CN201085994Y - Circulation fluidized bed smoke desulphurizing device - Google Patents
Circulation fluidized bed smoke desulphurizing device Download PDFInfo
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- CN201085994Y CN201085994Y CNU2007200261488U CN200720026148U CN201085994Y CN 201085994 Y CN201085994 Y CN 201085994Y CN U2007200261488 U CNU2007200261488 U CN U2007200261488U CN 200720026148 U CN200720026148 U CN 200720026148U CN 201085994 Y CN201085994 Y CN 201085994Y
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Abstract
The utility model discloses a circulating fluid bed flue gas desulphurization device with calcium-based desulphurizing agent as bed filler. The utility model is characterized in that a lime production and supply system comprises a main powder bin and a digester, a flue gas inlet structure, a circulating fluid bed desulphurization reaction tower, a first stage deduster and a second stage deduster connected with the frist stage deduster end-to-end, the lime production and supply system is connected with a venturi fluidizing throat in the lower part of the circulating fluid bed desulphurization reaction tower, a dust hopper for the first stage deduster is connected at the upstream of a recycled material distributing groove, the downstream of the recycled material distributing groove is connected with a discharge pipe and a recycled dust humidifying and activating device, and the humidified and activated recycled dust is introduced into the outlet port of the venturi pipe in the lower part of the circulating fluid bed desulphurization reaction tower. The utility mode has the advantages of: the desulphurization efficiency is remarkably improved under the same inlet water quantity; no or less water is sprayed in the desulphurization reaction tower, so as to effectively avoid wall adhension and scaling problems.
Description
Technical field:
The utility model belongs to industrial waste gas purifying environmental protection and chemical field, and particularly a kind of is the circulating fluid bed flue-gas desulfurizing device of bed material with the calcium-based desulfurizing agent.
Background technology:
Existing circulating fluid bed semi-drying method flue gas desulfurization method mostly is to utilize postdigestive lime (slurry) as absorbent, removes sulfur in smoke and other harmful substance by strong gas, liquid, solid three-phase effect in fluid bed reacting tower.Traditional way is the whitewashing technology, and its shortcoming is the lime white system that adopts, not only process system and equipment complexity, floor space is big, and easy fouling of mortar transfer pipeline and obstruction, reduced the availability of system, increased the operation maintenance and the maintenance cost of system simultaneously.In order to overcome this shortcoming, Chinese invention patent (number of patent application: 00128285.9) " a kind of dry cyclic suspension bed fume desulfurizing process and system thereof " and Chinese invention patent (number of patent application: the desulfurization ash under 03141860.0) " method and apparatus of material cyclic activation flue gas desulfurization " separates electrostatic precipitator (sack cleaner) mixes with fresh calcium hydroxide, water spray activate into certain moisture content bed expect to be recycled in the tower.This technology is to simplifying process system, improve system equipment reliability and service life the aspect, played better action.But in heat power plant boiler flue gas desulfurization technique improvement project, often be subjected to restriction and requirements such as but usage space is narrow and small, the blowing out transformation time is unsuitable long, dust emission is up to standard, more than two patent of invention technology on using, have big obstacle, reason has: (1) lime slaking must be arranged nearby, may be subjected to spatial constraints; (2) the grey quarrel absolute altitude of electrostatic precipitator (sack cleaner) is lower usually, is difficult to directly be recycled in the tower with air flume or conveying worm, if transform, then quantities is big, and furnace outage time is long; (3) electrostatic precipitator (sack cleaner) is used as outer separator, because of bigger than the electrostatic precipitator that causes (sack cleaner) inlet dust content, the difficult dust qualified discharge of realizing.
Summary of the invention:
The purpose of this utility model is to overcome above-mentioned the deficiencies in the prior art, and a kind of circulating fluid bed flue-gas desulfurizing device is provided.
The utility model can reach by following measure:
A kind of circulating fluid bed flue-gas desulfurizing device, mainly comprise lime preparation and supply system, the structure circulating fluidized bed desulfurization reaction tower of gas approach, the primary dust removing device, secondary ash collector, feed back distributing trough and circulating ash humidification activation device, wherein, the lime preparation comprises main powder storehouse and digester with supply system, the gas approach structure, desulfurization reaction tower of circulating fluid bed, the primary dust removing device, secondary ash collector is end to end, the lime preparation connects desulfurization reaction tower of circulating fluid bed bottom venturi fluidisation trunnion with supply system, feed back distributing trough upstream connects primary dust removing device ash bucket, the downstream connects drainage conduit and circulating ash humidification activation device, and the circulating ash behind the humidification activation enters Venturi tube exit, desulfurization reaction tower of circulating fluid bed bottom.
