NO136465B - - Google Patents
Download PDFInfo
- Publication number
- NO136465B NO136465B NO3083/72A NO308372A NO136465B NO 136465 B NO136465 B NO 136465B NO 3083/72 A NO3083/72 A NO 3083/72A NO 308372 A NO308372 A NO 308372A NO 136465 B NO136465 B NO 136465B
- Authority
- NO
- Norway
- Prior art keywords
- gas
- sulphide
- soot
- carbonyl sulphide
- catalyst
- Prior art date
Links
- 239000007789 gas Substances 0.000 claims description 114
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 claims description 40
- 239000003054 catalyst Substances 0.000 claims description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 239000004071 soot Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 23
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 18
- 239000002250 absorbent Substances 0.000 claims description 13
- 230000002745 absorbent Effects 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 13
- 230000003197 catalytic effect Effects 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000002485 combustion reaction Methods 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 239000000725 suspension Substances 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 230000007062 hydrolysis Effects 0.000 claims description 5
- 238000006460 hydrolysis reaction Methods 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003463 adsorbent Substances 0.000 claims description 3
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 claims description 3
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 claims description 2
- 229910001570 bauxite Inorganic materials 0.000 claims description 2
- 239000002826 coolant Substances 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 2
- 230000000737 periodic effect Effects 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- ZCUFMDLYAMJYST-UHFFFAOYSA-N thorium dioxide Chemical compound O=[Th]=O ZCUFMDLYAMJYST-UHFFFAOYSA-N 0.000 claims description 2
- 229910003452 thorium oxide Inorganic materials 0.000 claims description 2
- 239000004480 active ingredient Substances 0.000 claims 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims 1
- 239000004927 clay Substances 0.000 claims 1
- 238000001816 cooling Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 230000009466 transformation Effects 0.000 claims 1
- 239000002699 waste material Substances 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 150000004763 sulfides Chemical class 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000010763 heavy fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- XMYQHJDBLRZMLW-UHFFFAOYSA-N methanolamine Chemical compound NCO XMYQHJDBLRZMLW-UHFFFAOYSA-N 0.000 description 1
- 229940087646 methanolamine Drugs 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 238000001356 surgical procedure Methods 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
- Catalysts (AREA)
- Hydrogen, Water And Hydrids (AREA)
Description
Foreliggende oppfinnelse vedrører en prosess for rensing The present invention relates to a process for cleaning
av rågass som er dannet ved partiell forbrenning av et carbon- of raw gas that is formed by partial combustion of a carbon-
holdig brennstoff og som i det vesentlige inneholder hydrogen og carbonmonoxyd samt sot, hydrogensulfid og carbonylsulfid. Rå- containing fuel and which essentially contains hydrogen and carbon monoxide as well as soot, hydrogen sulphide and carbonyl sulphide. Raw-
gassen inneholder som regel også carbondioxyd og vanndamp samt eventuelt nitrogen. the gas usually also contains carbon dioxide and water vapor and possibly nitrogen.
Brennstoffet feom koks, kull, naturgass, råpetroleum eller The fuel includes coke, coal, natural gas, crude oil or
en rå eller raffinert petroleumsfraksjon) forbrennes med oxygen og/eller luft i et.i det vesentlige tomt reaksjonskammer ved normalt eller forhøyet trykk (eksempelvis ved 20-150 atm.) Det er velkjent innen teknikkens stand å fjerne sot, vanndamp, carbondioxyd, hydrogensulfid og carbonylsulfid fra den produserte rågass i den hensikt å fremstille en passende syntesegass. a crude or refined petroleum fraction) is combusted with oxygen and/or air in an essentially empty reaction chamber at normal or elevated pressure (for example at 20-150 atm.) It is well known in the state of the art to remove soot, water vapour, carbon dioxide, hydrogen sulphide and carbonyl sulphide from the produced raw gas with the intention of producing a suitable synthesis gas.
Vedden partielle forbrenning av et flytende hydrocarbon-brennstoff erholdes ofte sotprosenter på 0,2 - 2,0 vekt% og sulfid^ prosenter på eksempelvis 0,1-0,6 vekt% i rågassen. Av den totale mengde av de tilstedeværende sulfider utgjør hydrogensulfid 90- During the partial combustion of a liquid hydrocarbon fuel, soot percentages of 0.2-2.0% by weight and sulphide percentages of, for example, 0.1-0.6% by weight are often obtained in the raw gas. Of the total amount of sulphides present, hydrogen sulphide accounts for 90-
98 volum%, og resten utgjøres i det vesentlige av carbonylsulfid. 98% by volume, and the rest is made up essentially of carbonyl sulphide.
