CN109304080B - Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system - Google Patents
Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system Download PDFInfo
- Publication number
- CN109304080B CN109304080B CN201810307169.XA CN201810307169A CN109304080B CN 109304080 B CN109304080 B CN 109304080B CN 201810307169 A CN201810307169 A CN 201810307169A CN 109304080 B CN109304080 B CN 109304080B
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- stage absorption
- flue gas
- dust remover
- material returning
- 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.)
- Active
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 239000003546 flue gas Substances 0.000 title claims abstract description 46
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 32
- 230000023556 desulfurization Effects 0.000 title claims abstract description 32
- 238000010521 absorption reaction Methods 0.000 claims abstract description 82
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 32
- 239000000428 dust Substances 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 24
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 22
- 235000011116 calcium hydroxide Nutrition 0.000 claims abstract description 22
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000005243 fluidization Methods 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000002245 particle Substances 0.000 abstract description 16
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 230000003009 desulfurizing effect Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000007787 solid Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention provides an ultra-low SO 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system comprises a three-stage absorption tower, an atomized water nozzle, a lime hydrate bin, a first returning machine, a second returning machine, a dust remover, an ash bin and a chimney; the third-stage absorption tower comprises a first-stage absorption tower, a second-stage absorption tower and a third-stage absorption tower, the top end of the first-stage absorption tower is connected with the top end of the second-stage absorption tower, the bottom end of the second-stage absorption tower is connected with the bottom end of the third-stage absorption tower, a first material return port is arranged in the first-stage absorption tower, a second material return port is arranged in the third-stage absorption tower, and the joint of the second-stage absorption tower and the bottom end of the third-stage absorption tower is connected with the first material return port through a first material return machine; the bottom of the dust remover is connected with a second material returning opening through a second material returning machine. The invention increases the residence time of the slaked lime particles in the absorption tower, thereby prolonging the contact time of the flue gas and the slaked lime, and being beneficial to improving the utilization rate and the desulfurization efficiency of the slaked lime.
Description
Technical Field
The invention relates to the technical field of flue gas desulfurization, in particular to an ultra-low SO 2 And the discharged semi-dry circulating fluidized bed flue gas desulfurization system.
Background
The flue gas desulfurization technology adopted by the coal-fired power station mainly comprises three types of wet desulfurization, dry desulfurization and semi-dry desulfurization. Among them, the wet desulfurization technology has high desulfurization efficiency, but requires a large capital investment and consumes a large amount of water. In order to reduce the water consumption of desulfurization, semi-dry flue gas desulfurization technology has been developed. The circulating fluidized bed flue gas desulfurization technology is a semi-dry flue gas desulfurization technology developed in the last 80 th century, and the basic principle is as follows: the flue gas enters from the bottom of the absorption tower, enters into the main body section of the absorption tower after being accelerated by the Venturi tube, and the gas-solid two phases generate strong turbulence under the action of the air flow, so that the flue gas is contacted with the calcium-based desulfurizing agent to generate desulfurization reaction.
The circulating fluidized bed flue gas desulfurization system has simple structure and small water consumption, is very suitable for the national conditions of insufficient water resources in China, and is one of key technologies for technical development, popularization and application in the power environment-friendly industry. However, the conventional circulating fluidized bed flue gas desulfurization system has certain defects, and the utilization rate of the desulfurizing agent is low and the desulfurizing effect is poor due to insufficient residence time of the calcium-based desulfurizing agent in the absorption tower. With the continuous improvement of environmental protection requirements, SO 2 The emission standard of the flue gas desulfurization agent is higher and higher, and how to improve the utilization rate of the desulfurization agent and the desulfurization effect of the flue gas is a technical problem which needs to be solved at present.
Disclosure of Invention
In order to solve the problems of low utilization rate of the desulfurizing agent and poor desulfurizing effect in the prior art, the invention provides an ultralow SO 2 And the discharged semi-dry circulating fluidized bed flue gas desulfurization system.
The technical scheme of the invention is realized as follows:
ultralow SO 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system comprises a three-stage absorption tower, an atomized water nozzle, a lime hydrate bin, a first returning machine, a second returning machine, a dust remover, an ash bin and a chimney;
the three-stage absorption tower comprises a first-stage absorption tower, a second-stage absorption tower and a third-stage absorption tower which are vertically arranged, the top end of the first-stage absorption tower is connected with the top end of the second-stage absorption tower, the bottom end of the second-stage absorption tower is connected with the bottom end of the third-stage absorption tower, the bottom of the first-stage absorption tower is provided with a flue gas inlet, the top end of the third-stage absorption tower is provided with a flue gas outlet,
the first stage absorption tower is internally provided with a first Venturi fluidization section, a first divergent section and a first reaction main body section from bottom to top in sequence, an atomized water nozzle is arranged in the first divergent section, and a first returning port and a slaked lime inlet are arranged on the first divergent section;
a second venturi fluidization section, a second divergent section and a second reaction main body section are sequentially arranged in the third-stage absorption tower from bottom to top, and a second material returning port is arranged on the second divergent section;
the lime hydrate bin is connected with the first-stage absorption tower through a lime hydrate inlet, and the joint of the bottom ends of the second-stage absorption tower and the third-stage absorption tower is connected with a first material return port through a first material return machine; one end of the dust remover is connected with the flue gas outlet, the other end of the dust remover is connected with the chimney, the bottom of the dust remover is provided with two outlets, one outlet is connected with the second returning charge port through the second returning charge machine, and the other outlet is connected with the ash bin.
