CN201912889U - Flue gas desulfurization reactor for downlink recirculating fluidized bed - Google Patents
Flue gas desulfurization reactor for downlink recirculating fluidized bed Download PDFInfo
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- CN201912889U CN201912889U CN2010205628141U CN201020562814U CN201912889U CN 201912889 U CN201912889 U CN 201912889U CN 2010205628141 U CN2010205628141 U CN 2010205628141U CN 201020562814 U CN201020562814 U CN 201020562814U CN 201912889 U CN201912889 U CN 201912889U
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- flue gas
- gas desulfurization
- reactor
- fluid bed
- cycle fluid
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 239000003546 flue gas Substances 0.000 title claims abstract description 57
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 41
- 230000023556 desulfurization Effects 0.000 title claims abstract description 37
- 230000003134 recirculating effect Effects 0.000 title abstract description 4
- 239000007787 solid Substances 0.000 claims abstract description 36
- 230000002745 absorbent Effects 0.000 claims abstract description 27
- 239000002250 absorbent Substances 0.000 claims abstract description 27
- 230000003068 static effect Effects 0.000 claims abstract description 22
- 239000012530 fluid Substances 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 13
- 230000004913 activation Effects 0.000 claims description 6
- 239000004744 fabric Substances 0.000 claims description 4
- 238000009827 uniform distribution Methods 0.000 claims description 3
- 230000007935 neutral effect Effects 0.000 claims description 2
- 239000007921 spray Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 11
- 239000000428 dust Substances 0.000 abstract description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 abstract description 7
- 229910001861 calcium hydroxide Inorganic materials 0.000 abstract description 7
- 239000000920 calcium hydroxide Substances 0.000 abstract description 7
- 238000000926 separation method Methods 0.000 abstract description 5
- 230000003213 activating effect Effects 0.000 abstract 1
- 235000011116 calcium hydroxide Nutrition 0.000 abstract 1
- 239000004071 soot Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 12
- 238000001035 drying Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000008187 granular material Substances 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000000116 mitigating effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The utility model relates to a flue gas desulfurization technology of a downlink recirculating fluidized bed. Core equipment, i.e. a reactor, of the flue gas desulfurization technology structurally consists of a DC (direct current) streamline inlet flue, an absorbent (fresh slaked lime and circulating ash) uniform distributor, an acoustic wave soot blower, a static mixer, a reactor shell, a humidifying and activating nozzle, a cone swirl plate-type gas-solid separator, a gas-solid separation guide plate, a desulfurized flue gas outlet flue and a hyperbolic ash hopper from top to bottom sequentially. The reactor has reasonable allocation, so that the flue gas and an absorbent in the reactor are collided and mixed sufficiently; stable and uniform flow field, temperature field and pressure field are obtained; the absorbent has high circulation ratio and utilization rate; no problems of sticking on the wall, scaling and bed collapse cannot be generated; meanwhile, the dust content of the flue gas at an outlet is obviously reduced, the load of a bag dust collector at the rear part is greatly reduced, the device is ensured to operate safely and stably in a long period, and the technical difficult problem in a semidry flue gas desulfurization technology is effectively solved.
Description
Technical field
The present invention relates to flue gas desulfurization technique and equipment, be specifically related to a kind of semi-dry process flue gas desulphurization technology that is applicable to steel industry sintering machine, coal-burning power plant and waste incineration power plant.
Background technology
The semi-dry process flue gas desulphurization technology, reduced investment, take up an area of less, non-wastewater discharge, can not cause that secondary pollution, desulfuration efficiency height, operating cost are low, system substantially not burn into can tally with the national condition, thereby be favored with general carbon steel manufacturing.The semi-dry process flue gas desulphurization technology that technology is ripe both at home and abroad has at present: rotary spraying and drying method (SDA method), humidification ash cyclic semidry process (NID method), suspension recirculating fluidized bed method and dense-phase tower method.But they all have weakness separately:
1. rotary spraying and drying method (SDA method)
1. rotary nozzle costliness, the pulping system complexity;
2. flue gas flow rate is very low in the absorption tower, and the tower diameter is very big, and floor space is bigger;
3. the Ca/S mol ratio is up to 1.5, and needs the lime of higher quality, and the absorbent utilization rate only is～50%;
4. slurries band water need add water again and regulate, and causes the water route that is caused by temperature signal to regulate complicated;
5. flue gas after being purified can produce corrosion to the rear portion cleaner;
6. install in the running the easy dust stratification of tower wall, easily stifled ash at the bottom of the tower;
7. invest higherly, operating cost (power consumption) is higher;
8. the accessory substance major part is CaSO
3, being difficult to handle, value is not high.
