CA2001002A1 - Process for the removal of sulfur dioxide and hydrogen chloride from hot gases - Google Patents
Process for the removal of sulfur dioxide and hydrogen chloride from hot gasesInfo
- Publication number
- CA2001002A1 CA2001002A1 CA 2001002 CA2001002A CA2001002A1 CA 2001002 A1 CA2001002 A1 CA 2001002A1 CA 2001002 CA2001002 CA 2001002 CA 2001002 A CA2001002 A CA 2001002A CA 2001002 A1 CA2001002 A1 CA 2001002A1
- Authority
- CA
- Canada
- Prior art keywords
- hydrogen chloride
- acid
- water
- sulfuric acid
- removal
- 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.)
- Abandoned
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
- B01D53/68—Halogens or halogen compounds
-
- 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
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—Sulfur oxides
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)
- Catalysts (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
A PROCESS FOR THE REMOVAL OF SULFUR DIOXIDE AND HYDROGEN
CHLORIDE FROM HOT GASES
ABSTRACT OF THE DISCLOSURE
In the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which SO2 is catalytically oxidized to H2SO4 on moist active carbon and washed out as thin acid with water, the improvement which comprises concentrating the accumulating mixture of thin hydrochloric and sulfuric acid by evaporation of water and hydrogen chloride in the hot waste gas stream to a 40 to 80 Y. concentrated sulfuric acid, corresponding to the HCl-H2SO4-water equilibrium.
CHLORIDE FROM HOT GASES
ABSTRACT OF THE DISCLOSURE
In the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which SO2 is catalytically oxidized to H2SO4 on moist active carbon and washed out as thin acid with water, the improvement which comprises concentrating the accumulating mixture of thin hydrochloric and sulfuric acid by evaporation of water and hydrogen chloride in the hot waste gas stream to a 40 to 80 Y. concentrated sulfuric acid, corresponding to the HCl-H2SO4-water equilibrium.
Description
A_PROCESS FOR THE REMOVAL OF SULFUR DIOXIDE AND HYDROGEN
CHLORIDE FROM HOT GASES
This invention relates to a process for the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which SO2 is catalytically oxidized to H2SO~ on moist active carbon and washed out with water.
There is a real need for inexpensive, environmentally safe processes for the removal of sulfur dioxide and hydrogen chloride from gases which are formed in power stations or in the chemical industry. The most commonly used processes at present convert sulfur dioxide and hyd_ogen chloride into calcium compounds which are sent to dumps ~or disposal, generally after the removal of water, and hence are still a burden on the overall mass balance.
In ~ddi~i~n, ~E-A 34 35 931 ~ US 4 670 235 dQscrib-s ;-~ proc--- which produc~s a highly conc~n~rated su1~uric acid and hydrochloric acid u~ing ~he wast~ hea~ and ~h~
ca~ly~ic oxida~ion o~ ~u1~ur dioxid~ to H2S04 and absorp~icn o~ hy~rog~n chlorid~ in 5 ~o 25 X s~1~uric aci~ with ub-~qu~nt stripping of a mixture o~ high-conc~ntra~ion ~nd low-conc~ntration HC1-cont~ining sulfuric acid.
The effect of the equilibrium conditions unfavorable for this purpose is that a relatively large stream of hydrogen chloride is established in the plant which, on the one hand, passes into the gas phase during concentration, but which on the other hand cannot be satisfactorily strip-ped after absorption by the thin sulfuric acid because, in view of the lower concentration of sulfuric acid, a higher solubility of hydrogen chloride exists here than in the concentrator. Other substances, such as HF for example, :
Le A 26 177 can also accumulate where this procedure is adopted and can give rise to corrosion problems.
The object of the present invention is to provide an economical, operationally safe, environment-friendly and S simple process in which the described disadvantages do not arise.
This object is achieved in that, for cooling and to utilize the waste heat, the waste gas to be treated is first introduced into a scrubber operated with 40 to 80%
sulfuric acid.
Accordingly, the present invention relates to a process for the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which S0z is cata-lytically oxidized to H2S0~ on moist active carbon and washed out as thin acid with water, characterized in that the mixture of thin hydrochloric and sulfuric acid accumu-lating is concentrated by evaporation of water and hydrogen chloride in the hot waste gas stream to a 40 to 80%
concentrated sulfuric acid corresponding to the HCl-H2S0~-water equilibrium.