Sot fjernes generelt ved å vaske rågassen med vann i en vaskekolonne hvorved gassen avkjøles og et vandig sotslam.erholdes derved. Den avkjølte gass føres derefter til en absorberingsanordning hvor sulfider fjernes med en flytende absorbent. Imidlertid absorberer de kjente kjemiske absorbenter (slik som en vandig oppløsning av alkanolaminer) hydrogensulfid lettere enn carbonylsulf id, og det har derfor vært foreslått å utføre en katalytisk omdannelse av carbonylsulfid mellom vaskekolonnen og absorpsjons-anordningen. Carbonylsulfid kan derved omdannes til hydrogensulfid ved hjelp av hydrogen eller damp. Omdannelsen av carbonylsulfid med henholdsvis hydrogen og damp finner sted i henhold til de følgende reaksjonsligninger: Soot is generally removed by washing the raw gas with water in a washing column whereby the gas is cooled and an aqueous soot sludge is thereby obtained. The cooled gas is then fed to an absorption device where sulphides are removed with a liquid absorbent. However, the known chemical absorbents (such as an aqueous solution of alkanolamines) absorb hydrogen sulphide more easily than carbonyl sulphide, and it has therefore been proposed to carry out a catalytic conversion of carbonyl sulphide between the washing column and the absorption device. Carbonyl sulphide can thereby be converted into hydrogen sulphide with the help of hydrogen or steam. The conversion of carbonyl sulphide with hydrogen and steam, respectively, takes place according to the following reaction equations:
Denne katalytiske omdannelse har flere ulemper. Et hoved-problem er at katalysatoren ikke bør fuktes av den vanndampfylte rågass. Ytterligere vil en rask gjentetting av katalysatoren med sotpartikler som fremdeles bæres av den avkjølte rågass fra vaskekolonnen/gjøre prosessen uøkonomisk da det er nødvendig med hyppig regenerering av katalysatoren eller fornyelse av denne. This catalytic conversion has several disadvantages. A main problem is that the catalyst should not be wetted by the steam-filled raw gas. Furthermore, a quick re-clogging of the catalyst with soot particles which are still carried by the cooled raw gas from the washing column/will make the process uneconomic as it is necessary to frequently regenerate the catalyst or renew it.
Foreliggende oppfinnelse har til hensikt å unngå disse ulemper, og det er funnet at dette kan oppnås ved å forhindre at katalysatoren kommer i kontakt med soten som bæres av den avkjølte rågass som kommer fra vaskekolonnen. The present invention aims to avoid these disadvantages, and it has been found that this can be achieved by preventing the catalyst from coming into contact with the soot carried by the cooled raw gas coming from the washing column.
Oppfinnelsen angår således en fremgangsmåte ved rensing av rågass dannet ved partiell forbrenning av et carbonholdig brensel og inneholdende i det vesentlige hydrogen og carbonmonoxyd og dessuten sot, hydrogensulfid og carbonylsulfid, hvor rågassen vaskes med en slik mengde vann eller vanndamp at gassen mettes med vann, hvorefter gassen avkjøles og sot fjernes i stor grad i form av en vandig sotsuspensjon , og den avkjølte gass hvorfra den vandige sotsuspensjon er blitt fjernet, i fravær, av flytende vann The invention thus relates to a method for purifying raw gas formed by partial combustion of a carbonaceous fuel and containing essentially hydrogen and carbon monoxide and also soot, hydrogen sulphide and carbonyl sulphide, where the raw gas is washed with such an amount of water or water vapor that the gas is saturated with water, after which the gas is cooled and soot is largely removed in the form of an aqueous soot suspension, and the cooled gas from which the aqueous soot suspension has been removed, in the absence, of liquid water
bringes i kontakt med en katalysator for omdannelse av carbonylsulfid og derefter behandles med et adsorpsjonsmiddel eller absorpsjonsmiddel for å fjerne hydrogensulfid, og fremgangsmåten ér sær-preget ved at den avkjølte rågass i fravær av flytende vann føres gjennom en hul gasskanal eller gjennom en rekke i det vesentlige parallelle hule gasskanaler som har et (felles) gassinnløp i én ende og et (felles) gassutløp i den annen ende og som har én eller flere vegger med en katalysator for omdannelse av carbonylsulf id anordnet på, i eller bak de nevnte vegger slik at katalysatoren er fritt tilgjengelig for gassen som føres gjennom gass-kanalen(e) fra gassinnløpet til gassutløpet. is brought into contact with a catalyst for the conversion of carbonyl sulphide and then treated with an adsorptive agent or absorbent to remove hydrogen sulphide, and the method is characterized by the fact that the cooled raw gas in the absence of liquid water is passed through a hollow gas channel or through a series of substantially parallel hollow gas channels which have a (common) gas inlet at one end and a (common) gas outlet at the other end and which have one or more walls with a catalyst for the conversion of carbonyl sulphide arranged on, in or behind the said walls so that the catalyst is freely accessible to the gas that is passed through the gas channel(s) from the gas inlet to the gas outlet.