2. humidification ash cyclic semidry process (NID method)
1. (～18m/s) operation is equivalent to strength and carries simultaneously from bottom to top at a high speed with flue gas to enter humidification ash in the reactor.The two almost is synchronized with the movement, and phase mutual friction, collision probability are low, and reaction effect is relatively poor;
2. the reactor resistance drop is bigger, serious wear (needing to adopt the abrasion-resistant stee manufacturing);
3. the reactor outlet dust content is very high, advances before the deduster of rear portion, should establish pre-cleaner;
4. absorbent (being the humidification ash) amount of water limited (≤5%), circulating ratio lower (～25), utilization rate is lower, and desulfuration efficiency is lower.
3. suspension recirculating fluidized bed method
1. the flow field is inhomogeneous, even serious bias current or local eddy currents;
2. reactor resistance drop big (more than the 1500pa);
3. the sticking wall of desulfurization ash, the bed that lumps, collapses, stifled tower have generation more, and device is difficult to keep long period, stable operation.
4. dense-phase tower method
1. lack operating experience, technology maturity is lower;
2. the flue gas flow field bias current is very serious in the reactor, and flue gas is walked short circuit greatly:
3. desulfuration efficiency is lower.
Summary of the invention
Purpose of the present invention is to overcome the above-mentioned deficiency of prior art, provides a kind of rational in infrastructure, and flue gas flow field, temperature field, pressure field be " downlink cycle fluid bed flue gas desulfurization reactor " very uniformly.
The objective of the invention is to be achieved through the following technical solutions.
The present invention's " downlink cycle fluid bed flue gas desulfurization reactor ", from top to bottom the structure of (see figure 1) is followed successively by: guide shell, desulfurization exhanst gas outlet flue and hyperbola ash bucket are separated in the streamlined inlet flue duct of direct current, absorbent (fresh calcium hydroxide and circulating ash) uniform device, acoustic wave ash ejector, static mixer, reactor shell, humidification activation nozzle, the board-like gas-solid separator of taper eddy flow, gas-solid.
The structure division of each parts is as follows:
The streamlined inlet flue duct of described direct current is square sectional, in establish 3 not isometric circle arc airflow uniform distribution deflectors, other connects diffuser.
Described absorbent (fresh calcium hydroxide and circulating ash) uniform device has 6 cloth tubes, and each cloth mouth of pipe is aimed at each self-corresponding static mixer center respectively.
Described acoustic wave ash ejector is located at the neutral gear place at 6 static mixer centers.
Described static mixer is the SK type, is positioned at absorbent (fresh calcium hydroxide and circulating ash) uniform device below, the top of reactor shell, and its bottom plate center is a round hole.
Described reactor shell is circular cross-section.
Described humidification activation nozzle is two-fluid spray nozzle, is located at the below of static mixer group switching centre.
The board-like gas-solid separator of described taper eddy flow is located at the centre of reactor shell bottom.
Guide shell is separated in described gas-solid, and arrival end stretches into the board-like gas-solid separator inner bottom part of taper eddy flow, and the bottom has an awl section.
Described hyperbola ash bucket is positioned at reactor bottom.
Described desulfurization exhanst gas outlet flue is square sectional, is positioned at reactor shell below one side, separates guide shell with the gas-solid of the board-like gas-solid separator of taper eddy flow below and joins.This flue is provided with the pinnacle that the dust landing is got off above the inside reactor branch.
The present invention adopts actual project data, through rigorous technology Calculation, and uses Fluent software to carry out flow field analysis, and effect is very good.
The present invention disposes rationally, makes the flue gas in the reactor fully collide, mix with absorbent; And acquisition stabilized uniform flow field, temperature field and pressure field; Absorbent obtains high circulating ratio and utilization rate; And do not have sticking wall, fouling, collapse the bed problem; Obviously reduce simultaneously the dustiness of outlet flue gas, alleviated the load of rear portion sack cleaner greatly, efficiently solved the technical barrier in the semi-dry process flue gas desulphurization technology.
Description of drawings
Fig. 1 is the structural representation of the present invention's " downlink cycle fluid bed flue gas desulfurization reactor ".
Among the figure: 1. the streamlined inlet flue duct of direct current, 2. absorbent uniform device, 3. acoustic wave ash ejector, 4. static mixer, 5. reactor shell, 6. humidification activation nozzle, the 7. board-like gas-solid separator of taper eddy flow, 8. guide shell, 9. desulfurization exhanst gas outlet flue, 10. hyperbola ash bucket are separated in gas-solid.
The cross-sectional view that Fig. 2 distributes for the reactor static mixer.
Fig. 3 is the board-like gas-solid separator front view of taper eddy flow.
Fig. 4 is the board-like gas-solid separator vertical view of taper eddy flow.
