GB2174082A - A process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace - Google Patents
A process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace Download PDFInfo
- Publication number
- GB2174082A GB2174082A GB08527455A GB8527455A GB2174082A GB 2174082 A GB2174082 A GB 2174082A GB 08527455 A GB08527455 A GB 08527455A GB 8527455 A GB8527455 A GB 8527455A GB 2174082 A GB2174082 A GB 2174082A
- Authority
- GB
- United Kingdom
- Prior art keywords
- flue gases
- furnace
- hydroxide
- sulphur
- calcium
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- 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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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Chimneys And Flues (AREA)
- Gas Separation By Absorption (AREA)
Abstract
In addition to a sulphur-containing material (4) to be burned and an oxygen-containing gas (5), a pulverous calcium or magnesium hydroxide (6) is fed, in excess proportion to the sulphur dioxide gas produced into the combustion chamber of the furnace (1), and water (9) or steam is sprayed separately into the flue gases (8) containing calcium oxide or magnesium oxide either in the furnace or into the flue gases leaving the furnace. Alternatively and preferably, the pulverous hydroxide (6') can be fed directly into the flue gases leaving the furnace (1), either in a flue gas conduit (7) or in a reactor (2) downstream of it, where the hydroxide is activated by means of water (9) or steam. <IMAGE>
Description
SPECIFICATION
A process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace
The present invention relates to a process for removing gaseous sulphur compounds, and especially sulphur dioxide, from the flue gases of a furnace which burns sulphur-containing fuels, such as coal or oil.
It is already known to decrease the sulphur dioxide content of the flue gases of a furnace by feeding calcium oxide, calcium carbonate or some other alkaline compound into the combustion chamber of the furnace. In a fluidized-bed furnace with a circulating bed it is possible by means of a calcium addition to decrease the sulphur dioxide content of the flue gases by as much as 90% when the furnace is operating within the temperature range which is optimal for the chemical reactions, i.e. 800-1000"C. The sulphur dioxide thus absorbed leaves the furnace in the form of gypsum, along with the fly ash.
In other furnaces, in which it is necessary to use temperatures higher than those mentioned above and in which the retention time of the additive is short due to the nature of the combustion, it is to be expected that the decrease in the sulphur dioxide content of the flue gases would remain substantially lower, about 50% or less, and therefore this process has not been applied on an industrial scale to such furnaces.
On the other hand, it is known that the sulphur dioxide content of flue gases can be decreased by various absorption processes outside the furnace. One such process, known perse, is the so-called semi-dry process, in which the flue gas emerging from the furnace is led into a separate reactor, into which an aqueous slurry of calcium hydroxide is sprayed in the form of small droplets through specific nozzles. The reactor is typically a rather large vessel, in which the velocity of the flue gases is allowed to decrease and the aqueous slurry is sprayed downwards from the upper part of the vessel. The temperature of the reactor is at this time about 50-80 C, and the control of the spraying of the aqueous slurry of calcium hydroxide is very important, since drops which are too large will remain as liquid on the bottom of the reactor.The density of the aqueous slurry of calcium hydroxide should be maintained so high that the heat content in the flue gases would evaporate the water entering the reactor, so that the adsorption product can be recovered in the form of dry powder. By this process, it is possible to remove as much as 90% of the sulphur dioxide. The disadvantages of the process include the tendency of the nozzles to become clogged, the need for an additional preparing and batching apparatus for the aqueous slurry of calcium hydroxide, which raises the investment costs, and the problem of controlling the drop size during spraying.
It is an object of the present invention to provide a process for removing gaseous sulphur compounds, such as sulphur dioxide, from the flue gases of a furnace, by means of which the gaseous sulphur compounds can be converted to solid sulphur compounds which can easily be separated from the gases and thereby effectively removed from the flue gases of the furnace in a simple and economical manner.
According to the invention, there is provided a process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace, comprising the steps of
(a) feeding to said furnace, in addition to sulphur-containing material to be burned and an oxygencontaining gas, a pulverous material comprising an alkali metal hydroxide and/or alkaline earth metal hydroxide, and/or feeding said pulverous material into the flue gases leaving said furnace,
(b) separately feeding water and/or steam into said furnace and/or said flue gases leaving said furnace, and finally
(c) separating from the flue gases a solid reaction product containing alkali metal and/or alkaline earth metal sulphate and possibly sulphite.