Ved den tidligere kjente fremgangsmåte føres gassen gjennom et katalysatorlag som vil forårsake et trykkfall i rågassen. In the previously known method, the gas is passed through a catalyst layer which will cause a pressure drop in the raw gas.
Ved den foreliggende fremgangsmåte føres gassen langs katalysatoren som er tilstede i, på eller bak kanalveggen(e), hvorved gasskomponentene lett bringes i kontakt med katalysatoren ved diffusjon gjennom kanalveggen(e). Ved denne kontakt vil carbonylsulf id i rågassen omdannes til hydrogensulfid. På den annen side kan sotpartikler som finnes i gassen/passere fra innløpet til ut-løpet gjennom den hule gasskanal(er), hvilket resulterer i at gjen-tetning av systemet unngås. In the present method, the gas is passed along the catalyst which is present in, on or behind the channel wall(s), whereby the gas components are easily brought into contact with the catalyst by diffusion through the channel wall(s). During this contact, carbonyl sulphide in the raw gas will be converted into hydrogen sulphide. On the other hand, soot particles present in the gas/can pass from the inlet to the outlet through the hollow gas channel(s), resulting in the re-sealing of the system being avoided.
En ytterligere fordel ved fremgangsmåten ifølge foreliggende oppfinnelse er at gassen som omdannes, er mettet eller nesten mettet med vanndamp like før omdannelsen av carbonylsulfid og er ved den rette temperatur for denne omdannelse. Følgelig fremmes omdannelsesgraden. A further advantage of the method according to the present invention is that the gas which is converted is saturated or almost saturated with water vapor just before the conversion of carbonyl sulphide and is at the right temperature for this conversion. Consequently, the conversion rate is promoted.
Det er gunstig å utføre carbonylsulfidomdannelsen i et apparat som omfatter én eller flere blokker eller elementer fremstilt av et inert basismateriale og katalysatoren, og som har åpne gasskanaler som løper derigjennom. Således er katalysatoren tilstede i gasskanalveggene. It is advantageous to carry out the carbonyl sulphide conversion in an apparatus which comprises one or more blocks or elements made of an inert base material and the catalyst, and which has open gas channels running therethrough. Thus, the catalyst is present in the gas channel walls.
Det er også gunstig å utføre carbonylsulfidomdannelsen i et apparat omfattende et system av i det vesentlige parallelle gasskanaler og katalysatorkamre, og hvor gasskanalene hver har minst én gasspermeabel vegg felles med et tilstøtende katalysatorkammer. Gasskanalene kan være adskilt fra katalysatorkamrene ved rektan-gulære ark fremstilt av netting, og som i det vesentlige utstrekker seg parallelt til motsatte sidevegger i et hus med felles gassinn-løp og felles gassutløp for gasskanalene, i hvilket hus arkene er innmontert. Det er. også mulig at gasskanalene er adskilt fra katalysatorkamrene ved hjelp av nettingsylindre som har forskjellige diametre og en felles akse. It is also advantageous to carry out the carbonyl sulphide conversion in an apparatus comprising a system of substantially parallel gas channels and catalyst chambers, and where the gas channels each have at least one gas-permeable wall in common with an adjacent catalyst chamber. The gas channels can be separated from the catalyst chambers by rectangular sheets made of netting, which essentially extend parallel to opposite side walls in a house with common gas inlet and common gas outlet for the gas channels, in which house the sheets are installed. It is. also possible that the gas channels are separated from the catalyst chambers by means of mesh cylinders that have different diameters and a common axis.
