CA2511311C - Process for removal of so2 from off-gases by reaction with h2o2 - Google Patents
Process for removal of so2 from off-gases by reaction with h2o2 Download PDFInfo
- Publication number
- CA2511311C CA2511311C CA2511311A CA2511311A CA2511311C CA 2511311 C CA2511311 C CA 2511311C CA 2511311 A CA2511311 A CA 2511311A CA 2511311 A CA2511311 A CA 2511311A CA 2511311 C CA2511311 C CA 2511311C
- Authority
- CA
- Canada
- Prior art keywords
- gas
- gases
- removal
- reaction
- acid
- 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 - Lifetime
Links
- 239000007789 gas Substances 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000006243 chemical reaction Methods 0.000 title description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 10
- 235000011149 sulphuric acid Nutrition 0.000 claims abstract description 10
- 239000000443 aerosol Substances 0.000 claims abstract description 9
- 239000001117 sulphuric acid Substances 0.000 claims abstract description 8
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 6
- 239000007864 aqueous solution Substances 0.000 claims abstract description 5
- 238000005507 spraying Methods 0.000 claims abstract description 4
- 239000000243 solution Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims description 2
- 229910003556 H2 SO4 Inorganic materials 0.000 abstract 1
- 239000002253 acid Substances 0.000 description 12
- 239000003595 mist Substances 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000012719 wet electrostatic precipitator Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229920000136 polysorbate Polymers 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
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
-
- 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
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
- F23J2217/102—Intercepting solids by filters electrostatic
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/40—Sorption with wet devices, e.g. scrubbers
Abstract
A process for removal of SO2 in off-gases having a temperature of 30-150~C and containing 0.001-1 vol% SO2 in which the SO2 is oxidised to H2 SO4 by spraying an aqueous solution of H2O2 into the off-gas upstream of an aerosol filter removing the produced sulphuric acid from the off-gas.
Description
Process for Removal of S02 from Off Gases by Reaction with H2O2 The present invention relates to a process for removal of SO~ from off-gases by reaction with H202.
It has been known for more than 30 years that SO~, as de-scribed in the publication 2164e from Lurgi/Sudchemie AG, August 1989, can be removed from off-gases by contacting the off-gas in an absorption tower with circulating solu-tion of dilute sulphuric acid containing H20~, whereby SOZ
is dissolved and oxidised to H2S04 in the solution. The circulating solution typically contains 30-60o H2S04 and 0.1-0.5% H~O2. The absorption is typically carried out at a temperature of 50-80°C of the circulating solution. H~02 is added either as a concentrated aqueous solution of H20~ to the circulating acid, or it is produced by electrolysis of a side stream of the circulating acid. The produced acid is drawn off from the circulating acid.
The known process usually requires installation of a low velocity aerosol filter downstream of the absorption tower to remove sulphuric acid aerosol (acid mist) in order to meet acid mist emission regulations requiring less than about 5 mol ppm H~S04 in the stack gas. Fine acid mist (aerosol) that may be present in the off-gas is not removed efficiently in the absorption tower. Fine acid mist is also formed in the absorption tower itself by reaction between S02 and H~02 vaporised from the absorbing liquid.
It is a disadvantage of the known process that it requires installation of both an absorption tower and a low velocity mist filter.
It has been known for more than 30 years that SO~, as de-scribed in the publication 2164e from Lurgi/Sudchemie AG, August 1989, can be removed from off-gases by contacting the off-gas in an absorption tower with circulating solu-tion of dilute sulphuric acid containing H20~, whereby SOZ
is dissolved and oxidised to H2S04 in the solution. The circulating solution typically contains 30-60o H2S04 and 0.1-0.5% H~O2. The absorption is typically carried out at a temperature of 50-80°C of the circulating solution. H~02 is added either as a concentrated aqueous solution of H20~ to the circulating acid, or it is produced by electrolysis of a side stream of the circulating acid. The produced acid is drawn off from the circulating acid.
The known process usually requires installation of a low velocity aerosol filter downstream of the absorption tower to remove sulphuric acid aerosol (acid mist) in order to meet acid mist emission regulations requiring less than about 5 mol ppm H~S04 in the stack gas. Fine acid mist (aerosol) that may be present in the off-gas is not removed efficiently in the absorption tower. Fine acid mist is also formed in the absorption tower itself by reaction between S02 and H~02 vaporised from the absorbing liquid.
