CN201296732Y - Device for preparing calvital by utilizing a dry flue gas desulfurization method - Google Patents
Device for preparing calvital by utilizing a dry flue gas desulfurization method Download PDFInfo
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- CN201296732Y CN201296732Y CNU2007201905904U CN200720190590U CN201296732Y CN 201296732 Y CN201296732 Y CN 201296732Y CN U2007201905904 U CNU2007201905904 U CN U2007201905904U CN 200720190590 U CN200720190590 U CN 200720190590U CN 201296732 Y CN201296732 Y CN 201296732Y
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Abstract
A device for preparing calvital by utilizing a dry flue gas desulfurization method relates to the technical field of the gas purification. The structure of the device is characterized in that calcium lime powder (CaO) enters into a primary reactor through a belt weigher and is uniformly mixed with water that is sprayed by a group of water nozzles above the reactor, and the mixture enters into a secondary reactor to further undertake the lime slaking reaction, and the mixture is slaked to generate white lime (Ca(OH2)); the white lime is sent to a pipeline that is connected with a desulfurization absorption tower through a helical conveyer and is jetted into the desulfurization absorption tower through a Roots blower. Large particles are discharged through a slag discharging port, and the upper part of the secondary reactor is connected with a bag-type dehumidifier, and an outlet of the dehumidifier is connected with the desulfurization absorption tower. The device adopts the calcium oxide as the raw material, and has the advantages of compact structure, high transformation ratio of the desulfurization agent, high activity of the desulfurization agent, non-blocking, on-line preparation of the desulfurization agen according to the load of the boiler, and the like. The device is applicable to the preparation of desulfurization agent by utilizing a dry flue gas desulfurization system.
Description
Technical field
The utility model belongs to the flue gases purification field, especially for the calcium hydroxide preparation facilities of dry flue gas desulphurization.
Background technology
It is main energy sources that the energy structure of China remains with the coal, and using in a large number of coal produces a large amount of pollutents such as sulfurous gas.It is one of principal pollutant that cause problem of environmental pollutions such as Greenhouse effect, acid rain, and China has begun to carry out large-scale sulfur dioxide pollution improvement work.
General flue gas desulfurization technique can be divided into wet method, semidrying and dry method three major types.The wet process of FGD technology, though the desulfuration efficiency height, complex process, one-time investment is big, working cost is high, floor space is big.The desulfurization product of dry flue gas desulphurization technology is a dry powder, system is difficult for blocking, well overcome some problem and shortage of wet process of FGD technology, desulfurization by dry method has that system is simple, investment cost is low, floor space is little, the collection desulfurization and dedusting is advantages such as one.In recent years along with the research and development, the particularly development of circulating fluid bed flue-gas desulfurizing technology (CFBFGD) of Technology, make the dry flue gas desulphurization technology obtain application more and more widely.
In dry method flue gas desulfur device, sweetening agent sprays into the absorption tower with dry powder, and water sprays into the absorption tower by water spouting nozzle, removes acid pollution gas in the flue gas with the flue gas thorough mixing in the absorption tower.Wherein, size and the active height that sprays into the sorbent particle particle diameter is to influence the utilization ratio of sweetening agent and the important factor of desulphurization system desulfuration efficiency.The operation of sweetening agent preparation system continous-stable is one of key of desulphurization system steady running.
The source of sweetening agent has two, and one is to buy finished product dry hydrate (Ca (OH)
2), these dry hydrate prices are higher, increased the working cost of desulphurization system.Because it is not dry hydrate is not an on-site preparation, desulphurizing activated high after sweetening agent is placed for some time on the other hand, easily harden after the suction, influenced the desulfuration efficiency of desulphurization system.
Another method is to buy comparatively cheap calcium lime powder (CaO), and the scene disappears to close and makes dry hydrate (Ca (OH)
2).But present several unslaked limes disappear attach together put have that operation stability poor (easily block), sweetening agent transformation efficiency are low, product poor activity and can't can't satisfy the requirement of dry flue gas desulphurization system process according to shortcomings such as the online preparations of boiler load.
Summary of the invention
In order to solve above-mentioned problems of the prior art, the purpose of this utility model proposes a kind of calcium hydroxide efficient production device that is specifically designed to dry flue gas desulphurization.Its adopts calcium oxide is raw material, has compact construction, desulfurizer activity height, sweetening agent transformation efficiency height, is difficult for blocking, according to advantages such as the online preparations of boiler load.
