CN101262929B - Sulfur trioxide removal from a flue gas stream - Google Patents
Sulfur trioxide removal from a flue gas stream Download PDFInfo
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- CN101262929B CN101262929B CN200680033934.9A CN200680033934A CN101262929B CN 101262929 B CN101262929 B CN 101262929B CN 200680033934 A CN200680033934 A CN 200680033934A CN 101262929 B CN101262929 B CN 101262929B
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- flue gas
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- 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
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Abstract
A method of removing SO3 from a flue gas stream having increased amounts of SO3 formed by a NOx removal system, includes injecting a sorbent composition into the flue gas stream. The sorbent composition includes an additive and a sodium sorbent such as mechanically refined trona or sodium bicarbonate. The additive is selected magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide, and mixtures thereof. The concentration of the SO3 in the flue gas stream is reduced and the formation of a liquid phase NaHSO4 reaction product is minimized.
Description
Technical field
The present invention relates to gas cleaning, and relate more specifically to a kind of purification and contain for example SO of pernicious gas
3The method of flue gas.
Background technology
SO
3It is the pernicious gas that the sulfurous fuels burning produces.Work as SO
3When being present in the flue gas, can form acid mist, the condensation in precipitator, pipeline or dust storage chamber of described acid mist causes corrosion.Concentration is low to moderate the SO of 5～10ppm in the waste gas
3Also can in atmosphere, produce white, purple or black feathering than cooling in the cold air owing to hot flue gases.
Reduce the NO of coal-fired power plant by selective catalytic reactor (selective catalytic reactor, SCR)
xThe effort of discharging has caused the SO that does not expect
2Be oxidized to SO
3Thereby so that SO
3The result that increases of total discharging.Adding NH
3Situation under, SCR utilizes catalyst (typically being vanadium pentoxide) with NO
xBe converted into N
2And H
2O, but also undesirably with SO
2Be oxidized to SO
3Although SO
3This higher flue concentration remain relatively low, its discharging produces the secondary feathering of highly-visible sometimes, although this secondary feathering is irregular, but it still can produce many problems.Make great efforts to reduce SO
3Level is to can't see secondary SO
3The degree of feathering, this may hinder the collection of particle for the situation that adopts precipitator (electrostatic precipitator, ESP).SO in the flue gas
3Be adsorbed onto on the fly ash granule, and reduced the resistivity of flying dust, thereby make ESP catch particle by the static facility.In the practice, SO sprays in some factories when ash content resistivity is too high
3To reduce the resistivity of flying dust.
In the flue gas duct of coal-fired plant, SO
3With steam reaction and formation H
2SO
4Steam.Part in these steam condenses in air heater baskets.If the temperature of pipeline is excessively low, another part sulfuric acid vapor may condensation in pipeline, thus corrosion pipeline.All the other acid vapors are in feathering condensation during quenching with the contact of relative cold atmosphere, perhaps condensation in the quench zone at washer when using wet scrubber to carry out flue gas desulfurization (flue gas desulfurization, FGD).The cooling acid vapor produces thin acid mist fast in the FGD tower.Drop is usually too tiny, to such an extent as to be adsorbed in the FGD tower, perhaps is trapped in the demister.Therefore, the FGD tower is to SO
3Removal only be limited.If the sulfuric acid level of discharging from flue is enough high, secondary feathering will appear.
Utilized dry sorbent injection (dry sorbent injection, DSI) to adopt multiple absorbent to come from flue gas, to remove SO
3With other gas.But because equipment and materials, for example the dust storage chamber medium can not bear higher temperature, therefore in the past usually is being lower than about 370
Under carry out DSI.In addition, many sorbent materials are being higher than about 400
Temperature under sintering or fusing, this renders a service it when removing gas lower.Another problem is that the product of many sorbent materials adheres on the e-quipment and pipe under specific temperature and gas concentration condition, and this needs continually cleaning procedure equipment.
Summary of the invention
On the one hand, provide a kind of from containing by NO
xThe SO of the recruitment that the system of removing forms
3Flue gas stream in remove SO
3Method, comprise absorbent composition is ejected in the described flue gas stream.Described absorbent composition comprises additive and sodium absorbent, and described sodium absorbent is trona or the sodium acid carbonate of machine finish for example.Additive is selected from magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture.Reduced SO in the flue gas stream
3Concentration, and so that liquid phase NaHSO
4The formation of product minimizes.