Preferably, the dust remover also comprises an induced draft fan, and the dust remover is connected with the chimney through the induced draft fan.
Further preferably, the first and second return machines are both screw return machines.
Compared with the prior art, the invention prolongs the residence time of the slaked lime particles in the absorption tower by additionally arranging the dust remover and the returning charge machine, thereby prolonging the contact time of the flue gas and the slaked lime particles and improving the utilization efficiency and the desulfurization efficiency of the slaked lime particles. Meanwhile, due to the adoption of tower circulation, the total height of the absorption tower is reduced.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions of the prior art, the drawings which are used in the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the description below are only some embodiments of the invention, and that other drawings can be obtained according to these drawings without inventive faculty for a person skilled in the art.
Fig. 1 is a schematic structural view of the present invention.
In the figure: 1. a three-stage absorption tower; 11. a first stage absorber; 111. a first venturi fluidization section; 112. a slaked lime inlet; 113. a first return port; 114. a first diverging section; 12. a second-stage absorption column; 13. a third stage absorption tower; 131. a second venturi fluidization section; 132. a second return port; 133. a second diverging section; 14. a flue gas inlet; 15. a flue gas outlet; 2. a lime slaking bin; 3. a first return machine; 4. a second returning charge machine; 5. a dust remover; 6. an ash bin; 7. an induced draft fan; 8. a chimney; 9. an atomized water nozzle.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
As shown in fig. 1: ultralow SO 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system comprises a three-stage absorption tower 1, an atomized water nozzle 9, a lime hydrate bin 2, a first material returning machine 3, a second material returning machine 4, a dust remover 5, an ash bin 6 and a chimney 8;
the three-stage absorption tower 1 comprises a first-stage absorption tower 11, a second-stage absorption tower 12 and a third-stage absorption tower 13 which are vertically arranged, the top end of the first-stage absorption tower 11 is connected with the top end of the second-stage absorption tower 12, the bottom end of the second-stage absorption tower 12 is connected with the bottom end of the third-stage absorption tower 13, the bottom of the first-stage absorption tower 11 is provided with a flue gas inlet 14, the top end of the third-stage absorption tower 13 is provided with a flue gas outlet 15,
a first venturi fluidization section 111, a first divergent section 114 and a first reaction main body section are sequentially arranged in the first-stage absorption tower 11 from bottom to top, the atomized water nozzle 9 is arranged in the first divergent section 114, and a first returning opening 113 and a slaked lime inlet 112 are arranged on the first divergent section 114;
a second venturi fluidization section 131, a second divergent section 133 and a second reaction main body section are sequentially arranged in the third-stage absorption tower 13 from bottom to top, and a second material returning opening 132 is arranged on the second divergent section 133;
the lime hydrate bin 2 is connected with the first-stage absorption tower 11 through a lime hydrate inlet 112, and the joint of the bottom ends of the second-stage absorption tower 12 and the third-stage absorption tower 13 is connected with a first material return port 113 through a first material return machine 3; one end of the dust remover 5 is connected with the flue gas outlet 15, the other end is connected with the chimney 8, the bottom of the dust remover 5 is provided with two outlets, one outlet is connected with the second returning charge port 132 through the second returning charge machine 4, and the other outlet is connected with the ash bin 6.
