NO854681L - PROCEDURE FOR SELECTIVE REMOVAL OF H2O FROM GAS MIXTURES. - Google Patents
PROCEDURE FOR SELECTIVE REMOVAL OF H2O FROM GAS MIXTURES.Info
- Publication number
- NO854681L NO854681L NO854681A NO854681A NO854681L NO 854681 L NO854681 L NO 854681L NO 854681 A NO854681 A NO 854681A NO 854681 A NO854681 A NO 854681A NO 854681 L NO854681 L NO 854681L
- Authority
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- Norway
- Prior art keywords
- zone
- water
- absorption
- stripping
- outside
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 13
- 239000000203 mixture Substances 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000007789 gas Substances 0.000 claims abstract description 39
- 238000010521 absorption reaction Methods 0.000 claims abstract description 26
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 10
- 150000003512 tertiary amines Chemical class 0.000 claims abstract description 10
- 230000008929 regeneration Effects 0.000 claims abstract description 9
- 238000011069 regeneration method Methods 0.000 claims abstract description 9
- 238000009835 boiling Methods 0.000 claims abstract description 8
- 239000003960 organic solvent Substances 0.000 claims abstract description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 4
- 230000006833 reintegration Effects 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 150000001412 amines Chemical class 0.000 description 16
- 239000000243 solution Substances 0.000 description 8
- 239000002253 acid Substances 0.000 description 5
- UEEJHVSXFDXPFK-UHFFFAOYSA-N N-dimethylaminoethanol Chemical compound CN(C)CCO UEEJHVSXFDXPFK-UHFFFAOYSA-N 0.000 description 4
- 239000012972 dimethylethanolamine Substances 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 3
- SJRJJKPEHAURKC-UHFFFAOYSA-N N-Methylmorpholine Chemical compound CN1CCOCC1 SJRJJKPEHAURKC-UHFFFAOYSA-N 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 229960002887 deanol Drugs 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- MCTWTZJPVLRJOU-UHFFFAOYSA-N 1-methyl-1H-imidazole Chemical compound CN1C=CN=C1 MCTWTZJPVLRJOU-UHFFFAOYSA-N 0.000 description 1
- SWKPGMVENNYLFK-UHFFFAOYSA-N 2-(dipropylamino)ethanol Chemical compound CCCN(CCC)CCO SWKPGMVENNYLFK-UHFFFAOYSA-N 0.000 description 1
- BFSVOASYOCHEOV-UHFFFAOYSA-N 2-diethylaminoethanol Chemical compound CCN(CC)CCO BFSVOASYOCHEOV-UHFFFAOYSA-N 0.000 description 1
- FGQBGDBLZZPFCM-UHFFFAOYSA-N 4-methylmorpholin-3-one Chemical compound CN1CCOCC1=O FGQBGDBLZZPFCM-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- -1 dialkyl ether monoethylene glycols Chemical class 0.000 description 1
- 150000001983 dialkylethers Chemical class 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- ZYWUVGFIXPNBDL-UHFFFAOYSA-N n,n-diisopropylaminoethanol Chemical compound CC(C)N(C(C)C)CCO ZYWUVGFIXPNBDL-UHFFFAOYSA-N 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 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
- B01D53/14—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 by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
- Industrial Gases (AREA)
Abstract
Fremgangsmåte for selektiv fjerning av hydrogensulfid fra gassblandinger som også inneholder karbondioksyd, som i alt vesentlig omfatter en abosrbering ved hjelp av en blanding av et lavt-kokende tertiært amin og et organisk løsningsmiddel, med et vanninnhold på høyst 25 vekt*, og en regenerering i en strippe-kolonne av absorbsjons-løsningen og eventuelt et ekspansjons-trinn mellom absorbsjons-sonen og regenerasjons-sonen,at gass-strømmene fra ovennevnte sone bringes i kontakt med vann i den øvre absorbsjons-sone, eller i en utenforliggende sone, og i den øvre strippe-sone, eller i en utenforliggende sone.Process for the selective removal of hydrogen sulphide from gas mixtures which also contain carbon dioxide, which essentially comprises an absorption by means of a mixture of a low-boiling tertiary amine and an organic solvent, with a water content not exceeding 25% by weight *, and a regeneration in a stripping column of the absorption solution and optionally an expansion step between the absorption zone and the regeneration zone, that the gas streams from the above zone are brought into contact with water in the upper absorption zone, or in an outer zone, and in the upper stripping zone, or in an outer zone.
