CN109304080A - A kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge - Google Patents
A kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge Download PDFInfo
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- CN109304080A CN109304080A CN201810307169.XA CN201810307169A CN109304080A CN 109304080 A CN109304080 A CN 109304080A CN 201810307169 A CN201810307169 A CN 201810307169A CN 109304080 A CN109304080 A CN 109304080A
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- Prior art keywords
- absorption tower
- returning charge
- level absorption
- level
- charge machine
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 239000003546 flue gas Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 14
- 230000003134 recirculating effect Effects 0.000 title claims abstract description 10
- 238000010521 absorption reaction Methods 0.000 claims abstract description 79
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 24
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 24
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000003818 cinder Substances 0.000 claims abstract description 9
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 14
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 238000005243 fluidization Methods 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 7
- 235000011116 calcium hydroxide Nutrition 0.000 abstract description 22
- 238000006477 desulfuration reaction Methods 0.000 abstract description 17
- 239000002245 particle Substances 0.000 abstract description 17
- 230000023556 desulfurization Effects 0.000 description 12
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000032258 transport Effects 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention proposes a kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, including three-level absorption tower, atomizing water nozzle, niter ash cellar, the first returning charge machine, the second returning charge machine, deduster, cinder tank and chimney；Three-level absorption tower includes first order absorption tower, second level absorption tower and third level absorption tower, the top on first order absorption tower is connected with the top on second level absorption tower, the bottom end on second level absorption tower is connected with the bottom end on third level absorption tower, the first return port is equipped in first order absorption tower, the second return port is equipped in third absorption tower, second level absorption tower is connect by the first returning charge machine with the first return port with the bottom end junction on third level absorption tower；The bottom of deduster is connect by the second returning charge machine with the second return port.The residence time that invention increases hydrated lime particles in absorption tower then extends the time of contact of flue gas and calcium hydroxide, helps to improve the utilization rate and desulfuration efficiency of calcium hydroxide.
Description
Technical field
The present invention relates to flue gas desulfurization technique fields, particularly relate to a kind of ultralow SO2That discharges is semidry-method recirculating fluidized bed
Flue gas desulphurization system.
Background technique
The flue gas desulfurization technique that coal fired power plant uses mainly includes wet desulphurization, dry desulfurization and three kinds of semi-dry desulphurization.
Wherein, Wet Flue Gas Desulfurization Technique desulfuration efficiency is high, but needs biggish capital investment and water consumption is big.In order to reduce the consumption of desulfurization
Water, Summary of Semi-dry Flue Gas Desulfurization come into being.Circulating Fluidized Bed Flue Gas Desulfurization Technology is to develop the last century 80's
A kind of Summary of Semi-dry Flue Gas Desulfurization come, the basic principle is that: flue gas enters from absorb the bottom of the tower, after through enturi tube acceleration
Into absorbent tower body section, gas-particle two-phase generates strong turbulence under airflow function, then makes flue gas and calcium-based desulfurizing agent
It is able to contact and desulphurization reaction occurs.
Stack gas desulfurization system of circulating fluid bed structure is simple, water consumption is small, is very suitable to the insufficient national conditions of China's water resource,
It is one of the research and development of power environment protection industry technology and the focus technology promoted and applied.But traditional circulating fluid bed flue-gas desulfurizing
There is also certain deficiencies to lead to the utilization of desulfurizing agent since residence time of the calcium-based desulfurizing agent in absorption tower is inadequate for system
Rate is low, and desulfurization effect is bad.With the continuous improvement of environmental requirement, SO2Discharge standard it is higher and higher, how to improve desulfurizing agent
Utilization rate, improve the desulfurization effect of flue gas, be current technical problem urgently to be solved.
Summary of the invention
For solution, sorbent utilization is low in the prior art, the bad problem of desulfurization effect, and the present invention proposes a kind of ultralow
SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge.
The technical scheme of the present invention is realized as follows:
A kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, including three-level absorption tower, atomized water spray
Mouth, niter ash cellar, the first returning charge machine, the second returning charge machine, deduster, cinder tank and chimney；
Three-level absorption tower includes the first order absorption tower, second level absorption tower and third level absorption tower being vertically arranged, and first
The top on grade absorption tower is connected with the top on second level absorption tower, the bottom end on second level absorption tower and the bottom end on third level absorption tower
It is connected, the bottom on first order absorption tower is equipped with gas inlet, and the top on third level absorption tower is equipped with exhanst gas outlet,
It is anti-that the first Venturi tube fluidisation section, the first divergent segment and first are disposed in first order absorption tower from lower to upper
Main paragraph is answered, atomizing water nozzle is set in the first divergent segment, and the first return port and calcium hydroxide import are provided on the first divergent segment；
The second Venturi tube fluidisation section, the second divergent segment and the second reaction are disposed in third absorption tower from lower to upper
Main paragraph is provided with the second return port on the second divergent segment；
Niter ash cellar is connect by calcium hydroxide import with first order absorption tower, second level absorption tower and third level absorption tower
Bottom end junction is connect by the first returning charge machine with the first return port；Deduster one end is connect with exhanst gas outlet, the other end and cigarette
Chimney connection, the bottom of deduster are set there are two outlet, and one outlet is connect by the second returning charge machine with the second return port, another
Outlet is connect with cinder tank.
It preferably, further include air-introduced machine, deduster is connect by air-introduced machine with chimney.
It is further preferred that the first returning charge machine and the second returning charge machine are spiral returning charge machine.
Compared with prior art, the present invention extends hydrated lime particle on absorption tower by adding deduster and returning charge machine
In residence time, then extend the time of contact of flue gas and hydrated lime particle, improve the utilization efficiency of hydrated lime particle
And desulfuration efficiency.Simultaneously as using tower circulation, the total height on absorption tower is reduced.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention without any creative labor, may be used also for those of ordinary skill in the art
To obtain other drawings based on these drawings.
Fig. 1 is the structural diagram of the present invention.
In figure: 1, three-level absorption tower；11, first order absorption tower；111, the first Venturi tube fluidizes section；112, calcium hydroxide into
Mouthful；113, the first return port；114, the first divergent segment；12, second level absorption tower；13, third level absorption tower；131, the second literary mound
In pipe fluidize section；132, the second return port；133, the second divergent segment；14, gas inlet；15, exhanst gas outlet；2, niter ash cellar；
3, the first returning charge machine；4, the second returning charge machine；5, deduster；6, cinder tank；7, air-introduced machine；8, chimney；9, atomizing water nozzle.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
A kind of ultralow SO as shown in Figure 1:2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, including three-level absorb
Tower 1, atomizing water nozzle 9, niter ash cellar 2, the first returning charge machine 3, the second returning charge machine 4, deduster 5, cinder tank 6 and chimney 8；
Three-level absorption tower 1 includes first order absorption tower 11, second level absorption tower 12 and the third level absorption tower being vertically arranged
13, the top on first order absorption tower 11 is connected with the top on second level absorption tower 12, the bottom end on second level absorption tower 12 and third
The bottom end on grade absorption tower 13 is connected, and the bottom on first order absorption tower 11 is equipped with gas inlet 14, the top on third level absorption tower 13
Equipped with exhanst gas outlet 15,
The first Venturi tube fluidisation section 111, the first divergent segment 114 are disposed in first order absorption tower 11 from lower to upper
With the first reactive agent section, atomizing water nozzle 9 is set in the first divergent segment 114, is provided with the first returning charge on the first divergent segment 114
Mouth 132 and calcium hydroxide import 112；
The second Venturi tube fluidisation section 131,133 and of the second divergent segment are disposed in third absorption tower 13 from lower to upper
Second reactive agent section is provided with the second return port 132 on the second divergent segment 133；
Niter ash cellar 2 is connect by calcium hydroxide import 112 with first order absorption tower 11, second level absorption tower 12 and the third level
The bottom end junction on absorption tower 13 is connect by the first returning charge machine 3 with the first return port 113；5 one end of deduster and exhanst gas outlet
15 connections, the other end connect with chimney 8, and the bottom of deduster 5 is set there are two outlet, one outlet pass through the second returning charge machine 4 and
The connection of second return port 132, another outlet is connect with cinder tank 6.
Working principle: flue gas enters from gas inlet 14, enters after the first Venturi tube fluidisation section 111 accelerates upper
Row.The calcium hydroxide stored in niter ash cellar 2 enters first order absorption tower 11 by calcium hydroxide import 112, flue gas after acceleration with
Hydrated lime particle is sufficiently mixed, on the one hand the atomized water then sprayed into from atomizing water nozzle 9 increases the humidity of hydrated lime particle,
Another aspect cooled flue gas, so that flue-gas temperature is kept above 15~25 DEG C of flue gas dew point, to allow calcium hydroxide and SO2Complete from
Subtype desulphurization reaction.Flue gas carries part hydrated lime particle, and on 11 top of first order absorption tower, turning enters second level absorption tower
12 top downlinks.In 12 lower part of second level absorption tower, turning enters 13 lower part of third level absorption tower, herein due to gravity, centrifugal force
Effect has a large amount of particle to deposit, and the first returning charge machine 3 being arranged herein can be by the complete hydrated lime particle of unreacted through first
Return port 113 is transmitted back in first order absorption tower 11 that the reaction was continued.Flue gas continues through the second literary mound on third level absorption tower 13
In pipe fluidisation section 131 accelerate after enter uplink, from 13 top of the third level absorption tower outflow enter deduster 5 in.Consolidating in flue gas
Body particle is trapped by deduster 5, wherein the hydrated lime particle and desulfuration byproduct that do not react completely containing some, flying
Ash etc..A part in these solid particles is transmitted back to third by the second returning charge machine 4 via the one outlet of 5 lower part of deduster
In grade absorption tower 13, another part is exported from another to be sent into the storage of cinder tank 6, transports.The clean flue gas come out from deduster 5
It is discharged from chimney 8.
Compared with prior art, the invention has the following beneficial effects:
1, it is additionally arranged deduster and returning charge machine, residence time of the hydrated lime particle in absorption tower is extended, then extends
The time of contact of flue gas and hydrated lime particle, improve the utilization efficiency and desulfuration efficiency of hydrated lime particle；
2, using three-level absorption tower, tower circulation carries out sulphur removal, reduces the total height on absorption tower.
As a kind of perferred technical scheme, one more embodiment of the present invention further includes air-introduced machine 7, and deduster 5 is by drawing
Blower 7 is connect with chimney 8, and the clean flue gas come out from deduster 11 is discharged by air-introduced machine 13 from chimney 8.
As a kind of perferred technical scheme, another embodiment of the present invention, the first returning charge machine 3 and the second returning charge machine 4 are
For spiral returning charge machine.When spiral returning charge machine loopback solid particle, revolving speed should be ensured that gas will not play a reversed role.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (3)
1. a kind of ultralow SO2The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, it is characterised in that: including three-level absorption tower
(1), atomizing water nozzle (9), niter ash cellar (2), the first returning charge machine (3), the second returning charge machine (4), deduster (5), cinder tank (6)
And chimney (8)；
Three-level absorption tower (1) includes that the first order absorption tower (11), second level absorption tower (12) and the third level being vertically arranged absorb
The top of tower (13), first order absorption tower (11) is connected with the top of second level absorption tower (12), second level absorption tower (12)
Bottom end is connected with the bottom end of third level absorption tower (13), and the bottom of first order absorption tower (11) is equipped with gas inlet (14), third
The top on grade absorption tower (13) is equipped with exhanst gas outlet (15),
The first Venturi tube fluidisation section (111), the first divergent segment are disposed in first order absorption tower (11) from lower to upper
(114) it is set in the first divergent segment (114) with the first reactive agent section, atomizing water nozzle (9), the first divergent segment is set on (114)
It is equipped with the first return port (132) and calcium hydroxide import (112)；
The second Venturi tube fluidisation section (131), the second divergent segment (133) are disposed in third absorption tower (13) from lower to upper
With the second reactive agent section, the second return port (132) are provided on the second divergent segment (133)；
Niter ash cellar (2) is connect by calcium hydroxide import (112) with first order absorption tower (11), and second level absorption tower (12) and the
The bottom end junction on three-level absorption tower (13) is connect by the first returning charge machine (3) with the first return port (113)；Deduster (5) one
End connect with exhanst gas outlet (15), the other end is connect with chimney (8), the bottom of deduster (5) set there are two export, described in one
Outlet is connect by the second returning charge machine (4) with the second return port (132), another described outlet is connect with cinder tank (6).
2. ultralow SO according to claim 12The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, it is characterised in that:
It further include air-introduced machine (7), deduster (5) is connect by air-introduced machine (7) with chimney (8).
3. ultralow SO according to claim 22The semidry-method recirculating fluidized bed flue gas desulphurization system of discharge, it is characterised in that:
First returning charge machine (3) and the second returning charge machine (4) are spiral returning charge machine.
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 true CN109304080A (en) | 2019-02-05 |
| CN109304080B CN109304080B (en) | 2024-01-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201810307169.XA Active CN109304080B (en) | 2018-04-08 | 2018-04-08 | Ultralow SO 2 Exhaust semi-dry circulating fluidized bed flue gas desulfurization system |
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Cited By (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 |
| CN110368799A (en) * | 2019-07-30 | 2019-10-25 | 福建龙净脱硫脱硝工程有限公司 | A kind of semidry process desulfurizer and method |
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| 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 |
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| US20160089631A1 (en) * | 2013-10-15 | 2016-03-31 | Institute Of Process Engineering, Chinese Academy Of Sciences | Combined desulfuration, denitration, and demercuration apparatus and method using semi-dry process in circulating fluidized 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 |
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| 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 |
| US20160089631A1 (en) * | 2013-10-15 | 2016-03-31 | Institute Of Process Engineering, Chinese Academy Of Sciences | Combined desulfuration, denitration, and demercuration apparatus and method using semi-dry process in circulating fluidized bed |
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Cited By (3)
| 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 |
| CN110368799A (en) * | 2019-07-30 | 2019-10-25 | 福建龙净脱硫脱硝工程有限公司 | A kind of semidry process desulfurizer and method |
| 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 |
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| Publication number | Publication date |
|---|---|
| CN109304080B (en) | 2024-01-05 |
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