On the other hand, provide a kind of method of carrying dry absorbent to be used for flue gas injection, comprise providing trona.By making described trona and the additive combination that is selected from magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture form absorbent composition.Described absorbent composition in the container is transported to the flue gas injection place.From described container, unload described absorbent composition, and it is ejected in the described flue gas stream.Make additive and the described trona of q.s make up to improve the flowability that described absorbent composition flows out from described container.
Aforementioned paragraphs provides as general the introduction, is not the scope that is intended to limit claims.By also understanding well the preferred embodiments of the invention and other advantages by reference to the accompanying drawings with reference to following detailed description.
Description of drawings
Fig. 1 is for showing trona and SO
3Product as effluent gas temperature and SO
3The phasor of the function of concentration.
Fig. 2 is the schematic diagram of an embodiment of FGD system.
Describe the present invention with reference to the accompanying drawings, wherein identical part represents by identical Reference numeral.Understand better relation and the function of the different parts of the present invention by following detailed description.But the present invention's embodiment as described below only is for for example, and the invention is not restricted to the embodiment shown in the accompanying drawing.
Dry sorbent injection (DSI) is as removing SO
3Spray-drying or the low-cost replacement scheme of wet scrubbing system.In the DSI method, store absorbent and with its dry-type jetting in flue, react at absorbent described in the flue and sour gas.Under some process conditions, the product of absorbent and sour gas is sticky ash.Sticky ash adheres on process equipment and the pipeline easily, thereby needs frequent clean.Therefore, adopt so that the minimized technique of the amount of sticky ash product is favourable.
Can be used for removing SO
3A kind of concrete absorbent be trona.Trona is a kind of 85～95% concentrated crystal soda (Na that have an appointment that contain
2CO
3NaHCO
32H
2O) mineral.A large amount of mineral trona mineral deposits has been found near the green river place in the west and south in the Wyoming State.Used term " trona " comprises other sources of sodium sesquicarbonate in this article.Operable another kind of absorbent is sodium acid carbonate.Term " flue gas " comprises from any type combustion process waste gas of (comprising coal, oil, natural gas etc.).Flue gas generally includes for example SO of sour gas
2, HCl, SO
3And NO
x
When 275
Or heating is during concentrated crystal soda under the higher temperature, and the contained sodium acid carbonate quick burning of concentrated crystal soda is sodium carbonate, shown in following reaction:
2[Na
2CO
3·NaHCO
3·2H
2O]→3Na
2CO
3+5H
2O+CO
2
Absorbent composition and SO
3Preferred chemical reaction as follows:
Na
2CO
3+SO
3→Na
2SO
4+CO
2
But under given conditions, the reaction that can occur not expect produces niter cake.If concentrated crystal soda with SO
3Following reaction not exclusively then occurs in calcining before the reaction:
NaHCO
3+SO
3→NaHSO
4+SO
3
Under given conditions, the reaction of not expecting in addition produces niter cake, and is as follows:
Na
2CO
3+SO
3+H
2SO
4→2NaHSO
4+CO
2
Niter cake is the low acid salt of melt temperature, and it is at high temperature unstable, presses reaction decomposes shown in the following formula:
2NaHSO
4→Na
2S
2O
7
Na
2CO
3With SO
3The type of product depend on SO
3Concentration and the temperature of flue gas.Fig. 1 is for showing trona and SO
3Typical reaction product and effluent gas temperature and SO
3The phasor of the functional relation of concentration.Particularly, at specific SO
3Under the concentration conditions, depend on the temperature of flue gas, product can be solid state N aHSO
4, liquid NaHSO
4, Na
2SO
4Or Na
2S
2O
7
Liquid NaHSO
4Do not expect especially, because it is " viscosity ", adhere on the process equipment easily, and so that other particles for example flying dust also adhere on the equipment.Therefore, wish so that liquid NaHSO
4The described technique of operation under the minimized condition of the amount of product.Among Fig. 1 370
More than, liquid NaHSO
4With solid state N a
2SO
4The line of demarcation can use equation " log[SO
3]=0.009135T-2.456 " expression, wherein [SO
3] be SO
3Ppm concentration denary logarithm, T be flue gas temperature (with
Meter).Therefore, about 370
To about 525
Temperature under, with at SO
3Concentration be higher than " log[SO
3]=0.009135T-2.456 " when spraying trona in the flue gas in the situation of determined amount, form liquid phase NaHSO
4Product.