In order to reach the foregoing invention purpose, the technical solution of the utility model realizes as follows:
A kind of calcium hydroxide preparation facilities that is used for dry flue gas desulphurization, it mainly comprises: lime silo, belt weigher, water spouting nozzle A reactor, second reactor, pocket type moisture trap, slag notch, front apron, rear deflector door and worm conveyor.Its constructional feature is: action of low-voltage pulse formula pocket type moisture trap is installed in the second reactor top, and two muck removal mouths, front apron and rear deflector doors are established in the second reactor bottom.The A reactor top is provided with the single fluid nozzle of two row's (group) staggered arrangement.
In above-mentioned calcium hydroxide preparation facilities, the pocket type moisture trap is positioned at the second reactor top, is connected as a single entity with second reactor, the air outlet is positioned at moisture trap top, the filter bag filtrate is polyphenylene sulfide (PPS) filtrate, the negative pressure operation, and the air outlet directly connects desulfuration absorbing tower.
In above-mentioned calcium hydroxide preparation facilities, two slag notches are positioned at the latter half of second reactor, and the rear deflector door height is higher than front apron, and aspect ratio is 2:1.
In above-mentioned calcium hydroxide preparation facilities, nozzle is along A reactor main center line, and spray direction is along under the A reactor main center alignment.
In above-mentioned calcium hydroxide preparation facilities, the transfer rate of belt weigher, nozzle injection flow rate and worm conveyor rotating speed are all along with boiler load is adjustable.
The utility model compared with prior art has the following advantages and positively effect:
(1) the utility model adopts two-stage reactor technology, and the decoration form of A reactor nozzle is excessive with the water that sprays into A reactor, and sweetening agent residence time in second reactor is 6 minutes～12 minutes.These measures have guaranteed sweetening agent high reactivity and high conversion.
(2) second reactor sets out cinder notch and baffle plate, has both prevented system's macrobead sweetening agent choke system, and macrobead is separated, and has guaranteed the activity of finished product sweetening agent.
(3) traditional sweetening agent preparation technology hardens because dry hydrate is easy to suction, causes system congestion, have a strong impact on the steady running of equipment, the utility model is drawn the superfluous water steam by the pocket type moisture trap on second reactor top, and the superfluous water steam is directly introduced desulfuration absorbing tower.This has prevented the equipment obstruction on the one hand, and water vapour is directly introduced the absorption tower on the other hand, by the physical adsorption of sweetening agent in the absorption tower to water vapor, further improves the ability that dry method flue gas desulfur device absorbs sulfurous gas.
(4) transfer rate of belt weigher, nozzle injection flow rate and worm conveyor rotating speed have guaranteed the online preparation of sweetening agent all along with boiler load is adjustable, effectively prevent the inactivation of sweetening agent.
Below in conjunction with the drawings and specific embodiments the utility model is described further.
Description of drawings
Accompanying drawing is the structure principle chart of the utility model device.
Embodiment
Referring to accompanying drawing, this device comprises: lime silo 1, belt weigher 2, water spouting nozzle 6, A reactor 7, second reactor 9, pocket type moisture trap 12, slag notch 10, front apron 14, rear deflector door 15 and worm conveyor 17.Action of low-voltage pulse formula pocket type moisture trap 12 is installed in second reactor 9 tops, and two muck removal mouths 10, front apron 14 and rear deflector door 15 are established in second reactor 9 bottoms.A reactor 7 tops are provided with the single fluid nozzle 6 of two row's (group) staggered arrangement.Pocket type moisture trap 12 is positioned at second reactor 9 tops, is connected as a single entity with second reactor, and air outlet 11 is positioned at moisture trap top, and filter bag 13 filtrates are polyphenylene sulfide (PPS) filtrate, the negative pressure operation, and the air outlet directly connects desulfuration absorbing tower.Two slag notches 10 are positioned at the latter half of second reactor 9, and rear deflector door 15 highly is higher than front apron 14, and aspect ratio is 2:1.Nozzle 6 is along A reactor 7 main center's lines, and spray direction is along under A reactor 7 main center's alignments.The transfer rate of belt weigher 2, nozzle 6 injection flow rates and worm conveyor 17 rotating speeds are all adjustable with boiler load.