It is a disadvantage of the known process that it requires installation of both an absorption tower and a low velocity mist filter.
2 In the process according to the present invention, SOz in off-gases is removed by reaction with H~Oz without the use of an absorption tower by spraying a solution of H20~ in water or dilute sulphuric acid into the off-gas upstream of a low velocity aerosol filter or wet electrostatic precipi-tator (WESP) .
A preferred embodiment of the invention is shown in Fig. 1.
A solution of 0.1-30% H~OZ in line 1 is sprayed by the spray nozzles 3 into a stream of off-gas in line 2 contain-ing typically between 100-1000 ppm S02 and having a tem-perature typically in the range of 50-120°C. The nozzles are placed in duct 4, so that the spray is evenly distrib-uted in the gas stream upstream of the mist filter 5 in which the gas is passed in parallel through a number of low velocity'filter candles 6. Even distribution of the drop-lets in the gas is desirable for the process and the most even distribution of the droplets is achieved by using air-atomising nozzles producing very small droplets. The H2S04 formed in the process accumulates in the filter elements or candles from which it is drained off through line~7. Most or all of the mass of the droplets evaporate before the gas enters the filter candles, whereby most of the H202 evapo-rates and reacts in the gas phase under formation of sul-phuric acid aerosol. However, it is not necessary that the droplets are completely evaporated before the gas enters the filter elements. The reaction between SOZ and H~OZ will be completed and the thermal equilibrium will be estab-lished in the mist filter elements without decreasing the efficiency of the S02-removal.
A preferred embodiment of the invention is shown in Fig. 1.
A solution of 0.1-30% H~OZ in line 1 is sprayed by the spray nozzles 3 into a stream of off-gas in line 2 contain-ing typically between 100-1000 ppm S02 and having a tem-perature typically in the range of 50-120°C. The nozzles are placed in duct 4, so that the spray is evenly distrib-uted in the gas stream upstream of the mist filter 5 in which the gas is passed in parallel through a number of low velocity'filter candles 6. Even distribution of the drop-lets in the gas is desirable for the process and the most even distribution of the droplets is achieved by using air-atomising nozzles producing very small droplets. The H2S04 formed in the process accumulates in the filter elements or candles from which it is drained off through line~7. Most or all of the mass of the droplets evaporate before the gas enters the filter candles, whereby most of the H202 evapo-rates and reacts in the gas phase under formation of sul-phuric acid aerosol. However, it is not necessary that the droplets are completely evaporated before the gas enters the filter elements. The reaction between SOZ and H~OZ will be completed and the thermal equilibrium will be estab-lished in the mist filter elements without decreasing the efficiency of the S02-removal.
3 Thus, the injection of the aqueous solution H~Oz serves two purposes:
Firstly, it adds to the off-gas the amount of HzO~, which is required for achieving the desired conversion of SOz into H2S04 by the reaction H~02 + SOz = HzS04 Most of the conversion takes place by reaction in the gas phase between S02 and vaporised Hz02 under formation of acid mist or between S0~ and Hz02 dissolved in the droplets. The reaction is completed in the aerosol filter in which re-maining S02 is absorbed and reacts with remaining H~02 Con-tamed in the dilute sulphuric acid wetting the fibre mate-rial.
Secondly, the water comprised in the solution cools off the off-gas in line 2 by evaporation of the droplets, whereby the off-gas is cooled off to a desired temperature of the filter elements or candles typically to a temperature be-tween 50°C and 70°C. The concentration of HzS04 in the pro-duced acid will be the equilibrium concentration of H2S04 at the actual temperature and HBO partial pressure in the gas phase.
Up to 98o S02-removal can be achieved at, typically, about 95 o utilisation of the H~02 .
Firstly, it adds to the off-gas the amount of HzO~, which is required for achieving the desired conversion of SOz into H2S04 by the reaction H~02 + SOz = HzS04 Most of the conversion takes place by reaction in the gas phase between S02 and vaporised Hz02 under formation of acid mist or between S0~ and Hz02 dissolved in the droplets. The reaction is completed in the aerosol filter in which re-maining S02 is absorbed and reacts with remaining H~02 Con-tamed in the dilute sulphuric acid wetting the fibre mate-rial.
Secondly, the water comprised in the solution cools off the off-gas in line 2 by evaporation of the droplets, whereby the off-gas is cooled off to a desired temperature of the filter elements or candles typically to a temperature be-tween 50°C and 70°C. The concentration of HzS04 in the pro-duced acid will be the equilibrium concentration of H2S04 at the actual temperature and HBO partial pressure in the gas phase.