In a following scrubber, the hydrogen chloride can be partly absorbed by 5 to 15% hydrochloric acid. The concen-tration of the hydrochloric acid is controlled by addition 2S of fresh water and removal of acid.
In one preferred embodiment of the process according to the invention, therefore, the hydrogen chloride to be removed is converted into hydrochloric acid by washing out the gas stream.
In another advantageous embodiment, however, the hydrogen chloride to be removed can be converted into hydrochloric acid by washing out only a partial ~tream.
A proportion of the hydrogen chloride corresponding to the vapor pressure continues with the gas stream into the active carbon reactor where the gas flows through a bed of Le A 26 177 2 ~ "~ ", " ",, ", . .
20010()2 active c~rbon.
The catalytic oxidation of sulfur dioxide to H2SO~
takes place on the moist active carbon sprinkled intermit-tently or continuously with water, the remaining hydrogen chloride also being absorbed by the solution. The cleaned gas leaves the plant. The mixture of hydrochloric and sul~uric acid formed passes into a scrubber. The desired concentration of acid in the scrubber can be controlled within limits by addition of water.
One preferred embodiment of the process according to the invention is characterized in that the hydrogen chloride is washed out in several scrubbers with different acid concentrations arranged in parall~l or series.
The process acoording to the invention is described in detail in the aco~}ucying drawing wherein Figure 1 i9 schematlc flow sheet of a plant providing a clean gas with an S02 oontent of less than 400 mg/m3n and an HCl oontent of less than 30 mg/m3n. ~t the same time, the waste heat is u~sd for the ooncentration of sulfuric and hydro-chloric acid.
The waste gas (1) is introduced into the scrubber (2) where it is washed with 40 to 80% sulfuric acid. After addition of the thin acid (3) from the active-carbon reac-tor (4), the sulfuric acid from the sump o~ the scrubber (2) is sprayed in the hot waste gas (1) Yia the pump (5) and the nozzles (6) in the upper part of the scrubber (2).
An equilibrium state is established. In other words, the gas cools down and takes up water from the washing liquid (7). The temperature in the scrubber (2) is determined by the gas entry temperature, the initial moisture and the quantity o~ water (81 removed in the active-carbon reactor.
The gas exit temperature (9) is between 80 and llO-C, depending on the desired concentration of acid.
The 40 to 80% sulfuric acid obtained is removed through the submerged overflow (13~.
In the scrubber (2), the gas stream (1) is enriched Le A 26 177 3 -with hydrogen chloride from the thin acid stream (3).
The waste gas (9) is introduced into the scrubber (11) through the droplet separator ~10). The droplets separated in the droplet 6eparator (10) are returned to the scrubber (2) through the pipe (20).
In the scrubber (2), the inflowing waste gas (12) is wa~hed in countercurrent with the hydrochloric acid from the sump of the scrubber (11). The washing liquid is circulated Yi~ the pump (21) and the nozzles (14). Water (15) is fed into the scrubber (11) in such a quantity that a) the necessary concentration of hydrogen chloride is established in the clean gas (16) and b) a highly concentrated hydrochloric acid is obtained in the submerged overflow (17).
The ~olubility of S02 in hydrochloric acid decreases with increasing hydrochloric acid concentration so that only a minimal S02 content is found in the hydrochloric acid flowing off.
The waste gas (12) is further cooled in the scrubber (11) and enters the active-carbon reactor (4) with a tem-perature of 50 to 70-C and substantially saturated with steam.
In the active carbon reactor (4) ~ S2 i6 catalytically oxidized to S03 on the active carbon. A thin sulfuric acid is then formed with the water (8) and, in addition, takes up the hydrogen chloride which was not absorbed in the scrubber (11). The acid mixture (3) formed is introduced into the scrubber (2). The cleaned waste gas (16) is removed Yi~ the fan (18) with a temper~ture of 50 to 70-C.
The reduced-pressure method of operation with a following fan (1~) is advantageous because, in the event of repairs and maintenance work, no waste gas is able to escape from the scrubbers.
