NO751818L - - Google Patents
Info
- Publication number
- NO751818L NO751818L NO751818A NO751818A NO751818L NO 751818 L NO751818 L NO 751818L NO 751818 A NO751818 A NO 751818A NO 751818 A NO751818 A NO 751818A NO 751818 L NO751818 L NO 751818L
- Authority
- NO
- Norway
- Prior art keywords
- sulfur
- hydrogen peroxide
- solution
- exhaust gas
- gas stream
- Prior art date
Links
- 239000007789 gas Substances 0.000 claims description 93
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 70
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 45
- 238000000034 method Methods 0.000 claims description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 38
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 28
- 229910052717 sulfur Inorganic materials 0.000 claims description 28
- 239000011593 sulfur Substances 0.000 claims description 27
- 239000000243 solution Substances 0.000 claims description 20
- 239000002912 waste gas Substances 0.000 claims description 20
- 239000007864 aqueous solution Substances 0.000 claims description 17
- 150000003568 thioethers Chemical class 0.000 claims description 16
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 15
- -1 aliphatic thiols Chemical class 0.000 claims description 13
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims description 12
- 239000005864 Sulphur Substances 0.000 claims description 11
- 150000002898 organic sulfur compounds Chemical class 0.000 claims description 9
- 229930192474 thiophene Natural products 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 7
- 150000003577 thiophenes Chemical class 0.000 claims description 7
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 5
- 230000001590 oxidative effect Effects 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 4
- SUVIGLJNEAMWEG-UHFFFAOYSA-N propane-1-thiol Chemical compound CCCS SUVIGLJNEAMWEG-UHFFFAOYSA-N 0.000 claims description 4
- 238000007710 freezing Methods 0.000 claims description 3
- 230000008014 freezing Effects 0.000 claims description 3
- 229920001021 polysulfide Polymers 0.000 claims description 3
- WQAQPCDUOCURKW-UHFFFAOYSA-N butanethiol Chemical compound CCCCS WQAQPCDUOCURKW-UHFFFAOYSA-N 0.000 claims description 2
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 description 21
- 230000003647 oxidation Effects 0.000 description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 238000010521 absorption reaction Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 7
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 4
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- LJSQFQKUNVCTIA-UHFFFAOYSA-N diethyl sulfide Chemical compound CCSCC LJSQFQKUNVCTIA-UHFFFAOYSA-N 0.000 description 4
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 4
- 230000009931 harmful effect Effects 0.000 description 4
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 150000003464 sulfur compounds Chemical class 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RGHNJXZEOKUKBD-SQOUGZDYSA-N D-gluconic acid Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C(O)=O RGHNJXZEOKUKBD-SQOUGZDYSA-N 0.000 description 2
- CETBSQOFQKLHHZ-UHFFFAOYSA-N Diethyl disulfide Chemical compound CCSSCC CETBSQOFQKLHHZ-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical class [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical class [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 231100001231 less toxic Toxicity 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 239000003440 toxic substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 1
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical class [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- RGHNJXZEOKUKBD-UHFFFAOYSA-N D-gluconic acid Natural products OCC(O)C(O)C(O)C(O)C(O)=O RGHNJXZEOKUKBD-UHFFFAOYSA-N 0.000 description 1
- HTIRHQRTDBPHNZ-UHFFFAOYSA-N Dibutyl sulfide Chemical compound CCCCSCCCC HTIRHQRTDBPHNZ-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Chemical class 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical class [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 239000008139 complexing agent Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Chemical class 0.000 description 1
- XYWDPYKBIRQXQS-UHFFFAOYSA-N di-isopropyl sulphide Natural products CC(C)SC(C)C XYWDPYKBIRQXQS-UHFFFAOYSA-N 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- VDQVEACBQKUUSU-UHFFFAOYSA-M disodium;sulfanide Chemical compound [Na+].[Na+].[SH-] VDQVEACBQKUUSU-UHFFFAOYSA-M 0.000 description 1
- 150000002019 disulfides Chemical class 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000174 gluconic acid Substances 0.000 description 1
- 235000012208 gluconic acid Nutrition 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000011630 iodine Substances 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical class [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- WXEHBUMAEPOYKP-UHFFFAOYSA-N methylsulfanylethane Chemical compound CCSC WXEHBUMAEPOYKP-UHFFFAOYSA-N 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 150000008427 organic disulfides Chemical class 0.000 description 1
- 150000008116 organic polysulfides Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000005077 polysulfide Substances 0.000 description 1
- 150000008117 polysulfides Polymers 0.000 description 1
- 239000011736 potassium bicarbonate Substances 0.000 description 1
- 235000015497 potassium bicarbonate Nutrition 0.000 description 1
- 229910000028 potassium bicarbonate Inorganic materials 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 235000011181 potassium carbonates Nutrition 0.000 description 1
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000005297 pyrex Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-N sulfonic acid Chemical compound OS(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-N 0.000 description 1
- 125000004434 sulfur atom Chemical group 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 239000002351 wastewater Substances 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
Landscapes
- 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)
Description
"Fremgangsmåte til fjerning av"Procedure for removal of
svovel fra gasser" sulfur from gases"
Denne oppfinnelse angår fjerning av svovelholdige gasser fra en avgasstrøm før gassene slippes til atmosfæren. Mer spe-sielt angår oppfinnelsen en fremgangsmåte til samtidig å absorbere og oksydere svovelholdige gasser som foreligger i én avgass-strøm, på en énkéltog bekvem måte. This invention relates to the removal of sulfur-containing gases from an exhaust gas stream before the gases are released to the atmosphere. More specifically, the invention relates to a method for simultaneously absorbing and oxidizing sulphur-containing gases present in one exhaust gas stream, in a convenient single-pass manner.
