CA1193829A - Method of removing sulfur and nitrogen oxides by dry process - Google Patents
Method of removing sulfur and nitrogen oxides by dry processInfo
- Publication number
- CA1193829A CA1193829A CA000411111A CA411111A CA1193829A CA 1193829 A CA1193829 A CA 1193829A CA 000411111 A CA000411111 A CA 000411111A CA 411111 A CA411111 A CA 411111A CA 1193829 A CA1193829 A CA 1193829A
- Authority
- CA
- Canada
- Prior art keywords
- ammonia
- moving bed
- nitrogen oxides
- waste gas
- carbonaceous adsorbent
- 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.)
- Expired
Links
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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
TITLE OF THE INVENTION
A method of removing sulfur and nitrogen oxides by dry process ABSTRACT OF THE DISCLOSURE
In a method of removing sulfur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, this invention provides an improvement characterized in that ammonia is directly added to the moving bed of the carbonaceous adsorbent.
A method of removing sulfur and nitrogen oxides by dry process ABSTRACT OF THE DISCLOSURE
In a method of removing sulfur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, this invention provides an improvement characterized in that ammonia is directly added to the moving bed of the carbonaceous adsorbent.
Description
~ ~L93~Z~
1. Field of the Invention This invention relates to a method of removing sul~ur and nitrogen oxides by dry process and more particularly, it is concerned with a method for the separation of sulfur and nitrogen oxides from a waste gas using a carbonaceous adsorbent to which ammonia is added.
The accompanying drawings are to illustrate the principle and merits of the present invention in more detail:
Fig. 1 and Fig. 2 are schematic views of the prior art systems of adding ammonia.
Fig. 3 and Fig. 4 are schematic views of the systems of addin~ ~mmon;a according to the present invention.
Fig. 5 and Fig. 6 are gxaphs showing the change of pressuxe loss of a waste gas passing through a moving bed with the passage of time respectivel~ in the case of the prior art and the present invention.
1. Field of the Invention This invention relates to a method of removing sul~ur and nitrogen oxides by dry process and more particularly, it is concerned with a method for the separation of sulfur and nitrogen oxides from a waste gas using a carbonaceous adsorbent to which ammonia is added.
The accompanying drawings are to illustrate the principle and merits of the present invention in more detail:
Fig. 1 and Fig. 2 are schematic views of the prior art systems of adding ammonia.
Fig. 3 and Fig. 4 are schematic views of the systems of addin~ ~mmon;a according to the present invention.
Fig. 5 and Fig. 6 are gxaphs showing the change of pressuxe loss of a waste gas passing through a moving bed with the passage of time respectivel~ in the case of the prior art and the present invention.
2. Description of the Prior Art A method of removing sulfur and nitrogen oxides by 2D dry process has been known wherein a waste gas is passed through a moving bed formed of a carbonaceous adsorbent to remove sulfur oxides in the waste gas, while ammonia is addea to remove nitrogen oxides. In this case, ammonia gas alone or diluted with another suitable gas is added to a duct of the waste gas before the moving bed as shown in Fig. 1.
Referring to Fig. 1, waste gas 1 and ammonia gas or an ammonia-cont~in;ng gas 3 fed by means of ammonia mixing device 6 are brought into contact with moving bed 4 consisting of carbonaceous adsorbent 2 in a transverse direction.
However, this prior art method has the disadvantage that 3132~
1 ammonia sul~ate or ammonium hydrogensulfate is formed, cleposited and grown in a waste gas flue and inlet por-tion formed of a louver or perforated plate to the moving bed and the passage area of waste gas is thus reduced to increase the pressure loss o~ waste gas, to cause a deflection of waste gas and to lower the removal efficiency of sulfur and nitrogen oxides.
The temperature of a waste gas to be processed in an apparatus for removing sulfur and nitrogen oxides by dry process is generally within a range of room temperature to 180C. In this temperature range, the reaction'of ammonia and sulfur oxides precedes that of ammonia and nitrogen oxides, so in the prior art method wherein a single moving ' bed is used and ammonia is added to a waste gas before flowing in the moving bed, disadvantages are unavoidable that a large removal efficiency of nitrogen oxides cannot be given ; and the consumption of ammonia is markedly increased. In order to overcome this disadvantage, there has been proposed a method wherein in a system comprising two moving beds 'l and 5 of carbonaceous adsorbent 2'as shown in Fig. 2, waste gas l is passed through first moving bed 4 with adding a small amount of ammonia 3' or without adding ammonia before first moving bed 4, in which desulfurization is mainly carried out by the adsorption action of the carbonaceous adsorbent, the waste gas passing through first moving bed 4 is then mixed with ammonia 3 and passed through second moving bed 5 in which denitrification is mainly carried out. This method needs two moving beds resulting in increase of the, installation cost.
