CN1052261A - The purification method of flue gas and equipment - Google Patents
The purification method of flue gas and equipment Download PDFInfo
- Publication number
- CN1052261A CN1052261A CN90109921A CN90109921A CN1052261A CN 1052261 A CN1052261 A CN 1052261A CN 90109921 A CN90109921 A CN 90109921A CN 90109921 A CN90109921 A CN 90109921A CN 1052261 A CN1052261 A CN 1052261A
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- venturi
- gas
- particle
- pollutant
- carrier 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
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Biomedical Technology (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The method of gas pollutant in the process for purifying gas, gas contacts with absorbent, reacts to make it to be converted into separable particulate pollutant.Superabsorbent particles is dispersed in the carrier gas, quicken carrier gas and particle wherein, contact with pressurized fluid stream, liquid stream is finely dispersed in particle surface before particle is sent into process gas, use the equipment of this method, comprise: the space that process gas contacts with absorbent (5) make superabsorbent particles be dispersed in device (20) in the carrier gas.This device links to each other with placing the Venturi (6) in it, it have quicken carrier gas and wherein particle the convergent inlet part, be configured in the inlet part downstream and pressurized fluid stream supplied with carrier gas and be accelerated and weep sub inlet opening and carrier gas and humidification particle are sent into the exit portion of space (5).
Description
The present invention relates to contain the purification method and the equipment such as the process gas of flue gas of gas pollutant, described gas pollutant such as sulfur dioxide, sulfur trioxide, hydrogen chloride and hydrogen fluoride, the method is by contacting with this gas with the absorbent of for example lime of gas pollutant reaction, making these pollutants be converted into separable particulate pollutant.
The sour gas that discharges from for example coal-burning power plant is (as SO
2) become great environmental problem.For reducing the discharging of this pollutant, several diverse ways had been tested.
For this purpose, proposed purifying fuel, in burning, taken measures and purify the methods such as flue gas of generation.Some pollutant such as nitrogen oxide can dissolve and generate harmless object.Optimize combustion process and also may offset its effect owing to generating pollutant.But only can be and processed, and inaccurately discharge with uncontrollable mode in any form as residual product as other material of sulphur.For removing desulfuration, generally add absorbent.This absorbent contains the material that can generate stable compound with sulphur, and it can add in the combustion chamber or special-purpose flue gas cleaning system.
Generally levigate or slightly thick pulverous lime stone or dolomite are added in the combustion chamber.Usually add levigate lime stone or calcium hydroxide water slurry for flue gas cleaning system.Also the someone proposes to send into dried absorbent in flue gas.But most of absorbents cheap and easy to get reactivity under low temperature and low temperature is all very low, the effect of using the technology of dried absorbent to be difficult to obtain.
Be the example of some prior aries below.SE-8005571-8 has described sorbent injection and has gone into the combustion chamber, DE-36,07,357 have described the wet cleaning of flue gas, and SE-7904382-4 has described the wet clean of flue gas, EP-0,177,896 absolutely dry purification and the SE-8505269-4 that introduced flue gas have introduced comprehensive solution.
The major defect that absorbent is sent into the combustion chamber is that the utilization rate of absorbent is very low.The wet washing tower of flue gas is much effective in this respect, but investment cost is high and the need maintenance.
Wet-clean investment cost of flue gas can reduce, and compares the selected absorbent of needs but beat flue gas wet washing tower, thereby has improved the price of absorbent.For avoiding moisture to condense in flue gas, in wet-dry process, the dispersion or the water yield that infeeds absorbent that suspends are lacked to being lower than the water yield required below the saturation temperature than cooling stack gas.Because the absorbent that suspends must be sent in the flue gas with the form of fine water droplet, so that form the evaporation fully that big evaporating surface is enough to guarantee institute's output, so suspension can not be made than finely divided allow thicker.Like this, the absorbed dose of radiation of the amount of liquid of supply and therefore adding just is subjected to the quantitative limitation of flue gas thermal capacitance.
The investment cost of absolutely dry method that is used for flue gas cleaning system is minimum, but usually needs selected thereby expensive absorbent, and can not carry out senior purification.Its main cause is that solid phase reaction is very slow under the common temperature that keeps behind the coal-burning boiler.