Have been found that and use the absorbent composition comprise machine finish trona and additive so that the amount of the sticky ash that forms in the described method minimizes.Can replace trona with sodium acid carbonate.Additive is selected from magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and composition thereof.Additive preferably includes magnesium carbonate, calcium carbonate or its mixture, most preferably comprises calcium carbonate.Additive is preferably 0.1% to 5% of trona or other sodium absorbent weight, most preferably is 0.5% to 2%.Absorbent composition is ejected in the flue gas stream.Keep absorbent composition to contact time enough with flue gas so that partially absorb the agent composition and part SO
3Reaction, thus SO in the flue gas stream reduced
3Concentration.Preferably, so that liquid phase NaHSO
4The formation of product minimizes, thereby so that does not almost have sticky ash to form.Although do not want to be subject to theory, think additive and the H that is present in the flue gas stream
2SO
4Reaction is to remove H from flue gas stream
2SO
4, thus so that liquid phase NaHSO
4Generation minimize.
Therefore, can when not having additive, can form liquid phase NaHSO
4Temperature and SO
3Operating said system in the concentration range.In one embodiment, the effluent gas temperature at injection trona place is about 370
To about 500
The temperature of flue gas preferably is higher than about 370
, more preferably be higher than about 385
The temperature of flue gas preferably is lower than about 500
, more preferably less than about 450
, most preferably be lower than about 415
Effluent gas temperature most preferably is about 385
To about 415
Scheme as an alternative, temperature range can be expressed as SO
3The function of concentration.Therefore, can be at temperature and SO
3Concentration meets " log[SO
3]＞0.009135T-2.456 " condition under implement described method, wherein [SO
3] be SO
3Ppm concentration, T be flue gas temperature (with
Meter).
The SO of pending flue gas stream
3Concentration more generally is that about 10ppm is to about 200ppm usually at least about 3ppm.The outlet SO of desirable gas stack
3Concentration preferably is lower than about 50ppm, more preferably less than about 20ppm, more preferably less than about 10ppm, most preferably is lower than about 5ppm.Collect the accessory substance of reaction with flying dust.
Trona is similar to most alkaline reagent, tend at first with air-flow in react more rapidly than strong acid, then after staying for some time, react with weaker acid.Such as HCl and SO
3This class gas component be strong acid, trona and these sour reaction speeds than with weak acid SO for example
2Reaction speed faster.Therefore, the compound of reaction that sprays can be used for selectively removing the SO in the flue gas stream
3, and basically do not reduce SO
2Amount.
Fig. 2 shows the schematic diagram of an embodiment of described method.Give stove or burner 10 source 12 that fuels, for example then coal is provided with air 14 with combustion fuel source 12.Burning gases are guided to heat exchanger or air heater 30 from burner 10.Can spray surrounding air 32 to reduce effluent gas temperature.Can use SCR (selective catalytic reduction, SCR) equipment 20 to remove NO
x Gas.Bypass valve 22 can open to shunt the flue gas that SCR produces.The outlet of heat exchanger or air heater 30 is connected with particle collection device 50.Be directed to optional wet scrubber 54, then be gas stack 60 with before discharging that in flue gas particle collection device 50 is removed the particle that forms in the combustion process, for example flying dust from flue gas.Particle collection device 50 can be precipitator (ESP).The particle collection device of other types for example dust storage chamber also can be used for removing solid.Dust storage chamber comprises for the filter of isolating the particle that produces the combustion process from flue gas.
SO
3The system of removing comprises source of sorbent composition 40.Absorbent composition comprises additive and sodium absorbent, for example trona or concentrated crystal soda.The sodium absorbent is preferably trona.Preferably take average grain diameter as about 10 microns to about 40 microns, most preferably from about 24 microns forms to about 28 microns particles provide trona.The average grain diameter of additive usually can be with trona roughly the same, be preferably about 10 microns to about 25 microns.Absorbent composition is preferably dried particle form.