Svovelholdige avfallsgasser er skadelige, ofte giftige, og dannes som biprodukter ved mange industrielle proéesser. Svovelholdige gasser foreligger eksempelvis i røkgasser, smelteovns-gasser, avgasser fra kjemiske og mineraloljeprosesser og gasser som dannes ved forbrenning »v svovelholdige hydrokarbcn-brenn-stoffer. Disse gasser inneholder hydrogensulfid, svoveldioksyd, alifatiske tioler og organiske sulfidforbindelser innbefattende sulfider, disulfider, polysulfider, og tiofener og blandinger derav. Uttrykket "organiske sulfidforbindelser" betyr her organiske forbindelser som inneholder et toverdig svovelatom som ikke er bundet til et hydrogenatom. Forurensning av omgivelsene med slike gasser har vært generende for den som bor rundfetférurens-ningskilden, på grunn av de skadelige gassers blotte tilstede-værelse i atmosfæren og/eller på grunn av deres skadevirkninger, på naturen forøvrig. Sulfur-containing waste gases are harmful, often toxic, and are formed as by-products in many industrial processes. Sulphur-containing gases exist, for example, in flue gases, smelter gases, exhaust gases from chemical and mineral oil processes and gases that are formed by the combustion of sulphur-containing hydrocarbon fuels. These gases contain hydrogen sulfide, sulfur dioxide, aliphatic thiols, and organic sulfide compounds including sulfides, disulfides, polysulfides, and thiophenes and mixtures thereof. The term "organic sulphide compounds" here means organic compounds containing a divalent sulfur atom which is not bonded to a hydrogen atom. Contamination of the environment with such gases has been a nuisance for those who live at the source of round fat pollution, due to the harmful gases' mere presence in the atmosphere and/or due to their harmful effects on nature in general.
Mange fremgangsmåter er blitt foreslått til fjerning av svovelholdige gasser fra avgasser. En av de tidligste var forbrenning smefeoden. Ifølge denne ble giftig hydrogensulfid og organiske sulfider omdannet til de mindre giftige og mindre generende svoveldioksyd 3pg svoveltrioksyd ved luftoksydasjon ved høye temperaturer. Denne fremgangsmåte omdannet giftige stoffer Many methods have been proposed for the removal of sulfur-containing gases from exhaust gases. One of the earliest was combustion smefeod. According to this, toxic hydrogen sulfide and organic sulfides were converted into the less toxic and less bothersome sulfur dioxide 3pg sulfur trioxide by air oxidation at high temperatures. This procedure converted toxic substances
til mindre giftige stoffer, men sistnevnte var fremdeles skadelig .... og potensielt farlige for>omgivelsene. to less toxic substances, but the latter was still harmful .... and potentially dangerous to the environment.
For å unngå de problemer som er forbundet med forbrennings-met<p>den, ér det blitt foreslått talirike kjemiske prosesser. US Paifeent nr. 3 716 620 angår oksydasjon av hydrogensulfid og tioler med jod i nærvær av et organisk løsningsmiddel. Skjønt denne prosess er téknisk effektiv når det gjelder å oksydere disse spesi-fikke gasser, ér prosessen ikke brukbar i teknisk målestokk, da de forbindelser som anvendes er kostbare, og selv sraå tap av disse forbindelser gjør prosessen uøkonomisk i praksis. US Patent nr. 3 475 122 beskriver eh fremgangsmåte til gjenvinning av svoveldioksyd fra en gasstrøm ved at denne ledes gjennom en vandig ba- sisk løsning, for eksempel av kaliumhydroksyd, under dannelse av en bisulfitt-løsning. Denne behandles for gjenvinning av svoveldioksyd og resirkuleres deretter for gjenvinning av ytterligere svoveldioksyd. Denne prosess er imidlertid spesifikk for gjenvinning av svoveldioksyd og eliminerer ikke de forurensningspro-blemer som er forbundet med utslipp av det gjenvunne svoveldioksyd. Britisk patent nr. 421 970 beskriver en firétrihnsvprosess for oksydasjon av hydrogensulfid med hydrogenperoksyd. I det første trinn blir hydrogensulfid absorbert i en alkalisk løsning. To avoid the problems associated with the combustion method, a number of chemical processes have been proposed. US Patent No. 3,716,620 relates to the oxidation of hydrogen sulfide and thiols with iodine in the presence of an organic solvent. Although this process is technically efficient when it comes to oxidizing these specific gases, the process is not usable on a technical scale, as the compounds used are expensive, and even a steep loss of these compounds makes the process uneconomical in practice. US Patent No. 3,475,122 describes a method for recovering sulfur dioxide from a gas stream by passing it through an aqueous base sic solution, for example of potassium hydroxide, forming a bisulphite solution. This is treated to recover sulfur dioxide and is then recycled to recover further sulfur dioxide. However, this process is specific to the recovery of sulfur dioxide and does not eliminate the pollution problems associated with the emission of the recovered sulfur dioxide. British Patent No. 421,970 describes a four-step process for the oxidation of hydrogen sulfide with hydrogen peroxide. In the first step, hydrogen sulphide is absorbed in an alkaline solution.
I det annet trinn surgjøres løsningen ved behandling med karbon-dioksyd. I det tredjé trinn kokes løsningen for avdrivning av størstedelen av det absorberte hydrogensulfid. I det fjernde trinn behandles løsningen med et oksydasjonsmiddel, hvorved det resterende hydrogensulfid oksyderes. Skjønt det i patentet angis at det oppnås en ti gangers reduksjon av hydrogensulfidmengden i avløpet fra vaskeren i løpet av 15 minutter, er denne prosess ikke brukbar i industrien, først og fremst på grunn av den tid som kreves for utførelse av den fullstendige prosess. In the second step, the solution is acidified by treatment with carbon dioxide. In the third step, the solution is boiled to drive off most of the absorbed hydrogen sulphide. In the distant stage, the solution is treated with an oxidizing agent, whereby the remaining hydrogen sulphide is oxidised. Although it is stated in the patent that a tenfold reduction of the amount of hydrogen sulphide in the effluent from the washer is achieved within 15 minutes, this process is not usable in industry, primarily because of the time required to carry out the complete process.
Ovennevnte prosesser viser at det lenge har vært et behov for en effektiv, industriell prosess som kan muliggjøre en hurtig fjerning av en. rekke forskjellige svovelholdige gasser i avfails-gassér på en enkel og bekvem måte uten dannelse av forurensende biprodukter. The above processes show that there has long been a need for an efficient, industrial process that can enable the rapid removal of a. range of different sulfur-containing gases in waste gases in a simple and convenient way without the formation of polluting by-products.