For the senior purification that utilizes simple flue gas cleaning system, promptly this system does not comprise generation, conveying and finely divided adsorbent water slurry device, has proposed several technology, is characterized between dry method and wet-dry process.
For example, SE-7908674-0 suggestion, before flue gas was sent into the topped bag hose that calcium hydroxide dirt cake arranged, other added the humidification of a pair of flue gas.SE-8504675-3 then points out another kind of scheme: absorbent is first water humidification before sending into flue gas.But it is the water yield that powder type allowed that amount of water must be not more than the maintenance absorbent.In addition, can not absorbent be entered flue gas with the screw feeder shown in the figure.But according to existing environmental standard, described these technology all can not reach the effective purification to flue gas.
The problem of a needs solution has proposed, and promptly needs to provide a kind of the gas pollutant such as sulfur dioxide in the flue gas is reached satisfied separation, and do not use the method for absorbent aqueous suspensions.
Therefore, one object of the present invention just provide a kind of from flue gas for example the effective straightforward procedure of divided gas flow pollutant, the method needn't infeed the aqueous suspensions of absorbent in dusty gas.
Another object of the present invention provides a kind of simple device that uses the method.
According to the present invention, solved the problems referred to above, promptly provide a kind of method of satisfaction from the process gas of for example flue gas, to separate for example gas pollutant of sulfur dioxide.The present invention makes in a kind of carrier gas that can be dispersed in air for example with the particulate absorbent of for example lime of gas pollutant reaction, quicken described carrier gas and dispersion superabsorbent particles wherein, with under high speed, contacting of continuing with a kind of pressurized fluid stream of for example water, contact with process gas so that before wherein pollutant was converted into separable particulate pollutant, liquid stream was finely dispersed in the surface of described particle at particle.
Because in carrier gas and disperse wherein particle, be accelerated at a high speed, so on particle surface, just obtained very finely divided liquid and flow with before pressurized fluid stream contact.Because this absorbent is made up of the thin high reaction activity particle through humidification, thereby reacts with regard to the gas pollutant in very fast and the gas, and these gas pollutants are converted into separable particulate pollutant by absorption process when contacting with flue gas.
Carrier gas and dispersion humidification particle wherein are decelerated before being preferably in and sending into process gas.
The flow quantity of supplying with carrier gas preferably should make for liquid to the mass ratio that is scattered in the superabsorbent particles in the carrier gas in the scope of 0.1-10, particularly about 0.5.
For the gas pollutant in the separating technology gas according to the method described above, be provided with one superabsorbent particles is dispersed in as the device in the carrier gas of air, make this device for example make with one that the process gas of flue gas links to each other with the contacted space of the particulate absorbent of for example lime.Process gas contains gas pollutant, and particulate absorbent can these gas pollutant reactions.This device places the Venturi in described space to link to each other with at least one.This Venturi has: convergent inlet part that is used for quickening carrier gas and disperses particle wherein, the pressurized fluid stream of water for example of being suitable for that at least one is configured in the inlet part downstream are supplied with described carrier gas and are disperseed the inlet opening of the particle that is accelerated wherein and be used for carrier gas and disperse wherein humidification particle to supply with the exit portion in described space.
The venturi of Venturi preferably has constant sectional area, promptly constant hydraulics internal diameter.
The exit portion of Venturi can be a flaring, with in carrier gas and disperse they to be slowed down before wherein humidification particle sends into process gas.The inlet opening of Venturi is arranged on exit portion, best downstream near venturi.
The exit portion of Venturi also can have constant sectional area, and the inlet opening of Venturi can be arranged in the venturi, best upstream near exit portion.
The cross section of Venturi is preferably circular, and the inlet opening of Venturi can be configured in the inner surface of flaring exit portion symmetrically or be configured in the inner surface of venturi symmetrically, and be in the perpendicular plane of the symmetry axis of described Venturi in.
Each inlet opening forms the mouth of a feed tube, and preferably the symmetry axis angulation scope of its center line and Venturi is 10 °-80, particularly 45 °.
Narrate the present invention in more detail below with reference to accompanying drawing.
Fig. 1 is the system schematic that a cover purifies the flue gas of spontaneous combustion coal center boiler, and this cover flue gas cleaning system comprises according to an equipment of the present invention.