The downward air discharge cyclone separator that primary dust removing device described in the utility model can be an efficient low-resistance also can be a louver separator, and separative efficiency requires to reach 90-98%.
The utility model secondary ash collector can be electrostatic precipitator or sack cleaner, and the desulfurization ash under it separates is recycled in the reaction tower, also can not loopback.
Flue gas of the present utility model enters from the desulphurization reaction tower bottom of Venturi tube fluidisation, contact with circulating ash with fluidised desulfurizing agent and react at Ta Nei, desulfurizing byproduct is in the deduster that flue gas enters with desulfurization reaction tower is connected, most of circulating ash under this deduster separates is delivered in the tower through the humidification activation device, remaining desulfurization ash is sent to grey storehouse, after can entering secondary ash collector, discharges the flue gas behind this deduster, and also can be directly by smoke stack emission.
Desulfurization reaction tower is for adopting the vertical tower body of Venturi tube fluidisation in the utility model, and the bed material in the tower mainly is a slaked lime powder, and other composition comprises flying dust, impurity and moisture etc.Higher granule density can strengthen heat transfer and the mass transfer between gas-solid.Moisture mainly adds by circulating ash is carried out humidification activation, so the moisture overwhelming majority in the tower exists with the moisture film form on bed material surface, rather than exists with the form of droplet, therefore can guarantee that desulphurization reaction takes place in the mode of ion.The bed material that reacted is taken out of the top of desulfurization reaction tower, and with primary dust removing device that desulfurization reaction tower top links to each other in separate.Still contain a certain amount of unreacted desulfurizing agent in this part desulfurization ash, therefore, major part will be recycled in the tower, to increase the utilization rate of desulfuration efficiency and desulfurizing agent.Desulfurization ash remaining in the flue gas can separate by the electrostatic precipitator or the sack cleaner in downstream.
The utility model and other semidry process compare, and its advantage is:
The 1 primary dust removing device by efficient low-resistance recycles the desulfurization ash, and the granule density in the desulfurization reaction tower is very high.Enter in the tower because moisture is the moisture film with the circulating ash particle surface, the bed material in the desulfurization reaction tower is dry rapidly in the desulphurization reaction process, can effectively avoid spraying sticking wall and the scale problems that lime white causes.
The existence of 2 moisture films can make desulphurization reaction carry out with ionic reaction fast, can guarantee that moisture removes in 1-2 finishes sulfur dioxide before the evaporate to dryness in second wet method, and its desulfuration efficiency is higher than will the spray pulverized limestone and the semi-dry desulphurization system that independently carries out of water spray.
3 efficiently the mechanical type separator make sorbent particle carry out circulations up to a hundred time, can reach the time of contact of desulfurizing agent and flue gas more than 30 minutes, improved the utilization rate of desulfurizing agent greatly.
4 system architectures are simple, arrange compactness, and cheap, operation and maintenance cost is low.
Description of drawings:
Fig. 1 is the utility model structural representation.
Mark among the figure: 1 is main powder storehouse, and 2 are the digestion water inlet, and 3 is digester, 4 are the slaked lime powder inlet, 5 is the gas approach structure, and 6 is desulfurization reaction tower of circulating fluid bed, and 7 is the primary dust removing device, 8 is secondary ash collector, 9 is the feed back distributing trough, and 10 is drainage conduit, and 11 is the humidification water inlet, 12 is circulating ash humidification activation device, and 13 are the circulating ash inlet.
The specific embodiment:
Below in conjunction with accompanying drawing the utility model is further described:
As shown in drawings, the utility model comprises lime preparation and supply system, gas approach structure (5), desulfurization reaction tower of circulating fluid bed (6), primary dust removing device (7), secondary ash collector (8), feed back distributing trough (8) and circulating ash humidification activation device (12).Wherein, the lime preparation comprises main powder storehouse (1) and digester (3) with supply system.Gas approach structure (5), desulfurization reaction tower of circulating fluid bed (6), primary dust removing device (7), secondary ash collector (8) are end to end, the lime preparation connects desulfurization reaction tower of circulating fluid bed (6) bottom venturi fluidisation trunnion with supply system, feed back distributing trough (9) upstream connects primary dust removing device (7) ash bucket, the downstream connects drainage conduit (10) and circulating ash humidification activation device (12), and the circulating ash behind the humidification activation enters Venturi tube exit, desulfurization reaction tower of circulating fluid bed (6) bottom.
