CN101450791A - Calcium hydrate preparation method for dry flue gas desulfurization and apparatus thereof - Google Patents
Calcium hydrate preparation method for dry flue gas desulfurization and apparatus thereof Download PDFInfo
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- CN101450791A CN101450791A CNA2007101787476A CN200710178747A CN101450791A CN 101450791 A CN101450791 A CN 101450791A CN A2007101787476 A CNA2007101787476 A CN A2007101787476A CN 200710178747 A CN200710178747 A CN 200710178747A CN 101450791 A CN101450791 A CN 101450791A
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Abstract
The invention provides a method and a device for preparing calcium hydroxide for dry flue gas desulphurization, which relates to the technical field of flue gas purification. The method is characterized in that quicklime powder (CaO) enters a primary reactor through a belt metering balance, is well mixed with water sprayed from a group of water nozzles above the reactor, and then is stirred for reaction; a mixture enters a secondary reactor and is further subjected to lime nitration, so as to generate slaked lime (Ca(OH)2) powder through nitration; the slaked lime powder is conveyed to a pipeline connected with a desulphurization absorption tower through a screw conveyor and is sprayed in to the desulphurization absorption tower through a Roots blower; large particles are discharged through a slag outlet; and steam in the secondary reactor is directly led into the desulphurization absorption tower through a bag-type dehumidifier above the secondary reactor. The device adopts calcium oxide as raw materials, and has the advantages of compact structure, high desulfurizer conversion rate, high desulfurizer activity, block insusceptibility, capability of preparing desulfurizer on line according to boiler load and the like. The invention is applicable to the preparation of the desulfurizer for dry flue gas desulphurization systems.
Description
Technical field
The invention belongs to the flue gases purification field, especially for the calcium hydroxide preparation method and the device thereof 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, purpose of the present invention proposes a kind of calcium hydroxide high efficiency preparation method and device thereof 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, technical scheme of the present invention realizes as follows: the calcium lime powder in the lime silo (CaO) enters A reactor through the belt weigher, with the one group of water that water spouting nozzle sprays in reactor top, uniformly mix reaction, enter second reactor then, further carry out the lime slaking reaction, digestion reaction generates white lime (Ca (OH)
2) powder, be delivered to the pipeline that links to each other with thionizer by worm conveyor, spray into desulfuration absorbing tower by roots blower.The macrobead sweetening agent is discharged by slag notch, and the water vapour in the second reactor is directly introduced desulfuration absorbing tower by the pocket type moisture trap of its top.
Described invention comprises the custom-designed reactor of two-stage, is characterized in, the water that sprays into A reactor is excessive, the mol ratio of water and calcium lime powder is 1:1.3, by the pocket type moisture trap on second reactor top, draw excessive moisture, excessive moisture is directly introduced desulfuration absorbing tower.
Described invention, the sweetening agent residence time in second reactor is 6 minutes～12 minutes.
Described invention, the transfer rate of belt weigher, nozzle injection flow rate and worm conveyor rotating speed are all along with boiler load is adjustable.
Realize above-mentioned calcium hydroxide preparation method's device, 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, worm conveyor.It is characterized in that: 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; Its feature is that also the A reactor top is provided with the single fluid nozzle of two row's (group) staggered arrangement.
In said apparatus, the pocket type moisture trap is positioned at the second reactor top, is connected as a single entity with second reactor, and the air outlet is positioned at moisture trap top, and the filter bag filtrate is polyphenylene sulfide (PPS) filtrate, the negative pressure operation, and the air outlet directly connects desulfuration absorbing tower.Its effect is to draw the unnecessary water vapour of second reactor.
In said apparatus, 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.
Described invention finished product white lime is the dry powder attitude, and activity improves greatly, and particle size range is lower than the particle of 20um more than 85%.
The present invention compared with prior art has the following advantages and positively effect:
(1) the present invention 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 present invention draws 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.
The present invention will be further described below in conjunction with the drawings and specific embodiments.
Description of drawings
Accompanying drawing is the structure principle chart of apparatus of the present invention.