Fig. 2 is the detail drawing of a present device part among Fig. 1.
Fig. 3 is the detail drawing of the another embodiment of this part among Fig. 2.
The flue gas that generates during center boiler 1 fire coal shown in Figure 1 imports the air preheater 2 that is suitable for the heat of flue gas is passed to combustion air, and combustion air is that mat air blast 3 is sent into the center boiler via pipeline 2a.
Flue gas is not carried out the pre-separation of flying dust and is imported in the elongated tubular reactor 5 via pipeline 4 then.Flue gas is mixed with the absorbent of gas pollutant reaction in energy and the flue gas in reactor 5.Absorbent is to see Fig. 2 or 3 via the Venturi 6(that is positioned at reactor lower part) send into reactor with the particulate forms of thin humidification.How these particles produce, and will further describe in this specification back part.
In tubular reactor 5, superabsorbent particles is mixed with flue gas effectively, the water capacity of supplying with particle is evaporated when contacting with flue gas, simultaneously owing to gas pollutant and these particles as sulfur dioxide in the flue gas reacts, thereby is converted into particulate pollutant.Because be with respect to the temperature of flue gas select the water capacity of confession, so flue gas is not cooled to below the saturation temperature, so just can avoid condensing of moisture.
Because the sectional area of tubular reactor 5 is identical with pipeline 4 roughly, therefore its speed can obviously not reduce when flue gas importing tubular reactor.Flue gas just can keep sufficiently high speed, also be entrained in the particulate pollutant that generates in the reaction than the flying dust in heavy particle, unreacted superabsorbent particles and the flue gas, to a precipitator 7 that is positioned at the tubular reactor downstream.In depositor, isolate the particle in the flue gas, the flue gas of having removed particle and gas pollutant feeds flue gas blower 9 via pipeline 8.Air blast 9 enters chimney 11 with peace and quiet flue gas via pipeline 10 and is discharged in the atmosphere.
The particle collection of telling in depositor is in three laying dust buckets 12,13 and 14 that the depositor bottom forms.Be collected in the particle in the first dirt bucket 12, account for 90% of dirt total amount, be sent in the recycle tank 16 via pipeline 15.The particle that is collected in dirt bucket 13 and 14 then is sent to a storage tank (not shown) via pipeline 17 in addition.
Be stored in isolated particle in the circulating slot 16 in pipeline 19 be stored in groove 18 in fresh, do superabsorbent particles (preferably calcium hydroxide) and mix mutually.Determine to send into the amount of the fresh absorbent of pipeline 19 with the method for routine, promptly measure the discharge capacity of the residual contaminants in the pipeline 8 behind the depositor from groove 18.Determine to send into the amount of the recirculation absorbing material of pipeline 19 according to the amount of the fresh absorbing material of sending into, under a certain load, just can in tubular reactor 5, supply with the absorbing material of constant number like this.
Air blast or compressor 20 are supplied with fresh airs to pipeline 19 under the pressure of about 0.5 crust, this air can make the fresh superabsorbent particles and the mix particles of recirculation, and with these particles with the form feeder that disperses in the Venturi of pipeline 19 upper ends 6.
In the embodiment shown in Fig. 2, Venturi 6 is formed by the annular section 21 and 22 that connects in the nut 23 by two.First 21 installs the upper end at pipeline 19 regularly, it is included in a length of upstream extremity between 40 and 90 millimeters, usually about 60 millimeters, internal diameter is between 40 and 120 millimeters, usually about 80 millimeters, convergent inlet part 21a, and internal diameter is constant and be situated between between 20 and 60 millimeters, usually about 40 millimeters venturi part 21b.Second portion 22 also comprises a venturi part 22a with venturi part 21b same inner diameter, it forms a length between 20 and 40 millimeters with venturi part 21b, about 30 millimeters usually, venturi, with in length of downstream between 20 and 80 millimeters, usually about 30 millimeters and internal diameter be between 30 and 80 millimeters, usually about 50 millimeters flaring exit portion 22b.Venturi part 22a has a toroidal cavity 24, and penstock 25 is introduced in its upper shed.