Provide two most preferred embodiments of the present utility model below.
Embodiment 1
Certain station boiler discharging flue gas 120,000 Nm
3/ hour, 145 ℃ of flue-gas temperatures, sulfur content 3770mg/Nm
3, desulfurizer adopts single tower structure, joins single cyclone separator, desulfurizing tower diameter 3.5m, and cyclone separator diameter 4m, two ash ports of cyclone design, separative efficiency is 92%.The humidification activation device adopts mechanical agitation, work of water sprinkling for better material moisture, humidification water consumption 4.2T/h.Secondary ash collector adopts four electric field electrostatic precipitator, and the desulfurization ash part of preceding two electric fields is recycled to desulfurizing tower, and the desulfurization ash of latter two electric field is directly delivered to grey storehouse.Adopt slaked lime powder as desulfurizing agent, fineness 150-300 order, the Ca/S mol ratio of employing is 1.3.
Hot flue gas enters desulfurization reaction tower of circulating fluid bed (6) through gas approach structure (5), with the slaked lime powder that sprays into desulfurizing tower (6) by slaked lime powder inlet (4), and by the circulating ash that circulating ash inlet (13) flows into desulfurizing towers (6) strong mixing, heat transfer, mass transfer and chemical reaction, the SO in the flue gas take place
2With desulfurizing agent Ca (OH)
2Reaction generates calcium sulfite and calcium sulfate, and mixes with the bed material.The evaporation that is dried of the moisture film on Solid Bed material surface, flue-gas temperature drops to about 75 ℃ simultaneously.To desulfurizing tower (6) outlet, the completely dried substantially dry state that forms of bed material enters cyclone separator (7) subsequently.During normal the operation, the nearly 50T/h of circulating ash that cyclone separator (7) separates all is recycled to desulfurizing tower after circulating ash humidification activation device (12) fragmentation, work of water sprinkling for better material moisture.The solid particle that enters secondary ash collector (8) still contains the not desulfurizing agent of complete reaction, therefore, in order to improve sorbent utilization, in order to guarantee higher granule density in the desulfurizing tower (6), the grey part of the desulfurization of preceding two electric fields is recycled to desulfurizing tower (6) simultaneously.For making finally discharged exhaust gas dust concentration discharge up to standard, the desulfurization ash of latter two electric field is directly delivered to grey storehouse.
Embodiment 2
Certain station boiler discharging flue gas 210,000 Nm
3/ hour, 145 ℃ of flue-gas temperatures, sulfur content 3500mg/Nm
3, desulfurizer adopts Double-Tower Structure, joins bispin wind separator, desulfurizing tower diameter 3.2m, and cyclone separator diameter 3.6m, two ash ports of cyclone design, separative efficiency is 95%.The humidification activation device adopts mechanical agitation, steam humidifying, humidification water consumption 7.2T/h.Secondary ash collector adopts four electric field electrostatic precipitator, and its desulfurization ash is directly delivered to grey storehouse.Adopt slaked lime powder as desulfurizing agent, fineness 150-300 order, the Ca/S mol ratio of employing is 1.3.
During normal the operation, the nearly 80T/h of circulating ash that cyclone separator (6) separates all is recycled to desulfurizing tower (6) after circulating ash humidification activation device (12) fragmentation, work of water sprinkling for better material moisture.
Claims (5)
1. circulating fluid bed flue-gas desulfurizing device, it is characterized in that device mainly comprises lime preparation and supply system, gas approach structure (5), desulfurization reaction tower of circulating fluid bed (6), primary dust removing device (7), secondary ash collector (8), feed back distributing trough (9) and circulating ash humidification activation device (12), wherein, the lime preparation comprises main powder storehouse (1) and digester (3) with supply system, gas approach structure (5), desulfurization reaction tower of circulating fluid bed (6), primary dust removing device (7), secondary ash collector (8) is end to end, the lime preparation connects desulfurization reaction tower of circulating fluid bed (6) bottom venturi fluidisation trunnion with supply system, feed back distributing trough (9) upstream connects primary dust removing device (7) ash bucket, the downstream connects drainage conduit (10) and circulating ash humidification activation device (12), and the circulating ash behind the humidification activation enters Venturi tube exit, desulfurization reaction tower of circulating fluid bed (6) bottom.
2. according to the described a kind of circulating fluid bed flue-gas desulfurizing device of claim 1, it is characterized in that described primary dust removing device (7) is the downward air discharge cyclone separator of efficient low-resistance.