Suitable source of trona is T-200
Trona, it is the machine finish natural alkali mine product that can derive from Solvay Chemicals.T-200
Trona contains 97.5% the concentrated crystal soda of having an appointment, and average grain diameter is about 24-28 micron.This system can also comprise the grinding machine of ball mill pulverizer or other types, for reducing and/or the particle diameter of control trona or other absorbent compositions.
Have been found that additive is joined the flowability that can improve described trona in the trona.The method of carrying dry absorbent to be used for flue gas injection comprises makes additive and trona make up to form absorbent composition.Additive can be magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and composition thereof.Absorbent composition in the container is transported to the flue gas injection place.From described container, unload described absorbent composition, and it is ejected in the described flue gas stream, wherein so that the additive of q.s and trona make up to improve the flowability of the described absorbent composition in the described container.
Absorbent composition is transported to injector 42 from source of sorbent composition 40.Can pneumaticly transport absorbent composition or transport absorbent composition by other appropriate method arbitrarily.As shown in Figure 2, injector 42 is directed to flue gas duct section 44 with absorbent composition, and this flue gas duct section 44 is arranged on the upstream position of dust storage chamber entrance, and preferably is arranged on the downstream position of heat exchanger outlet.Preferably spraying system is designed to so that the SO in absorbent composition and the flue gas stream
3Contact maximization.Can use any type injection apparatus well known in the prior art that absorbent composition is guided in the gas pipeline.For example, can use the injector of compressed air-driven directly to finish injection.
If store absorbent composition and with its dried being sprayed onto in its flue 44 that reacts with sour gas, then the method does not need slurry equipment or reaction vessel.But the method also can be used with the humidification of flue gas or the wet shotcrete technology of absorbent composition.In addition, if the method is used for the cleaning washing of acid mist, then can pass through wet scrubber 54 wet type collecting granules.Particularly, can operate FGD system, so that realize SO in the flue gas by absorbent composition is ejected into
3Removal, remove most of SO by wet scrubber 54 simultaneously
2
Also can change the method with the control effluent gas temperature.For example, can regulate the effluent gas temperature of trona or other sodium absorbent upstreams to obtain the effluent gas temperature at desirable injection absorbent composition place.In addition, surrounding air 32 can be incorporated in the flue gas stream to reduce the temperature of flue gas, and spray absorbent composition place monitoring effluent gas temperature.Other methods that can be used for controlling effluent gas temperature comprise uses heat exchanger and/or aerial cooler.The method can also change the trona eject position or comprise a plurality of absorbent composition eject positions.
In order to realize desulfurization, preferably with respect to SO
3The certain flow of flow is sprayed absorbent composition, to provide about 1.0 or larger sodium and the normalizing stoichiometric proportion (normalizedstoichiometric ratio, NSR) of sulphur.NSR is amount the measuring with respect to the amount that needs in theory of institute's reagent injected.NSR represents the stoichiometry with the required absorbent of whole acid gas reactions.For example, 1.0 NSR means to have sprayed is enough in theory 100% SO that removes in the gas approach gas
3Material; 0.5 NSR remove in theory 50% SO
3SO
3With the reaction of sodium carbonate very rapidly and efficiently, therefore only be about 1 NSR and normally remove SO
3Needed.Preferential and the SO of absorbent composition
3Rather than SO
2Therefore reaction even there is a large amount of SO
2Exist, still can remove SO
3Preferably, adopt to be lower than 2.0 NSR, perhaps more preferably adopt to be lower than 1.5 NSR, so that the SO in the flue gas
2Can be owing to reacting the remarkable reduction that causes concentration with excessive absorbent.
Because NO
xThe system of removing is easily with the SO that exists
2Be oxidized to SO
3, so described spraying system is all right and NO
xThe system of removing is combined.Described trona injection system can also with such as other the SO such as sodium acid carbonate, lime, lime stone
xThe system of removing is combined, to improve performance or to remove other pernicious gases for example HCl, NO
xDeng.
