CN1498673A - A method and device for integrating flue gas desulfurization and dust removal in a circulating fluidized bed - Google Patents
A method and device for integrating flue gas desulfurization and dust removal in a circulating fluidized bed Download PDFInfo
- Publication number
- CN1498673A CN1498673A CNA021467579A CN02146757A CN1498673A CN 1498673 A CN1498673 A CN 1498673A CN A021467579 A CNA021467579 A CN A021467579A CN 02146757 A CN02146757 A CN 02146757A CN 1498673 A CN1498673 A CN 1498673A
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- CN
- China
- Prior art keywords
- reaction tower
- fluidized bed
- flue gas
- sack cleaner
- recirculating fluidized
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
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- 239000000428 dust Substances 0.000 title claims abstract description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 239000003546 flue gas Substances 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 16
- 230000023556 desulfurization Effects 0.000 title claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000002245 particle Substances 0.000 claims abstract description 18
- 239000002002 slurry Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000007921 spray Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 33
- 230000003134 recirculating effect Effects 0.000 claims description 29
- 239000012530 fluid Substances 0.000 claims description 14
- 239000002594 sorbent Substances 0.000 claims description 11
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 8
- 238000013459 approach Methods 0.000 claims description 7
- 230000003009 desulfurizing effect Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000004071 soot Substances 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 4
- 238000013517 stratification Methods 0.000 claims description 3
- 230000005514 two-phase flow Effects 0.000 claims description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 229910052717 sulfur Inorganic materials 0.000 claims description 2
- 239000011593 sulfur Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 25
- 238000005516 engineering process Methods 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 2
- 239000010882 bottom ash Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
一种循环流化床烟气脱硫除尘一体化的方法及其装置，属于烟气净化技术领域。本发明在保证除尘效率的同时能有效提高脱硫剂的利用率和烟气脱硫效率。本发明方法的步骤为：1)热烟气进入反应塔，同时向循环流化床反应塔内喷入雾化的脱硫剂浆液和水；2)脱硫剂颗粒和烟气中的二氧化硫在反应塔中发生化学反应，脱除掉二氧化硫；3)烟气在预除尘器内进行初步的分离；4)烟气再经过袋式除尘器除去大部分灰尘，排入烟囱；5)从袋式除尘器分离出来的脱硫剂颗粒经过空气输送斜槽，进入反应塔循环使用或者通过排灰管道排出；6)袋式除尘器分离下来的灰尘，从空气斜槽的尾部排出；7)循环流化床反应塔底部的积灰通过积灰斗排到排灰管道。
A circulating fluidized bed flue gas desulfurization and dust removal integrated method and device thereof belong to the technical field of flue gas purification. The invention can effectively improve the utilization rate of the desulfurizer and the desulfurization efficiency of the flue gas while ensuring the dust removal efficiency. The steps of the method of the present invention are: 1) hot flue gas enters the reaction tower, and simultaneously sprays atomized desulfurizer slurry and water into the circulating fluidized bed reaction tower; 3) The flue gas is initially separated in the pre-dust collector; 4) The flue gas passes through the bag filter to remove most of the dust and is discharged into the chimney; 5) From the bag filter The separated desulfurizer particles pass through the air delivery chute and enter the reaction tower for recycling or discharge through the ash discharge pipe; 6) The dust separated by the bag filter is discharged from the tail of the air chute; 7) Circulating fluidized bed reaction The ash at the bottom of the tower is discharged to the ash discharge pipe through the ash hopper.
Description
Technical field
The present invention relates to the flue gases purification field, relate in particular to the incorporate method of stack gas desulfurization and dust removal of circulating fluid bed and realize the device of this method.
Background technology
Flue gas ash removal is two emphasis aspects that control environment and pollute with removing sulfur dioxide.Along with country's more and more tight to environmental protection requirement, not only improved the discharge standard of flue dust, and strengthened control the discharging oxysulfide.But in the prior art dedusting and desulfur technology often two independently system bear, the technical application of present desulphurizing and dust-removing integral and technical limitation be clearly.System's operational reliability of existing desulphurizing and dust-removing integral technology is relatively poor, and the coordinated operation of desulphurization system and dust pelletizing system is difficult to realize.These problems have seriously restricted the development of desulphurizing and dust-removing integral technology.