I henhold til den foreliggende oppfinnelse tilveiebringes en fremgangsmåte til samtidig å absorbere,og oksydere Svovelholdige gasser som foreligger i én avgasstrøm, hvor den svovelholdige gass er hydrogensulfid, svoveldioksyd eller alifatiske dioler eller blandinger derav og også kan inneholde oksyderbare gasser så som organiske sulfider, tiofener og lignende, og fremgangsmåten §&r ut på at avgassen bringes i kontakt .med en vandig hydrogenperolfcsyd--løsning med en pH over 7,0 ved en temperatur over løsningens frysepunkt/men under dens kokepunkt, i tilstrekkelig lang tid til samtidig å absorbere og oksydere de svovelholdige gasser. Fremgangsmåten ifølge oppfinnelsen gjør det mulig å fjerne hovedsakelig alle svovelholdige gasser som foreligger i en strøm av avfallsgasser, ned til konsentrasjoner som er påvisbare ved kon-, vensjonelt utstyr, i løpet av noen sekunder. De svovelholdige gasser oksyderes til ikke-forurensende alkaiisulfater og -sulfo-nater. Disse materialer kan slippes direkte til elver<p>g inn-sjøer uten skade for den naturlige fauna eller flora. According to the present invention, a method is provided to simultaneously absorb and oxidize sulfur-containing gases present in one exhaust gas stream, where the sulfur-containing gas is hydrogen sulfide, sulfur dioxide or aliphatic diols or mixtures thereof and may also contain oxidizable gases such as organic sulfides, thiophenes and the like, and the method involves bringing the exhaust gas into contact with an aqueous hydrogen peroxide solution with a pH above 7.0 at a temperature above the solution's freezing point/but below its boiling point, for a sufficiently long time to simultaneously absorb and oxidize the sulphurous gases. The method according to the invention makes it possible to remove essentially all sulfur-containing gases present in a stream of waste gases, down to concentrations that are detectable by conventional equipment, within a few seconds. The sulphur-containing gases are oxidized to non-polluting alkali sulphates and -sulphonates. These materials can be released directly into rivers and lakes without harming the natural fauna or flora.
De svovelholdige gasser som fjernes fra avgasstrømmen i henhold til den foreliggende fremgangsmåte, ér hydrogensulfid; The sulphur-containing gases which are removed from the exhaust gas stream according to the present method are hydrogen sulphide;
svoveldioksydr og alifatiske tioler (merkaptaner) innéholdende 1-12 karbonatbmér, så som metantipl, etantiol, propantiol og. butantiol. Disse svovelholdige gasser er de gasser som utgjør ho-veddelen av innholdet av svovelholdig gass i de fleste avfallsgasser. I tillegg til de ovennevnte svovelholdige gasser kan også organiske sulfidforbindelser innbefattende organiske disulfider, polysulfider, tiofener<p>g lignende også være tilstede i avgass-strømmen. Disse forbind&lser innbefatter organiske sulfider, så som dimetylsulfid, dietylsulfid, dibutylsulfid og metyletylsulfid; sulfur dioxide and aliphatic thiols (mercaptans) containing 1-12 carbon atoms, such as methanethiol, ethanethiol, propanethiol and. butanethiol. These sulfur-containing gases are the gases that make up the majority of the sulfur-containing gas content in most waste gases. In addition to the above-mentioned sulphurous gases, organic sulphide compounds including organic disulphides, polysulphides, thiophenes and the like can also be present in the exhaust gas stream. These compounds include organic sulfides, such as dimethyl sulfide, diethyl sulfide, dibutyl sulfide, and methyl ethyl sulfide;
organiske disulfider, så som dimetyldisulfid, dietylsulfid; organiske polysulfider, så som dimetyldisulfid; tiofen og substituerte tiofener. De organiske sulf idforbindelser, er ikke pH-avhengige skjønt de absorberes og oksyderes av den vandige hydrogenperoksyd-oppløsning til ikke forurensende forbindelser. De organiske sul-fid forbinde Ise r blir følgelig behandlet samtidig med de andre svovelholdige gasser, nemlig hydrogensulfid, svoveldioksyd og alifatiske tioler, hvorved man unngår kostbare og vanskelige separå-sjonsprosesser og påfølgende prosesstrinn. organic disulfides, such as dimethyl disulfide, diethyl sulfide; organic polysulfides, such as dimethyl disulfide; thiophene and substituted thiophenes. The organic sulphide compounds are not pH-dependent, although they are absorbed and oxidized by the aqueous hydrogen peroxide solution to non-polluting compounds. The organic sulphide compounds are consequently treated at the same time as the other sulphur-containing gases, namely hydrogen sulphide, sulfur dioxide and aliphatic thiols, thereby avoiding expensive and difficult separation processes and subsequent process steps.
Konsentrasjonene av svovelholdige gasser som behandles kan variere innen vide grenser. Den svovelholdige gassens konsentrasjon er vanligvis avhengig av kilden og varierer fra noen mg/l til flere prosent, fer eksempel 5 vekt%. Framgangsmåten er meget øko-nomisk hvis konsentrasjonen av svovelholdig gass i avgasstrømmen holdes mindre enn 2 vekt%. Senkes konsentrasjonen av svovelholdig gass til mindre enn 2%, for eksempel ved fortynning av gassen med luft, vil den mengde hydrogenperoksyd som ernnødvéndig for oksydasjon av en enhetsmengde svovelholdig gass, reduseres betydelig. The concentrations of sulfur-containing gases that are treated can vary within wide limits. The concentration of the sulfur-containing gas usually depends on the source and varies from a few mg/l to several percent, for example 5% by weight. The method is very economical if the concentration of sulphurous gas in the exhaust gas stream is kept below 2% by weight. If the concentration of sulphurous gas is lowered to less than 2%, for example by diluting the gas with air, the amount of hydrogen peroxide that is necessary for the oxidation of a unit quantity of sulphurous gas will be significantly reduced.