Up to 98o S02-removal can be achieved at, typically, about 95 o utilisation of the H~02 .
4 EXAMPLE
An off-gas stream of 1000 Nm3/h at 100°C contains 200 ppm S02 + 10% H20 and has a temperature of 100°C. 96% SO~ re-moval is desired. The aerosol filter is designed for opera-s tion at maximum 70°C. Operation at 67-70°C is chosen in or-der to achieve the highest possible acid strength and low content of remaining Hz02 in the produced acid.
The process is conducted as follows: 15.7 kg/h water con-taming 2.0 wt% H20z is injected into the off-gas, whereby the off-gas is cooled to 65-70°C in thermal equilibrium.
The mist filter is 75 mm thick and has a flow area of 2.5 m2. The diameter of the fibres is about 8 ~,m. Experiments carried out under these conditions show that about 96% of the SOz is removed under production of 1.7 kg/h 50% H~S04 with about 500 ppm H20~. The treated gas contains less than 2 ppm HZS04 and the content of H~02 is below the detection limit.
An off-gas stream of 1000 Nm3/h at 100°C contains 200 ppm S02 + 10% H20 and has a temperature of 100°C. 96% SO~ re-moval is desired. The aerosol filter is designed for opera-s tion at maximum 70°C. Operation at 67-70°C is chosen in or-der to achieve the highest possible acid strength and low content of remaining Hz02 in the produced acid.
The process is conducted as follows: 15.7 kg/h water con-taming 2.0 wt% H20z is injected into the off-gas, whereby the off-gas is cooled to 65-70°C in thermal equilibrium.
The mist filter is 75 mm thick and has a flow area of 2.5 m2. The diameter of the fibres is about 8 ~,m. Experiments carried out under these conditions show that about 96% of the SOz is removed under production of 1.7 kg/h 50% H~S04 with about 500 ppm H20~. The treated gas contains less than 2 ppm HZS04 and the content of H~02 is below the detection limit.
Claims (3)
1. A process for removal of SO2 in off-gases having a temperature of 30-150°C and containing 0.001-1 vol% SO2 in which the SO2 is oxidized to H2SO4 by spraying an aqueous solution of H2O2 into the off-gas upstream of an aerosol filter removing the produced sulphuric acid from the off-gas.
2. A process as in claim 1, in which the off-gas is cooled by evaporation of the water comprised in the solution being sprayed into the off-gas upstream of the filter.
3. A process for removal of SO2 in off-gases having a temperature of 30-150°C and containing 0.001-1 vol% SO2 in which the SO2 is oxidized to H2SO4 by spraying an aqueous solution of H2O2 into the off-gas upstream of a wet electro-static separator removing the produced sulphuric acid from the off-gas.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DKPA200201992 | 2002-12-21 | ||
| DKPA200201992 | 2002-12-21 | ||
| PCT/EP2003/013699 WO2004056449A2 (en) | 2002-12-21 | 2003-12-04 | Process for removal of so2 from off-gases by reaction with h202 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2511311A1 CA2511311A1 (en) | 2004-07-08 |
| CA2511311C true CA2511311C (en) | 2011-09-20 |
Family
ID=32668631
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2511311A Expired - Lifetime CA2511311C (en) | 2002-12-21 | 2003-12-04 | Process for removal of so2 from off-gases by reaction with h2o2 |
Country Status (13)
| Country | Link |
|---|---|
| US (1) | US7776299B2 (en) |
| EP (1) | EP1578517B1 (en) |
| JP (1) | JP2006512190A (en) |
| KR (1) | KR20050084454A (en) |
| CN (1) | CN100354028C (en) |
| AT (1) | ATE388751T1 (en) |
| AU (1) | AU2003288228B2 (en) |
| BR (1) | BR0317462B1 (en) |
| CA (1) | CA2511311C (en) |
| DE (1) | DE60319738T2 (en) |