~93~2~
SU~M~RY OF THE INVENTION
It is an object of the presen-t invention to provide a method of removing sulfur and nitrogen oxides by dry process whereby the above described disadvantages are overcome.
It is another object of the present invention to provide an improved method oE adding ammonia to a system wherein removal of sulfur and nitrogen oxides is carried out using a carbonaceous adsorbent.
These objects can be attained by a method of removing sulfur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, characterized in that ammonia is directly added to the moving bed of the carbon-aceous adsorbe~t.
DETAILED DESCRIPTION OF THE INVENTION
The inventors have made ef~orts to overcome the above described disadvantages of the prior art and consequently, have found that this object can be accomplished by adding ammonia directly to a moving bed of carbonaceous adsorbent.
That is to say, in accordance with the present inven-tion, there is provided a method of removing sulur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, characterized in that ammonia is directly added to the moving bed of the carbonaceous adsorbent.
Useful examples of the carbonaceous adsorbent are !
,
Referring to Fig. 1, waste gas 1 and ammonia gas or an ammonia-cont~in;ng gas 3 fed by means of ammonia mixing device 6 are brought into contact with moving bed 4 consisting of carbonaceous adsorbent 2 in a transverse direction.
However, this prior art method has the disadvantage that 3132~
1 ammonia sul~ate or ammonium hydrogensulfate is formed, cleposited and grown in a waste gas flue and inlet por-tion formed of a louver or perforated plate to the moving bed and the passage area of waste gas is thus reduced to increase the pressure loss o~ waste gas, to cause a deflection of waste gas and to lower the removal efficiency of sulfur and nitrogen oxides.
The temperature of a waste gas to be processed in an apparatus for removing sulfur and nitrogen oxides by dry process is generally within a range of room temperature to 180C. In this temperature range, the reaction'of ammonia and sulfur oxides precedes that of ammonia and nitrogen oxides, so in the prior art method wherein a single moving ' bed is used and ammonia is added to a waste gas before flowing in the moving bed, disadvantages are unavoidable that a large removal efficiency of nitrogen oxides cannot be given ; and the consumption of ammonia is markedly increased. In order to overcome this disadvantage, there has been proposed a method wherein in a system comprising two moving beds 'l and 5 of carbonaceous adsorbent 2'as shown in Fig. 2, waste gas l is passed through first moving bed 4 with adding a small amount of ammonia 3' or without adding ammonia before first moving bed 4, in which desulfurization is mainly carried out by the adsorption action of the carbonaceous adsorbent, the waste gas passing through first moving bed 4 is then mixed with ammonia 3 and passed through second moving bed 5 in which denitrification is mainly carried out. This method needs two moving beds resulting in increase of the, installation cost.
~93~2~
SU~M~RY OF THE INVENTION
It is an object of the presen-t invention to provide a method of removing sulfur and nitrogen oxides by dry process whereby the above described disadvantages are overcome.
It is another object of the present invention to provide an improved method oE adding ammonia to a system wherein removal of sulfur and nitrogen oxides is carried out using a carbonaceous adsorbent.
These objects can be attained by a method of removing sulfur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, characterized in that ammonia is directly added to the moving bed of the carbon-aceous adsorbe~t.
DETAILED DESCRIPTION OF THE INVENTION
The inventors have made ef~orts to overcome the above described disadvantages of the prior art and consequently, have found that this object can be accomplished by adding ammonia directly to a moving bed of carbonaceous adsorbent.
That is to say, in accordance with the present inven-tion, there is provided a method of removing sulur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, characterized in that ammonia is directly added to the moving bed of the carbonaceous adsorbent.
Useful examples of the carbonaceous adsorbent are !