Method steps during the utility model operation is: the calcium lime powder in the lime silo 1 (CaO) enters A reactor 7 through belt weigher 2 by feeding mouth 3, water is by A reactor 7 top water inlet pipes 4 and arm 5, spray into by one group of nozzle 6, in A reactor 7, water and calcium lime powder uniformly mix reaction, enter second reactor 9 by one-level discharge port 8 then, further carry out the lime slaking reaction, digestion reaction forms white lime (Ca (OH)
2) powder, by secondary discharge port 16, enter worm conveyor 17, be transported to the pipeline that links to each other with desulfuration absorbing tower by worm conveyor 17, spray into desulfuration absorbing tower by roots blower.Macrobead will be intercepted by front apron 14 and rear deflector door 15 respectively in the second reactor 9, discharge by slag notch 10.Second reactor 9 connects pocket type moisture traps 12, and unnecessary water vapour in the second reactor 9 through the filter bag 13 of pocket type moisture trap 12, is introduced dry desulfurization absorbing towers by pocket type moisture trap outlet 11.
Claims (5)
1. calcium hydroxide preparation facilities that is used for dry flue gas desulphurization, it mainly comprises: lime silo (1), belt weigher (2), water spouting nozzle (6), A reactor (7), second reactor (9), pocket type moisture trap (12), slag notch (10), front apron (14), rear deflector door (15) and worm conveyor (17) is characterized in that: action of low-voltage pulse formula pocket type moisture trap (12) is installed in second reactor (9) top, and two muck removal mouths (10), front apron (14) and rear deflector door (15) are established in second reactor (9) bottom; A reactor (7) top is provided with the single fluid nozzle (6) of two row's (group) staggered arrangement.
2. according to the described calcium hydroxide preparation facilities of claim 1, it is characterized in that: pocket type moisture trap (12) is positioned at second reactor (9) top, be connected as a single entity with second reactor, air outlet (11) is positioned at moisture trap top, filter bag (13) filtrate is polyphenylene sulfide (PPS) filtrate, the negative pressure operation, the air outlet directly connects desulfuration absorbing tower.
3. according to claim 1 or 2 described calcium hydroxide preparation facilitiess, it is characterized in that: two slag notches (10) are positioned at the latter half of second reactor (9), and rear deflector door (15) highly is higher than front apron (14), and aspect ratio is 2:1.
4. according to the described calcium hydroxide preparation facilities of claim 3, it is characterized in that: nozzle (6) is along A reactor (7) main center line, and spray direction is along under A reactor (7) the main center alignment.
5. according to the described calcium hydroxide preparation facilities of claim 4, it is characterized in that: the transfer rate of belt weigher (2), nozzle (6) injection flow rate and worm conveyor (17) rotating speed are all adjustable with boiler load.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201905904U CN201296732Y (en) | 2007-12-05 | 2007-12-05 | Device for preparing calvital by utilizing a dry flue gas desulfurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201905904U CN201296732Y (en) | 2007-12-05 | 2007-12-05 | Device for preparing calvital by utilizing a dry flue gas desulfurization method |
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| Publication Number | Publication Date |
|---|---|
| CN201296732Y true CN201296732Y (en) | 2009-08-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007201905904U Expired - Fee Related CN201296732Y (en) | 2007-12-05 | 2007-12-05 | Device for preparing calvital by utilizing a dry flue gas desulfurization method |
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| CN (1) | CN201296732Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101983943A (en) * | 2010-11-05 | 2011-03-09 | 浙江菲达脱硫工程有限公司 | Quicklime coupling and digesting device |
| CN102059044A (en) * | 2010-11-25 | 2011-05-18 | 武汉钢铁(集团)公司 | Process for preparing calcium-based sorbent through normal pressure dry slaking |
-
2007
- 2007-12-05 CN CNU2007201905904U patent/CN201296732Y/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101983943A (en) * | 2010-11-05 | 2011-03-09 | 浙江菲达脱硫工程有限公司 | Quicklime coupling and digesting device |
| CN102059044A (en) * | 2010-11-25 | 2011-05-18 | 武汉钢铁(集团)公司 | Process for preparing calcium-based sorbent through normal pressure dry slaking |
| CN102059044B (en) * | 2010-11-25 | 2012-09-26 | 武汉钢铁(集团)公司 | Process for preparing calcium-based sorbent through normal pressure dry slaking |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090826 Termination date: 20111205 |