Description
Foreliggende oppfinnelse vedrører en fremgangsmåte for fjerning av hydrogen-sulfid fra gassblandinger som også inneholder karbondioksyd, hvori det anvendes en blanding av et lavt-kokende tertiært amin og et organisk oppløsningsmiddel i vandig løsning som absorbsjons-middel. The present invention relates to a method for removing hydrogen sulphide from gas mixtures which also contain carbon dioxide, in which a mixture of a low-boiling tertiary amine and an organic solvent in aqueous solution is used as absorbent.
Anvendelsen er kjent fra norsk patentansøkning nr. 2120/81The application is known from Norwegian patent application no. 2120/81
av blandinger av tertiære aminer og organiske oppløsnings-midler, med et vanninnhold på 10 vekt% eller mindre, som absorbsj onsmidier. of mixtures of tertiary amines and organic solvents, with a water content of 10% by weight or less, as absorption media.
Anvendelsen av lavt-kokende tertiære aminer i vandige løsninger viser endel ulemper som skyldes at ovennevnte tertiære aminer har en tendens til å fordampe over i den behandlede gassen, noe som gjør at en anvendelse av dem blir problematisk. The use of low-boiling tertiary amines in aqueous solutions shows several disadvantages due to the fact that the above-mentioned tertiary amines tend to evaporate into the treated gas, which makes their use problematic.
Man har nå funnet en fremgangsmåte for selektiv fjerning av hydrogen-sulfid fra hydrokarbon-blandinger som også inneholder karbondioksyd, som også tillater anvendelse av vandige løsninger av lavt-kokende tertiære aminer, uten store tap av aminer. A method has now been found for the selective removal of hydrogen sulphide from hydrocarbon mixtures which also contain carbon dioxide, which also allows the use of aqueous solutions of low-boiling tertiary amines, without large losses of amines.
Fremgangsmåten i henhold til den foreliggende oppfinnelse omfatter i alt vesentlig absorbsjon ved hjelp av lavt-kokende tertiære aminer, og av et organisk oppløsningsmiddel, med et vanninnhold på 25 vekt% eller mindre, og.en regenerering i en strippe-kolonne av den samme absorberende løsningen, og muligens en ekspansjon mellom absorbsjons-sonen og regenerasjons-sonen, og den foreliggende oppfinnelse erkarakterisert vedat gass-strømmene fra de ovennevnte soner anbringes i kontakt med vann i den øvre absorbsjons-sonen eller i en sone utenfor denne, og i den øvre strippe-sonen eller i en sone utenfor denne. The process according to the present invention essentially comprises absorption by means of low-boiling tertiary amines, and of an organic solvent, with a water content of 25% by weight or less, and regeneration in a stripping column of the same absorbent the solution, and possibly an expansion between the absorption zone and the regeneration zone, and the present invention is characterized in that the gas flows from the above-mentioned zones are placed in contact with water in the upper absorption zone or in a zone outside this, and in the upper the stripping zone or in a zone outside this.
I det tilfelle der et ekspansjons-trinn har tilveiebragt mellom absorbsjons-sonen og regenerasjons-sonen, dvs. ved anvendelse av en "flash - ekspansjonsbeholder" sendes gass- strømmene fra ekspansjons-sonen enten til den nedre del av absorbsjons-sonen, eller ut av anlegget, i det annet tilfelle er det nødvendig å bringe ovennevnte gass-strømmer i kontakt med vann i den øvre delen av ekspansjons-sonen, eller i en sone utenfor denne. In the case where an expansion step has been provided between the absorption zone and the regeneration zone, i.e. when using a "flash - expansion container", the gas flows from the expansion zone are sent either to the lower part of the absorption zone, or out of the plant, in the second case it is necessary to bring the above-mentioned gas streams into contact with water in the upper part of the expansion zone, or in a zone outside this.
De lavt-kokende tertiære aminene, som kan anvendes entenThe low-boiling tertiary amines, which can be used either
som rene forbindelser eller i blanding, i overensstemmelse med oppfinnelsen, velges blant dimetyletan-olamin, dietyletanolamin, dipropyletanolamin, diisopropyletanolamin, N-metylmorfolin. as pure compounds or in a mixture, in accordance with the invention, are chosen from dimethylethanolamine, diethylethanolamine, dipropylethanolamine, diisopropylethanolamine, N-methylmorpholine.