Embodiment
Referring to accompanying drawing, method steps during this device 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 (8)
1. calcium hydroxide preparation method who is used for dry flue gas desulphurization, the steps include: that the calcium lime powder (CaO) in the lime silo (1) enters A reactor (7) through belt weigher (2), the water that sprays into the one group of water spouting nozzle in reactor top (6), uniformly mix reaction, enter second reactor (9) then, further carry out the lime slaking reaction, digestion reaction generates white lime (Ca (OH)
2) powder, be delivered to the pipeline that links to each other with thionizer by worm conveyor (17), spray into desulfuration absorbing tower by roots blower.The macrobead sweetening agent is discharged by slag notch (10), and the water vapour in the second reactor (9) is directly introduced desulfuration absorbing tower by the pocket type moisture trap (12) of its top.
2. according to the described calcium hydroxide preparation method of claim 1, it is characterized in that: the water that sprays into A reactor (7) is excessive, the mol ratio of water and calcium lime powder is 1:1.3, pocket type moisture trap (12) by second reactor (9) top, draw excessive moisture, excessive moisture is directly introduced desulfuration absorbing tower.
3. according to the described calcium hydroxide preparation method of claim 1, sweetening agent residence time in second reactor (9) is 6 minutes～12 minutes.
4. according to the described calcium hydroxide preparation method of claim 1, the transfer rate of belt weigher (2), nozzle (6) injection flow rate and worm conveyor (17) rotating speed are all adjustable with boiler load.
5. realize the described calcium hydroxide preparation method's of claim 1 device, 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), worm conveyor (17).It 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; Its feature is that also A reactor (7) top is provided with the single fluid nozzle (6) of two row's (group) staggered arrangement.
6. according to the described calcium hydroxide preparation facilities of claim 5, 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.
7. according to the described calcium hydroxide preparation facilities of claim 5, 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.
8. according to the described calcium hydroxide preparation facilities of claim 5, nozzle (6) is along A reactor (7) main center line, and spray direction is along under A reactor (7) the main center alignment.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007101787476A CN101450791A (en) | 2007-12-05 | 2007-12-05 | Calcium hydrate preparation method for dry flue gas desulfurization and apparatus thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2007101787476A CN101450791A (en) | 2007-12-05 | 2007-12-05 | Calcium hydrate preparation method for dry flue gas desulfurization and apparatus thereof |
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| CN101450791A true CN101450791A (en) | 2009-06-10 |
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| CNA2007101787476A Pending CN101450791A (en) | 2007-12-05 | 2007-12-05 | Calcium hydrate preparation method for dry flue gas desulfurization and apparatus thereof |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102001836A (en) * | 2010-12-08 | 2011-04-06 | 浙江菲达脱硫工程有限公司 | Combined high-efficiency quicklime slaking device |
| CN110327766A (en) * | 2019-07-15 | 2019-10-15 | 淮南聚生化工科技有限公司 | A kind of steel mill energy-saving vulcanizing tower |
| CN110732235A (en) * | 2019-10-28 | 2020-01-31 | 新疆金禾山能源科技有限公司 | flue gas desulfurization equipment based on circulating semidry method |
| CN112551920A (en) * | 2020-10-27 | 2021-03-26 | 莱歇研磨机械制造(上海)有限公司 | Modular high-temperature material digestion system |
| CN115246735A (en) * | 2022-08-01 | 2022-10-28 | 河北浩锐陶瓷制品有限公司 | Production process of energy-saving environment-friendly ceramic tile |
-
2007
- 2007-12-05 CN CNA2007101787476A patent/CN101450791A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102001836A (en) * | 2010-12-08 | 2011-04-06 | 浙江菲达脱硫工程有限公司 | Combined high-efficiency quicklime slaking device |
| CN110327766A (en) * | 2019-07-15 | 2019-10-15 | 淮南聚生化工科技有限公司 | A kind of steel mill energy-saving vulcanizing tower |
| CN110327766B (en) * | 2019-07-15 | 2022-04-12 | 山西新唐工程设计股份有限公司 | Energy-saving vulcanizing tower of steel plant |
| CN110732235A (en) * | 2019-10-28 | 2020-01-31 | 新疆金禾山能源科技有限公司 | flue gas desulfurization equipment based on circulating semidry method |
| CN112551920A (en) * | 2020-10-27 | 2021-03-26 | 莱歇研磨机械制造(上海)有限公司 | Modular high-temperature material digestion system |
| CN112551920B (en) * | 2020-10-27 | 2024-08-02 | 莱歇研磨机械制造(上海)有限公司 | Modularized high-temperature material digestion system |
| CN115246735A (en) * | 2022-08-01 | 2022-10-28 | 河北浩锐陶瓷制品有限公司 | Production process of energy-saving environment-friendly ceramic tile |
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Open date: 20090610 |