The follow Examples are intended to illustrate the invention without limiting it in any way.
Le A 26 177 4 ' ~ ';, ;2001002 Example The components of the individual gas streams are shown in 8he following Example along with the associated temperatures.
The components are: :
1. Water H20 2. Hydrogen chloride HCl 3. Sulfuric acid H2S04 4. Air 5. Sulfur dioxide So2 Waste aas stream ~1~ to ~crubber (2~ kg~h 1. H20 11200 .
2. HCl 76 4. Air .82560 5. S02 143 Temperature ~-C]: 180 93979 Wa~te aas (9~ ~rom scrubber (2~ to scrubber (11~ ~gGh ao 1. H2O 17290 2. HCl 108 . .:.
4. Air 82560 , 5. SO2 143 ; : .
Temperature t-C]: 100 100101 W~a~te gas (19) from scrubber (11) to active-carbon reactor ~4~
kg/h l. H2O . 19421 2. HCl 32 . Air 82560 5. SO2 143 Temperature ~-C]: 72 102156 Le A 26 177 5 ,.~
Waste qas ~16~ from active-carbon reactor 14~ ~
kg/h ..
1. H20 18841 2. HCl 4. Air 82560 5. S02 24 Temperature t-C]: 67 101426 The concentration of S02 in the waste gas is a function o~ the active carbon bed and the temperature Water ~8) to active-carbon reactor t4 ~h 1. H20 6758 Temperature [-C]: 20 Acid mixture ~3) from active-carbon reactor to scrubber t2~
kq~ . .
1. H20 6290 2. HCl 31 3. H2S0~ 183 Temperature t-C]: 67 6504 Sulfuric acid ~13) from scrubber (2) ka/h 1. H20 162 2. HCl 0.03 :. ;
3. H2S0~ j 183 = 53 %
. ~.
T~mperature t-C]: 100 345 Water (15~ to scrubber rll) k~h ~ .
1. H20 3 0OO .
Temperature t-C]: 20 . ~ ' -" ': ;',' Le A 26 177 6 ,'"~' XOO100~
Hydrochloric acid (17) from scrubber ~
ka/h 1. H20 869 2. HCl 75 - 8%
Te~perature ~-C]: 72 944 ~he concentration of hydrogen chloride in the waste gas i~ a ~unction of the hydrochloric acid concentration ~17).
I~ will be apprecia~ed ~ha~ ~he ins~an~ ~peci~iea~ion and claims are 5e~ ror~h by way o~ illu~ra~ion and no~
li~Sa~ion, and ~ha~ various modifications and changes may b- m~d- wi~hou~ depar~ing ~rom ~he ~piri~ and ~cope o~ ~he precen~ inven~ion.
, .':
: ' " ''.''''' ~', ;
, ~.
~" , ~ .
Le A 26 177 7 - ' .'' ' ,:
.. , , ... , . ,. .... , . ~ . . . . .
CHLORIDE FROM HOT GASES
This invention relates to a process for the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which SO2 is catalytically oxidized to H2SO~ on moist active carbon and washed out with water.
There is a real need for inexpensive, environmentally safe processes for the removal of sulfur dioxide and hydrogen chloride from gases which are formed in power stations or in the chemical industry. The most commonly used processes at present convert sulfur dioxide and hyd_ogen chloride into calcium compounds which are sent to dumps ~or disposal, generally after the removal of water, and hence are still a burden on the overall mass balance.
In ~ddi~i~n, ~E-A 34 35 931 ~ US 4 670 235 dQscrib-s ;-~ proc--- which produc~s a highly conc~n~rated su1~uric acid and hydrochloric acid u~ing ~he wast~ hea~ and ~h~
ca~ly~ic oxida~ion o~ ~u1~ur dioxid~ to H2S04 and absorp~icn o~ hy~rog~n chlorid~ in 5 ~o 25 X s~1~uric aci~ with ub-~qu~nt stripping of a mixture o~ high-conc~ntra~ion ~nd low-conc~ntration HC1-cont~ining sulfuric acid.