In the process according to the present invention, a material which reacts with gaseous sulphur compounds, and particularly with sulphur dioxide, and water are fed into the process separately, whereby the problems of preparing, handling and feeding in a slurry are avoided.
The basic idea of the invention is thus that the hydroxide is fed into the flue gases in the form of powder and is activated only in situ in the flue gases by means of water and/or steam, whereupon it reacts with sulphur dioxide or other gaseous sulphur compounds to form a sulphate/sulphite mixture which can thereafter be effectively removed from the flue gases by conventional physical ash separation methods.
A pulverous hydroxide may be fed into the combustion chamber of the furnace, and/or into the flue gases emerging from the furnace, in accordance with the sulphur content of the fuel in such a way that the amount of alkali and/or earth alkaline metal in the molar ratio in accordance with the reaction formula, is at least the equivalent to the sulphur; preferably, however, it is greater than the amount necessary for the reaction. By feeding hydroxide in the form of powder separately into the combustion chamber of the furnace, or into the flue gas conduit for flue gases leaving the furnace, it is possible to use simple feeding devices, e.g.
pneumatic devices, so that the clogging of the nozzles and the need to use additional preparing and batching devices for an aqueous slurry are avoided. Contrary to this, the feeding of water and steam through nozzles is uncomplicated and easy.
The feeding of water or steam into the flue gases is in practice carried out in the temperature range 50-800 C, preferably within the temperature range 90-200 C. If it is desired to recover the absorption product substantially in the form of dry powder, water is used in the spraying step only in such an amount that the thermal energy of the flue gases suffices to evaporate it.
The invention is described below in greater detail with reference to the accompanying drawing, which depicts diagrammatically an apparatus suitableforcarrying outthe process according to the invention.
In the drawing the furnace in general is indicated by reference numeral 1. The sulphur-containing material 4 to be burned, an oxygen-containing gas 5, and a pulverous calcium and/or magnesium hydroxide 6, are fed into the combustion chamber of the furnace 1 ,the pulverous material preferably being fed in an amount in excess in proportion to the sulphur dioxide gas produced in the combustion chamber. By the expression "in excess" is meant in this context that the amount of the calcium or magnesium compound, or calcium and magnesium compounds, is greater than would in theory be needed, according to the reaction formula, to react with all of the sulphur fed into the combustion chamber in the fuel.
The hydroxide fed into the furnace is first dehydrated in the furnace to oxide. The oxide, for its part, can react with the sulphur dioxide, first forming sulphite and thereafter on oxidation, sulphate. Owing to the short retention time in the furnace, only part of the oxide has time to react with the sulphur dioxide at a temperature sufficiently high for the reaction to take place, and for this reason flue gases 8 containing calcium oxide and/or magnesium oxide and which contain combustion residue and steam, and also unabsorbed sulphur dioxide, leave the combustion chamber of the furnace through a flue gas conduit 7.
In practice the temperature of the flue gases 8 is so low that the reaction between the calcium and/or magnesium oxide and sulphur dioxide is relatively weak, and under such conditions, the oxides can be regarded as inactive in terms of sulphur removal. When the temperature of the flue gases decreases, the oxides may react with the steam present in the flue gases and be reconverted to hydroxide. It is therefore preferable to feed the pulverous hydroxide directly into the flue gas conduit 7 or into a reactor 2 downstream thereof. In addition, the flue gases 8 can be used in a heat exchanger 12 to preheat the air 5 to be fed into the furnace 1.
The sulphur dioxide-containing flue gases emerging from the combustion chamber of the furnace 1, which contain calcium and/or magnesium oxide and possibly calcium and/or magnesium hydroxide, are thereafter directed into the reactor 2. In order to activate the oxide and/or hydroxide, water or more steam is sprayed at 9 into the flue gases in the reactor 2, and this water or steam reacts with the calcium and/or magnesium oxide and forms the respective hydroxide, activating it and also activating any hydroxide which may already be present in the flue gases. The hydroxide for its part reacts with the sulphur dioxide still present in the flue gases 8, thereby forming the respective sulphite, which, in the presence of oxygen, at least in part further oxidizes to the respective sulphate.The amount of water 9 fed into the reactor 2 is adjusted to so low a value that the heat of the flue gases 8 suffices to evaporate the water so fed. Thereupon, the substantially dry, fly ash-like reaction poduct can be removed, in the same manner as other ash, in a conventional ash separator 3, from which the flue gases 11 are further directed into a flue 13 and the separated dust 12 is directed to possible further treatment.