The specific embodiment
In generating equipment, adopt hot side precipitator (ESP) and do not use dust storage chamber.Described equipment uses removes NO
xCatalyst, cause the SO in the flue gas
3Level raises.SO in the flue gas
3Concentration be about 100ppm about 125ppm extremely.Injection is from the T-200 of Solvay Chemicals
Trona is to remove SO from flue gas
3
Embodiment does not use additive, 400 as a comparison
NSR value with about 1.5 is sprayed trona.ESP perforated plate in this equipment shows obvious solid accumulation, needs frequent clean.
400
The absorbent composition that NSR value with about 1.5 will contain trona and 1% calcium carbonate is ejected in the flue gas.At operation SO
3After removing system, the ESP perforated plate in this equipment does not have the solid accumulation comparatively speaking.
With under the same process condition, use trona but do not use the method for additive to compare, additive used according to the invention has reduced SO
3Remove the amount of cohesive waste in the technique.
Illustrative and nonrestrictive with embodiment shown in this article as mentioned above.Scope of the present invention represents by claim rather than aforementioned description and accompanying drawing.The present invention can be presented as other particular forms and not deviate from spirit of the present invention.Therefore, these and any other change in the claim scope all are intended to be contained in the scope of the present invention.
Claims (37)
1. one kind from containing by NO
xThe SO of the recruitment that the system of removing forms
3Flue gas in remove SO
3Method, described method comprises absorbent composition is ejected in the described flue gas to reduce SO in the described flue gas
3Concentration and make liquid phase NaHSO
4The formation of product minimizes, described absorbent composition comprises sodium absorbent and additive, wherein said sodium absorbent is selected from trona, sodium acid carbonate and its mixture of machine finish, and described additive is selected from magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture
Wherein said additive is 0.1% to 5% of described trona weight.
2. method claimed in claim 1, the temperature of wherein said flue gas is 370 °F to 500 °F.
3. method claimed in claim 1, the temperature of wherein said flue gas is 385 °F to 450 °F.
4. method claimed in claim 1, wherein said additive is 0.5% to 2% of described trona weight.
5. method claimed in claim 1, wherein said additive is selected from magnesium carbonate, calcium carbonate and composition thereof.
6. method claimed in claim 1, wherein said additive package contains calcium carbonate.
7. method claimed in claim 1, wherein in the upstream of spraying described absorbent composition place, described flue gas comprises at least SO of 3ppm
3
8. method claimed in claim 1, wherein in the upstream of spraying described absorbent composition place, described flue gas comprises the SO of 10ppm to 200ppm
3
9. method claimed in claim 1, wherein said sodium absorbent comprise average grain diameter less than 40 microns described trona.
10. it is 24 microns to 28 microns described trona that method claimed in claim 1, wherein said sodium absorbent comprise average grain diameter.
11. method claimed in claim 1, wherein said absorbent composition sprays with the dry form.
12. method claimed in claim 1, wherein said SO
3Concentration greater than equation log[SO
3The determined amount of]＞0.009135T-2.456, wherein T in °F the temperature of flue gas, SO
3Be ppm concentration.
13. one kind from containing by NO
xThe SO of the recruitment that the system of removing forms
3Flue gas in remove SO
3Method, described method comprises:
● absorbent composition is provided, and described absorbent composition comprises the trona of machine finish and is selected from the additive of magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture;
● described absorbent composition is ejected in the described flue gas, and the temperature of wherein said flue gas is greater than 370 °F and less than 450 °F; With
● keep described absorbent composition to contact time enough with described flue gas, so that partially absorb agent composition and part SO
3Reaction, thus SO in the flue gas reduced
3Concentration and make liquid phase NaHSO
4The formation of product minimizes,
Wherein said additive is 0.1% to 5% of described trona weight.
14. the described method of claim 13, wherein said additive are 0.5% to 2% of described trona weight.
15. the described method of claim 13, wherein said additive is selected from magnesium carbonate, calcium carbonate and composition thereof.
16. the described method of claim 13, wherein said additive package contains calcium carbonate.
17. the described method of claim 13, the average grain diameter of wherein said additive are 20 microns to 25 microns.
18. the described method of claim 13, wherein in the upstream of spraying described absorbent composition place, described flue gas comprises at least SO of 3ppm
3
19. the described method of claim 13, wherein in the upstream of spraying described absorbent composition place, described flue gas comprises the SO of 10ppm to 200ppm
3
20. the described method of claim 13, wherein said SO
3Concentration greater than equation log[SO
3The determined amount of]＞0.009135T-2.456, wherein T in °F the temperature of flue gas, SO
3Be ppm concentration.