De organiske oppløsningsmidlene, som bestanddeler av absorbsjons-løsningen, som kan anvendes enten som rene løsninger eller som blandinger, er sulfolan, N-metylpyrrolidon, N-metyl-3-morfolon, dialkyleter-monoetylenglykoler, dialkyleter-polyetylenglykoler (hvori hver alkyl-gruppe inneholder fra 1 til 4 karbonatomer), etylen-glykol, dietylen-glykol, trietylen-glykol, N,N-dimetylformamid, N-formylmorfolin, N,N-dimetylimidazolidin-2-on og N-metylimidazol. The organic solvents, as components of the absorption solution, which can be used either as pure solutions or as mixtures, are sulfolane, N-methylpyrrolidone, N-methyl-3-morpholone, dialkyl ether monoethylene glycols, dialkyl ether polyethylene glycols (in which each alkyl group contain from 1 to 4 carbon atoms), ethylene glycol, diethylene glycol, triethylene glycol, N,N-dimethylformamide, N-formylmorpholine, N,N-dimethylimidazolidin-2-one and N-methylimidazole.
Gass-strømmenes kontakt med vann er et trinn som viser egenskaper og funksjoner som er helt forskjellige fra vann-vaskingen som ofte anvendes på den rensede gassen som strømmer ut fra øvre del av absorbsjons-kolonnen på de ikke-amin-selektive anleggene. Dette er vist i de ikke-selektive anleggene, ved det at man må vise den største forsiktighet for å minimalisere amin-innholdet i vaskevannet, mens man i foreliggende oppfinnelse eksperimentelt har funnet at vannet som anvendes alltid er svært virkningsfullt, selv når amin-konsentrasjonen blir svært høy. Forsøkene utføres ved at gassen som har fått fjernet f^S, men ennå inneholder CC>2 / bobles gjennom vann. Ved utløpet, var innholdet av aminer (dimetyletanolamin) alltid redusert til ca. 3 ppm, i motsetning til amin-innholdet ved innløpet som var ca. 300 ppm, til tross for stor akkumulering av amin i vannet. Mengden CO^som var absorbert i vannet var støkiometrisk proporsjonal med aminet, noe som klart indikerer dannelse av bikarbonat. Dette vises tydelig i den følgende tabell, hvori DMEA = dimetyletanolamin. The contact of the gas streams with water is a step that shows properties and functions that are completely different from the water washing that is often applied to the purified gas that flows out from the upper part of the absorption column in the non-amine-selective plants. This is shown in the non-selective plants, in that the utmost care must be taken to minimize the amine content in the washing water, while in the present invention it has been experimentally found that the water used is always very effective, even when the amine concentration becomes very high. The experiments are carried out by bubbling through water the gas which has had f^S removed, but still contains CC>2 /. At the outlet, the content of amines (dimethylethanolamine) was always reduced to approx. 3 ppm, in contrast to the amine content at the inlet which was approx. 300 ppm, despite large accumulation of amine in the water. The amount of CO2 absorbed in the water was stoichiometrically proportional to the amine, clearly indicating formation of bicarbonate. This is clearly shown in the following table, where DMEA = dimethylethanolamine.
Måtene man anvender vann på kan være veldig forskjellige. Man bør merke seg, at i de anleggene der man har selektiv fjerning av f^S, er det alltid nødvendig med en liten mengde reintegrasjons-vann, som erstatter vannet som går tapt under avdamping til de sure gassene, til ekspansjons-gassen og til den behandlede gassen. Rågassen er imidlertid vanligvis mettet med vann, men ekspansjonsgassen og de sure gassene er mettet ved lavere trykk, dessuten har den behandlede gassen, ekspansjonsgassen og de sure gassene svært ofte en høyere temperatur enn rågassen, og alt dette fører til et visst vanntap, som må reintegreres fra utsiden. Reintegrasjons-vannet er vanligvis destillert vann eller ionefritt vann. men uansett er vannet fritt for f^S, slik at det med sikkerhet kommer i kontakt med den behandlede gassen. The ways in which water is used can be very different. It should be noted that in those facilities where there is selective removal of f^S, a small amount of reintegration water is always required, which replaces the water lost during evaporation to the acid gases, to the expansion gas and to the treated gas. However, the raw gas is usually saturated with water, but the expansion gas and the sour gases are saturated at lower pressures, moreover the treated gas, the expansion gas and the sour gases very often have a higher temperature than the raw gas, and all this leads to a certain loss of water, which must reintegrated from the outside. The reintegration water is usually distilled water or ion-free water. but in any case the water is free from f^S, so that it is sure to come into contact with the treated gas.