The order in which the water and the hydroxide are added is in no way critical. Thus, it is possible, for example, to feed the water or steam into the furnace and the pulverous hydroxide only at a point subsequent to the furnace, either into the flue gas conduit 7 or into the reactor 2 downstream of it.
One of the further advantages of the present invention is that the process can be applied to a furnace provided with any type of burner. The size of the furnace is not a restricting factor, and it is not necessary to circulate the calcium and/or magnesium hydroxide inthe combustion chamber, whereby the expensive circulating-bed alternative with its complicated circulation devices, and at the same time the excessive dust due to its principle of operation and also the need for dust separation are avoided. Compared with the already known spray method, the spraying of water or steam into the reactor 2 is, moreover, considerably less complicated and easier to implement than when using a slurry which clogs the nozzles and is difficult to mix.
The invention is illustrated by the following examples:
Example I
Coal having a sulphur content of 1.4% by weight is fed at a rate of 70 tn/h into a 600 MW pulverized-coal furnace, operating at full capacity. An excess of combustion air is fed in, so that the oxygen content in the flue gases is 4% by volume.
Crude calcium hydroxide having a calcium hydroxide content of 90% is fed into the furnace at a predetermined varying proportion with respect to the amount of sulphur entering the furnace in the fuel. The theoretical equivalent amount is about 2.5 tn/h of the said calcium hydroxide.
Calcium hydroxide and water and/or steam are sprayed into the flue gases either in the flue gas conduit or in a separate reactor located at a point downstream of the flue gas conduit.
In terms of energy economy, it is most advantageous to increase the moisture content of the flue gases by spraying water into them in a separate reactor located at a point subsequent to all heat recovery surfaces.
The increased moisture content of the flue gases makes the calcium hydroxide highly reactive, whereupon it reacts rapidly with the sulphur oxides present in the flue gases. The higher the moisture content of the flue gases upon leaving, the more effectively is the sulphur dioxide removed from the flue gases. In terms of energy economy it is, however, advantageous to operate in such a way that the heat released in the chemical reactions will suffice to evaporate the amount of water added. If it is desired to raise the final temperature of the flue gases, this may be done either by using external heat or by means of a warm flue gas flow.
The results obtained are given in Table 1 below, which shows as a percentage how much sulphur dioxide was removed from the flue gases when varying amounts of calcium hydroxide were fed into the furnace in accordance with the present invention; the amounts of the calcium hydroxide added are indicated as molar proportions of the calcium content of the pulverous calcium hydroxide to the sulphur content of the fuel fed into the furnace. The temperatures of the flue gases were measured immediately prior to the feeding point of the water or steam, except at 800 C, at which temperature the water or steam was fed directly into the furnace.
TABLE 1
Ca/S Flue gas B) Flue gas SO2
Tin Tout reduction
0.48 800OCA) 1080C 42%
0.52 500C 65 C 56%
1.52 2020C 740C 77%
1.56 90 C 680C 82%
2.20 2000C 720C 87%
2.22 1200C 620C 96%
2.3 11 00C 680C 93%
2.5 900C 660C 97%
4.1 8000C 1100C 72%
4.0 1 200C 68 C 98%
A) water or steam fed into the furnace
B) immediately priorto the feeding point of water Example 2
A calcium-magnesium hydroxide which contains calcium hydroxide 45% by weight, magnesium
hydroxide 45% by weight and impurities 10% by weight is fed into the furnace in accordance with the
procedure of Example 1, under similar conditions. Calcium-magnesium hydroxide and water and/or steam
are fed into the flue gases either in the furnace or in a separate reactor located at a point subsequent to the furnace.
The increase in the moisture content makes calcium hydroxide in particular highly reactive, whereupon it
rapidly reacts with the oxides of sulphur present in the flue gases. If the molar ratio of the calcium contained
in the calcium hydroxide to the sulphur present is at least 1, reaction occurs primarily between the calcium
hydroxide and the oxides of sulphur, whilst the magnesium hydroxide, being slower, passes through the
reaction zone substantially unchanged.