21. the described method of claim 13, the average grain diameter of wherein said trona are 10 microns to 40 microns.
22. the described method of claim 13, the temperature of wherein said flue gas are 385 °F to 415 °F.
23. the described method of claim 13 is wherein with respect to SO
3The certain flow of flow is sprayed described absorbent composition, so that 1.0～1.5 sodium and the normalizing stoichiometric proportion of sulphur to be provided.
24. the described method of claim 13, wherein said absorbent composition sprays with the dry form.
25. the described method of claim 13 also is included in described absorbent composition is transported to described flue gas position before with described additive and the combination of described trona.
26. one kind from comprising 3ppm to 200ppm SO
3Flue gas in remove SO
3Method, described method comprises:
● absorbent composition is provided, and described absorbent composition comprises trona and is selected from the additive of magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture; With
● described absorbent composition is ejected in the flue gas, and the temperature of wherein said flue gas is 370 °F to 450 °F,
Wherein said additive is 0.5% to 2% of described trona weight.
27. the described method of claim 26, wherein said additive is selected from magnesium carbonate, calcium carbonate and composition thereof.
28. the described method of claim 26, wherein the average grain diameter of trona is 24 microns to 28 microns.
29. the described method of claim 26, the temperature of wherein said flue gas are 385 °F to 415 °F.
30. the described method of claim 26, wherein said SO
3Concentration greater than equation log[SO
3The determined amount of]＞0.009135T-2.456, wherein T in °F the temperature of flue gas, SO
3Be ppm concentration.
31. a method of carrying dried absorbent to be used for flue gas injection comprises:
● trona is provided;
● to form absorbent composition, described additive is selected from magnesium carbonate, calcium carbonate, magnesium hydroxide, calcium hydroxide and its mixture with described trona and additive combination;
● the described absorbent composition in the container is transported to the flue gas injection place;
● from described container, unload described absorbent composition, and described absorbent composition be ejected in the described flue gas, wherein make the additive of q.s and described trona make up to improve the flowability that described absorbent composition flows out from described container,
Wherein said additive is 0.1% to 5% of described trona weight.
32. the described method of claim 31, wherein said additive are 0.5% to 2% of described trona weight.
33. the described method of claim 31, wherein said additive is selected from magnesium carbonate, calcium carbonate and composition thereof.
34. the described method of claim 31, wherein said additive package contains calcium carbonate.
35. the described method of claim 31, the average grain diameter of wherein said trona is less than 40 microns.
36. the described method of claim 31, the average grain diameter of wherein said trona are 24 microns to 28 microns.
37. the described method of claim 31, the average grain diameter of wherein said additive are 20 microns to 25 microns.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US22905605A | 2005-09-15 | 2005-09-15 | |
| US11/229,056 | 2005-09-15 | ||
| PCT/EP2006/066359 WO2007031552A1 (en) | 2005-09-15 | 2006-09-14 | Sulfur trioxide removal from a flue gas stream |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101262929A CN101262929A (en) | 2008-09-10 |
| CN101262929B true CN101262929B (en) | 2013-01-09 |
Family
ID=37311371
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200680033934.9A Active CN101262929B (en) | 2005-09-15 | 2006-09-14 | Sulfur trioxide removal from a flue gas stream |
Country Status (7)
| Country | Link |
|---|---|
| EP (1) | EP1937391A1 (en) |
| JP (1) | JP2009507632A (en) |
| CN (1) | CN101262929B (en) |