Summary of the invention
Problem at above-mentioned prior art situation and existence, technical problem to be solved by this invention provides incorporate method of a kind of stack gas desulfurization and dust removal of circulating fluid bed and device thereof, can effectively improve the utilization rate and the smoke desulfurization efficiency of desulfurizing agent when guaranteeing efficiency of dust collection.
In order to reach the foregoing invention purpose, technical scheme of the present invention realizes as follows:
The incorporate method of a kind of stack gas desulfurization and dust removal of circulating fluid bed, the steps include: 1) the hot flue gas that comes out from boiler, enter reaction tower from the gas approach of recirculating fluidized bed reaction tower bottom, in the recirculating fluidized bed reaction tower, spray into simultaneously the desulfurizer slurry and the water of atomizing, and mix with hot flue gas in the reflection tower; 2) chemical reaction takes place in fluidised sorbent particle and sulfur in smoke in reaction tower, removes sulfur dioxide; 3) flue gas carries the exhanst gas outlet discharge of the sorbent particle of not abundant reaction from the desulfurizing tower top, and the sack cleaner through the band pre-duster carries out preliminary separation in pre-duster; 4) remove most of dust through sack cleaner again through the flue gas of initial gross separation, flue gas after being purified enters chimney through air-introduced machine; 5) the soot particle process air conveyer flume of separating from sack cleaner that contains sorbent particle that does not fully react, entering reaction tower again recycles, guarantee fluid bed endoparticle steady concentration, unnecessary soot particle is discharged by removing ash pipeline from the afterbody of air flume; 6) dust that separates of sack cleaner is discharged from the afterbody of air flume; 7) dust stratification of recirculating fluidized bed reaction tower bottom is discharged to removing ash pipeline by ash bucket.
Realize the device of above-mentioned stack gas desulfurization and dust removal of circulating fluid bed integral method, comprise recirculating fluidized bed reaction tower and sack cleaner.The bottom of described recirculating fluidized bed reaction tower is provided with gas approach, desulfurizer slurry nozzle and (operating) water nozzle, recirculating fluidized bed reaction tower top is provided with exhanst gas outlet, the bottom of recirculating fluidized bed reaction tower is provided with ash bucket, and the bottom opening and the removing ash pipeline of ash bucket join.Sack cleaner has pre-duster, is provided with clean exhanst gas outlet at an end of described sack cleaner, also is provided with ash bucket in the bottom of described pre-duster and described sack cleaner.Its design feature is, the exhanst gas outlet of described recirculating fluidized bed reaction tower is connected with the pre-dedusting device of sack cleaner, the ash bucket of described pre-duster and sack cleaner links to each other with the air conveyer flume of inclination by pipeline, the end that air conveyer flume is lower links to each other with the circulating ash pipeline, the other end of circulating ash pipeline inserts the bottom of recirculating fluidized bed reaction tower, air conveyer flume is near the lower end opening, and and removing ash pipeline join.
The device of above-mentioned realization stack gas desulfurization and dust removal of circulating fluid bed integral method, the desulfurizer slurry nozzle adopts the two phase flow atomizer.In adopting, the pre-dedusting device of sack cleaner is provided with the diffuser pattern of gas baffling plate.
The present invention compared with prior art has the following advantages and good effect:
(1) the outer circulation utilization of sorbent particle has guaranteed the granule density in the fluid bed,
Prolong the time of staying of desulfurizing agent, thereby improved the utilization rate of desulfurizing agent greatly
And smoke desulfurization efficiency.
(2) outer circulation of the sorbent particle of setting up between desulfurization reaction tower and deduster system
System, stable, reliable.
(3) kept pre-duster before the sack cleaner, made the grit that enters sack cleaner
Concentration reduces greatly, has reduced SR, has improved efficiency of dust collection.