Gasskanalene kan løpe gjennom et fast lag av katalysatoi?-partikler som inneholdes i et hus hvor gasskanalene er dannet av rør med gasspermeable vegger. I dette tilfelle er katalysatoren tilstede bak gassveggene. The gas channels can run through a solid layer of catalyst particles contained in a housing where the gas channels are formed by pipes with gas-permeable walls. In this case, the catalyst is present behind the gas walls.
Gasskanalene har fortrinnsvis en bredde på 3 - 50 mm, målt perpendikulært på gasskanalveggene, og hvor hver gasskanal er av-grenset på begge sider av et katalysatorkammer og hvor avgrens-ningene er dannet av gasspermeable nettingark som er understøttet i huset i et adskilt og rektangulært forhold. Katalysatorkamrene har fortrinnsvis en bredde på 1-15 mm i en retning perpendikulær på katalysatorkammerveggene. Nettingen har åpninger med et tverr-snitt på 0,5 mm eller mindre, avhengig av katalysatorens partikkel-størrelse. The gas channels preferably have a width of 3 - 50 mm, measured perpendicular to the gas channel walls, and where each gas channel is delimited on both sides by a catalyst chamber and where the delimitations are formed by gas-permeable mesh sheets which are supported in the housing in a separate and rectangular relationship. The catalyst chambers preferably have a width of 1-15 mm in a direction perpendicular to the catalyst chamber walls. The mesh has openings with a cross-section of 0.5 mm or less, depending on the particle size of the catalyst.
Generelt inneholder rågassen, efter at sot er fjernet fra denne ved vannvasking, nok vanndamp til å tillate en i det vesentlige fullstendig hydrolyse av tilstedeværende carbonylsulfid. Hvis ikke tilstrekkelig vanndamp er tilstede, kan ytterligere vanndamp innføres. In general, the raw gas, after soot has been removed from it by water washing, contains enough water vapor to allow substantially complete hydrolysis of the carbonyl sulphide present. If sufficient water vapor is not present, additional water vapor can be introduced.
Det nye carbonylsulfidomdannelsestrinn ifølge foreliggende oppfinnelse er spesielt, men ikke utelukkende, anvendbart på gasser som forlater vaskekolonnen mens de inneholder 10 - 1000 mg sot pr. Nm"^ gass. The new carbonyl sulphide conversion step according to the present invention is particularly, but not exclusively, applicable to gases leaving the scrubbing column while containing 10 - 1000 mg of soot per Nm"^ gas.
Det er foretrukket at den katalytiske omdannelse av carbonylsulfid utføres i en slik grad (men ikke lengere) at den nødvendige kontakttid for å fjerne hydrogensulfid ved hjelp av en absorbent også er tilstrekkelig til å fjerne det gjenværende carbonylsulfid. Ved å omdanne kun endel av det tilstedeværende carbonylsulfid, og således dra nytte av den begrensede mulighet for absorbenten til å absorbere noe carbonylsulfid, kan den nødvendige lengde av kanalen(e) hvori den katalytiske omdannelse utføres, reduseres. It is preferred that the catalytic conversion of carbonyl sulphide is carried out to such an extent (but no longer) that the contact time required to remove hydrogen sulphide by means of an absorbent is also sufficient to remove the remaining carbonyl sulphide. By converting only part of the carbonyl sulphide present, and thus taking advantage of the limited possibility for the absorbent to absorb some carbonyl sulphide, the necessary length of the channel(s) in which the catalytic conversion is carried out can be reduced.
Temperaturen.av rågassen som kommer fra vaskekolonnen, har under den katalytiske omdannelse av carbonylsulfid en temperatur som fortrinnsvis er 120-250°C, og trykket kan i det vesentlige være lik det trykk som anvendes i forbrenningssonen, og trykket vil imidlertid ikke med hensikt i de fleste tilfelle senkes. Trykk på mellom 30 og 150 atm foretrekkes. The temperature of the raw gas coming from the scrubbing column during the catalytic conversion of carbonyl sulphide has a temperature which is preferably 120-250°C, and the pressure can essentially be equal to the pressure used in the combustion zone, and the pressure will not, however, intentionally in most cases are lowered. Pressures of between 30 and 150 atm are preferred.