If the calcium-magnesium hydroxide is fed into hot flue gases, the consequence may be either that the
magnesium hydroxide breaks down into magnesium oxide and water or that the entire calcium-magnesium
hydroxide breaks down into calcium oxide and magnesium oxide and water. In this case each oxide can as such react with the oxides of sulphur and, when the flue gases cool and the moisture content increases,
reform hydroxide, which further reacts with the oxides of sulphur. If the molar proportion of the calcium to the sulphur is at least 1, the reaction results and conditions are substantially in accordance with the corresponding values in Table 1, owing to the ability of the calcium compound to react more rapidly.
Claims (8)
1. A process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace, comprising the steps of
(a) feeding to said furnace, in addition to sulphur-containing material to be burned and an oxygencontaining gas, a pulverous material comprising an alkali metal hydroxide and/or alkaline earth metal hydroxide, and/or feeding said pulverous material into the flue gases leaving said furnace,
(b) separately feeding water and/or steam into said furnace and/or said flue gases leaving said furnace, and finally
(c) separating from the flue gases a solid reaction product containing alkali metal and/or alkaline earth metal sulphate and possibly sulphite.
2. A process according to Claim 1, wherein said pulverous hydroxide is fed in an amount in excess in proportion to the amount of sulphur present in the flue gases.
3. A process according to Claim 1 or Claim 2, wherein the water and/or steam is sprayed while the temperature of the flue gases. is 50-800 C.
4. A process as claimed in Claim 3, wherein the temperature of said flue gases is 90-200 C.
5. A process according to any one of the preceding Claims, wherein water is sprayed into the flue gases at most in an amount that can be evaporated by the thermal energy produced by the flue gases and by the reactions taking place.
6. A process according to any one of the preceding Claims, wherein the hydroxide to be fed in is calcium hydroxide or a calcium-magnesium hydroxide mixture.
7. A process as claimed in Claim 1 for removing gaseous sulphur compounds from the flue gases of a furnace, substantially as hereinbefore described with reference to the drawing.
8. A process as claimed in Claim 1 for removing sulphur compounds from the flue gases of a furnace, substantially as hereinbefore described with reference to either of the Examples.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI851623A FI78846B (en) | 1985-04-24 | 1985-04-24 | FOERFARANDE FOER AVLAEGSNANDE AV GASFORMIGA SVAVELFOERENINGAR OCH SVAVELDIOXID UR ROEKGASER I EN PANNA. |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB8527455D0 GB8527455D0 (en) | 1985-12-11 |
| GB2174082A true GB2174082A (en) | 1986-10-29 |
| GB2174082B GB2174082B (en) | 1988-11-23 |
Family
ID=8520718
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08527455A Expired GB2174082B (en) | 1985-04-24 | 1985-11-07 | A process for removing gaseous sulphur compounds, particularly sulphur dioxide, from the flue gases of a furnace |
Country Status (24)
| Country | Link |
|---|---|
| JP (1) | JPS61287420A (en) |
| CN (1) | CN1005312B (en) |
| AU (1) | AU579902B2 (en) |
| BE (1) | BE903598A (en) |
| BG (1) | BG60231B1 (en) |
| CA (1) | CA1289336C (en) |
| CH (1) | CH672265A5 (en) |
| CS (1) | CS274270B2 (en) |
| DD (1) | DD240839A5 (en) |
| DE (1) | DE3539348A1 (en) |
| DK (1) | DK515485A (en) |
| ES (1) | ES8700307A1 (en) |
| FI (1) | FI78846B (en) |
| FR (1) | FR2580950B1 (en) |
| GB (1) | GB2174082B (en) |
| HU (1) | HU202422B (en) |
| IT (1) | IT1185833B (en) |
| NL (1) | NL8503081A (en) |
| NZ (1) | NZ213859A (en) |
| PL (1) | PL148176B1 (en) |
| RO (1) | RO93449A (en) |
| SE (1) | SE461958B (en) |
| YU (1) | YU44580B (en) |
| ZA (1) | ZA858476B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0250878A1 (en) * | 1986-05-29 | 1988-01-07 | Electric Power Research Institute, Inc | Method for reduction of sulfur products from flue gases by injection of powdered alkali sorbent at intermediate temperatures and apparatus therefor |