| BR (1) | BRPI0616068A2 (en) |
| CA (1) | CA2622549C (en) |
| EA (1) | EA015416B1 (en) |
| WO (1) | WO2007031552A1 (en) |
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| US7531154B2 (en) | 2005-08-18 | 2009-05-12 | Solvay Chemicals | Method of removing sulfur dioxide from a flue gas stream |
| KR101099073B1 (en) * | 2008-12-04 | 2011-12-26 | 주식회사 유니코정밀화학 | Composition for removing sox in exhausted gas |
| IT1401506B1 (en) * | 2010-08-03 | 2013-07-26 | Icico S R L | SORBENT COMPOSITION IN POWDER TO PURGE A GASEOUS EFFLUENT AND ITS USE |
| CN102527324A (en) * | 2012-01-05 | 2012-07-04 | 张泉 | Porous adsorbing material with health care function and preparation method of porous adsorbing material |
| KR101388179B1 (en) | 2012-05-03 | 2014-04-22 | 주식회사 유니코정밀화학 | COMPOSITION FOR REMOVING SOx IN EXHAUSTED GAS AND METHOD FOR REMOVING SOx IN EXHAUSTED GAS |
| JP6254012B2 (en) * | 2014-02-24 | 2017-12-27 | 三菱日立パワーシステムズ株式会社 | Exhaust gas treatment system and exhaust gas treatment method |
| CN105344326B (en) * | 2015-11-09 | 2018-03-16 | 建德丽园环保科技有限公司 | A kind of preparation method of ultra-fine sodium acid carbonate gas cleaning medicament |
| US20180361316A1 (en) * | 2015-12-14 | 2018-12-20 | Carmeuse Research And Technology | Powdered compostion comprising one or more double salt(s) for use in combustion gas purification |
| EP3187244A1 (en) | 2015-12-30 | 2017-07-05 | Lhoist Recherche et Développement S.A. | Composition for the purification of flue gas |
| EP3187243A1 (en) * | 2015-12-30 | 2017-07-05 | Lhoist Recherche et Développement S.A. | Composition for the purification of flue gas |
| CN105477995B (en) * | 2016-01-18 | 2019-03-19 | 北京清新环境技术股份有限公司 | A kind of method of sulfur trioxide in removing coal-fired flue-gas |
| JP7360378B2 (en) * | 2017-09-06 | 2023-10-12 | エス．ア．ロイスト ルシェルシュ エ デヴロップマン | Method of treating exhaust gas in CDS exhaust gas treatment |
| CN110170241B (en) * | 2019-06-27 | 2021-08-24 | 上海交通大学 | Method for inhibiting generation of sulfur trioxide in heavy non-ferrous metal smelting acid-making flue gas |
| CN111318142A (en) * | 2020-02-20 | 2020-06-23 | 中国神华能源股份有限公司国华电力分公司 | Sulfur trioxide removing device for coal combustion system |
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| CN86108162A (en) * | 1985-11-29 | 1988-06-08 | 通用电气公司 | The method of washing sulfur oxide and nitrogen oxide in the flue gas conduit |
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| JP2002263441A (en) * | 2001-03-12 | 2002-09-17 | Mitsubishi Heavy Ind Ltd | Blue smoke generation preventive equipment |
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- 2006-09-14 CA CA2622549A patent/CA2622549C/en not_active Expired - Fee Related
- 2006-09-14 WO PCT/EP2006/066359 patent/WO2007031552A1/en active Application Filing
- 2006-09-14 EA EA200800829A patent/EA015416B1/en not_active IP Right Cessation
- 2006-09-14 JP JP2008530530A patent/JP2009507632A/en not_active Ceased
- 2006-09-14 EP EP06793512A patent/EP1937391A1/en not_active Withdrawn
- 2006-09-14 BR BRPI0616068-9A patent/BRPI0616068A2/en not_active IP Right Cessation
- 2006-09-14 CN CN200680033934.9A patent/CN101262929B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0170355A2 (en) * | 1984-05-29 | 1986-02-05 | Ets, Inc. | Emission control process for combustion flue gases |
| CN86108162A (en) * | 1985-11-29 | 1988-06-08 | 通用电气公司 | The method of washing sulfur oxide and nitrogen oxide in the flue gas conduit |
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| Title |
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| JP昭63-175652A 1988.07.20 |
Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0616068A2 (en) | 2011-06-07 |
| EA015416B1 (en) | 2011-08-30 |
| EP1937391A1 (en) | 2008-07-02 |
| CN101262929A (en) | 2008-09-10 |
| EA200800829A1 (en) | 2008-08-29 |
| JP2009507632A (en) | 2009-02-26 |
| CA2622549C (en) | 2014-07-29 |
| CA2622549A1 (en) | 2007-03-22 |
| WO2007031552A1 (en) | 2007-03-22 |
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