The specific embodiment
Referring to Fig. 1, the downlink cycle fluid bed flue gas desulfurization reactor from top to bottom is followed successively by: guide shell 8, desulfurization exhanst gas outlet flue 9 and hyperbola ash bucket 10 are separated in the streamlined inlet flue duct 1 of direct current, absorbent uniform device 2, acoustic wave ash ejector 3, static mixer 4, reactor shell 5, humidification activation nozzle 6, the board-like gas-solid separator 7 of taper eddy flow, gas-solid.
The streamlined inlet flue duct of direct current, absorbent uniform device, acoustic wave ash ejector, static mixer, the board-like gas-solid separator of taper eddy flow, separate guide shell with the gas-solid that is positioned at this gas-solid separator below, and desulfurization exhanst gas outlet flue, the hyperbola ash bucket is unique texture of the present invention.
The outlet flue gas of the sintering device flue gas of steel industry, coal-burning power plant and waste incineration boiler of power plant, enter reactor from the streamlined inlet flue duct 1 of the direct current of this reactor head, through 3 not isometric circle arc airflow uniform distribution deflector enter reactor, continue to move downward, be full of the whole cross section of reactor equably; Fresh calcium hydroxide and circulating ash enter reactor by absorbent uniform device 2; Each outlet of absorbent uniform device (being generally 6), aim at the center of each self-corresponding SK type static mixer 4 (this type static mixer resistance minimum, obstruction least easily) respectively, by static mixer 3, absorbent collides, fully mixes with flue gas is fierce; After leaving static mixer 4, because the severe difference, there are speed difference in descending flue gas and absorbent (gas-solid mixture), continue collision, friction, mass transfer, heat transfer, reaction (in reactor internal reaction time～6 second) mutually; The desulfurization flue gas that carries a large amount of particles flows downward, the suction function that causes by the air-introduced machine at system rear portion, the desulfurization flue gas passes the impeller clearance of the board-like gas-solid separator 7 of taper eddy flow, formed swirling eddy, part solid phase particles thing is under effect of inertia, adsorbed by windward side eddy flow plate, along the downward landing of the arc groove of eddy flow panel edges, fall into bottom hyperbola ash bucket 10; The desulfurization flue gas then is sucked into gas-solid and separates guide shell 8 and desulfurization exhanst gas outlet flue 9; Be positioned at the acoustic wave ash ejector 3 at static mixer group switching centre position, time opening, make flue gas and dust granules in the reactor produce vibration, destruction and prevention dust granules are at board-like gas-solid separator 7 blades of taper eddy flow, and the combination between the wall of reactor, make it to be in the suspension fluidized state, so that taken away by flue gas; Through the desulfurization flue gas of preliminary gas solid separation, separate guide shell 8 and desulfurization exhanst gas outlet flue 9 through gas-solid, enter the sack cleaner at system rear portion, further carry out desulphurization reaction and gas solid separation; Through the flue gas that sack cleaner has purified, send chimney to by air-introduced machine, enter atmosphere; By the isolated solid phase of pocket type deduster (be the desulfurization ash, also claim circulating ash), most of by the strength conveying, be transmitted back to the absorbent uniform device 2 of reactor head, enter reactor and continue to participate in desulphurization reaction; Small part is delivered to grey storehouse, otherwise processed; Desulfurization ash in the reactor lower part hyperbola ash bucket 10 is regularly discharged, and delivers to grey storehouse.
The invention has the advantages that:
1) the streamlined inlet flue duct of direct current (comprising 3 not isometric circle arc deflector and diffusers): the natural streamline that meets flow of flue gas, form the inequality overcurrent at bend deflector cut section, effectively reduce the side direction eddy current, prevent the flue gas bias current, after making flue gas enter reactor, be full of equably the whole cross section of reactor, guarantee that flue gas flow field is evenly distributed in the reactor, and resistance drop be littler.
2) the absorbent uniform device can guarantee that absorbent (fresh calcium hydroxide and circulating ash) passes through each distributor pipe, aims at each self-corresponding static mixer center, injects static mixer.
3) static mixer can make the fierce collision of absorbent and flue gas, bring in constant renewal in the surface of absorbent, makes the two fully mixing, mass transfer, heat transfer and accelerates the carrying out of desulphurization reaction.
4) taper spiral-flow plate-type gas-solid separator can carry out preliminary gas solid separation to desulfurization fume, and particle Desulphurization bigger, that severe is bigger, that grade is not high is separated, thereby alleviates the load of rear portion sack cleaner, the power consumption of mitigation system.
5) acoustic wave ash ejector time opening, make flue gas and dust granules in the reactor produce vibration, destruction and prevention dust granules are at taper spiral-flow plate-type gas-solid separator blade, and the combination between the wall of reactor, make it to be in the suspension fluidized state, in order to taken away by flue gas, or fall into the hyperbola ash bucket of reactor lower part, guarantee the separative efficiency of taper spiral-flow plate-type gas-solid separator.