When air flows to the tapered portion 21a of Venturi with dispersion superabsorbent particles wherein, before air and particle inflow venturi 21b and 22a, promptly be accelerated in the velocity interval of 70-150 meter per second, particularly 100 meter per seconds.When air passed through inlet opening 27, it just with via pipeline 25, cavity 24, feed tube 26 and inlet opening 27 sent into Venturi inside, had been pressurized to the current contact of about 15 crust.This will cause ultra-fine dispersion of current height and cracked form with very little water droplet to stick to the surface of superabsorbent particles.Though this moment, absorbent contained certain moisture so that it has high reaction activity, adsorbent still keeps form of powder.The superabsorbent particles of this humidification is just sent into tubular reactor 5(via flaring exit portion 22b then and is seen Fig. 1).
Because in the flaring exit portion is to form feed tube like this, the center line that is feed tube becomes about 45 (see figure 2) also owing to their inlet opening is out in the downstream near venturi part 22a with the symmetry axis of Venturi, therefore can avoid water to be injected in the inside of Venturi, therefore also just can not pile up thereon has grit.Flying dust also can play with grit piles up opposite effect, and flying dust is present in the absorbing material of recirculation, and they contain the oxide of aluminium and silicon, thereby can play the effect of abrasive.
In the embodiment depicted in fig. 3, Venturi 6 is made up of two annular sections 31 and 32.First 31 installs the upper end at pipeline 19 regularly, it is included in a length of upstream extremity between 40 and 90 millimeters, usually about 60 millimeters, internal diameter is between 40 to 120 millimeters, usually about 80 millimeters convergent inlet part 31a and internal diameter is constant and between 20 and 60 millimeters, about 40 millimeters venturi part 31b usually.Second portion 32 also comprises a venturi part 32a with venturi part 31b same inner diameter, it forms a length between 20 and 60 millimeters with venturi part 31b, common about 40 millimeters venturi, and in length of downstream between 1 and 5 millimeter, usually about 2 millimeters and internal diameter is constant and between 20 and 60 millimeters, about 40 millimeters exit portion 32b usually.Venturi part 32a has a toroidal cavity 34, and penstock 35 is introduced in its upper shed.Cavity 34 communicates with the inside of Venturi by 4 feed tubes 36, and the inlet opening 37 of feed tube is configured in the inner surface of venturi part 32a symmetrically, and near the upstream of exit portion 32b.At venturi part 32a is to form feed tube like this, and promptly the center line of feed tube becomes about 45 with the symmetry axis of Venturi.
Be shown in the embodiment of the Venturi 6 of Fig. 3, its function and Venturi shown in Figure 2 are basic identical, and just the superabsorbent particles of humidification is before sending into tubular reactor 5, and the exit portion at a flaring is not decelerated.
Embodiment
Temperature is 166 ℃ of flow velocity 11 meter per seconds and 1020 milligrams/mark of content of sulfur dioxide rice
3Flue gas stream with 4900 mark rice
3/ hour infeed in the tubular reactor of 16 meters of 0.5 meter of a diameter and length.Therefore the time of staying of flue gas in reactor be about 1.6 seconds.The humidification absorbent of sending into tubular reactor hourly is made up of the dirt and 240 premium on currency of 7 kilograms of calcium hydroxides, 483 kilograms of circulations, and the water of adding therefore equals 0.49 to the mass ratio of absorbent.Saturation temperature in the tubular reactor equals 52 ℃.
In the downstream of precipitator, content of sulfur dioxide adds up to 95 milligrams/mark rice
3, 75 ℃ of temperature.The moisture content of isolated dirt is a 0.8%(weight in depositor).Purifying rate to sulfur dioxide is 91%.
Certainly, the invention is not restricted to above-mentioned embodiment, and can in the scope of the application's claim, make conversion in every way.
For example, available several (as 4) Venturi replaces single Venturi.But they all should be configured in identical height in the reactor, to avoid spraying mutually the danger of dirt.
Again for example, the circular cross-section of Venturi also can be used the square-section instead.