Fortynning med luft kan tjene til å redusere hydrogensulfidmengden i hydrogensulfidhoIdige gasser til under 4,3%, som er grensen for eksplosive blandinger. -For at de svovelholdige gasser skal bli absorbert og ok-sydert samtidig av den vandige hydrogenperoksydoppløsning må den vandige løsning ha en pH over 7,0 og fortrinnsvis 7,0-13,5. Den ønskede pH erholdes ved tilsetning av et alkali til den vandige hydrogeriperoksydoppløsning. Som alkali foretrekkes natriumhydrok-syd, som helt eller delvis kan erstattes med kaliumhydroksyd, magnesiumhydroksyd, kalsiumhydroksyd, natriumkarbonat, natriumbi-karbonat, kaliumkarbonat, kaliumbikarbonat og magnesiumkarbonat. Hvis den vandige oppløsningens pH faller under 7,0 under reaksjonen, tilsettes mer alkali inntil løsningens pH kommer over 7,0. Dét er vesentlig at pH-verdien holdes over 7,0, slik at svovelsyre og sulfonsyre som dannes under reaksjonen, nøytralise-res i Denne arbeidsmåte gjør det unødvendig med senere justerin-ger av pH før utslippet av den vandige løsning. Automatisk kon-troll og regulering av reaksjonsblandingens pH oppnås ved kjente midler og metoder. Dilution with air can serve to reduce the amount of hydrogen sulphide in hydrogen sulphide-containing gases to below 4.3%, which is the limit for explosive mixtures. - In order for the sulfur-containing gases to be absorbed and oxidized at the same time by the aqueous hydrogen peroxide solution, the aqueous solution must have a pH above 7.0 and preferably 7.0-13.5. The desired pH is obtained by adding an alkali to the aqueous hydrogen peroxide solution. As an alkali, sodium hydroxide is preferred, which can be completely or partially replaced by potassium hydroxide, magnesium hydroxide, calcium hydroxide, sodium carbonate, sodium bicarbonate, potassium carbonate, potassium bicarbonate and magnesium carbonate. If the pH of the aqueous solution falls below 7.0 during the reaction, more alkali is added until the pH of the solution rises above 7.0. It is essential that the pH value is kept above 7.0, so that sulfuric acid and sulphonic acid which are formed during the reaction are neutralized. This method of working makes it unnecessary to make subsequent adjustments of the pH before the discharge of the aqueous solution. Automatic control and regulation of the pH of the reaction mixture is achieved by known means and methods.
Den vandige hydrogenperoksydoppløsningens pH kan ennvidere justeres innenfor ovennevnte pH-områder med sikte på oppnåelse av optimal.absorpsjon og oksydasjon av spesielle svovelholdige gasser som foreligger i en gitt avgass. Når eksempelvis hydrogensulfid er den svovelholdige gass er pH fortrinnsvis mellom ca. 8,0 og ca. 13,5, aller helst mellom ca. 11,0 og ca. 13,0. Innenfor det foretrukne pH-område absorberes og oksyderes hydrogensulfid hurtig. Absorpsjons- og oksydasjonshastighetene er betydelig bédre ved relativt høye pH-verdier. Når svoveldioksyd er den svovelholdige gass, er pH fortrinnsvis over 7,0 men under ca. 12,0. I dette pH-område forbedres absorpsjonshastigheten betydelig. Når pH-verdien er over ca. 12,0, vil oksydasjonshastigheten for svoveldioksyd være altfor lav i praksis. Når alifatiske tioler er The pH of the aqueous hydrogen peroxide solution can further be adjusted within the above-mentioned pH ranges with a view to achieving optimal absorption and oxidation of special sulfur-containing gases present in a given exhaust gas. When, for example, hydrogen sulfide is the sulfur-containing gas, the pH is preferably between approx. 8.0 and approx. 13.5, preferably between approx. 11.0 and approx. 13.0. Within the preferred pH range, hydrogen sulphide is rapidly absorbed and oxidized. Absorption and oxidation rates are significantly better at relatively high pH values. When sulfur dioxide is the sulfur-containing gas, the pH is preferably above 7.0 but below approx. 12.0. In this pH range, the absorption rate is significantly improved. When the pH value is above approx. 12.0, the oxidation rate for sulfur dioxide will be far too low in practice. When aliphatic thiols are
den svovelholdige gass, er pH fortrinnsvis over 7,0 men under ca. 13,5. Når avgasstrømmene inneholder en blanding av de ovennevnte „,<B>VOveiho Idige gasser, er absorpsjons- og oksydas jonshastigheten optimal innenfor det foretrukne pH-område mellom 8,0 og ca. 12,0 for alle de svovelholdige gasser. Når det gjelder de organÉike sulfidforbindelser, er oksydasjonshastigheten ikke pH-avhengig, the sulfur-containing gas, the pH is preferably above 7.0 but below approx. 13.5. When the exhaust gas streams contain a mixture of the above mentioned „,<B>VOveiho Idige gases, the absorption and oxidation ion rate is optimal within the preferred pH range between 8.0 and approx. 12.0 for all sulphur-containing gases. In the case of the organic sulphide compounds, the rate of oxidation is not pH dependent,
og følgelig kan hvilken som helst pH anvendes ved oksydering av disse.gasser. and consequently any pH can be used when oxidizing these gases.
Hvilken som helst tilgjengelig kvalitet av vandig hydro-gehperoksyd kan anvendes, med 50% teknisk kvalitet som den foretrukne. Den nøyaktige mengåe av hydrogenperoksyd i den vandige løsning avhenger av konsentrasjonen av de svovelholdige gasser som foreligger i avgasstrøm, og av den ønskede rensegrad. Den vandige hydrogenperoksydoppløsning kan fremstilles ved bruk av avionisert, destillérttellér vanlig ledningsvann. Any available grade of aqueous hydrogen peroxide may be used, with 50% technical grade being preferred. The exact amount of hydrogen peroxide in the aqueous solution depends on the concentration of the sulfur-containing gases present in the exhaust gas stream, and on the desired degree of purification. The aqueous hydrogen peroxide solution can be prepared using deionized, distilled or ordinary tap water.