,
3~29 l activatecl carborls ac-tivated cokes, semi-cokes and the like wllich are co~monl used, and -the ar~monia is used in tne fol~m of am~onia gas alone or diluted wi-t~ another sllitable gas~
~lle moving bed is ordinaril-~ held at a tempera-ture of from oom temperature to 180 ~.
hig. ~ shows one embodiment of the present invention, in which ammonia gas or diluted ammonia ~as 3 is directly fed to mOVillg bed 4 formed of carbonaceous adsorbent 2 via ammonia dispersing device 7 provided in the interior of moving bed 4, while a waste gas 1 is passed through moving bed 4 in such a ma~ner as to be -transversely contacted with carbonaceous adsorbent 2.
According to the method of t-he p:esent invention 7 ammonia is directlr added to a moving bed of carbonaceous adsorbent, so ammonium sulfate or ammonium h-rdrogensulfate is formed on only the moving carbonaceous adsorben-t and continuously discharged therefrom. ~hereforej clogging of a flue and a perforated plate or louver at the inlet part of a moving bed due to formation, dopsition and growth of ~0 ammonium sulfate or ammonium hydrogensulfate can effective ly be avoided, thus decreasing remarkably the pressure loss of a waste gas, preventing a waste gas flow from deflection and holdin~ uniform for a long time.
Fig. 4 shows another embodiment OI the presen-t inven-tion, in which a plurality of ammonia dispersing devices 7 and 7' are provided in a single moving bed to feed ammonia dividedl~J. In this embodiment, substantially the same effects can be obtained as in the case o~ providing a plurality of moving beds and the removal efficienc7 of nitrogen oxides can be increased with a decreased consumption of ammonia by the use of a simple apparatus. ~hat is, the installa-tion cost and operation cost of this appara-tus can rnarkedly be ~9~
decreased.
Of course, the direct addition or Leed of ammonia accordinG to the present invention is no-t limited to the case of using a single moving bedO
The present invention ~Jill be explained in detail with re~erence to the following examples. It will be obvi-ous to -those skill in the art that various changes and modi~ications can be made in the components~ ratios, opera-tional order and the like wi-thout departing from the spirit of the present invention. Therefore, the present invention should not be construed as being limited to the following examples.
~xample 1 A waste gas from combustion of fuel oil cont~inin~
860 ppm of S02 and 170 ppm of N0x was transversel~ passed at a temperature of 155 C and a flow rate of 1000 Nm3/H through a moving bed of granular activated carbon downwardly moved at a rate of 40 1/H. Ammonia was diluted with the waste gas after passed through the moving bed and directly intro-duced into -the moving bed through a gas dispersing device provided just behind a louver at the waste gas inlet side.
The quantitv of ammonia added was 0O43 i~m3/H. The pressure loss of the waste gas in the moving bed was hardly changed with the passage o~ time as shown in ~ig. 6~ The concentra-tion of S02 in tne waste gas at the outlet of the moving bed after 100 hours was 80 ppm and that of M0x was 90 ppm.
~omparative Exam~le 1 The procedure o~ ~xample 1 was repeated except ~ing ammonia to a waste gas duct be~ore the moving bed. The pressure loss of the waste gas in the moving bed ~ras changed ~1~382~
1 with -the passa~e of time as shown in ~igJ 5. The pressure loss was g,aduall~- increased and amounted to 235 mmAq al~ter 16~ hollrs. ~he concentration of S02 in the ~las-te gas at the outlet of the moving bed alter 100 hours was 91 ppm and that o~ M0x was 100 ppM.
Example 2 A ~aste gas from combustion OI fuel oil containing 9 ppm of S02 and 300 ppm of N0~ was transversely passed at a temperature ol 155 C and a ~lo~r rate of 1000 Nm3/E through a moving bed o~ activated ~ormed coke do~mwardly moved at a ra-te o~ 80 1/H. Ammonia was diluted with the waste gas af-ter passed through the moving bed and dividedly introduced into the moving bed at a rate of 0.18 Nm3/E to the inlet portion of -the moving bed and at a rate of 0~27 Nm3/H to the middle portion ol the moving bed~ ~he concentration of S02 in the waste gas after passed through the moving bed was 0-2 ppm and that o~ N0x was 63 ppm.
-G
~lle moving bed is ordinaril-~ held at a tempera-ture of from oom temperature to 180 ~.
hig. ~ shows one embodiment of the present invention, in which ammonia gas or diluted ammonia ~as 3 is directly fed to mOVillg bed 4 formed of carbonaceous adsorbent 2 via ammonia dispersing device 7 provided in the interior of moving bed 4, while a waste gas 1 is passed through moving bed 4 in such a ma~ner as to be -transversely contacted with carbonaceous adsorbent 2.