En foretrukket utførelsesform av den foreliggende oppfinnelse omfatter at man først anvender reintegrasjons-vannet i den øvre absorbsjons-sonen, eller i en absorbsjons-sone utenfor denne, deretter i den øvre ekspansjons-sonen eller i en sone utenfor denne, og til slutt i den øvre strippe-sonen eller i en sone utenfor denne, idet man utnytter trykkfallet som normalt er tilstede mellom disse tre sonene: dette fører ikke til tap av aminer til tross for den stadig økende aminkonsentrasjonen i reintegrasjons-vannet. A preferred embodiment of the present invention includes first using the reintegration water in the upper absorption zone, or in an absorption zone outside this, then in the upper expansion zone or in a zone outside this, and finally in the the upper stripping zone or in a zone outside this, making use of the pressure drop that is normally present between these three zones: this does not lead to a loss of amines despite the ever-increasing amine concentration in the reintegration water.
Hvert trinn kan enten utføres i en plate-kolonne eller i en fylt kolonne, såvel som i passende et-trinns vasketårn. Each step can either be carried out in a plate column or in a packed column, as well as in suitable single-stage washing towers.
Anvendelse av vann i strippe-sonen, hvor de sure gassene fjernes, er noe spesielt. The use of water in the stripping zone, where the acid gases are removed, is something special.
Som i alle anlegg hvor det anvendes aminer, inneholder oppløsningsmiddel-regenerasj ons-kolonnen (strippe-kolonnen) en kort rektifikasjons-del med tilbakestrømning av vann, for å fjerne de organiske forbindelsene i absorbsjons-løsningen. Denne tilbakestrømningen er derimot uten noen effekt i tilfelle med lavt-kokende tertiære aminer. As in all facilities where amines are used, the solvent regeneration column (stripping column) contains a short rectification section with backflow of water, to remove the organic compounds in the absorption solution. This reflux, on the other hand, is without any effect in the case of low-boiling tertiary amines.
Topp-kondensatoren av den ovennevnte strippe-kolonne fjerner imidlertid en del aminer, om enn ikke fullstendig. However, the overhead condenser of the above-mentioned stripping column removes some amines, although not completely.
Man har overraskende funnet ved hjelp av forsøk at en fjerning av aminene helt ned til 3-5 ppm, oppnås ved at gass-strømmene fra strippe-sonen kommer i kontakt med vann, dvs. de sure gassene, i en kondensasjons-sone, utenfor strippe-sonen, med et trykkfall som er lik eller større enn It has surprisingly been found by means of experiments that a removal of the amines down to 3-5 ppm is achieved by the gas streams from the stripping zone coming into contact with water, i.e. the acidic gases, in a condensation zone, outside the stripping zone, with a pressure drop equal to or greater than
2 2
0,2 kg/cm .0.2 kg/cm .
Den foreliggende oppfinnelse er illustrert ved hjelp avThe present invention is illustrated by means of
en figur som representerer en utførelsesform ved oppfinnelsen. a figure representing an embodiment of the invention.
Gjennom rørene 1 tilføres gassen som skal behandles til absorbsjons-kolonnen 2, hvortil den absorberende oppløsningen tilsettes gjennom røret 3. Reintegrasjons-vannet 4 tilsettes til den øvre del av absorbsjons-kolonnen, for at aminet skal reagere med de sure gassene. Fra toppen av absorbsjons-kolonnen føres den behandlede gassen ut gjennom røret 5, mens oppløsningen føres ut i bunnen av kolonnen gjennom røret 6, og føres videre til regenerasjons-kolonnen 8 Through the pipes 1, the gas to be treated is supplied to the absorption column 2, to which the absorbent solution is added through the pipe 3. The reintegration water 4 is added to the upper part of the absorption column, so that the amine will react with the acidic gases. From the top of the absorption column, the treated gas is led out through pipe 5, while the solution is led out at the bottom of the column through pipe 6, and is carried on to the regeneration column 8
etter forvarming i 7.after preheating in 7.