Claims (10)
1, contain for example purification method of the process gas of for example flue gas of gas pollutant such as sulfur dioxide, described gas contacts with a kind of particulate absorbent of for example lime, this kind absorbent and the reaction of described gas pollutant, make described pollutant be converted into separable particulate pollutant, the particle of absorbent is dispersed in a kind of carrier gas of for example air, it is characterized in that, the particle that quickens described carrier gas and wherein disperse, with under high speed, contacting of continuing with a kind of pressurized fluid stream of for example water, before particle was sent into described process gas, liquid stream was finely dispersed in the surface of described particle.
2,, it is characterized in that described carrier gas and the humidification particle that wherein disperses were decelerated before sending into described process gas according to the method for claim 1.
3, according to the method for claim 1 or 2, the flow quantity that it is characterized in that supplying with described carrier gas should make for liquid to the mass ratio of superabsorbent particles in the scope of 0.1-10, particularly about 0.5.
4, use the equipment of claim 1 method, this equipment comprises: contain the space (5) that the process gas of for example flue gas of gas pollutant contacts with a kind of particulate absorbent of for example lime, this kind absorbent and the reaction of described gas pollutant make described pollutant be converted into separable particulate pollutant; With make superabsorbent particles be dispersed in device in the carrier gas of air for example, it is characterized in that described device and at least one place the Venturi (6) in the described space (5) to link to each other, this Venturi has a convergent inlet part (21a who quickens described carrier gas and disperse particle wherein; 31a), at least one be configured in the inlet part downstream be suitable for will be for example the pressurized fluid stream of water supply with described carrier gas and disperse the inlet opening of accelerated particle wherein and with described carrier gas and disperse wherein humidification particle to supply with the exit portion (22b of described space (5); 32b).
5, according to the equipment of claim 4, it is characterized in that described Venturi (6) form a venturi with constant sectional area (21b, 22a, 31b, 32a).
6, according to the equipment of claim 5, the exit portion (22b) that it is characterized in that described Venturi (6) is a flaring, with the inlet opening (27) of Venturi be to be placed in described exit portion, preferably near described venturi (21b, downstream 22a).
7, according to the equipment of claim 5, the sectional area that it is characterized in that the exit portion (32b) of described Venturi (6) is constant, with the inlet opening (37) of Venturi be to be placed in described trunnion (31b, 32a), preferably near the upstream of the exit portion (32b) of Venturi.
8, according to the equipment of claim 6, the cross section that it is characterized in that described Venturi is circular, the inlet opening of Venturi (27) is the inner surface that is configured in described flaring exit portion (22b) symmetrically, and be in the perpendicular plane of the symmetry axis of described Venturi in.
9, according to the equipment of claim 7, the cross section that it is characterized in that described Venturi is circular, the inlet opening of Venturi (37) be configured in symmetrically described venturi (31b, inner surface 32a), and be in the perpendicular plane of the symmetry axis of described Venturi in.
10,, it is characterized in that each inlet opening (27 according to arbitrary equipment of claim 4-9; 37) form a feed tube (26; 36) mouth, the symmetry axis angulation scope of the center line of this feed tube and described Venturi (6) are 10 °-80 ° particularly 45 °.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8904106 | 1989-12-05 | ||