According to the method of t-he p:esent invention 7 ammonia is directlr added to a moving bed of carbonaceous adsorbent, so ammonium sulfate or ammonium h-rdrogensulfate is formed on only the moving carbonaceous adsorben-t and continuously discharged therefrom. ~hereforej clogging of a flue and a perforated plate or louver at the inlet part of a moving bed due to formation, dopsition and growth of ~0 ammonium sulfate or ammonium hydrogensulfate can effective ly be avoided, thus decreasing remarkably the pressure loss of a waste gas, preventing a waste gas flow from deflection and holdin~ uniform for a long time.
Fig. 4 shows another embodiment OI the presen-t inven-tion, in which a plurality of ammonia dispersing devices 7 and 7' are provided in a single moving bed to feed ammonia dividedl~J. In this embodiment, substantially the same effects can be obtained as in the case o~ providing a plurality of moving beds and the removal efficienc7 of nitrogen oxides can be increased with a decreased consumption of ammonia by the use of a simple apparatus. ~hat is, the installa-tion cost and operation cost of this appara-tus can rnarkedly be ~9~
decreased.
Of course, the direct addition or Leed of ammonia accordinG to the present invention is no-t limited to the case of using a single moving bedO
The present invention ~Jill be explained in detail with re~erence to the following examples. It will be obvi-ous to -those skill in the art that various changes and modi~ications can be made in the components~ ratios, opera-tional order and the like wi-thout departing from the spirit of the present invention. Therefore, the present invention should not be construed as being limited to the following examples.
~xample 1 A waste gas from combustion of fuel oil cont~inin~
860 ppm of S02 and 170 ppm of N0x was transversel~ passed at a temperature of 155 C and a flow rate of 1000 Nm3/H through a moving bed of granular activated carbon downwardly moved at a rate of 40 1/H. Ammonia was diluted with the waste gas after passed through the moving bed and directly intro-duced into -the moving bed through a gas dispersing device provided just behind a louver at the waste gas inlet side.
The quantitv of ammonia added was 0O43 i~m3/H. The pressure loss of the waste gas in the moving bed was hardly changed with the passage o~ time as shown in ~ig. 6~ The concentra-tion of S02 in tne waste gas at the outlet of the moving bed after 100 hours was 80 ppm and that of M0x was 90 ppm.
~omparative Exam~le 1 The procedure o~ ~xample 1 was repeated except ~ing ammonia to a waste gas duct be~ore the moving bed. The pressure loss of the waste gas in the moving bed ~ras changed ~1~382~
1 with -the passa~e of time as shown in ~igJ 5. The pressure loss was g,aduall~- increased and amounted to 235 mmAq al~ter 16~ hollrs. ~he concentration of S02 in the ~las-te gas at the outlet of the moving bed alter 100 hours was 91 ppm and that o~ M0x was 100 ppM.
Example 2 A ~aste gas from combustion OI fuel oil containing 9 ppm of S02 and 300 ppm of N0~ was transversely passed at a temperature ol 155 C and a ~lo~r rate of 1000 Nm3/E through a moving bed o~ activated ~ormed coke do~mwardly moved at a ra-te o~ 80 1/H. Ammonia was diluted with the waste gas af-ter passed through the moving bed and dividedly introduced into the moving bed at a rate of 0.18 Nm3/E to the inlet portion of -the moving bed and at a rate of 0~27 Nm3/H to the middle portion ol the moving bed~ ~he concentration of S02 in the waste gas after passed through the moving bed was 0-2 ppm and that o~ N0x was 63 ppm.
-G
Claims (6)
1. In a method of removing sulfur oxides and nitrogen oxides by dry process wherein a waste gas containing sulfur and nitrogen oxides is passed through a moving bed formed of a carbonaceous adsorbent and nitrogen oxides are removed by the reducing action of ammonia simultaneously with sulfur oxides, an improvement characterized in that ammonia is di-rectly added to the moving bed of the carbonaceous adsorbent.
2. The method of Claim 1, wherein the ammonia is added in the form of ammonia gas alone or diluted with another gas.
3. The method of Claim 1, wherein the ammonia is divid-edly added through a plurality of dispersing devices provid-ed in a single moving bed.