| US5084256A (en) * | 1986-05-29 | 1992-01-28 | Electric Power Research Institute, Inc. | Method for reduction of sulfur products for gases by injection of powdered alkali sorbent at intermediate temperatures |
| GB2252967A (en) * | 1991-02-19 | 1992-08-26 | Intevep Sa | Effluent removal from combusted fuel off-gases downstream of combustion with injected sorbents |
| FR2698287A1 (en) * | 1992-11-24 | 1994-05-27 | Stein Industrie | Process for reducing pollutant emissions in circulating fluidized bed combustion plants |
| US5352647A (en) * | 1990-05-02 | 1994-10-04 | Ftu Gmbh | Composition for separating out noxious substances from gases and exhaust gases |
| US6228336B1 (en) | 1997-03-18 | 2001-05-08 | Hokkaido Electric Power Company, Inc. | Dust collecting method |
| WO2003004136A1 (en) * | 2001-07-05 | 2003-01-16 | Fortum Oyj | Flue gas purification process |
| CN100449208C (en) * | 2004-11-23 | 2009-01-07 | 河南大学 | Boiler desulfurizer and smoke activating dust-proof desulfurizer |
| WO2010092035A1 (en) * | 2009-02-12 | 2010-08-19 | Siemens Vai Metals Technologies Gmbh & Co | Method and device for treating exhaust gas from sintering or pelletizing systems |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3716566A1 (en) * | 1987-05-18 | 1988-12-01 | Fichtel Roland | Process for the production of reactive calcium hydroxides for exhaust gas purification |
| DE8717874U1 (en) * | 1987-05-18 | 1990-11-22 | FTU GmbH, 8130 Starnberg | Calcium hydroxide for exhaust gas purification |
| JPS6414517A (en) * | 1987-07-03 | 1989-01-18 | Gadelius Kk | Recovery of waste heat of exhaust gas |
| DE3817356A1 (en) * | 1988-01-18 | 1989-07-27 | Krupp Polysius Ag | Process and apparatus for the heat treatment of fine-grained material |
| JPH03154615A (en) * | 1989-11-09 | 1991-07-02 | Hitachi Zosen Corp | Semidry sulfurization |
| JP6199698B2 (en) * | 2013-11-01 | 2017-09-20 | 栗田工業株式会社 | Acid exhaust gas treatment method and exhaust gas treatment agent |
| CN108579356B (en) * | 2018-04-02 | 2021-06-01 | 安徽蓝天盈丰环保科技有限公司 | Boiler flue gas desulfurization and dust removal device and method |
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| GB1429427A (en) * | 1974-07-25 | 1976-03-24 | Asahi Fibreglass Co | Method of cleaning waste gases containing a fluorine component |
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| GB1504688A (en) * | 1975-04-11 | 1978-03-22 | Exxon Research Engineering Co | Mitigating or preventing environmental pollution by sulphur oxides in the treatment of sulphur-containing substance |
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- 1985-04-24 FI FI851623A patent/FI78846B/en not_active Application Discontinuation
- 1985-10-16 NZ NZ213859A patent/NZ213859A/en unknown
- 1985-10-22 JP JP60236246A patent/JPS61287420A/en active Granted
- 1985-10-24 HU HU854099A patent/HU202422B/en not_active IP Right Cessation
- 1985-10-24 DD DD85282039A patent/DD240839A5/en not_active IP Right Cessation
- 1985-10-25 AU AU49077/85A patent/AU579902B2/en not_active Ceased
- 1985-10-28 ES ES548285A patent/ES8700307A1/en not_active Expired
- 1985-11-04 FR FR858516281A patent/FR2580950B1/en not_active Expired - Lifetime
- 1985-11-04 CH CH4722/85A patent/CH672265A5/de not_active IP Right Cessation
- 1985-11-05 ZA ZA858476A patent/ZA858476B/en unknown
- 1985-11-06 BE BE0/215833A patent/BE903598A/en not_active IP Right Cessation
- 1985-11-06 BG BG072295A patent/BG60231B1/en unknown
- 1985-11-06 YU YU1732/85A patent/YU44580B/en unknown
- 1985-11-06 DE DE19853539348 patent/DE3539348A1/en not_active Ceased
- 1985-11-07 GB GB08527455A patent/GB2174082B/en not_active Expired
- 1985-11-07 SE SE8505270A patent/SE461958B/en not_active IP Right Cessation
- 1985-11-07 CN CN85108066.9A patent/CN1005312B/en not_active Expired
- 1985-11-08 RO RO85120717A patent/RO93449A/en unknown
- 1985-11-08 NL NL8503081A patent/NL8503081A/en not_active Application Discontinuation