(4) apparatus structure compactness of the present invention, resistance are little, stable, have realized succinct
Desulphurizing and dust-removing integral efficiently.
Description of drawings
Accompanying drawing is the structure principle chart of apparatus of the present invention.
The present invention is further illustrated below in conjunction with accompanying drawing and concrete embodiment.
The specific embodiment
Method of the present invention is narrated in summary of the invention, and scheme is identical, repeats no more.
Referring to accompanying drawing, the device of implementing the inventive method comprises recirculating fluidized bed reaction tower 1 and sack cleaner 7.The bottom of recirculating fluidized bed reaction tower 1 is provided with gas approach 2, the desulfurizer slurry nozzle 3 of (operating) water nozzle 4 and employing two phase flow atomizer is housed respectively on the top of gas approach 2, recirculating fluidized bed reaction tower 1 top is provided with exhanst gas outlet 5, the bottom of described recirculating fluidized bed reaction tower 1 is provided with ash bucket 9-1, and the bottom opening of ash bucket 9-1 and removing ash pipeline 12 join.Sack cleaner 7 has pre-duster 6, and the diffuser that is provided with the gas baffling plate in pre-duster 6 adopts is provided with clean exhanst gas outlet 8 at an end of sack cleaner 7, is provided with ash bucket 9-2 in the bottom of pre-duster 6 and sack cleaner 7.The other end of the exhanst gas outlet 5 of recirculating fluidized bed reaction tower 1 is connected with the pre-duster 6 of sack cleaner 7, the ash bucket 9-2 of pre-duster 6 and sack cleaner 7 links to each other with the air conveyer flume 10 of inclination, air conveyer flume 10 lower ends link to each other with circulating ash pipeline 11, the other end of circulating ash pipeline 11 inserts the bottom of recirculating fluidized bed reaction tower 1, air conveyer flume 10 joins near lower end opening and removing ash pipeline 12.
The hot flue gas that comes out from boiler, enter recirculating fluidized bed reaction tower 1 by gas approach 2, desulfurizer slurry and water are respectively by desulfurizer slurry nozzle 3 and (operating) water nozzle 4, enter recirculating fluidized bed reaction tower 1 after the atomizing, flue gas forms the high efficient gas-solid fluidization with sorbent particle and contacts in recirculating fluidized bed reaction tower 1, chemical reaction takes place, remove most sulfur dioxide, keep fluid bed endoparticle steady concentration by the pressure reduction in the control recirculating fluidized bed reaction tower 1, flue gas carries the sorbent particle that does not fully react and discharges from the exhanst gas outlet 5 at recirculating fluidized bed reaction tower 1 top, enter the pre-duster 6 before the sack cleaner 7, pre-duster 6 utilizes diffusion, sedimentation, collision, principles such as inertia, make the grit in the flue gas in pre-duster 6, obtain capturing, the dust particle concentration that enters sack cleaner 7 is reduced greatly, reduced SR.Carry out preliminary separation in pre-duster 6 after, remove most of dust through sack cleaner 7 again, flue gas after being purified is by clean exhanst gas outlet 8 dischargings.The sorbent particle that does not fully react among the ash bucket 9-2 of pre-duster 6 and sack cleaner 7 bottoms is by air conveyer flume 10, entering reaction tower 1 via circulating ash pipeline 11 recycles, the part soot particle is discharged from the removing ash pipeline 12 of air conveyer flume 10 tail ends, by the ash discharge amount of regulating air conveyer flume 10 tail ends, keep reaction tower endoparticle steady concentration.When reaching a certain height, the dust stratification of reaction tower 1 bottom ash bucket 9-1 discharges by removing ash pipeline 12.