4. The method of Claim 1, wherein the moving bed is held at a temperature of from room temperature to 180°C.
5. The method of Claim 1, wherein the carbonaceous adsorbent is at least one member selected from the group con-sisting of activated carbons, activated cokes and semi-cokes.
6. The method of Claim 1, wherein the waste gas is transversely contacted with the moving bed of the carbonaceous adsorbent.
FIG. 1 FIG. 2 FIG. 3 FIG. 4
FIG. 1 FIG. 2 FIG. 3 FIG. 4
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP141,702/1981 | 1981-09-10 | ||
| JP56141702A JPS5843223A (en) | 1981-09-10 | 1981-09-10 | Dry type desulfurization and denitration method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1193829A true CA1193829A (en) | 1985-09-24 |
Family
ID=15298207
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000411111A Expired CA1193829A (en) | 1981-09-10 | 1982-09-09 | Method of removing sulfur and nitrogen oxides by dry process |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JPS5843223A (en) |
| AU (1) | AU558983B2 (en) |
| CA (1) | CA1193829A (en) |
| DE (1) | DE3232544C2 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3523326A1 (en) * | 1985-06-29 | 1987-01-08 | Steag Ag | METHOD FOR SEPARATING NO (DOWN ARROW) X (DOWN ARROW) FROM GASES, ESPECIALLY SMOKE GASES |
| US5766555A (en) * | 1987-05-07 | 1998-06-16 | Grochowski; Horst | Feed inlet floor for mobile bed reactors |
| DE3732567A1 (en) * | 1987-05-07 | 1988-11-24 | Horst Dr Grochowski | ANSTROME FLOOR FOR WALKING BED REACTORS AND METHOD FOR OPERATING THIS DEVICE |
| DE4035468C1 (en) * | 1990-11-08 | 1992-10-01 | Bergwerksverband Gmbh, 4300 Essen, De | |
| DE19711840A1 (en) * | 1997-03-21 | 1998-10-01 | Petersen Hugo Verfahrenstech | Process for removing pollutants in low concentration, especially chlorinated hydrocarbons and possibly heavy metals, from exhaust gases |
| CN106268194B (en) * | 2016-10-12 | 2022-03-11 | 南京大学 | Gas washing tower for containing sublimable substances |
| AT520926B1 (en) * | 2018-08-17 | 2019-09-15 | Integral Eng Und Umwelttechnik Gmbh | Adsorber for purifying exhaust gases and method therefor |
| AT522436B1 (en) | 2019-04-26 | 2020-11-15 | Integral Eng Und Umwelttechnik Gmbh | Container and method for loading an adsorbent and / or absorbent with ammonia |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1594674A1 (en) * | 1966-05-12 | 1971-04-22 | Bergwerksverband Gmbh | Process for removing sulfur oxides from gases containing them |
| JPS504622B2 (en) * | 1972-10-09 | 1975-02-21 | ||
| JPS4960026A (en) * | 1972-10-13 | 1974-06-11 | ||
| JPS5219557B2 (en) * | 1972-10-24 | 1977-05-28 | ||
| DE2433076A1 (en) * | 1973-07-12 | 1975-02-06 | Takeda Chemical Industries Ltd | METHOD OF REMOVING NITROGEN OXYDES FROM EXHAUST GASES |
| DE2911712C2 (en) * | 1979-03-24 | 1991-10-31 | Bergwerksverband Gmbh, 4300 Essen | Process for removing sulfur oxides and nitrogen oxides from exhaust gases |
| JPS562828A (en) * | 1979-06-21 | 1981-01-13 | Sumitomo Heavy Ind Ltd | Simultaneous removal of sulfur oxide and nitrogen oxide contained in waste gas |
-
1981
- 1981-09-10 JP JP56141702A patent/JPS5843223A/en active Granted
-
1982
- 1982-08-31 AU AU87870/82A patent/AU558983B2/en not_active Ceased
- 1982-09-01 DE DE3232544A patent/DE3232544C2/en not_active Expired - Fee Related
- 1982-09-09 CA CA000411111A patent/CA1193829A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5843223A (en) | 1983-03-12 |
| AU558983B2 (en) | 1987-02-19 |
| JPH0366006B2 (en) | 1991-10-15 |
| DE3232544A1 (en) | 1983-06-30 |
| DE3232544C2 (en) | 1994-03-31 |
| AU8787082A (en) | 1983-03-17 |
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Legal Events
| Date | Code | Title | Description |
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| MKEX | Expiry |