For å redusere innholdet av svovelholdig gass i avfallsgassen til grensen for det påvisbare, anvender man hydrogenperoksyd i konsentrasjoner på ca; 0,01% til 50 vékt%.. Den mengde hydrogenperoksyd som skal anvendes ved oksydasjon av en gitt svovelholdig gass, kan lett bestemmes på basis, av reaksjonens stø-kiometri. For eksempel behøves 4 vektdeler hydrogenperoksyd for fullstendig oksydasjon av en vektdel hydrogensulfid. En vektdel hydrogenperoksyd kreves for fullstendig oksydasjon av en vektdel svoveldioksyd. Imidlertid kan man bruke hydrogenperoksyd-mengder noe over den støkiometriske mengde for å oksydere hydrogensulfid eller svoveldioksyd. De gassformige organiske svovelforbindelser krever et overskudd av hydrogenperoksyd ut over dén støkiomet-riske mengde, og man foretrekker en maksimaikonsentrasjon på 10% hydrogenperoksyd. Uttrykket "gassformige organiske svovelforbindelser" refererer seg til både de alifatiske tioler og de organiske sulfidforbindelser. In order to reduce the content of sulphurous gas in the waste gas to the detectable limit, hydrogen peroxide is used in concentrations of approx. 0.01% to 50% by weight. The amount of hydrogen peroxide to be used in the oxidation of a given sulphurous gas can be easily determined on the basis of the stoichiometry of the reaction. For example, 4 parts by weight of hydrogen peroxide are needed for complete oxidation of one part by weight of hydrogen sulphide. One part by weight of hydrogen peroxide is required for complete oxidation of one part by weight of sulfur dioxide. However, hydrogen peroxide amounts slightly above the stoichiometric amount can be used to oxidize hydrogen sulfide or sulfur dioxide. The gaseous organic sulfur compounds require an excess of hydrogen peroxide beyond the stoichiometric amount, and a maximum concentration of 10% hydrogen peroxide is preferred. The term "gaseous organic sulfur compounds" refers to both the aliphatic thiols and the organic sulfide compounds.
Bruken av hydrogenperoksyd under alkaliske betingelser for samtidig å absorbere og oksydere svovelholdige avfalisgasser er meget overraskende, fordi hydrogenperoksyd spaltes under alkaliske betingelser; Det ble imidlertid oppdaget at oksydasjonshastigheten for hydrogensulfid og svoveldioksyd er betydelig høyere enn hydrogenperoksydets spaltningshastighet når hydrogenperoksyd anvendes i støkiometriske mengder eller i noe over stø-kiometrisk mengde. Videre ble det oppdaget at hydrogenperoksyd-spaltningen holdes på et fullt tilfredsstillende nivå ved oksydasjon av hvilke som helst av de gassformige organiske svovelforbindelser selv ved bruk av mer enn støkiometrisk mengde hydrogenperoksyd hvis løsningens pH holdes mellom 7,0 og ca. 12,0. The use of hydrogen peroxide under alkaline conditions to simultaneously absorb and oxidize sulphurous waste gases is very surprising, because hydrogen peroxide decomposes under alkaline conditions; However, it was discovered that the oxidation rate for hydrogen sulphide and sulfur dioxide is significantly higher than the hydrogen peroxide's decomposition rate when hydrogen peroxide is used in stoichiometric amounts or in slightly above stoichiometric amounts. Furthermore, it was discovered that the hydrogen peroxide decomposition is maintained at a fully satisfactory level by oxidation of any of the gaseous organic sulfur compounds even using more than stoichiometric amount of hydrogen peroxide if the pH of the solution is kept between 7.0 and about. 12.0.
Den nødvendige kontakttid ved behandlingen av den svovelholdige avgass må være tilstrekkelig til samtidig å absorbere og oksydere de svovelholdige gasser. En kontakttid på 1 sekund eller mindre esrtilstrekkelig for fullstendig absorpsjon og oksydasjon av hydrogensulfid og svoveldioksyd. Lengre kontakttider er på- krevet for absorpsjon og oksydasjon av de gassformige organiske svovelforbindelser. Tiden kan være fra 1 til 60 sekund avhengig av hvilke organiske svovelforbindelser som behandles. For å be-grense spaltningen év hydrogenperoksyd véd bruk av relativt lang kontakttid kan man eventuelt stabilisere den vandige hydrogenper-oksydoppløsning ved konvensjonelle metoderå for eksempel ved bruk av magnesiumoksyd eller andre stabiliseringsmidler i den vandige hydrogenperoksydoppløsning. Det kan også anvendes en konvensjonell raetallkatalysator til hjelp ved oksydasjonsreaksjonen. Disee ka-talysatorer kan være salter av.jern, kobolt, nikkel, kobber, man-gan, molybden, vanadium, platina, palladium og sølv. Hvis det anvendes en katalysator, foretrekkes de fire første katalytiske The necessary contact time during the treatment of the sulphur-containing waste gas must be sufficient to simultaneously absorb and oxidize the sulphur-containing gases. A contact time of 1 second or less is sufficient for complete absorption and oxidation of hydrogen sulfide and sulfur dioxide. Longer contact times are required for absorption and oxidation of the gaseous organic sulfur compounds. The time can be from 1 to 60 seconds, depending on which organic sulfur compounds are being treated. In order to limit the decomposition of hydrogen peroxide by using a relatively long contact time, the aqueous hydrogen peroxide solution can optionally be stabilized by conventional methods, for example by using magnesium oxide or other stabilizing agents in the aqueous hydrogen peroxide solution. A conventional Raetal catalyst can also be used to aid in the oxidation reaction. These catalysts can be salts of iron, cobalt, nickel, copper, manganese, molybdenum, vanadium, platinum, palladium and silver. If a catalyst is used, the first four catalytic ones are preferred
salter. Katalysatorene kan anvendes med eller uten konvensjonelle kompleksdannende midler, så som glukonsyre og sitronsyre. Bruk av hydrogenperoksyd-stabiliseringsmidler og metallkatalysatorer kan også være tjenlig under absorpsjonen og oksydasjonen av hydrogensulfid og svoveldioksyd, men de er ikke nødvendige for reaksjonen. salts. The catalysts can be used with or without conventional complexing agents, such as gluconic acid and citric acid. The use of hydrogen peroxide stabilizers and metal catalysts may also be useful during the absorption and oxidation of hydrogen sulfide and sulfur dioxide, but they are not necessary for the reaction.