- 1985-11-08 CS CS808085A patent/CS274270B2/en not_active IP Right Cessation
- 1985-11-08 CA CA000494920A patent/CA1289336C/en not_active Expired - Lifetime
- 1985-11-08 DK DK515485A patent/DK515485A/en not_active Application Discontinuation
- 1985-11-08 IT IT67943/85A patent/IT1185833B/en active
- 1985-11-08 PL PL1985256163A patent/PL148176B1/en unknown
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| GB1351823A (en) * | 1970-10-27 | 1974-05-01 | Combustion Eng | Method and apparatus for preparing a reactant for introduction to a gas scrubber |
| GB1492605A (en) * | 1973-11-08 | 1977-11-23 | Celorio Mendoza F | Method for treating gases to remove contaminants therefro |
| GB1466218A (en) * | 1974-06-12 | 1977-03-02 | Ceskoslovenska Akademie Ved | Method and apparatus for neutralizing waste gases |
| GB1429427A (en) * | 1974-07-25 | 1976-03-24 | Asahi Fibreglass Co | Method of cleaning waste gases containing a fluorine component |
| GB1504688A (en) * | 1975-04-11 | 1978-03-22 | Exxon Research Engineering Co | Mitigating or preventing environmental pollution by sulphur oxides in the treatment of sulphur-containing substance |
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| GB1515046A (en) * | 1975-06-06 | 1978-06-21 | Us Energy | Method and apparatus for desulpherising flue gas |
| EP0044916A2 (en) * | 1980-05-24 | 1982-02-03 | Hölter, Heinz, Dipl.-Ing. | Process and apparatus for the separation of sulfur dioxide and other pollutants from flue gas |
| GB2084980A (en) * | 1980-10-08 | 1982-04-21 | Domtar Inc | Fluidized bed sulfur dioxide removal |
| GB2095654A (en) * | 1981-02-21 | 1982-10-06 | Steinmueller Gmbh L & C | Treating combustion waste gas |
| EP0104335A2 (en) * | 1982-09-24 | 1984-04-04 | Deutsche Babcock Anlagen Aktiengesellschaft | Process for the purification of exhaust gases |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0250878A1 (en) * | 1986-05-29 | 1988-01-07 | Electric Power Research Institute, Inc | Method for reduction of sulfur products from flue gases by injection of powdered alkali sorbent at intermediate temperatures and apparatus therefor |
| US5084256A (en) * | 1986-05-29 | 1992-01-28 | Electric Power Research Institute, Inc. | Method for reduction of sulfur products for gases by injection of powdered alkali sorbent at intermediate temperatures |
| US5352647A (en) * | 1990-05-02 | 1994-10-04 | Ftu Gmbh | Composition for separating out noxious substances from gases and exhaust gases |
| GB2252967A (en) * | 1991-02-19 | 1992-08-26 | Intevep Sa | Effluent removal from combusted fuel off-gases downstream of combustion with injected sorbents |
| GB2252967B (en) * | 1991-02-19 | 1995-09-13 | Intevep Sa | In-situ removal of effluents from a gaseous stream by injection of an effluent sorbent into downstream of the combustion zone |
| FR2698287A1 (en) * | 1992-11-24 | 1994-05-27 | Stein Industrie | Process for reducing pollutant emissions in circulating fluidized bed combustion plants |
| EP0599721A1 (en) * | 1992-11-24 | 1994-06-01 | Stein Industrie | Process for reducing the emission of pollutants in combustion devices with circulating fluidised bed |
| US5345884A (en) * | 1992-11-24 | 1994-09-13 | Stein Industrie | Method of reducing polluting emissions from circulating fluidized bed combustion intallations |
| US6228336B1 (en) | 1997-03-18 | 2001-05-08 | Hokkaido Electric Power Company, Inc. | Dust collecting method |
| WO2003004136A1 (en) * | 2001-07-05 | 2003-01-16 | Fortum Oyj | Flue gas purification process |
| CN100449208C (en) * | 2004-11-23 | 2009-01-07 | 河南大学 | Boiler desulfurizer and smoke activating dust-proof desulfurizer |
| WO2010092035A1 (en) * | 2009-02-12 | 2010-08-19 | Siemens Vai Metals Technologies Gmbh & Co | Method and device for treating exhaust gas from sintering or pelletizing systems |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 732E | Amendments to the register in respect of changes of name or changes affecting rights (sect. 32/1977) | ||
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 20031107 |