Working principle: the flue gas enters from the flue gas inlet 14, is accelerated by the first venturi fluidization section 111 and enters upward. The slaked lime stored in the slaked lime bin 2 enters the first stage absorption tower 11 through the slaked lime inlet 112, the accelerated flue gas is fully mixed with slaked lime particles, and then atomized water sprayed from the atomized water nozzle 9 increases the humidity of the slaked lime particles on one hand and cools the flue gas on the other hand, SO that the flue gas temperature is kept higher than the dew point of the flue gas by 15-25 ℃, thereby allowing the slaked lime and SO 2 And (3) finishing the ionic desulfurization reaction. The flue gas carries part of slaked lime particles to turn at the upper part of the first stage absorption tower 11 and enter the upper part of the second stage absorption tower 12 to descend. The second stage absorption tower 12 turns to enter the lower part of the third stage absorption tower 13, a large amount of particles are deposited due to gravity and centrifugal force, and the first returning machine 3 can return the unreacted and completely slaked lime particles to the first stage absorption tower 11 through the first returning opening 113 for continuous reaction. The flue gas continues to enter the upward after being accelerated by the second venturi fluidization section 131 of the third-stage absorption tower 13, and flows out from the upper part of the third-stage absorption tower 13 into the dust remover 5. The solid particles in the flue gas are captured by the dust separator 5, which contains a part of the slaked lime particles which are not completely reacted, and desulfurization byproducts, fly ash, etc. Part of the solid particles are returned to the third-stage absorption tower 13 through the second material returning machine 4 via one outlet at the lower part of the dust remover 5, and the other part is sent to the ash bin 6 from the other outlet for storage and transportation. Clean flue gas from the dust collector 5 is discharged from a chimney 8.
Compared with the prior art, the invention has the following beneficial effects:
1. the dust remover and the returning charge machine are additionally arranged, so that the residence time of the slaked lime particles in the absorption tower is prolonged, the contact time of the flue gas and the slaked lime particles is prolonged, and the utilization efficiency and the desulfurization efficiency of the slaked lime particles are improved;
2. and three stages of absorption towers are adopted, and the tower circulation is adopted for sulfur removal, so that the total height of the absorption towers is reduced.
As a preferred technical solution, a further embodiment of the present invention further comprises an induced draft fan 7, the dust remover 5 is connected with the chimney 8 through the induced draft fan 7, and clean flue gas from the dust remover 11 is discharged from the chimney 8 through the induced draft fan 13.
As a preferred solution, according to a further embodiment of the invention, the first and second return machines 3, 4 are both screw return machines. When the spiral returning machine returns solid particles, the rotating speed of the spiral returning machine should ensure that the gas cannot be reversely strung.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (3)
1. Ultralow SO 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system is characterized in that: comprises a three-stage absorption tower (1), an atomized water nozzle (9), a lime hydrate bin (2), a first material returning machine (3), a second material returning machine (4), a dust remover (5), an ash bin (6) and a chimney (8);
the three-stage absorption tower (1) comprises a first-stage absorption tower (11), a second-stage absorption tower (12) and a third-stage absorption tower (13) which are vertically arranged, the top end of the first-stage absorption tower (11) is connected with the top end of the second-stage absorption tower (12), the bottom end of the second-stage absorption tower (12) is connected with the bottom end of the third-stage absorption tower (13), the bottom of the first-stage absorption tower (11) is provided with a flue gas inlet (14), the top end of the third-stage absorption tower (13) is provided with a flue gas outlet (15),
a first venturi fluidization section (111), a first divergent section (114) and a first reaction main body section are sequentially arranged in the first-stage absorption tower (11) from bottom to top, an atomized water nozzle (9) is arranged in the first divergent section (114), and a first material returning opening (113) and a slaked lime inlet (112) are arranged on the first divergent section (114);
a second venturi fluidization section (131), a second divergent section (133) and a second reaction main body section are sequentially arranged in the third-stage absorption tower (13) from bottom to top, and a second material returning opening (132) is arranged on the second divergent section (133);
the lime hydrate bin (2) is connected with the first-stage absorption tower (11) through a lime hydrate inlet (112), and the joint of the bottom ends of the second-stage absorption tower (12) and the third-stage absorption tower (13) is connected with a first material returning opening (113) through a first material returning machine (3); one end of the dust remover (5) is connected with the flue gas outlet (15), the other end of the dust remover is connected with the chimney (8), two outlets are arranged at the bottom of the dust remover (5), one outlet is connected with the second returning opening (132) through the second returning machine (4), and the other outlet is connected with the ash bin (6).
2. The ultra low SO of claim 1 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system is characterized in that: the dust remover also comprises an induced draft fan (7), and the dust remover (5) is connected with a chimney (8) through the induced draft fan (7).