Claims (4)
1. incorporate method of stack gas desulfurization and dust removal of circulating fluid bed, the steps include: 1) the hot flue gas that comes out from boiler, enter reaction tower from the gas approach of recirculating fluidized bed reaction tower bottom, in the recirculating fluidized bed reaction tower, spray into simultaneously the desulfurizer slurry and the water of atomizing, and mix with hot flue gas in the reflection tower; 2) chemical reaction takes place in fluidised sorbent particle and sulfur in smoke in reaction tower, removes sulfur dioxide; 3) flue gas carries the exhanst gas outlet discharge of the sorbent particle of not abundant reaction from the desulfurizing tower top, and the sack cleaner through the band pre-duster carries out preliminary separation in pre-duster; 4) remove most of dust through sack cleaner again through the flue gas of initial gross separation, flue gas after being purified enters chimney through air-introduced machine; 5) the soot particle process air conveyer flume of separating from sack cleaner that contains sorbent particle that does not fully react, entering reaction tower again recycles, guarantee fluid bed endoparticle steady concentration, unnecessary soot particle is discharged by removing ash pipeline from the afterbody of air flume; 6) dust that separates of sack cleaner is discharged from the afterbody of air flume; 7) dust stratification of recirculating fluidized bed reaction tower bottom is discharged to removing ash pipeline by ash bucket.
2. realize the device of the described stack gas desulfurization and dust removal of circulating fluid bed integral method of claim 1, comprise recirculating fluidized bed reaction tower (1) and sack cleaner (7), the bottom of described recirculating fluidized bed reaction tower (1) is provided with gas approach (2), desulfurizer slurry nozzle (3) and (operating) water nozzle (4), the top of recirculating fluidized bed reaction tower (1) is provided with exhanst gas outlet (5), the bottom of recirculating fluidized bed reaction tower (1) is provided with ash bucket (9-1), and the bottom opening of ash bucket (9-1) and removing ash pipeline (12) join; Sack cleaner (7) has pre-duster (6), end at sack cleaner (7) is provided with clean exhanst gas outlet (8), bottom at pre-duster (6) and sack cleaner (7) is provided with ash bucket (9-2), it is characterized in that, the exhanst gas outlet (5) of described recirculating fluidized bed reaction tower (1) is connected with the pre-duster (6) of sack cleaner (7), the ash bucket (9-2) of pre-dedusting device (6) and sack cleaner (7) links to each other with tilted-putted air conveyer flume (10), the end that air conveyer flume (10) is lower links to each other with circulating ash pipeline (11), the other end of circulating ash pipeline (11) inserts the bottom of recirculating fluidized bed reaction tower (1), air conveyer flume (10) lower end opening, and and removing ash pipeline (12) join.
3. according to the device of the described realization stack gas desulfurization and dust removal of circulating fluid bed of claim 2 integral method, it is characterized in that: described desulfurizer slurry nozzle (3) adopts the two phase flow atomizer.
4. according to the device of claim 2 or 3 described realization stack gas desulfurization and dust removal of circulating fluid bed integral methods, it is characterized in that: the diffuser pattern that is provided with band gas baffling plate in the pre-duster (6) of described sack cleaner (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA021467579A CN1498673A (en) | 2002-11-06 | 2002-11-06 | A method and device for integrating flue gas desulfurization and dust removal in a circulating fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA021467579A CN1498673A (en) | 2002-11-06 | 2002-11-06 | A method and device for integrating flue gas desulfurization and dust removal in a circulating fluidized bed |
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| Publication Number | Publication Date |