The effect of the equilibrium conditions unfavorable for this purpose is that a relatively large stream of hydrogen chloride is established in the plant which, on the one hand, passes into the gas phase during concentration, but which on the other hand cannot be satisfactorily strip-ped after absorption by the thin sulfuric acid because, in view of the lower concentration of sulfuric acid, a higher solubility of hydrogen chloride exists here than in the concentrator. Other substances, such as HF for example, :
Le A 26 177 can also accumulate where this procedure is adopted and can give rise to corrosion problems.
The object of the present invention is to provide an economical, operationally safe, environment-friendly and S simple process in which the described disadvantages do not arise.
This object is achieved in that, for cooling and to utilize the waste heat, the waste gas to be treated is first introduced into a scrubber operated with 40 to 80%
sulfuric acid.
Accordingly, the present invention relates to a process for the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which S0z is cata-lytically oxidized to H2S0~ on moist active carbon and washed out as thin acid with water, characterized in that the mixture of thin hydrochloric and sulfuric acid accumu-lating is concentrated by evaporation of water and hydrogen chloride in the hot waste gas stream to a 40 to 80%
concentrated sulfuric acid corresponding to the HCl-H2S0~-water equilibrium.
In a following scrubber, the hydrogen chloride can be partly absorbed by 5 to 15% hydrochloric acid. The concen-tration of the hydrochloric acid is controlled by addition 2S of fresh water and removal of acid.
In one preferred embodiment of the process according to the invention, therefore, the hydrogen chloride to be removed is converted into hydrochloric acid by washing out the gas stream.
In another advantageous embodiment, however, the hydrogen chloride to be removed can be converted into hydrochloric acid by washing out only a partial ~tream.
A proportion of the hydrogen chloride corresponding to the vapor pressure continues with the gas stream into the active carbon reactor where the gas flows through a bed of Le A 26 177 2 ~ "~ ", " ",, ", . .
20010()2 active c~rbon.
The catalytic oxidation of sulfur dioxide to H2SO~
takes place on the moist active carbon sprinkled intermit-tently or continuously with water, the remaining hydrogen chloride also being absorbed by the solution. The cleaned gas leaves the plant. The mixture of hydrochloric and sul~uric acid formed passes into a scrubber. The desired concentration of acid in the scrubber can be controlled within limits by addition of water.
One preferred embodiment of the process according to the invention is characterized in that the hydrogen chloride is washed out in several scrubbers with different acid concentrations arranged in parall~l or series.
The process acoording to the invention is described in detail in the aco~}ucying drawing wherein Figure 1 i9 schematlc flow sheet of a plant providing a clean gas with an S02 oontent of less than 400 mg/m3n and an HCl oontent of less than 30 mg/m3n. ~t the same time, the waste heat is u~sd for the ooncentration of sulfuric and hydro-chloric acid.
The waste gas (1) is introduced into the scrubber (2) where it is washed with 40 to 80% sulfuric acid. After addition of the thin acid (3) from the active-carbon reac-tor (4), the sulfuric acid from the sump o~ the scrubber (2) is sprayed in the hot waste gas (1) Yia the pump (5) and the nozzles (6) in the upper part of the scrubber (2).
An equilibrium state is established. In other words, the gas cools down and takes up water from the washing liquid (7). The temperature in the scrubber (2) is determined by the gas entry temperature, the initial moisture and the quantity o~ water (81 removed in the active-carbon reactor.
The gas exit temperature (9) is between 80 and llO-C, depending on the desired concentration of acid.
The 40 to 80% sulfuric acid obtained is removed through the submerged overflow (13~.
In the scrubber (2), the gas stream (1) is enriched Le A 26 177 3 -with hydrogen chloride from the thin acid stream (3).
The waste gas (9) is introduced into the scrubber (11) through the droplet separator ~10). The droplets separated in the droplet 6eparator (10) are returned to the scrubber (2) through the pipe (20).
In the scrubber (2), the inflowing waste gas (12) is wa~hed in countercurrent with the hydrochloric acid from the sump of the scrubber (11). The washing liquid is circulated Yi~ the pump (21) and the nozzles (14). Water (15) is fed into the scrubber (11) in such a quantity that a) the necessary concentration of hydrogen chloride is established in the clean gas (16) and b) a highly concentrated hydrochloric acid is obtained in the submerged overflow (17).