Reaksjonstemperaturen er kritisk bare for såvidt som den må være over den vandige løsningens frysepunkt/ men under koke-punktet. Reaksjonen utføres fortrinnsvis mellom 25 og 85°C og aller helst mellom 45 og 65°C, som er de normale temperaturer i avfallsgasser. Når en av de gassformige organiske svovelforbindelser, skal oksyderes, foretrekkes temperaturer mellom ca. 60 og 70 O c. Ved disse temperaturer oksyderes de gassformige orgai1nis<ke>svovelforbindelser hurtig og med betydelig øket hastighet. Denne hurtige oksydasjon gjør det mulig å bruke bare støkiometriske mengder av hydrogenperoksyd, krever altså ikke et overskudd derav, for fullstendig oksydasjon av alle de gassformige. organiske svovelforbindelser som foreligger i avfallsgassen. The reaction temperature is critical only insofar as it must be above the freezing point of the aqueous solution/ but below the boiling point. The reaction is preferably carried out between 25 and 85°C and most preferably between 45 and 65°C, which are the normal temperatures in waste gases. When one of the gaseous organic sulfur compounds is to be oxidized, temperatures between approx. 60 and 70 O c. At these temperatures, the gaseous organic sulfur compounds are oxidized quickly and at a significantly increased rate. This rapid oxidation makes it possible to use only stoichiometric amounts of hydrogen peroxide, i.e. does not require an excess thereof, for complete oxidation of all the gaseous substances. organic sulfur compounds present in the waste gas.
Avgasstrømmen bringes i kontakt med den vandige hydrogen-peroksydløsning i hvilket som helst konvensjonelt apparat for slike formål. Man foretrekker å bruke en fylt kolonne eller tårn. Avgasstrømmen og den løsning som denne skal bringes i kontakt med, mates inn i apparatet enten i motstrøm, tverrstrøm eller medstrøm. Den behandlede avgass og brukt vandig hydrogenperoksyd-løsning slippes deretter direkte til avløp. The exhaust stream is brought into contact with the aqueous hydrogen peroxide solution in any conventional apparatus for such purposes. One prefers to use a filled column or tower. The exhaust gas stream and the solution with which it is to be brought into contact are fed into the apparatus either in counter-flow, cross-flow or co-flow. The treated exhaust gas and used aqueous hydrogen peroxide solution are then released directly into the drain.
Ved behandling av avgasser som bare krever støkiometriske mengder av hydrogenperoksyd for oksydasjon av de svovelholdige gasser, foretrekker man å føre avgasstrømmen og den vandige hyd-rogenperoksydløsning gjennom apparatet bare én gang. Ved behandling av avgasser som ktever et overskudd av hydrogenperoksyd ut over den støkiometriske mengde, foretrekker man å føre avgass-strømmen og den vandige hydrogenperoksydløsning ggennom apparatet, fraskille den brukte vandigé løsning og reaktivere den brukte vandige løsning ved tilsetning av hydrogenperoksyd til løsningen. - Denne reaktiverte løsning resirkuleres deretter til apparatet. When treating exhaust gases that only require stoichiometric amounts of hydrogen peroxide for oxidation of the sulfur-containing gases, it is preferred to pass the exhaust gas stream and the aqueous hydrogen peroxide solution through the apparatus only once. When treating exhaust gases that contain an excess of hydrogen peroxide beyond the stoichiometric amount, it is preferred to pass the exhaust gas stream and the aqueous hydrogen peroxide solution through the apparatus, separate the used aqueous solution and reactivate the used aqueous solution by adding hydrogen peroxide to the solution. - This reactivated solution is then recycled to the device.
Ved bruk;av denne, arbeidsmåte oppnår man på en effektiv og øko-nomisk måte at det stadig vil. være et overskudd av hydrogenperoksyd i apparatet. By using this way of working, one achieves in an efficient and economical way that it will always be. be an excess of hydrogen peroxide in the device.
Kommersielt tilgjengelige gassanalysatorer anvendes til å bestemme innholdet av svovelholdig gass både i den avgass som behandles og i avløpsgasseri. Hvis konsentrasjonen av svovelholdig gass i den tilførte;avgass endres, kan den nødvendige.mengde vandig hydrogenperoksydløsning tilsettes til apparatet enten manuelt eller automatiske Videre blir pH-verdien til den brukte vandige hydrogenperoksydløsning som fjernes fra apparatet, bestemt på i Commercially available gas analyzers are used to determine the content of sulphur-containing gas both in the waste gas being treated and in the waste gas plant. If the concentration of sulfur-containing gas in the supplied exhaust gas changes, the required amount of aqueous hydrogen peroxide solution can be added to the apparatus either manually or automatically. Furthermore, the pH value of the spent aqueous hydrogen peroxide solution removed from the apparatus is determined at
og for seg, kjent måte, hvorved hydrogenperoksydløsningens pH kan holdes over 7,0 under reaksjonen. Det ble funnet a. hvis pH-verdien til den vandige hydrogenperoksydløsning som tilføres appa-. ratet, er mellom 8,0 og 12,0, vil pH-yerdien til den vandige løs-ning som uttas, være over 7,0. and in a known manner, whereby the pH of the hydrogen peroxide solution can be kept above 7.0 during the reaction. It was found a. if the pH value of the aqueous hydrogen peroxide solution supplied to the appa-. rate, is between 8.0 and 12.0, the pH of the aqueous solution taken out will be above 7.0.
De følgende eksempler vil ytterligere illustrere oppfin-neIsen. Alle prosentangivéiser er basert på vekt med mindre annet er sagt. The following examples will further illustrate the invention. All percentages are based on weight unless otherwise stated.
Eksempel 1Example 1
En gasstrøm inneholdende 1 volum% H^ S i luft ble med en hastighet på 56 cm/sekund ført gjennom et kontakteringsapparat bestående, av et kjemisk motstandsdyktig og varmefast glassrør ("Pyrexj$L") med diameter på 5,08 cm inneholdende en 35,56 cm søyle av kjemisk motstandsdyktig keramisk fyllmateriale ("Intalox ?<M>") i form av 0,63 cm store sadler. Den totale gasstrøm A gas stream containing 1 vol.% H^S in air was passed at a velocity of 56 cm/second through a contacting apparatus consisting of a chemically resistant and heat-resistant glass tube ("Pyrexj$L") with a diameter of 5.08 cm containing a 35 .56 cm column of chemically resistant ceramic filler material ("Intalox ?<M>") in the form of 0.63 cm saddles. The total gas flow
var 50 l/min. En vandig løsning inneholdende 10 g/l NaOH og 4,3 g/l IIjO^ rued en pH yå 13,0 ble 'fremstilt av avionisert vann was 50 l/min. An aqueous solution containing 10 g/l NaOH and 4.3 g/l IIjO^ at a pH of 13.0 was prepared from deionized water
og ledet gjennom søylen i motstrøm ti! gasstrømmen, idet løs-ningens strømriingshastighet var 0,45 l/min. Den vandige løs-ningens temperatur var 25°C. Oppholdstidéri for gasstrømmen i and led through the column in countercurrent ten! the gas flow, the solution flow rate being 0.45 l/min. The temperature of the aqueous solution was 25°C. Residence time for the gas stream i
apparatet var 0,66 sekund. Fremgangsmåten ble utført kontinuer-lig i 1 time. Avløpsgassen inneholdt mindre enn 0,001 ppm (de-ler pr. million) HjS. Avløpsoppløsningen hadde en pH på 12,5.og inneholdt 0,5 mg/l uoksyderte sulfidforbindelser (H?S, NaHS og Na2S) . the apparatus was 0.66 seconds. The procedure was carried out continuously for 1 hour. The waste gas contained less than 0.001 ppm (parts per million) HjS. The effluent solution had a pH of 12.5 and contained 0.5 mg/l of unoxidised sulphide compounds (H2S, NaHS and Na2S).