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| CN1498673A true CN1498673A (en) | 2004-05-26 |
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|---|---|---|---|
| CNA021467579A Pending CN1498673A (en) | 2002-11-06 | 2002-11-06 | A method and device for integrating flue gas desulfurization and dust removal in a circulating fluidized bed |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100434146C (en) * | 2006-04-11 | 2008-11-19 | 中国科学院过程工程研究所 | A dry-type internal and external double circulation fluidized bed desulfurization device and desulfurization method |
| CN101354137B (en) * | 2008-09-26 | 2010-06-09 | 北京市琉璃河水泥有限公司 | Apparatus and method for conveying tertiary air waste heat boiler flue dust |
| CN102614747A (en) * | 2012-03-30 | 2012-08-01 | 蓝天环保设备工程股份有限公司 | Flue gas cleaning device and method for circulating fluidized bed through semi-dry method |
| CN102976101A (en) * | 2012-11-06 | 2013-03-20 | 镇江市电站辅机厂有限公司 | Desulfurized ash delivery device |
| CN103611383A (en) * | 2013-12-11 | 2014-03-05 | 北京龙电宏泰环保科技有限公司 | Device and method for synergetically removing ultrafine particles and micro-pollutants in flue gas of coal-fired boiler |
| CN109092059A (en) * | 2018-07-23 | 2018-12-28 | 长兴旗滨玻璃有限公司 | A kind of denitration of glass furnace fume ammonia-spraying grid online ash removal device and its ash removal method |
| CN111068500A (en) * | 2019-12-23 | 2020-04-28 | 山东师范大学 | Circulating fluidized bed flue gas desulfurization system |
| CN111686562A (en) * | 2020-06-16 | 2020-09-22 | 山东神华山大能源环境有限公司 | Circulating fluidized bed semi-dry desulfurization ash circulating system and control method |
| CN112316595A (en) * | 2020-12-01 | 2021-02-05 | 山东水发环境治理有限公司 | Bag-type dust collector, semi-dry desulfurization and dust removal system and circulating ash selection method |
| CN113230872A (en) * | 2021-05-20 | 2021-08-10 | 北京铝能清新环境技术有限公司 | Electrolytic flue gas semi-dry desulfurization circulating ash tower returning process |
-
2002
- 2002-11-06 CN CNA021467579A patent/CN1498673A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100434146C (en) * | 2006-04-11 | 2008-11-19 | 中国科学院过程工程研究所 | A dry-type internal and external double circulation fluidized bed desulfurization device and desulfurization method |
| CN101354137B (en) * | 2008-09-26 | 2010-06-09 | 北京市琉璃河水泥有限公司 | Apparatus and method for conveying tertiary air waste heat boiler flue dust |
| CN102614747A (en) * | 2012-03-30 | 2012-08-01 | 蓝天环保设备工程股份有限公司 | Flue gas cleaning device and method for circulating fluidized bed through semi-dry method |
| CN102614747B (en) * | 2012-03-30 | 2014-05-14 | 蓝天环保设备工程股份有限公司 | Flue gas cleaning device and method for circulating fluidized bed through semi-dry method |
| CN102976101A (en) * | 2012-11-06 | 2013-03-20 | 镇江市电站辅机厂有限公司 | Desulfurized ash delivery device |
| CN103611383A (en) * | 2013-12-11 | 2014-03-05 | 北京龙电宏泰环保科技有限公司 | Device and method for synergetically removing ultrafine particles and micro-pollutants in flue gas of coal-fired boiler |
| CN109092059A (en) * | 2018-07-23 | 2018-12-28 | 长兴旗滨玻璃有限公司 | A kind of denitration of glass furnace fume ammonia-spraying grid online ash removal device and its ash removal method |
| CN109092059B (en) * | 2018-07-23 | 2021-02-05 | 长兴旗滨玻璃有限公司 | Online ash removal device and method for denitration ammonia-spraying grid of glass kiln flue gas |
| CN111068500A (en) * | 2019-12-23 | 2020-04-28 | 山东师范大学 | Circulating fluidized bed flue gas desulfurization system |
| CN111686562A (en) * | 2020-06-16 | 2020-09-22 | 山东神华山大能源环境有限公司 | Circulating fluidized bed semi-dry desulfurization ash circulating system and control method |
| CN112316595A (en) * | 2020-12-01 | 2021-02-05 | 山东水发环境治理有限公司 | Bag-type dust collector, semi-dry desulfurization and dust removal system and circulating ash selection method |
| CN113230872A (en) * | 2021-05-20 | 2021-08-10 | 北京铝能清新环境技术有限公司 | Electrolytic flue gas semi-dry desulfurization circulating ash tower returning process |
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