| ES (1) | ES2300632T3 (en) |
| RU (1) | RU2346731C2 (en) |
| WO (1) | WO2004056449A2 (en) |
Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7404938B2 (en) * | 2004-05-11 | 2008-07-29 | The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration | Emission control system |
| DE102005041794A1 (en) * | 2005-09-02 | 2007-03-08 | Basf Ag | Method and apparatus for removing sulfur dioxide from a dry gas stream |
| CN100393393C (en) * | 2006-03-30 | 2008-06-11 | 国电科技环保集团有限公司 | Arrangement for sprinkling and pre-washing flue gas in entrance of flue gas-desulfurizing absorption tower |
| CN100463847C (en) * | 2006-06-23 | 2009-02-25 | 李开春 | Method for preparing vitriol from flue gas |
| DE102007020141A1 (en) * | 2007-04-26 | 2008-10-30 | Bayer Materialscience Ag | Recycle gas scrubber for the removal of SOx and sulfuric acid aerosols from chlorine-containing process gases |
| DE102007039926B4 (en) * | 2007-08-23 | 2012-03-22 | Götaverken Miljö AB | Method and device for exhaust gas purification |
| KR101039715B1 (en) * | 2009-01-23 | 2011-06-13 | 엘에스니꼬동제련 주식회사 | Method of Treating a By-product Gas from Copper Smelting |
| KR101341967B1 (en) * | 2012-06-22 | 2013-12-16 | 한국에너지기술연구원 | Method for producing hydrogen and sulfuric acid from sulfur dioxide using electrochemical process |
| US8877152B2 (en) * | 2013-02-27 | 2014-11-04 | Alstom Technology Ltd | Oxidation system and method for cleaning waste combustion flue gas |
| CN103657375B (en) * | 2014-01-07 | 2015-07-08 | 上海科洋科技股份有限公司 | Method and system for removing trace SO2 in tail gas by gas phase oxidation |
| WO2017202582A1 (en) | 2016-05-24 | 2017-11-30 | Haldor Topsøe A/S | A method for the removal of oxygen from an industrial gas |
| EP3582880A1 (en) | 2017-02-16 | 2019-12-25 | Haldor Topsøe A/S | A method for the removal of oxygen from an industrial gas feed |
| CA3055008A1 (en) * | 2017-03-08 | 2018-09-13 | Shell Internationale Research Maatschappij B.V. | Process for removing so2 from gas with so2 content that is temporarily very high |
| CN107970911B (en) * | 2017-12-01 | 2020-10-13 | 南京云高新型材料有限公司 | Environment-friendly energy-saving high-conversion-rate rare earth catalyst and preparation method thereof |
| CN110407181A (en) * | 2019-08-19 | 2019-11-05 | 广东新生环保科技股份有限公司 | A kind of tail gas sulphur dioxide relieving haperacidity recovery system |
| US11071947B2 (en) | 2019-10-30 | 2021-07-27 | W. L. Gore & Associates, Inc. | Catalytic efficiency of flue gas filtration |
| US10940471B1 (en) | 2019-10-30 | 2021-03-09 | W. L. Gore & Associates, Inc. | Catalytic efficiency of flue gas filtration |
Family Cites Families (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE436899C (en) | 1926-11-09 | August Henze | Freischaeler for beet harvesters | |
| US3503704A (en) | 1966-10-03 | 1970-03-31 | Alvin M Marks | Method and apparatus for suppressing fumes with charged aerosols |
| FR2106950A5 (en) * | 1970-09-30 | 1972-05-05 | Air Liquide | |
| US3760061A (en) * | 1971-03-02 | 1973-09-18 | Du Pont | High-strength acid containing h2o2 to scrub so2 |
| BE794918A (en) * | 1972-02-04 | 1973-08-02 | Oxysynthese | PROCESS FOR CLEANING INDUSTRIAL FUMES, COMBUSTION PRODUCTS AND GASEOUS EFFLENTS BEFORE RELEASE TO THE ATMOSPHERE |
| CA1069273A (en) | 1974-05-23 | 1980-01-08 | Fmc Corporation | Purification of sulfur-containing waste gases with hydrogen peroxide |
| JPS53135878A (en) | 1977-04-30 | 1978-11-27 | Ishikawajima Harima Heavy Ind Co Ltd | Wet denitrating or wet denitrating and desulurizing method |