Eksempel 2Example 2
Fremgangsmåten ifølge eksempel 1 ble gjentatt med unnta-gelse av at gasstrømmen inneholdt 0,1 yolum% H^S i luft og den vandige løsning inneholdt 0,165 g/l NaOH og 0,28 g/l H202og hadde en pH på 11,0. Avløpsgassen inneholdt mindre enn.0,001 ppm H2S. Avløpsløsningen hadde en pH på 10,4 og inneholdt 7 mg/l uoksyderte sulfidforbindelser. The procedure according to Example 1 was repeated with the exception that the gas stream contained 0.1 vol% H 2 S in air and the aqueous solution contained 0.165 g/l NaOH and 0.28 g/l H 2 O 2 and had a pH of 11.0. The waste gas contained less than 0.001 ppm H2S. The effluent solution had a pH of 10.4 and contained 7 mg/l of unoxidised sulphide compounds.
Eksempel 3 Example 3
Fremgangsmåten ifølge eksempel 1 ble gjentatt med unnta-gelse av et gasstrømmen inneholdt 0,006 voium% HjS i luft og den vandige løsning inneholdt 0,01 g/1 NaOH og 0,02 g/l H2°2og ^adde en pH på 9,5. Avløpsgassen inneholdt mindre enn 0,001 ppm HjS. Avløpsløsningen hadde en pH på 9,3 og inneholdt 1,7 mg/l uoksyderte sulf idfofbindelse r. The procedure according to Example 1 was repeated with the exception that the gas stream contained 0.006 vol.% H 2 S in air and the aqueous solution contained 0.01 g/l NaOH and 0.02 g/l H 2 ° 2 and added a pH of 9.5 . The waste gas contained less than 0.001 ppm HjS. The effluent solution had a pH of 9.3 and contained 1.7 mg/l of unoxidised sulphide compounds.
Eksempel 4Example 4
Fremgangsmåten ifølge eksempel 1 ble gjentatt med unnta-gelse av at gasstrømmen inneholdt 0,1 volum% S02i luft istedenfor H2S og den vandige løsning inneholdt 0,2 g/l NaOH og 0,16 g/l H202og hadde en pH på 11,2. Avløpsgassen inneholdt mindre enn 1 ppm S02. Avløpsvæsken hadde en pH på 9,0 og inneholdt 1 mg/l sulfitt-forbindelser (Na2S03, NaHSOg). The procedure according to example 1 was repeated with the exception that the gas stream contained 0.1 volume% S02 in air instead of H2S and the aqueous solution contained 0.2 g/l NaOH and 0.16 g/l H202 and had a pH of 11.2 . The waste gas contained less than 1 ppm SO2. The effluent had a pH of 9.0 and contained 1 mg/l sulphite compounds (Na2SO3, NaHSOg).
Eksempel 5Example 5
En gasstrøm inneholdende 1000 ppm metantiol i luft (på volumbasis) ble med en hastighet på ca. 35 cm/sekund ført gjennom et kontakteringsapparat bestående av et glassrør ("Pyrex TM") med diameter på 5,68 cm inneholdende en 71,12 cm søyle fyllt med 0,63 cm sadler av "Intalox TM". Den totale gasstrøm var åfitårfmin. En vandig løsning inneholdende 1,0 g/l NaOH og 1,0 g/l H2Q2 med en pH på 11,9 ble fremstilt av avionisert vann og ført gjennom søylen i motstrøm til gassen, idet løsningens strømMingshastighet til- svafcte 1,35 l/min. Den vandige løsningens temperatur var 25°C. Gassens oppholdstid i apparatet var 4,4 sekundJ Fremgangsmåten ble utført.kontinuerlig i en time.. Avløpsgassen inneholdt 4 ppm metantiol. Avløpsløsningen hadde en pH på 11,0, og innholdet av uoksyderte svovelforbindelser var under påviselige mengder. A gas stream containing 1000 ppm methanethiol in air (on a volume basis) was at a rate of approx. 35 cm/second passed through a contacting apparatus consisting of a 5.68 cm diameter glass tube ("Pyrex TM") containing a 71.12 cm column filled with 0.63 cm saddles of "Intalox TM". The total gas flow was at least An aqueous solution containing 1.0 g/l NaOH and 1.0 g/l H2Q2 with a pH of 11.9 was prepared from deionized water and passed through the column in countercurrent to the gas, the flow rate of the solution being 1.35 l /my. The temperature of the aqueous solution was 25°C. The residence time of the gas in the apparatus was 4.4 seconds. The procedure was carried out continuously for one hour. The waste gas contained 4 ppm methanethiol. The effluent solution had a pH of 11.0, and the content of unoxidised sulfur compounds was below detectable amounts.
Eksempel 6 Example 6
Fremgangsmåten ifølge eksempel 5 ble gjentatt med unnta-gelse av at gasstrømmen inneholdt 8000 ppm H^S på volumbasis og 200 ppm metantiol på volumbasis i luft. Avløpsgassen inneholdt ingen påviselige mengder av HjS og 2 ppm metantiol på volumbasis. Avløpsvæsken hadde en pH på 11,2 og innholdet av uoksyderte svovelforbindelser var under påviselige mengder. The procedure according to example 5 was repeated with the exception that the gas stream contained 8,000 ppm H 2 S on a volume basis and 200 ppm methanethiol on a volume basis in air. The waste gas contained no detectable amounts of HjS and 2 ppm methanethiol on a volume basis. The effluent had a pH of 11.2 and the content of unoxidised sulfur compounds was below detectable amounts.