6) guide shell is separated in gas-solid, is positioned at the below of taper spiral-flow plate-type gas-solid separator, and the desulfurization fume exhaust pass joins with this gas-solid separation guide shell, and the lower end of this guide shell is provided with a cone segments, separablely goes out a part of dust, falls into the hyperbola ash bucket. This structure can not affect the uniformity of flue gas flow field in the whole reactor.
7) the present invention (contains SO to the acidity of variable concentrations2、SO
3, HCl, HF etc.) flue gas, and the adaptability that flue gas load changes is very strong. When the flue gas acid ingredient is too high, can be by suitably improving the circulating ratio of circulating ash, or increase fresh calcium hydroxide consumption and solve; For adapting to the variation of exhaust gas volumn, the backflow flue need not be set.
8) the present invention can effectively reduce Ca/S mol ratio (≤1.3), improves the circulating ratio (〉=200) of absorbent, improves the utilization rate (～99%) of absorbent, guarantees that desulfuration efficiency is more than 95%.
9) whole sweetening process all is in drying regime, and the exhanst gas outlet temperature is higher than about 20 ℃ of dew points, without sewage discharge, and non-secondary pollution, equipment does not corrode substantially, and available ordinary carbon steel manufacturing need not be adopted anticorrosive measure, and construction costs is lower.
10) do not have the problem of sticking wall, fouling, the bed that collapses, stifled tower, in the reactor without any moving component, the reactor resistance drop little (≤800pa), device can be under good state, safety, stable, long-term operation.
Claims (10)
1. downlink cycle fluid bed flue gas desulfurization reactor, it is characterized in that: structure from top to bottom is followed successively by: guide shell, desulfurization exhanst gas outlet flue and hyperbola ash bucket are separated in the streamlined inlet flue duct of direct current, absorbent uniform device, acoustic wave ash ejector, static mixer, reactor shell, humidification activation nozzle, the board-like gas-solid separator of taper eddy flow, gas-solid.
2. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: the streamlined inlet flue duct of described direct current, be square sectional, in establish 3 not isometric circle arc airflow uniform distribution deflectors, other connects diffuser.
3. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described absorbent uniform device, have 6 cloth tubes, and each cloth mouth of pipe is aimed at each self-corresponding static mixer center respectively.
4. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described acoustic wave ash ejector is located at the neutral gear place at 6 static mixer centers.
5. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described static mixer is the SK type, is positioned at absorbent uniform device below, the top of reactor shell, and its bottom plate center is a round hole.
6. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described reactor shell is circular cross-section.
7. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described humidification activation nozzle is two-fluid spray nozzle.
8. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: the board-like gas-solid separator of described taper eddy flow is located at the centre of reactor shell bottom.
9. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: guide shell is separated in described gas-solid, and arrival end stretches into the board-like gas-solid separator inner bottom part of taper eddy flow, and the bottom has an awl section.
10. downlink cycle fluid bed flue gas desulfurization reactor according to claim 1 is characterized in that: described hyperbola ash bucket is positioned at reactor bottom.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205628141U CN201912889U (en) | 2010-10-15 | 2010-10-15 | Flue gas desulfurization reactor for downlink recirculating fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010205628141U CN201912889U (en) | 2010-10-15 | 2010-10-15 | Flue gas desulfurization reactor for downlink recirculating fluidized bed |
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| CN201912889U true CN201912889U (en) | 2011-08-03 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102441324A (en) * | 2010-10-15 | 2012-05-09 | 北京博朗环境工程技术股份有限公司 | Flue gas desulfurization reactor of descending circulating fluidized bed |
| CN111939748A (en) * | 2020-09-17 | 2020-11-17 | 辽宁远景产学研环保技术有限公司 | High-efficient desulfurization reaction unit |
| CN112304031A (en) * | 2020-11-12 | 2021-02-02 | 哈尔滨工业大学 | Cyclone fluidized bed dryer for rapidly drying large-particle materials |
-
2010
- 2010-10-15 CN CN2010205628141U patent/CN201912889U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102441324A (en) * | 2010-10-15 | 2012-05-09 | 北京博朗环境工程技术股份有限公司 | Flue gas desulfurization reactor of descending circulating fluidized bed |
| CN111939748A (en) * | 2020-09-17 | 2020-11-17 | 辽宁远景产学研环保技术有限公司 | High-efficient desulfurization reaction unit |
| CN112304031A (en) * | 2020-11-12 | 2021-02-02 | 哈尔滨工业大学 | Cyclone fluidized bed dryer for rapidly drying large-particle materials |
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Granted publication date: 20110803 Termination date: 20181015 |