| DE3237699A1 (en) | 1982-10-12 | 1984-04-12 | Toschi Produktions-Gesellschaft mbH, 2800 Bremen | METHOD FOR SEPARATING AIR POLLUTANTS FROM EXHAUST GAS, IN PARTICULAR FROM FLUE GAS, BY CONDENSATION |
| CA1159773A (en) * | 1981-09-30 | 1984-01-03 | George Drzewiecki | Wet electrostatic precipitator having removable nested hexagonal collector plates and magnetic aligning and rapping means |
| JPS60153923A (en) | 1984-01-25 | 1985-08-13 | Hitachi Zosen Corp | Recovery of available component in high temperature gas |
| US4678481A (en) * | 1986-09-02 | 1987-07-07 | Nalco Chemical Company | H2 O2 as a conditioning agent for electrostatic precipitators |
| DK168702B1 (en) * | 1988-06-02 | 1994-05-24 | Topsoe Haldor As | Process for preparing sulfuric acid and apparatus for use in the practice of the process |
| US5017350A (en) * | 1989-06-02 | 1991-05-21 | Union Carbide Canada Limited | Gas scrubbing process |
| DE4036899C2 (en) * | 1990-11-20 | 2001-10-25 | Degussa | Process for the desulphurisation of moist exhaust gases containing SO¶2¶ and device for carrying out the process |
| CN2133353Y (en) * | 1992-09-17 | 1993-05-19 | 王明环 | Smoke sweetening duster for coal boiler |
| JPH06142440A (en) | 1992-11-13 | 1994-05-24 | Nippon Steel Corp | Oxidation treatment of gas containing harmful gas and device for the same |
| DE4424367A1 (en) * | 1994-07-11 | 1996-01-18 | Siemens Ag | Process and appts. to purify flue gas |
| US5595713A (en) * | 1994-09-08 | 1997-01-21 | The Babcock & Wilcox Company | Hydrogen peroxide for flue gas desulfurization |
| CN1173386A (en) * | 1996-08-12 | 1998-02-18 | 中国科学院生态环境中心 | Flue gas desulphurization process |
| US20040062697A1 (en) * | 2002-10-01 | 2004-04-01 | Airborne Pollution Control Inc. | Flue gas purification method |
-
2003
- 2003-12-04 DE DE60319738T patent/DE60319738T2/en not_active Expired - Lifetime
- 2003-12-04 EP EP03780121A patent/EP1578517B1/en not_active Expired - Lifetime
- 2003-12-04 JP JP2004561212A patent/JP2006512190A/en active Pending
- 2003-12-04 US US10/539,604 patent/US7776299B2/en active Active
- 2003-12-04 CA CA2511311A patent/CA2511311C/en not_active Expired - Lifetime
- 2003-12-04 ES ES03780121T patent/ES2300632T3/en not_active Expired - Lifetime
- 2003-12-04 BR BRPI0317462-0A patent/BR0317462B1/en active IP Right Grant
- 2003-12-04 CN CNB2003801067013A patent/CN100354028C/en not_active Ceased
- 2003-12-04 AT AT03780121T patent/ATE388751T1/en active
- 2003-12-04 AU AU2003288228A patent/AU2003288228B2/en not_active Expired
- 2003-12-04 RU RU2005123041/15A patent/RU2346731C2/en active
- 2003-12-04 KR KR1020057011703A patent/KR20050084454A/en active Search and Examination
- 2003-12-04 WO PCT/EP2003/013699 patent/WO2004056449A2/en active IP Right Grant
Also Published As
| Publication number | Publication date |
|---|---|
| CA2511311A1 (en) | 2004-07-08 |
| US20060057047A1 (en) | 2006-03-16 |
| WO2004056449A2 (en) | 2004-07-08 |
| CN1729039A (en) | 2006-02-01 |
| DE60319738D1 (en) | 2008-04-24 |
| EP1578517B1 (en) | 2008-03-12 |
| AU2003288228A1 (en) | 2004-07-14 |
| BR0317462B1 (en) | 2013-02-05 |
| JP2006512190A (en) | 2006-04-13 |
| RU2005123041A (en) | 2006-01-27 |
| CN100354028C (en) | 2007-12-12 |
| DE60319738T2 (en) | 2009-04-02 |
| US7776299B2 (en) | 2010-08-17 |
| KR20050084454A (en) | 2005-08-26 |
| RU2346731C2 (en) | 2009-02-20 |
| BR0317462A (en) | 2005-11-16 |
| ATE388751T1 (en) | 2008-03-15 |
| AU2003288228B2 (en) | 2009-08-06 |
| WO2004056449A3 (en) | 2004-09-30 |
| EP1578517A2 (en) | 2005-09-28 |
| ES2300632T3 (en) | 2008-06-16 |
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Effective date: 20231204 |