Slike katalysatorer som kan anvendes for den katalytiske hydrolyse av carbonylsulfid med damp til hydrogensulfid og carbondioxyd, innbefatter blant annet aluminiumoxyd, bauxitt, aktiverte leirer, aluminiumfosfat, thoriumoxyd og magnesiumklorid, skjønt oxydinneholdende materialer for tiden er foretrukket. Hvis hydrogenering av carbonylsulfid med hydrogen til hydrogensulfid og carbonmonoxyd er påtenkt, kan katalysatoren fortrinnsvis inneholde minst ett metall fra gruppen VI og/eller et metall fra y gruppen VIII i det periodiske system for grunnstoffene, enten som sådanne eller som et oxyd eller sulfid derav. Andre metaller eller metallforbindelser kan også være tilstede. En egnet katalysator for hydrolyse av carbonylsulfid består av coboltmolybdat på aluminiumoxyd. Such catalysts which can be used for the catalytic hydrolysis of carbonyl sulphide with steam to hydrogen sulphide and carbon dioxide include among others aluminum oxide, bauxite, activated clays, aluminum phosphate, thorium oxide and magnesium chloride, although oxide-containing materials are currently preferred. If hydrogenation of carbonyl sulphide with hydrogen to hydrogen sulphide and carbon monoxide is envisaged, the catalyst can preferably contain at least one metal from group VI and/or a metal from group VIII in the periodic table of the elements, either as such or as an oxide or sulphide thereof. Other metals or metal compounds may also be present. A suitable catalyst for the hydrolysis of carbonyl sulfide consists of cobalt molybdate on aluminum oxide.
Før rågassen føres gjennom gasskanalen(e) bør den imidlertid først avkjøles fra den temperatur som hersker i forbrenningskammeret,. og som generelt er over 1000°C. Dette utføres fortrinnsvis ved å føre rågassen gjennom en spillvannskoker som kan bestå av et antall spiralformede rør gjennom hvilke rågassen føres, og rundt hvilke et kjølemiddel strømmer. Denne indirekte varmeutveksling bør avkjøle gassen generelt til en temperatur på 150-500°C, og fortrinnsvis til 200-350°C. Derefter føres den partielt avkjølte gass til et vasketårn hvor vann og/eller damp innføres i gass-strømmen for å avkjøle denne til en temperatur som er noe under duggpunktet, eksempelvis (avhengig av-trykket) til eri temperatur på 75-250°C, og mer foretrukket til en temperatur på 120 - 200°C. Efter fraskillelse av den dannede vandige sotsuspensjon gjøres rågassen fortrinnsvis noe mer umettet ved å oppvarme den noe, eller ved å senke trykketnoe, hvorefter gassen innføres i omdannelsessonen. Before the raw gas is passed through the gas channel(s), however, it should first be cooled from the temperature that prevails in the combustion chamber. and which is generally above 1000°C. This is preferably carried out by passing the raw gas through a waste water boiler which can consist of a number of spiral-shaped tubes through which the raw gas is fed, and around which a coolant flows. This indirect heat exchange should generally cool the gas to a temperature of 150-500°C, and preferably to 200-350°C. The partially cooled gas is then led to a washing tower where water and/or steam is introduced into the gas flow to cool it to a temperature slightly below the dew point, for example (depending on the pressure) to a temperature of 75-250°C, and more preferably at a temperature of 120 - 200°C. After separation of the formed aqueous soot suspension, the raw gas is preferably made somewhat more unsaturated by heating it somewhat, or by lowering the pressure somewhat, after which the gas is introduced into the conversion zone.
Efter at omdannelsen av carbonylsulfid er utført, føres rågassen til en vasker for å fjerne eventuell gjenværende sot, hvorefter gassen føres til en absorberingsanordning hvori en absorbent eller adsorbent opptar hydrogensulfid og de spor av carbonylsulfid som fremdeles måtte være tilstede. Fortrinnsvis fjernes også carbondioxyd og vann fra den rensede gass på dette trinn. Blant de absorbenter som kan absorbere H^ S og COS, er forskjellige aminer og substituerte aminer, enten som slike eller i form av en vandig oppløsning. Eksempler på egnede absorbenter er vandige oppløs-ninger av ethanolamin, og fortrinnsvis di-n-propanolamin, di-iso-propanolamin og methanolamin. Blandinger av cyclotetramethylen-sulfon (eller derivater derav) med alkanolaminer, eventuelt sammen med vann, er også egnede absorbenter. Egnede absorbenter innbefatter faste midler som binder hydrogensulfid, som aktivt carbon,.\ jernoxyd og sinkoxyd. After the conversion of carbonyl sulphide has been carried out, the raw gas is sent to a scrubber to remove any remaining soot, after which the gas is sent to an absorption device in which an absorbent or adsorbent absorbs hydrogen sulphide and any traces of carbonyl sulphide that may still be present. Preferably, carbon dioxide and water are also removed from the purified gas at this stage. Among the absorbents that can absorb H 2 S and COS are various amines and substituted amines, either as such or in the form of an aqueous solution. Examples of suitable absorbents are aqueous solutions of ethanolamine, and preferably di-n-propanolamine, di-iso-propanolamine and methanolamine. Mixtures of cyclotetramethylene sulfone (or derivatives thereof) with alkanolamines, possibly together with water, are also suitable absorbents. Suitable absorbents include solid agents that bind hydrogen sulfide, such as activated carbon, iron oxide and zinc oxide.