3. according to the described a kind of circulating fluid bed flue-gas desulfurizing device of claim 1, it is characterized in that described primary dust removing device (7) is a louver separator.
4. according to the described a kind of circulating fluid bed flue-gas desulfurizing device of claim 1, it is characterized in that described secondary ash collector (8) is an electrostatic precipitator, the desulfurization ash under it separates is recycled in the reaction tower.
5. according to the described a kind of circulating fluid bed flue-gas desulfurizing device of claim 1, it is characterized in that described secondary ash collector (8) is a sack cleaner, the desulfurization ash under it separates is recycled in the reaction tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200261488U CN201085994Y (en) | 2007-07-31 | 2007-07-31 | Circulation fluidized bed smoke desulphurizing device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200261488U CN201085994Y (en) | 2007-07-31 | 2007-07-31 | Circulation fluidized bed smoke desulphurizing device |
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| CN201085994Y true CN201085994Y (en) | 2008-07-16 |
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| CNU2007200261488U Expired - Fee Related CN201085994Y (en) | 2007-07-31 | 2007-07-31 | Circulation fluidized bed smoke desulphurizing device |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101972600A (en) * | 2010-08-31 | 2011-02-16 | 宇星科技发展(深圳)有限公司 | Flue gas desulfurization system for sintering machines |
| CN102494335A (en) * | 2011-12-30 | 2012-06-13 | 东南大学 | Split self-excited serial electric-cyclone gas-solid separating device of circulating fluidized bed boiler |
| CN101670237B (en) * | 2008-09-10 | 2012-08-22 | 中国科学院工程热物理研究所 | Method and device for desulfurizing and dechlorinating flue gas of circulating fluidized bed |
| CN105056749A (en) * | 2015-07-20 | 2015-11-18 | 清华大学 | System and method for removing nitric oxides and sulfur oxides in flue gas simultaneously |
| CN107308797A (en) * | 2017-08-29 | 2017-11-03 | 哈尔滨蔚蓝环保设备制造有限公司 | A kind of flue gas circulating fluidized bed desulfurization and wet type desulfurizing combination minimum discharge technique |
| CN108273375A (en) * | 2017-12-29 | 2018-07-13 | 铜陵铜冠神虹化工有限责任公司 | The hot carbonizer flue gas desulfurization device and technique in vulcanized sodium production |
-
2007
- 2007-07-31 CN CNU2007200261488U patent/CN201085994Y/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101670237B (en) * | 2008-09-10 | 2012-08-22 | 中国科学院工程热物理研究所 | Method and device for desulfurizing and dechlorinating flue gas of circulating fluidized bed |
| CN101972600A (en) * | 2010-08-31 | 2011-02-16 | 宇星科技发展(深圳)有限公司 | Flue gas desulfurization system for sintering machines |
| CN102494335A (en) * | 2011-12-30 | 2012-06-13 | 东南大学 | Split self-excited serial electric-cyclone gas-solid separating device of circulating fluidized bed boiler |
| CN102494335B (en) * | 2011-12-30 | 2014-02-19 | 东南大学 | Circulating fluidized bed boiler split type self-excited serial power-cyclone gas-solid separation device |
| CN105056749A (en) * | 2015-07-20 | 2015-11-18 | 清华大学 | System and method for removing nitric oxides and sulfur oxides in flue gas simultaneously |
| CN107308797A (en) * | 2017-08-29 | 2017-11-03 | 哈尔滨蔚蓝环保设备制造有限公司 | A kind of flue gas circulating fluidized bed desulfurization and wet type desulfurizing combination minimum discharge technique |
| CN108273375A (en) * | 2017-12-29 | 2018-07-13 | 铜陵铜冠神虹化工有限责任公司 | The hot carbonizer flue gas desulfurization device and technique in vulcanized sodium production |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: JIANGSU LANSHAN ENVIRONMENTAL TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: HUANG SHENGZHU Effective date: 20120315 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 264200 WEIHAI, SHANDONG PROVINCE TO: 210037 NANJING, JIANGSU PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20120315 Address after: 210037 No. 40, Nanchang Road, Gulou District, Jiangsu, Nanjing Patentee after: Jiangsu Lanshan Environment Technology Co., Ltd. Address before: 264200 Weihai Cultural Road West, Shandong, No. 2 Patentee before: Huang Shengzhu |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080716 Termination date: 20150731 |
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| EXPY | Termination of patent right or utility model |