Eksempel 7Example 7
Fremgangsmåten ifølge eksempel 5.ble gjentatt meduunnta-gelse av at gasstrømmen inneholdt 1000 ppm etantiol på volumbasis, 1000 ppm dimetylsulfid på volumbasis og 100 ppm tiofen. Avløps-gassen inneholdt ingen påviselige mengder av svovelforbindelser. Avløpsvæsken hadde en pH på 11,9 og inneholdt ca. 5 mg/l dietyl-disulfid. The procedure according to example 5 was repeated with the exception that the gas stream contained 1000 ppm ethanethiol on a volume basis, 1000 ppm dimethyl sulphide on a volume basis and 100 ppm thiophene. The waste gas contained no detectable amounts of sulfur compounds. The wastewater had a pH of 11.9 and contained approx. 5 mg/l diethyl disulphide.
Claims (11)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US47260274A | 1974-05-23 | 1974-05-23 |
Publications (1)
Publication Number | Publication Date |
---|---|
NO751818L true NO751818L (en) | 1975-11-25 |
Family
ID=23876186
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
NO751818A NO751818L (en) | 1974-05-23 | 1975-05-22 |
Country Status (11)
Country | Link |
---|---|
BE (1) | BE829372A (en) |
CA (1) | CA1069273A (en) |
CH (1) | CH598857A5 (en) |
DE (1) | DE2522279A1 (en) |
ES (1) | ES437900A1 (en) |
FR (1) | FR2271862B1 (en) |
GB (1) | GB1499536A (en) |
IT (1) | IT1037847B (en) |
NL (1) | NL7505539A (en) |
NO (1) | NO751818L (en) |
SE (1) | SE7505913L (en) |
Families Citing this family (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4574076A (en) * | 1976-11-04 | 1986-03-04 | Fmc Corporation | Removal of hydrogen sulfide from geothermal steam |
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 |
US4311680A (en) * | 1980-11-20 | 1982-01-19 | The Goodyear Tire & Rubber Company | Method for removal of sulfur compounds from a gas stream |
FR2498083B1 (en) * | 1981-01-19 | 1986-05-23 | Charbonnages De France | |
FR2503130B1 (en) * | 1981-03-31 | 1985-10-31 | Interox | TREATMENT OF WATER AND EMISSION GAS CONTAINING SULPHIDIC ORGANIC COMPOUNDS |
DE3151133A1 (en) * | 1981-12-23 | 1983-06-30 | Peroxid-Chemie GmbH, 8023 Höllriegelskreuth | METHOD FOR REMOVING H (DOWN ARROW) 2 (DOWN ARROW) S FROM NATURAL GAS, PETROLEUM, AND THEIR MIXTURES |
US4435371A (en) * | 1982-02-26 | 1984-03-06 | The Goodyear Tire & Rubber Company | Sulfur removal from a gas stream |
GB8525047D0 (en) * | 1985-10-10 | 1985-11-13 | Interox Chemicals Ltd | Waste treatment |
AT395829B (en) * | 1991-10-25 | 1993-03-25 | Waagner Biro Ag | Process for scrubbing out gases having a strong odour |
US5523069A (en) * | 1993-11-05 | 1996-06-04 | Nalco Fuel Tech | Carbonyl sulfide abatement in fluids |
US5595713A (en) * | 1994-09-08 | 1997-01-21 | The Babcock & Wilcox Company | Hydrogen peroxide for flue gas desulfurization |
DE60319738T2 (en) | 2002-12-21 | 2009-04-02 | Haldor Topsoe A/S | PROCESS FOR REMOVING SO2 FROM EXHAUST GASES BY MITH2O2 REACTION |
FR2950820A1 (en) * | 2009-10-06 | 2011-04-08 | Air Liquide | Method for eliminating nitrogen oxide and sulfur oxide from gas stream of thermal power plant, involves washing gas stream with strong oxidant in liquid phase, and purging aqueous solution that contains sulfuric acid and nitric acid |
CN113385005A (en) * | 2021-06-28 | 2021-09-14 | 中石化南京化工研究院有限公司 | Formula of novel metal complex sulfide removal compound |
CN113578014B (en) * | 2021-08-12 | 2022-05-03 | 九江中星医药化工有限公司 | Tail gas treatment method for preparing DL-homocystine |
-
1975
- 1975-04-14 CA CA224,491A patent/CA1069273A/en not_active Expired
- 1975-05-05 IT IT23003/75A patent/IT1037847B/en active
- 1975-05-12 NL NL7505539A patent/NL7505539A/en not_active Application Discontinuation
- 1975-05-13 GB GB20144/75A patent/GB1499536A/en not_active Expired
- 1975-05-20 DE DE19752522279 patent/DE2522279A1/en not_active Withdrawn
- 1975-05-21 FR FR7515780A patent/FR2271862B1/fr not_active Expired
- 1975-05-22 NO NO751818A patent/NO751818L/no unknown
- 1975-05-22 BE BE156607A patent/BE829372A/en not_active IP Right Cessation
- 1975-05-23 CH CH663375A patent/CH598857A5/xx not_active IP Right Cessation
- 1975-05-23 SE SE7505913A patent/SE7505913L/en unknown
- 1975-05-23 ES ES437900A patent/ES437900A1/en not_active Expired
Also Published As
Publication number | Publication date |
---|---|
BE829372A (en) | 1975-11-24 |
SE7505913L (en) | 1975-11-24 |
GB1499536A (en) | 1978-02-01 |
DE2522279A1 (en) | 1975-12-04 |
NL7505539A (en) | 1975-11-25 |
FR2271862B1 (en) | 1982-02-05 |
CH598857A5 (en) | 1978-05-12 |
AU8022575A (en) | 1976-10-21 |
FR2271862A1 (en) | 1975-12-19 |
CA1069273A (en) | 1980-01-08 |
IT1037847B (en) | 1979-11-20 |
ES437900A1 (en) | 1977-01-01 |
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