Eksempel Example
To sammenlignbare eksperimenter ble utfort, dvs. ett for-sbk med en sveveskiktreaktor, og en med en reaktor utstyrt med et antall parallelle gasskanaler og katalysatorkamre (som i det efterfol-gende kalles parallell gjennomgangsreaktor), begge reaktorer inneholdt det samme koboltmolybdat på aluminiumoxydkatalysator. Den fdrstnevn-te reaktor (anerkjent innen teknikkens stand) og den sistnevnte reaktor (påtenkt i henhold til foreliggende oppfinnelse) ble forbundet med en syklon for adskillelse av medbårne vanndråper fra. en syntesegass, mettet med vanndamp. Like mengder rå syntesegass ble innfort i hver separat reaktor. Denne syntesegass var erholdt ved partiell forbrenning av en tung fyringsolje i nærvær av damp ved en temperatur på ca. 1300°C og et trykk på 50 atm. Rågassen var ytterligere blitt avkjolt i en spillvannskoker til en temperatur på 300°C. En storre mengde sot var derefter fjernet ved å vaske rågassen med vann, og gassene som ble utfort fra syklonen hadde en temperatur på- 150°C og et trykk på 28 atm. Rågassen som ble bragt frem til reaktoren var svakt umettet med hensyn til vanndamp, og hadde den omtrentlige sam-mensetning som vist i tabell I, forste spalte. I" annen og tredje spalte i tabell I er angitt komposisjonen av gassen efter henholdsvis gjennomgang av de to nevnte separate reaktorer (verdier som målt efter innsjalting av reaktorene i produksjonsstrengen, efter en "by-pas-s" på flere timer for oppstartningsformål) . Two comparable experiments were carried out, i.e. one trial with a fluidized bed reactor, and one with a reactor equipped with a number of parallel gas channels and catalyst chambers (which is hereinafter called a parallel flow reactor), both reactors containing the same cobalt molybdate on aluminum oxide catalyst. The first-mentioned reactor (recognized in the state of the art) and the last-mentioned reactor (conceived according to the present invention) were connected with a cyclone for separating entrained water droplets from. a synthesis gas, saturated with water vapor. Equal amounts of raw synthesis gas were introduced into each separate reactor. This synthesis gas was obtained by partial combustion of a heavy fuel oil in the presence of steam at a temperature of approx. 1300°C and a pressure of 50 atm. The raw gas was further cooled in a waste water boiler to a temperature of 300°C. A large amount of soot was then removed by washing the raw gas with water, and the gases discharged from the cyclone had a temperature of -150°C and a pressure of 28 atm. The raw gas that was brought to the reactor was slightly unsaturated with respect to water vapor, and had the approximate composition as shown in Table I, first column. In the second and third columns of table I, the composition of the gas is indicated after respectively reviewing the two separate reactors mentioned (values measured after switching on the reactors in the production line, after a "bypass" of several hours for start-up purposes).
Utldpsgassen fra de respektive reaktorer ble fort direkte gjennom en absorpsjonskolonne med et antall bunner hvor gassene ble behandlet med en frisk, vandig 25 vekt%'s oppldsning av di-isopropan-olamin, hvorved H0S-irmholdet i begge tilfelle ble redusert til under 20 volumdeler H,,S pr. IO volumdeler gass (ppm). COS-innholdet var under 70 ppm pr. volum efter absorpsjonstrinnet i begge tilfelle. The exhaust gas from the respective reactors was quickly passed directly through an absorption column with a number of bottoms where the gases were treated with a fresh, aqueous 25% by weight solution of di-isopropanolamine, whereby the H0S content in both cases was reduced to below 20 parts by volume H,,S per IO parts by volume of gas (ppm). The COS content was below 70 ppm per volume after the absorption step in both cases.