3. The ultra low SO of claim 2 2 The discharged semi-dry circulating fluidized bed flue gas desulfurization system is characterized in that: the first material returning machine (3) and the second material returning machine (4) are spiral material returning machines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810307169.XA CN109304080B (en) | 2018-04-08 | 2018-04-08 | Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810307169.XA CN109304080B (en) | 2018-04-08 | 2018-04-08 | Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109304080A CN109304080A (en) | 2019-02-05 |
| CN109304080B true CN109304080B (en) | 2024-01-05 |
Family
ID=65225841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810307169.XA Active CN109304080B (en) | 2018-04-08 | 2018-04-08 | Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109304080B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109663471A (en) * | 2019-02-11 | 2019-04-23 | 王脯胜 | A kind of semi-dry process flue gas desulphurization three-level minimum discharge method and apparatus |
| CN110368799B (en) * | 2019-07-30 | 2022-05-27 | 福建龙净脱硫脱硝工程有限公司 | Semi-dry desulfurization device and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102228788A (en) * | 2011-06-24 | 2011-11-02 | 中国科学院过程工程研究所 | Device and method for removing sulfur dioxide and dioxin from sintering flue gas |
| CN103007711A (en) * | 2012-12-06 | 2013-04-03 | 中钢集团新型材料（浙江）有限公司 | Equipment and tail gas treatment method for synchronously treating tail gas of multiple graphitization furnaces |
| CN103557697A (en) * | 2013-10-30 | 2014-02-05 | 江西自立资源再生有限公司 | Novel rotary kiln |
| CN204358713U (en) * | 2014-12-30 | 2015-05-27 | 中国电力工程顾问集团华北电力设计院有限公司 | A kind of high circulating ratio stack gas desulfurization system of circulating fluid bed |
| CN209005536U (en) * | 2017-12-15 | 2019-06-21 | 山西国峰煤电有限责任公司 | A kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103566725B (en) * | 2013-10-15 | 2016-03-02 | 中国科学院过程工程研究所 | A kind of circulating fluid bed semi-drying method combined desulfurization and denitration mercury removal device and method |
-
2018
- 2018-04-08 CN CN201810307169.XA patent/CN109304080B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102228788A (en) * | 2011-06-24 | 2011-11-02 | 中国科学院过程工程研究所 | Device and method for removing sulfur dioxide and dioxin from sintering flue gas |
| CN103007711A (en) * | 2012-12-06 | 2013-04-03 | 中钢集团新型材料（浙江）有限公司 | Equipment and tail gas treatment method for synchronously treating tail gas of multiple graphitization furnaces |
| CN103557697A (en) * | 2013-10-30 | 2014-02-05 | 江西自立资源再生有限公司 | Novel rotary kiln |
| CN204358713U (en) * | 2014-12-30 | 2015-05-27 | 中国电力工程顾问集团华北电力设计院有限公司 | A kind of high circulating ratio stack gas desulfurization system of circulating fluid bed |
| CN209005536U (en) * | 2017-12-15 | 2019-06-21 | 山西国峰煤电有限责任公司 | A kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109304080A (en) | 2019-02-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202700306U (en) | Efficient wet type venturi pipe combined dedusting desulfurizer | |
| CN103768908B (en) | What a kind of wet type integrated desulfurizing denitration demercuration took off PM2.5 removes tower and technique | |
| CN201168563Y (en) | Pneumatic flow guide dust removing and desulferizing device | |
| CN205672756U (en) | A kind of double tower Two-way Cycle lime stone gypsum wet flue gas desulfurizing device | |
| CN103846005A (en) | Wet process flue gas desulfurization device and method for classified washing | |
| CN109304080B (en) | Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system | |
| CN102266718B (en) | Semi dry process flue gas desulfurization method of circulating fluidized bed based on circulation, and apparatus thereof | |
| CN203725021U (en) | Efficient integrated desulfurizing, dedusting and demisting device | |
| CN201085994Y (en) | Circulation fluidized bed smoke desulphurizing device | |
| CN209501361U (en) | Novel energy-conserving Complexing Iron desulphurization plant | |
| CN203469805U (en) | Absorption tower device capable of simultaneously desulfurizing and denitrifying smoke through bubbling and spraying | |
| CN204320088U (en) | The desulfurization integrated spray absorber of high-effective dust-removing | |
| CN201880473U (en) | Venturi spraying and wet static electricity combined type flue gas treatment reactor | |
| CN206881311U (en) | Demisting separator | |
| CN204358713U (en) | A kind of high circulating ratio stack gas desulfurization system of circulating fluid bed | |
| CN206621985U (en) | A kind of coal steam-electric plant smoke sulfur dioxide and waste water coprocessing system | |
| CN201389423Y (en) | Flue gas desulphurization dust removing tower for coal burning boiler | |
| CN206295800U (en) | A kind of semi-dry flue gas desulfurization device | |
| CN201949801U (en) | Flue gas desulfurization device of thermal power generating unit of burning high-sulfur coal | |
| CN104624029A (en) | Device for integrating cooling tower, desulfurizing tower and chimney, and desulfurizing method | |
| CN103301745A (en) | Cyclone separator desulfurization device | |
| CN201015729Y (en) | Multiple layer spray water circulating fluidized bed flue-gas desulfurizing device | |
| CN202538566U (en) | Dust and sulfur removing device for tail gas | |
| CN101972594A (en) | Water-covered type dedusting and desulphuration method and device | |
| CN102441324A (en) | Flue gas desulfurization reactor for descending circulating fluidized bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |