CN1167450A - Method for seperating gaseous pollutants from hot process gases - Google Patents
Method for seperating gaseous pollutants from hot process gases Download PDFInfo
- Publication number
- CN1167450A CN1167450A CN95196504A CN95196504A CN1167450A CN 1167450 A CN1167450 A CN 1167450A CN 95196504 A CN95196504 A CN 95196504A CN 95196504 A CN95196504 A CN 95196504A CN 1167450 A CN1167450 A CN 1167450A
- Authority
- CN
- China
- Prior art keywords
- blender
- dust
- gas
- deduster
- process gas
- 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.)
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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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D53/81—Solid phase processes
Abstract
Hot process gases are passed through a contact reactor (10), in which a particulate absorbent material, which is reactive with gaseous pollutants in the gases, is introduced into the gases to convert the gaseous pollutants into separable dust. The process gases are then passed through a dust separator (5). The major part of the dust separated in the dust separator (5) is passed to a mixer (11), in which it is mixed and moistened, whereupon it is recirculated as absorbent material by being introduced, together with fresh absorbent, into the process gases. Burnt lime is added as fresh absorbent. The dust is kept so long in the mixer and recirculated so many times that the total residence time of the burnt lime in the mixer in moistened state is sufficiently long for the burnt lime to react substantially completely with water supplied to the mixer and form slaked lime.
Description
The present invention relates to from thermal process gas, as divided gas flow pollutant in the flue gas, method as sulfur dioxide, in the method, process gas is by a contact reactor, join under moisture state at this particulate absorbent material that a kind of and gas pollutant are reacted and to make gas pollutant change into separable dust in the process gas, process gas is isolated dust by a deduster from process gas subsequently, purifies the back process gas and discharges from deduster.The isolated a part of dust of deduster is sent in the blender, mixed and add water-wet, send in the process gas with the fresh absorbent gas circulation of adding as absorber material subsequently.
Above-mentioned from thermal process gas the method for divided gas flow pollutant can from Swedish patent 8504675-3 and Swedish patent 8904106-5, recognize.According to these two parts of files, preferably use granular calcium hydroxide (calcium hydroxide) as fresh absorbent.With this absorbent with in dedusting gas device in the process gas isolated mix dust, in mixed material, add water subsequently, under moisture state, send in the flue gas of contact reactor.Because the calcium hydroxide cost is more expensive, thereby, use more cheap quick lime (calcium oxide) to replace calcium hydroxide to carry out all gases experiment.In these experiments, must use a device earlier with quicklime slaking, promptly joining before the purification process, with calcium oxide and water reaction generation calcium hydroxide.A kind of like this lime slaking device is expensive, can not look to profit when this means with quick lime replacement calcium hydroxide.
The purpose of this invention is to provide a kind of from thermal process gas the method for divided gas flow pollutant, can use quick lime to replace calcium hydroxide, and not need costliness, independent quicklime slaking device.
According to the present invention, this purpose is to realize by class methods of being introduced in the preamble, it is characterized in that adding quick lime as fresh absorbent, the isolated most of dust of deduster is supplied with blender in the mode of continuous-flow basically and from blender, discharge, long-time stop of dust and circulation are repeatedly in blender, quick lime in the blender keeps sufficiently long total residence time under moisture state, quick lime and the water of supplying with blender are reacted basically fully and generate calcium hydroxide.Fresh absorbent is preferably supplied with blender with the quick lime form, but also can join in that part of dust of the isolated supply blender of deduster.Another kind of way is that quick lime is directly joined in the flue gas of contact reactor.
Suitably to blender air supply stream, so that incite somebody to action mixing dust fluidization wherein and improve this mixture.
With reference now to a burning central heating device, effluent gas purification equipment signal accompanying drawing elaborates the present invention, and this purifier has been equipped with the equipment that the method according to this invention purifies.
This figure has illustrated to illustrate the effluent gas purification equipment of a burning central heating device 1, contains dust in the said flue gas, as the gentle body pollution thing of flying dust, as sulfur dioxide.A preheating device 2 is set is used for the heat transferred air blast 3 of high-temperature flue gas is sent into through pipeline 2a the combustion air of central heating device 1.Hot flue gas is conveyed into deduster 5 through pipeline 4, and illustrated in embodiments is an electrostatic precipitator that three continuous deduster unit are housed.Flue gas is purified through these deduster unit.Flue gas after being purified enters flue gas air blast 7 through pipeline 6 by this way, is discharged in the atmosphere after pipeline 8 is sent into chimney 9.This deduster also can be a kind of bag filter.
Pipeline 4 has a vertical portion to divide formation contact reactor 10.Blender 11 is connected with the lower end of contact reactor 10.Blender 11 is sent to the particulate absorbent material that gas pollutant in a kind of and the flue gas reacts in the flue gas of contact reactor 10 lower ends under moisture state.This absorber material is converted into dust with gas pollutant, and the latter is separated in deduster 5.
Isolated dust granules is collected in the hopper 12 of deduster unit in the deduster 5.The major part of collected dust granules circulates in system in the mode that describes in detail below.The remaining dust granules of collecting will not add the mode of detailed description by adopting, and for example use a spiral/conveyer to transport.
Blender 11 is one type that is introduced among the Swedish patent 9404104-3.Thereby blender 11 is the boxed-section shape of double bottom basically.One chamber 14 was arranged between the two-layer end, and the polyester material cloth 13 that its upper strata is used by the confession fluidisation of tension constitutes, and the air that is used for fluidisation blender 11 particulate absorbent materials is sent into chamber through air conduit 15.Water enters blender 11 through water supply conduit 16 and the nozzle 17 that is installed in the blender top.The granular materials that need to mix enters blender 11 through two material inlets 18 and 19 that are located at the mixer entrance end.In addition, blender 11 is equipped with a mechanical mixture device 20, and its agitator by two synergies, gas arranged side by side is formed (only drawing one among the figure), and each agitator has a horizontal drive shaft, and the elliptical flat-plate leaf of a plurality of inclinations is housed above.The exit gas end of blender 11 puts in the contact reactor 10, so that supply with mixed uniformly wetting absorber material continuously through overflow pipe 21.
The part that the dust granules of collecting in the hopper 12 of deduster unit need circulate in system is sent into blender 11 through inlet tube 19.Particle quick lime (calcium oxide) is supplied with blender 11 through inlet tube 18 and is mixed mutually with the dust granules of sending into through inlet tube 19.The mixed material water-wet of sending into through nozzle 17.The water that nozzle 17 is sent into also is used for digesting the quick lime of sending into blender 11.Because the fluidization of the material particles of this structure of mechanical mixture device 20 and supply blender 11, blender has produced even wetting, mixed uniformly material particles, and its overflow pipe 21 through blender 11 is supplied with contact reactor 10 continuously as absorber material.The time of staying of material particles is about 5～60S in blender 11, particularly 10～20S.
The time of staying of material particles in the above-mentioned blender 11 (10～20S), that is to say that lime particle is in moisture state in this time, quick lime does not have time enough and digests the water complete reaction that adds and generate calcium hydroxide.The digestion reaction of lime is slow, spend time a few minutes.
Now the present invention is carried out more detailed explanation by following theoretical example.This example has illustrated A, B and C point in the drawings respectively, i.e. the inlet of the deduster 5 at conduit 4 places of blender 11 fronts, in blender 11 subsequent reactor 10 and at the dominance condition in the exit of deduster 5.
A B C
Gas flow (Nm
3/ h) 100,000 103,993 103,993
Gas temperature (℃) 125 65 65
SO
2Concentration (ppm) 1,150 280 172
Dust concentration (g/Nm
3) 20 1,000＜0.03
At A point dust is flying dust basically, and is flying dust and absorber material at B point dust.At the D point, per hour discharge 2, the 930kg dust, wherein 2,000kg is a flying dust.
In this example, the particulate absorbent material comprises the quick lime that digesting about 35 times (1.0 * 103,933/2,930 ≈ 35) that on average circulated system before the D point is discharged.Therefore, the total residence time of absorber material is 350～700S in the blender 11, that is to say about 6～12min, and chien shih quicklime slaking when enough is arranged.
Total water consumption is 3,366 1/h in the above-mentioned example, 152 1/h is wherein arranged for lime slaking.When these water were consumed, the water content of the absorber material of discharging from blender 11 was approximately 6%.But water content can suitably change in 2～15% scopes according to the composition of mixed material.
In above-mentioned example, if fly ash content is zero in A point flue gas, promptly when D point dust discharge rate is 930kg/h, analogize by above-mentioned situation, cycle-index is about (0.980 * 103,993/930 ≈ 110) 110 times, and then to cause the time of staying be 1100～2200S, promptly about 18～37min.
Claims (5)
1. one kind from thermal process gas, as divided gas flow pollutant in the flue gas, method as sulfur dioxide, process gas is through a contact reactor (10) in the method, in this contact reactor, the particulate absorbent material that a kind of and gas pollutant react joins under moisture state in the process gas and gas pollutant to be changed into separable dust, process gas is through deduster (5) subsequently, at this dust is isolated from process gas, the process gas that purifies is discharged from deduster, the isolated a part of dust of deduster (5) is sent in the blender (11), dust is through mixing and add water-wet in this blender, circulate with the fresh absorbent of adding as absorber material subsequently and join in the process gas, this method is characterised in that the fresh absorbent of adding is a quick lime, and isolated most of dust is supplied with blender (11) in the mode of continuous-flow basically and discharge from blender (11) in the deduster (5), dust in blender long-time stop and circulation repeatedly so that the total residence time of quick lime under moisture state looked and is enough to make quick lime and the water of supplying with blender complete reaction and generate calcium hydroxide basically in the blender (11).
2. the method that requires according to claim 1 is characterized in that fresh absorbent is with quick lime form supply blender (11).
3. the method that requires according to claim 1, it is isolated and supply with that part of dust of blender (11) from deduster (5) to it is characterized in that fresh absorbent joins with the quick lime form.
4. the method that requires according to claim 1 is characterized in that fresh absorbent directly joins in the flue gas in the contact reactor (10) with the quick lime form.
5. the method for any one in requiring according to aforesaid right is characterized in that supplying with blender (11) air stream so that make wherein mixing dust fluidisation.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE9404105A SE504440C2 (en) | 1994-11-28 | 1994-11-28 | Ways to separate gaseous pollutants from hot process gases |
| SE9404105-0 | 1994-11-28 | ||
| SE94041050 | 1994-11-28 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1167450A true CN1167450A (en) | 1997-12-10 |
| CN1080137C CN1080137C (en) | 2002-03-06 |
Family
ID=20396125
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95196504A Expired - Lifetime CN1080137C (en) | 1994-11-28 | 1995-11-24 | Method for seperating gaseous pollutants from hot process gases |
Country Status (20)
| Country | Link |
|---|---|
| EP (1) | EP0804273A1 (en) |
| JP (1) | JP3640674B2 (en) |
| KR (1) | KR100384589B1 (en) |
| CN (1) | CN1080137C (en) |
| AU (1) | AU692014B2 (en) |
| BR (1) | BR9509831A (en) |
| CZ (1) | CZ157497A3 (en) |
| EE (1) | EE04049B1 (en) |
| FI (1) | FI972233A0 (en) |
| HU (1) | HU220402B (en) |
| MD (1) | MD1020C2 (en) |
| PL (1) | PL320426A1 (en) |
| RO (1) | RO115421B1 (en) |
| RU (1) | RU2147919C1 (en) |
| SE (1) | SE504440C2 (en) |
| SI (1) | SI9520141A (en) |
| SK (1) | SK66197A3 (en) |
| UA (1) | UA52592C2 (en) |
| WO (1) | WO1996016722A1 (en) |
| ZA (1) | ZA959876B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101513589B (en) * | 2009-03-03 | 2011-07-20 | 桑德环境资源股份有限公司 | Method and device for purification of flue gases by semidry process |
| CN104667734A (en) * | 2013-11-26 | 2015-06-03 | 阿尔斯通技术有限公司 | Dry scrubber system with low load distributor device |
| CN111032192A (en) * | 2017-09-06 | 2020-04-17 | 勒瓦研究开发股份有限公司 | Method for treating flue gas in CDS flue gas treatment |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT404565B (en) * | 1997-06-05 | 1998-12-28 | Scheuch Alois Gmbh | METHOD FOR PURIFYING POLLUTANT-GASES |
| SE514592C2 (en) | 1998-05-18 | 2001-03-19 | Flaekt Ab | Method and apparatus for flue gas purification with extinguishing lime in immediate connection with flue gas purification |
| SE512227C2 (en) * | 1998-06-24 | 2000-02-14 | Flaekt Ab | Ways to clean flue gases during the start-up of a boiler |
| US6290921B1 (en) * | 1999-11-03 | 2001-09-18 | Foster Wheeler Enegeria Oy | Method and apparatus for binding pollutants in flue gas |
| SE523667C2 (en) | 2002-09-20 | 2004-05-11 | Alstom Switzerland Ltd | Method and apparatus for separating gaseous pollutants from hot gases by particulate absorbent material and mixer for wetting the absorbent material |
| EP1815903B1 (en) | 2006-02-06 | 2008-08-06 | ALSTOM Technology Ltd | Method and device for controlling the absorption of gaseous pollutants from hot process gases |
| EP1875953B2 (en) | 2006-07-04 | 2015-01-21 | Alstom Technology Ltd | Method and system for the separation of gaseous pollutants from hot process gases |
| AT504426B8 (en) * | 2006-10-24 | 2008-09-15 | Scheuch Gmbh | APPARATUS FOR MOISTURIZING A SORPTION AGENT |
| US7766997B2 (en) | 2007-12-21 | 2010-08-03 | Alstom Technology Ltd | Method of reducing an amount of mercury in a flue gas |
| US7850936B2 (en) | 2008-02-18 | 2010-12-14 | Alstom Technology Ltd | Dry sulfur dioxide (SO2) scrubbing |
| US8192529B2 (en) * | 2009-03-10 | 2012-06-05 | Gatton Jr Lawrence H | Integrated dry scrubber system |
| ES2593812T3 (en) | 2010-11-24 | 2016-12-13 | General Electric Technology Gmbh | Method of purifying a combustion gas rich in carbon dioxide and a boiler system |
| US8728211B2 (en) | 2012-03-30 | 2014-05-20 | Alstom Technology Ltd | Nozzle for spraying liquid and a mixer comprising the nozzle |
| US9457366B2 (en) | 2012-07-13 | 2016-10-04 | General Electric Technology Gmbh | Spray lance arrangement |
| US8663586B1 (en) | 2012-08-07 | 2014-03-04 | Alstom Technology Ltd | High performance mercury capture |
| US8906333B1 (en) * | 2013-11-27 | 2014-12-09 | Alstom Technology Ltd | Dry scrubber system with air preheater protection |
| CN105617851B (en) * | 2016-03-16 | 2018-08-28 | 中国科学院城市环境研究所 | A kind of method and its device of efficient double tower semi-dry desulphurization |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3308927A1 (en) | 1983-03-12 | 1984-09-13 | L. & C. Steinmüller GmbH, 5270 Gummersbach | Process for binding gaseous pollutants contained in flue gases |
| SE453570B (en) * | 1985-10-09 | 1988-02-15 | Flaekt Ab | Plant for sepg. acid components from gas mixt. |
| SE458095B (en) * | 1986-06-27 | 1989-02-27 | Flaekt Ab | Sepn. system for pollutants from gas-form medium |
| FI76931B (en) * | 1986-12-12 | 1988-09-30 | Imatran Voima Oy | FOERFARANDE FOER RENING AV ROEKGASER. |
| JP3035015B2 (en) * | 1991-08-13 | 2000-04-17 | 三菱重工業株式会社 | Desulfurization method |
-
1994
- 1994-11-28 SE SE9404105A patent/SE504440C2/en not_active IP Right Cessation
-
1995
- 1995-11-21 ZA ZA959876A patent/ZA959876B/en unknown
- 1995-11-24 SI SI9520141A patent/SI9520141A/en not_active IP Right Cessation
- 1995-11-24 RO RO97-00951A patent/RO115421B1/en unknown
- 1995-11-24 BR BR9509831A patent/BR9509831A/en not_active IP Right Cessation
- 1995-11-24 AU AU41264/96A patent/AU692014B2/en not_active Ceased
- 1995-11-24 WO PCT/SE1995/001403 patent/WO1996016722A1/en active IP Right Grant
- 1995-11-24 EP EP95939455A patent/EP0804273A1/en not_active Withdrawn
- 1995-11-24 PL PL95320426A patent/PL320426A1/en unknown
- 1995-11-24 UA UA97063196A patent/UA52592C2/en unknown
- 1995-11-24 SK SK661-97A patent/SK66197A3/en unknown
- 1995-11-24 CN CN95196504A patent/CN1080137C/en not_active Expired - Lifetime
- 1995-11-24 HU HU9800501A patent/HU220402B/en not_active IP Right Cessation
- 1995-11-24 MD MD97-0166A patent/MD1020C2/en unknown
- 1995-11-24 CZ CZ971574A patent/CZ157497A3/en unknown
- 1995-11-24 RU RU97111848A patent/RU2147919C1/en not_active IP Right Cessation
- 1995-11-24 JP JP51717096A patent/JP3640674B2/en not_active Expired - Lifetime
- 1995-11-24 KR KR1019970703389A patent/KR100384589B1/en not_active IP Right Cessation
- 1995-11-24 EE EE9700215A patent/EE04049B1/en not_active IP Right Cessation
-
1997
- 1997-05-27 FI FI972233A patent/FI972233A0/en not_active IP Right Cessation
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101513589B (en) * | 2009-03-03 | 2011-07-20 | 桑德环境资源股份有限公司 | Method and device for purification of flue gases by semidry process |
| CN104667734A (en) * | 2013-11-26 | 2015-06-03 | 阿尔斯通技术有限公司 | Dry scrubber system with low load distributor device |
| CN111032192A (en) * | 2017-09-06 | 2020-04-17 | 勒瓦研究开发股份有限公司 | Method for treating flue gas in CDS flue gas treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| SE504440C2 (en) | 1997-02-10 |
| CZ157497A3 (en) | 1997-11-12 |
| SE9404105D0 (en) | 1994-11-28 |
| WO1996016722A1 (en) | 1996-06-06 |
| JPH10509914A (en) | 1998-09-29 |
| PL320426A1 (en) | 1997-09-29 |
| EE04049B1 (en) | 2003-06-16 |
| RU2147919C1 (en) | 2000-04-27 |
| JP3640674B2 (en) | 2005-04-20 |
| SK66197A3 (en) | 1997-10-08 |
| SI9520141A (en) | 1997-10-31 |
| ZA959876B (en) | 1996-07-15 |
| RO115421B1 (en) | 2000-02-28 |
| HU220402B (en) | 2002-01-28 |
| AU692014B2 (en) | 1998-05-28 |
| BR9509831A (en) | 1997-09-30 |
| FI972233A (en) | 1997-05-27 |
| MD1020C2 (en) | 1999-07-31 |
| CN1080137C (en) | 2002-03-06 |
| EP0804273A1 (en) | 1997-11-05 |
| SE9404105L (en) | 1996-05-29 |
| AU4126496A (en) | 1996-06-19 |
| EE9700215A (en) | 1998-02-16 |
| HUT77637A (en) | 1998-06-29 |
| UA52592C2 (en) | 2003-01-15 |
| KR100384589B1 (en) | 2003-08-21 |
| FI972233A0 (en) | 1997-05-27 |
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| C14 | Grant of patent or utility model | ||
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| ASS | Succession or assignment of patent right |
Owner name: ABB NORTON HOLDINGS LTD. Free format text: FORMER OWNER: ABB TECHNOLOGY FLB AB Effective date: 20130125 Owner name: ABB PARTICIPATION LTD. Free format text: FORMER OWNER: ABB NORTON HOLDINGS LTD. Effective date: 20130125 Owner name: ALSTOM TECHNOLOGY LTD. Free format text: FORMER OWNER: ABB NORTON HOLDINGS LTD. Effective date: 20130125 |
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Owner name: ABB TECHNOLOGY FLB AB Free format text: FORMER NAME: ABB FLAKT AB Owner name: ABB NORTON HOLDINGS LTD. Free format text: FORMER NAME: ABB PARTICIPATION LTD. |
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| CP01 | Change in the name or title of a patent holder |
Address after: Swedish Weiss Dreas Patentee after: ABB Norton Holdings Ltd. Address before: Swedish Weiss Dreas Patentee before: ABB equity holdings Ltd. Address after: Stockholm Patentee after: ABB TECHNOLOGY FLB AB Address before: Stockholm Patentee before: ABB FLAKT AB |
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| TR01 | Transfer of patent right |
Effective date of registration: 20130125 Address after: Baden, Switzerland Patentee after: ALSTOM TECHNOLOGY Ltd. Address before: Swedish Weiss Dreas Patentee before: ABB Norton Holdings Ltd. Effective date of registration: 20130125 Address after: Swedish Weiss Dreas Patentee after: ABB equity holdings Ltd. Address before: Sweden Sollentuna Patentee before: ABB Norton Holdings Ltd. Effective date of registration: 20130125 Address after: Sweden Sollentuna Patentee after: ABB Norton Holdings Ltd. Address before: Stockholm Patentee before: ABB Technology FLB AB |
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