidisation beds have two kinds of arrangements, and one is evenly to arrange along the unit width; Another kind of for evenly to arrange along the circumferencial direction of tower body, and bed constituted between the fluidization regions of desulfurizing tower by these fluidisations.
9. the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 1 and 2, it is characterized in that being furnished with the multiple jet flow inlet of recirculation clean flue gas at desulfurizing tower tower body middle part, form the high intensity turbulent mixed zone at desulfurizing tower middle part, strengthen the intensity of overall desulphurization reaction
10. the dry flue gas desulphurization reaction tower of many complicated variation structures according to claim 8 is characterized in that being furnished with smoke deflector in the flue gas mixing-chamber of desulfurizing tower bottom, flue gas is evenly distributed in the flue gas induction apparatus of each fluidisation bed.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125294 CN1281297C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur reaction tower with variation structure |
| PCT/CN2004/000959 WO2005035103A1 (en) | 2003-08-19 | 2004-08-18 | A reaction tower for dry desulfurizating flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125294 CN1281297C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur reaction tower with variation structure |
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| Publication Number | Publication Date |
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| CN1513583A true CN1513583A (en) | 2004-07-21 |
| CN1281297C CN1281297C (en) | 2006-10-25 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03125294 Expired - Fee Related CN1281297C (en) | 2003-08-19 | 2003-08-19 | Dry process stack gas desulfur reaction tower with variation structure |
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| Country | Link |
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| CN (1) | CN1281297C (en) |
| WO (1) | WO2005035103A1 (en) |
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| CN100351003C (en) * | 2005-06-24 | 2007-11-28 | 哈尔滨工业大学 | Internal circulating multistaged spray fluidized flue gas desulfurization tower |
| CN100427181C (en) * | 2006-09-29 | 2008-10-22 | 清华大学 | Wet type reaction tower for flue gas desulfurization |
| CN101862587A (en) * | 2010-05-10 | 2010-10-20 | 上海电气石川岛电站环保工程有限公司 | Wet flue-gas desulfurization tower based on baffle air distribution |
| CN101642676B (en) * | 2009-08-20 | 2011-06-22 | 武汉凯迪电力股份有限公司 | Bidirectional air inlet type high-efficiency low-impedance semidry flue gas desulfurization tower |
| CN104492248A (en) * | 2014-12-24 | 2015-04-08 | 西昌市蓝鼎环保科技有限公司 | Dry desulfurization system for high-sulfur concentration smoke |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP0248855A1 (en) * | 1985-12-04 | 1987-12-16 | Hölter, Heinz, Dipl.-Ing. | PROCESS FOR SINGLE OR MULTI-PHASE PREFERABLY SIMULTANEOUS SO 2? AND NO x? SEPARATION FROM FLUE GASES IN A WET PROCESS |
| US5567215A (en) * | 1994-09-12 | 1996-10-22 | The Babcock & Wilcox Company | Enhanced heat exchanger flue gas treatment using steam injection |
| CN1087645C (en) * | 1996-01-11 | 2002-07-17 | 彭斯干 | Method and equipment for desulfurizing flue gas by circulation and fluidization |
-
2003
- 2003-08-19 CN CN 03125294 patent/CN1281297C/en not_active Expired - Fee Related
-
2004
- 2004-08-18 WO PCT/CN2004/000959 patent/WO2005035103A1/en active Application Filing
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100351003C (en) * | 2005-06-24 | 2007-11-28 | 哈尔滨工业大学 | Internal circulating multistaged spray fluidized flue gas desulfurization tower |
| CN100427181C (en) * | 2006-09-29 | 2008-10-22 | 清华大学 | Wet type reaction tower for flue gas desulfurization |
| CN101642676B (en) * | 2009-08-20 | 2011-06-22 | 武汉凯迪电力股份有限公司 | Bidirectional air inlet type high-efficiency low-impedance semidry flue gas desulfurization tower |
| CN101862587A (en) * | 2010-05-10 | 2010-10-20 | 上海电气石川岛电站环保工程有限公司 | Wet flue-gas desulfurization tower based on baffle air distribution |
| CN104492248A (en) * | 2014-12-24 | 2015-04-08 | 西昌市蓝鼎环保科技有限公司 | Dry desulfurization system for high-sulfur concentration smoke |
| CN105727662A (en) * | 2016-04-28 | 2016-07-06 | 安徽工业大学 | Iron ore sintering flue gas PM10 and PM2.5 emission reduction method |
| CN107837673A (en) * | 2017-12-04 | 2018-03-27 | 上海环境卫生工程设计院有限公司 | Dry powder pharmaceutical and flue gas mixed reactor |
| CN107837673B (en) * | 2017-12-04 | 2024-05-10 | 上海环境卫生工程设计院有限公司 | Dry powder medicament and flue gas mixing reaction device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1281297C (en) | 2006-10-25 |
| WO2005035103A1 (en) | 2005-04-21 |
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