| SE8904106A SE466943B (en) | 1989-12-05 | 1989-12-05 | PROCEDURE AND DEVICE FOR CLEANING A PROCESS GAS |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1052261A true CN1052261A (en) | 1991-06-19 |
Family
ID=20377696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN90109921A Pending CN1052261A (en) | 1989-12-05 | 1990-12-05 | The purification method of flue gas and equipment |
Country Status (12)
| Country | Link |
|---|---|
| EP (1) | EP0502945A1 (en) |
| JP (1) | JPH05502617A (en) |
| KR (1) | KR920703185A (en) |
| CN (1) | CN1052261A (en) |
| AU (1) | AU635597B2 (en) |
| CA (1) | CA2070295A1 (en) |
| FI (1) | FI922591A (en) |
| PL (1) | PL288082A1 (en) |
| SE (1) | SE466943B (en) |
| TR (1) | TR25007A (en) |
| WO (1) | WO1991008042A1 (en) |
| YU (1) | YU230690A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100434141C (en) * | 2003-06-26 | 2008-11-19 | 阿尔斯托姆科技有限公司 | Method and device for separating sulphur dioxide from a gas |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT404565B (en) * | 1997-06-05 | 1998-12-28 | Scheuch Alois Gmbh | METHOD FOR PURIFYING POLLUTANT-GASES |
| CN100422643C (en) * | 2006-06-23 | 2008-10-01 | 杭州新世纪能源环保工程股份有限公司 | Smoke purifier of domestic refuse incinerator |
| DE102006060156A1 (en) | 2006-12-18 | 2008-06-19 | Evonik Stockhausen Gmbh | Water-absorbing polymer structures produced using polymer dispersions |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4206186A (en) * | 1975-02-06 | 1980-06-03 | Holter Gesellschaft Fur Patentverwertungsverfahren Mbh | Refuse pyrolysis |
| AT363918B (en) * | 1975-05-06 | 1981-09-10 | Hoelter Heinz | METHOD AND DEVICE FOR PURIFYING GAS |
| DE3136914A1 (en) * | 1981-09-17 | 1983-03-31 | Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck | "Process for the cleaning of flue gas downstream of power stations, producing gypsum at the same time in a dry process" |
| SE452413B (en) * | 1984-12-04 | 1987-11-30 | Flaekt Ab | MEDIUM MIXING NOZE, INTENDED TO BE USED IN A CONTACT REACTOR |
| FI78401B (en) * | 1985-04-24 | 1989-04-28 | Tampella Oy Ab | FOERFARANDE OCH ANORDNING FOER ATT BRINGA ROEKGASERNAS GASFORMIGA SVAVELFOERENINGAR SAOSOM SVAVELDIOXID ATT REAGERA TILL FASTA FOERENINGAR SOM SEPARERAS FRAON ROEKGASERNA. |
| US4795619A (en) * | 1987-03-20 | 1989-01-03 | Lerner Bernard J | Removal of acid gases in dry scrubbing of hot gases |
| DE3803652A1 (en) * | 1987-10-01 | 1989-08-10 | Hoelter Heinz | Use of alkaline porous support materials for dry separation of pollutant gas with increase of moisture |
-
1989
- 1989-12-05 SE SE8904106A patent/SE466943B/en not_active IP Right Cessation
-
1990
- 1990-11-23 AU AU69005/91A patent/AU635597B2/en not_active Ceased
- 1990-11-23 CA CA002070295A patent/CA2070295A1/en not_active Abandoned
- 1990-11-23 EP EP91900391A patent/EP0502945A1/en not_active Ceased
- 1990-11-23 KR KR1019920701326A patent/KR920703185A/en not_active Application Discontinuation
- 1990-11-23 JP JP3501012A patent/JPH05502617A/en active Pending
- 1990-11-23 WO PCT/SE1990/000766 patent/WO1991008042A1/en not_active Application Discontinuation
- 1990-12-04 PL PL28808290A patent/PL288082A1/en unknown
- 1990-12-04 TR TR90/1135A patent/TR25007A/en unknown
- 1990-12-05 YU YU230690A patent/YU230690A/en unknown
- 1990-12-05 CN CN90109921A patent/CN1052261A/en active Pending
-
1992
- 1992-06-04 FI FI922591A patent/FI922591A/en not_active Application Discontinuation
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100434141C (en) * | 2003-06-26 | 2008-11-19 | 阿尔斯托姆科技有限公司 | Method and device for separating sulphur dioxide from a gas |
Also Published As
| Publication number | Publication date |
|---|---|
| SE466943B (en) | 1992-05-04 |
| PL288082A1 (en) | 1991-12-02 |
| SE8904106L (en) | 1991-06-06 |
| FI922591A0 (en) | 1992-06-04 |
| JPH05502617A (en) | 1993-05-13 |
| SE8904106D0 (en) | 1989-12-05 |
| YU230690A (en) | 1994-05-10 |
| WO1991008042A1 (en) | 1991-06-13 |
| TR25007A (en) | 1992-09-01 |
| KR920703185A (en) | 1992-12-17 |
| CA2070295A1 (en) | 1991-06-06 |
| FI922591A (en) | 1992-06-04 |
| AU6900591A (en) | 1991-06-26 |
| AU635597B2 (en) | 1993-03-25 |
| EP0502945A1 (en) | 1992-09-16 |
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