Av tabell I kan der sees at den katalytiske omdannelse av COS reduserer det initiale COS-innhold på 500 ppm av gassen i tilfdr-selsledningen for hver av de respektive reaktorer til en verdi på 70 ppm og 80 ppm. Dette innhold kan ytterligere reduseres ved absorp-sjon til ca. 90 % av det innhold gassen har ved utlopet av reaktoren. It can be seen from Table I that the catalytic conversion of COS reduces the initial COS content of 500 ppm of the gas in the supply line for each of the respective reactors to a value of 70 ppm and 80 ppm. This content can be further reduced by absorption to approx. 90% of the content of the gas at the outlet of the reactor.
Efter én dags operasjon ble målingene gjentatt. De er-holdte verdier er vist i tabell II. After one day of surgery, the measurements were repeated. The actual values are shown in Table II.
Som det vil sees av tabell II er den katalytiske omdannelse av COS efter én dag fremdeles meget effektiv for den parallelle gjennomgangsreaktor hvor innholdet er redusert fra 600 ppm til 90 ppm. Imidlertid kan det sees at for sveveskiktsreaktoren er aktiviteten av katalysatoren blitt redusert i slik grad at COS-innholdet av gassen som forlater reaktoren fremdeles er ca. 500 ppm. As will be seen from Table II, the catalytic conversion of COS after one day is still very efficient for the parallel flow reactor where the content has been reduced from 600 ppm to 90 ppm. However, it can be seen that for the fluidized bed reactor the activity of the catalyst has been reduced to such an extent that the COS content of the gas leaving the reactor is still approx. 500 ppm.
Det viste seg igjen at absorpsjonen fjerner nesten all It turned out again that the absorption removes almost all
H2S og ca. 10 % av COS. H2S and approx. 10% of COS.
F^S-innholdet av gassene efter utlopet av absorpsjonsko-lonnen var i begge tilfelle mindre enn 20 ppm. The F^S content of the gases after the outlet of the absorption column was in both cases less than 20 ppm.
COS-innholdet av gassene som lop ut av absorpsjonskolon- The COS content of the gases that ran out of the absorption column
nen var henholdsvis 80 ppm for gassen som var fort gjennom den paral- nen was respectively 80 ppm for the gas that was fast through the parallel
lelle gjennomgangsreaktor, og ca. 440 ppm for gassen som var fort gjennom sveveskiktsreaktoren. small flow reactor, and approx. 440 ppm for the gas that was fast through the fluidized bed reactor.
En sammenligning av data for COS-innholdet i tabeller I A comparison of COS content data in Tables I
og II viser at den parallelle gjennomgangsreaktor som heri beskrevet, and II shows that the parallel flow reactor as herein described,
gir en bedre katalysatoreffektivitet og en mindre deaktivering av katalysatoren. gives a better catalyst efficiency and less deactivation of the catalyst.
Claims (16)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB4079371A GB1404581A (en) | 1971-09-01 | 1971-09-01 | Process for the removal of soot and sulphur compounds from the crude gas generated by the partial combustion of a carbonaceous fuel |
Publications (2)
Publication Number | Publication Date |
---|---|
NO136465B true NO136465B (en) | 1977-05-31 |
NO136465C NO136465C (en) | 1977-09-07 |
Family
ID=10416633
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
NO3083/72A NO136465C (en) | 1971-09-01 | 1972-08-30 | PROCEDURES FOR REMOVING SOOT AND SULFUR COMPOUNDS FROM A COMBUSTION GAS. |
Country Status (10)
Country | Link |
---|---|
JP (1) | JPS4834905A (en) |
BE (1) | BE788068A (en) |
CA (1) | CA968529A (en) |
DE (1) | DE2242543A1 (en) |
FR (1) | FR2150963B1 (en) |
GB (1) | GB1404581A (en) |
IT (1) | IT964288B (en) |
NL (1) | NL7211786A (en) |
NO (1) | NO136465C (en) |
SE (1) | SE381277B (en) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5563926U (en) * | 1978-10-26 | 1980-05-01 | ||
DE3923840C1 (en) * | 1989-07-19 | 1991-01-17 | Rheinische Braunkohlenwerke Ag, 5000 Koeln, De | Prodn. of fuel gas - by partial combustion of carbonaceous materials, cooling, removing suspended solid matter, etc. |