The ~olubility of S02 in hydrochloric acid decreases with increasing hydrochloric acid concentration so that only a minimal S02 content is found in the hydrochloric acid flowing off.
The waste gas (12) is further cooled in the scrubber (11) and enters the active-carbon reactor (4) with a tem-perature of 50 to 70-C and substantially saturated with steam.
In the active carbon reactor (4) ~ S2 i6 catalytically oxidized to S03 on the active carbon. A thin sulfuric acid is then formed with the water (8) and, in addition, takes up the hydrogen chloride which was not absorbed in the scrubber (11). The acid mixture (3) formed is introduced into the scrubber (2). The cleaned waste gas (16) is removed Yi~ the fan (18) with a temper~ture of 50 to 70-C.
The reduced-pressure method of operation with a following fan (1~) is advantageous because, in the event of repairs and maintenance work, no waste gas is able to escape from the scrubbers.
The follow Examples are intended to illustrate the invention without limiting it in any way.
Le A 26 177 4 ' ~ ';, ;2001002 Example The components of the individual gas streams are shown in 8he following Example along with the associated temperatures.
The components are: :
1. Water H20 2. Hydrogen chloride HCl 3. Sulfuric acid H2S04 4. Air 5. Sulfur dioxide So2 Waste aas stream ~1~ to ~crubber (2~ kg~h 1. H20 11200 .
2. HCl 76 4. Air .82560 5. S02 143 Temperature ~-C]: 180 93979 Wa~te aas (9~ ~rom scrubber (2~ to scrubber (11~ ~gGh ao 1. H2O 17290 2. HCl 108 . .:.
4. Air 82560 , 5. SO2 143 ; : .
Temperature t-C]: 100 100101 W~a~te gas (19) from scrubber (11) to active-carbon reactor ~4~
kg/h l. H2O . 19421 2. HCl 32 . Air 82560 5. SO2 143 Temperature ~-C]: 72 102156 Le A 26 177 5 ,.~
Waste qas ~16~ from active-carbon reactor 14~ ~
kg/h ..
1. H20 18841 2. HCl 4. Air 82560 5. S02 24 Temperature t-C]: 67 101426 The concentration of S02 in the waste gas is a function o~ the active carbon bed and the temperature Water ~8) to active-carbon reactor t4 ~h 1. H20 6758 Temperature [-C]: 20 Acid mixture ~3) from active-carbon reactor to scrubber t2~
kq~ . .
1. H20 6290 2. HCl 31 3. H2S0~ 183 Temperature t-C]: 67 6504 Sulfuric acid ~13) from scrubber (2) ka/h 1. H20 162 2. HCl 0.03 :. ;
3. H2S0~ j 183 = 53 %
. ~.
T~mperature t-C]: 100 345 Water (15~ to scrubber rll) k~h ~ .
1. H20 3 0OO .
Temperature t-C]: 20 . ~ ' -" ': ;',' Le A 26 177 6 ,'"~' XOO100~
Hydrochloric acid (17) from scrubber ~
ka/h 1. H20 869 2. HCl 75 - 8%
Te~perature ~-C]: 72 944 ~he concentration of hydrogen chloride in the waste gas i~ a ~unction of the hydrochloric acid concentration ~17).
I~ will be apprecia~ed ~ha~ ~he ins~an~ ~peci~iea~ion and claims are 5e~ ror~h by way o~ illu~ra~ion and no~
li~Sa~ion, and ~ha~ various modifications and changes may b- m~d- wi~hou~ depar~ing ~rom ~he ~piri~ and ~cope o~ ~he precen~ inven~ion.
, .':
: ' " ''.''''' ~', ;
, ~.
~" , ~ .
Le A 26 177 7 - ' .'' ' ,:
.. , , ... , . ,. .... , . ~ . . . . .
Claims (4)
1. In the removal of sulfur dioxide and hydrogen chloride from waste gases with simultaneous production of sulfuric acid and hydrochloric acid, in which SO2 is catalytically oxidized to H2SO4 on moist active carbon and washed out as thin acid with water, the improvement which comprises concentrating the accumulting mixture of thin hydrochloric and sulfuric acid by evaporation of water and hydrogen choride in the hot waste gas stream to a 40 to 80% concentrated sulfuric acid, corresponding to the HCl-H2SO4-water equilibrium.
2. The process according to claim 1, wherein the hydrogen chloride to be removed is converted into hydrochloric acid by washing out the gas stream.
3. The process according to claim 1, wherein the hydrogen chloride to be removed is converted into hydrochloric acid by washing out a partial gas stream.
4. The process according to claim 1, wherein the hydrogen chloride to be removed is washed out in several scrubbers with different acid concentrations arranged in parallel or in series.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19883835934 DE3835934A1 (en) | 1988-10-21 | 1988-10-21 | METHOD FOR REMOVING SULFUR DIOXIDE AND HYDROGEN CHLORIDE FROM HOT GASES |
| DEP3835934.0 | 1988-10-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2001002A1 true CA2001002A1 (en) | 1990-04-21 |
Family
ID=6365648
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2001002 Abandoned CA2001002A1 (en) | 1988-10-21 | 1989-10-19 | Process for the removal of sulfur dioxide and hydrogen chloride from hot gases |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP0367998A3 (en) |
| JP (1) | JPH02160020A (en) |
| CA (1) | CA2001002A1 (en) |
| DE (1) | DE3835934A1 (en) |
| FI (1) | FI894979A0 (en) |
| NO (1) | NO893954L (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2694001B1 (en) * | 1992-07-23 | 1994-09-02 | Atochem Elf Sa | Process for the synthesis of chloracetic acid in which the hydrochloric acid is purified by product. |
| DE19521200B4 (en) * | 1995-06-10 | 2006-06-29 | Fluorchemie Dohna Gmbh | Process for the removal of hydrogen chloride from hydrofluoric acid |
| DE19849021A1 (en) * | 1998-10-23 | 2000-04-27 | Abb Research Ltd | Reduction of corrosion in refuse incinerators by preventing the formation of free chlorine as flue gas, high in sulfur dioxide, is recirculated into the combustion chamber |
| TWI300011B (en) | 2004-11-10 | 2008-08-21 | Ind Tech Res Inst | Method and apparatus for treating inorganic acid gas |
| KR100634173B1 (en) * | 2006-06-23 | 2006-10-16 | 주식회사 이즈컨텍 | waste gas purification apparatus |
| LU92547B1 (en) * | 2014-09-17 | 2016-03-18 | Cppe Carbon Process & Plant Engineering S A | METHOD FOR THE CATALYTIC REMOVAL OF SULFUR DIOXIDE FROM EXHAUST GASES |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5023383B1 (en) * | 1970-07-29 | 1975-08-07 | ||
| DE2235123A1 (en) * | 1972-07-18 | 1974-02-07 | Metallgesellschaft Ag | Removal of sulphur dioxide from waste gases - by upward flow through catalyst beds and conversion to sulphuric acid |
| JPS5929521B2 (en) * | 1980-02-20 | 1984-07-21 | チッソ株式会社 | Manufacturing method of purified hydrochloric acid |
| DE3435931A1 (en) * | 1984-09-29 | 1986-04-03 | Bayer Ag, 5090 Leverkusen | METHOD FOR DESULFURING SMOKE GASES |
| DE3629765A1 (en) * | 1986-09-02 | 1988-03-03 | Bayer Ag | METHOD FOR PURIFYING EXHAUST GASES |
-
1988
- 1988-10-21 DE DE19883835934 patent/DE3835934A1/en not_active Withdrawn
-
1989
- 1989-10-04 NO NO89893954A patent/NO893954L/en unknown
- 1989-10-07 EP EP19890118690 patent/EP0367998A3/en not_active Withdrawn
- 1989-10-17 JP JP1268305A patent/JPH02160020A/en active Pending
- 1989-10-19 FI FI894979A patent/FI894979A0/en not_active Application Discontinuation
- 1989-10-19 CA CA 2001002 patent/CA2001002A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| DE3835934A1 (en) | 1990-04-26 |
| NO893954D0 (en) | 1989-10-04 |
| EP0367998A3 (en) | 1990-09-26 |
| NO893954L (en) | 1990-04-23 |
| EP0367998A2 (en) | 1990-05-16 |
| FI894979A0 (en) | 1989-10-19 |
| JPH02160020A (en) | 1990-06-20 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Dead |