PL2943556T3 (en) * | 2013-01-09 | 2020-09-21 | Thyssenkrupp Industrial Solutions Ag | Process for the hydrogenation of carbon sulphide using a sulphidic cobalt molybdenum catalyst on an aluminium oxide carrier |
US9677018B2 (en) | 2013-01-09 | 2017-06-13 | Thyssenkrupp Industrial Solutions Ag | Process for the production of synthesis gas from hard coal |
DE102013009885A1 (en) * | 2013-01-09 | 2014-07-10 | Thyssenkrupp Uhde Gmbh | Manufacture of synthesis gas used for chemical reactions, involves forming gas mixture of hydrogen and methane by pyrolyzing dry coal, hydrogenating gas mixture using cobalt-molybdenum sulfide catalyst and separating hydrogen sulfide |
-
0
- BE BE788068D patent/BE788068A/en unknown
-
1971
- 1971-09-01 GB GB4079371A patent/GB1404581A/en not_active Expired
-
1972
- 1972-07-26 CA CA148,016A patent/CA968529A/en not_active Expired
- 1972-08-25 IT IT28531/72A patent/IT964288B/en active
- 1972-08-30 SE SE7211236A patent/SE381277B/en unknown
- 1972-08-30 NO NO3083/72A patent/NO136465C/en unknown
- 1972-08-30 FR FR7230740A patent/FR2150963B1/fr not_active Expired
- 1972-08-30 DE DE2242543A patent/DE2242543A1/en active Pending
- 1972-08-30 JP JP47086378A patent/JPS4834905A/ja active Pending
- 1972-08-30 NL NL7211786A patent/NL7211786A/xx not_active Application Discontinuation
Also Published As
Publication number | Publication date |
---|---|
SE381277B (en) | 1975-12-01 |
BE788068A (en) | 1973-02-28 |
JPS4834905A (en) | 1973-05-23 |
NO136465C (en) | 1977-09-07 |
CA968529A (en) | 1975-06-03 |
DE2242543A1 (en) | 1973-03-08 |
IT964288B (en) | 1974-01-21 |
GB1404581A (en) | 1975-09-03 |
FR2150963B1 (en) | 1975-01-03 |
FR2150963A1 (en) | 1973-04-13 |
NL7211786A (en) | 1973-03-05 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US4863489A (en) | Production of demercurized synthesis gas, reducing gas, or fuel gas | |
JP3776152B2 (en) | Method for removing coke on catalytic material | |
US9624106B2 (en) | Supersulf-a process with internal cooling and heating reactors in subdewpoint sulfur recovery and tail gas treating systems | |
US4797268A (en) | Sulfur recovery process using metal oxide absorbent with regenerator recycle to Claus catalytic reactor | |
EA013794B1 (en) | Removal of carbon dioxide from a gas stream | |
US4100107A (en) | Desulfurization of fuel gas at high temperature using supported molten metal carbonate absorbent | |
EA019187B1 (en) | Process for producing purified natural gas | |
CN1101933A (en) | Partial oxidation process for producing a stream of hot purified gas | |
EA012879B1 (en) | Process for producing a gas stream depleted of hydrogen sulphide | |
DK175009B1 (en) | Process for refining raw gases | |
EA014412B1 (en) | Process for producing a purified gas stream | |
US4377396A (en) | Process of purifying exhaust air laden with organic pollutants | |
CN101193690A (en) | Treatment of fuel gas | |
US9023309B1 (en) | Process of conversion sulfur compounds to elemental sulfur by using direct reduction and oxidation catalysts in Claus units | |
JP5217295B2 (en) | Coal gasification gas purification method and apparatus | |
JP3602268B2 (en) | Method and apparatus for removing sulfur compounds contained in natural gas and the like | |
NO136465B (en) | ||
JP4594239B2 (en) | Gas purification system and gas purification method | |
US6960548B2 (en) | Method for regenerating used absorbents derived from treatment of thermal generator fumes | |
JPH0218360B2 (en) | ||
CN107567350B (en) | For removing and recovering H from a gas stream2Improved method of S | |
SU598553A3 (en) | Method of obtaining hydrogen-containing gas | |
JP4651014B2 (en) | Material gasification system and material gasification method | |
JP6576288B2 (en) | Carbon dioxide gas recovery device and carbon dioxide gas manufacturing method | |
Kiani et al. | Syngas conditioning (catalyst, process: sulfur and tar Cl, F) |