Gassene som stiger oppover inne i kolonnen 8 vaskes ved hjelp av noen rektifikasjons-plater, ved hvis utløp de består av sure gasser, damp og rest-aminer. Dampen kondenseres ved at den blandes med kaldt vann, som går i motstrøm med dampen inne i fyllingen 10. Som i fyllingens øvre del forblir temperaturen lav, og aminet kan reagere med de sure gassene, og kan gjenvinnes. De sure gassene føres ut av anlegget gjennom røret 11. Pumpen 12 sirkulerer vannet, som er avkjølt i varmeveksleren 13. Det meste av vannet tilføres fyllingen 10 gjennom røret 14, mens en liten del føres tilbake som en tilbakestrømning til rektifikasjons-delen under ved hjelp av røret 15. The gases that rise up inside the column 8 are washed by means of some rectification plates, at the outlet of which they consist of acid gases, steam and residual amines. The steam is condensed by mixing it with cold water, which goes countercurrently with the steam inside the filling 10. As in the upper part of the filling, the temperature remains low, and the amine can react with the acid gases, and can be recovered. The acid gases are led out of the plant through the pipe 11. The pump 12 circulates the water, which is cooled in the heat exchanger 13. Most of the water is supplied to the filling 10 through the pipe 14, while a small part is led back as a return flow to the rectification part below using of the pipe 15.
Fra bunnen av kolonnen 8 føres den regenererte løsningen 16 ut, hvorpå den resirkuleres ved hjelp av pumpen 17 til absorbsjons-kolonnen 2 etter at den er blitt avkjølt i 7, ved hjelp av varmeveksling med løsningen 6, og i 18. From the bottom of the column 8, the regenerated solution 16 is fed out, after which it is recycled by means of the pump 17 to the absorption column 2 after it has been cooled in 7, by means of heat exchange with the solution 6, and in 18.
Claims (8)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT23740/84A IT1177325B (en) | 1984-11-26 | 1984-11-26 | PROCEDURE FOR THE SELECTIVE REMOVAL OF HYDROGEN SULFUR FROM GASEOUS MIXTURES ALSO CONTAINING CARBON DIOXIDE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO854681L true NO854681L (en) | 1986-05-27 |
Family
ID=11209582
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO854681A NO854681L (en) | 1984-11-26 | 1985-11-22 | PROCEDURE FOR SELECTIVE REMOVAL OF H2O FROM GAS MIXTURES. |
Country Status (14)
| Country | Link |
|---|---|
| JP (1) | JPS61136422A (en) |
| AU (1) | AU5005085A (en) |
| BR (1) | BR8506066A (en) |
| DD (1) | DD239728A5 (en) |
| DE (1) | DE3541797A1 (en) |
| DK (1) | DK544285A (en) |
| ES (1) | ES8607182A1 (en) |
| FR (1) | FR2573672A1 (en) |
| GB (1) | GB2167738A (en) |
| HU (1) | HUT41996A (en) |
| IT (1) | IT1177325B (en) |
| NO (1) | NO854681L (en) |
| PL (1) | PL256451A1 (en) |
| SE (1) | SE8505462L (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1244687B (en) * | 1991-01-24 | 1994-08-08 | Snam Progetti | PROCESS FOR THE REMOVAL OF ACID GASES FROM GASEOUS MIXTURES |
| DE19753903C2 (en) * | 1997-12-05 | 2002-04-25 | Krupp Uhde Gmbh | Process for the removal of CO¶2¶ and sulfur compounds from technical gases, in particular from natural gas and raw synthesis gas |
| EP1022046A1 (en) * | 1999-01-22 | 2000-07-26 | Krupp Uhde GmbH | Process for removing carbon dioxide, sulphur compounds, water and aromatic and higher aliphatic hydrocarbons from technical gases |
| JP3969949B2 (en) | 2000-10-25 | 2007-09-05 | 関西電力株式会社 | Amine recovery method and apparatus, and decarbonation gas apparatus provided with the same |
| JP4625478B2 (en) * | 2007-03-26 | 2011-02-02 | 関西電力株式会社 | Amine recovery method and apparatus, and decarbonation apparatus equipped with the same |
| JP6925936B2 (en) * | 2017-10-31 | 2021-08-25 | 三菱重工エンジニアリング株式会社 | Acid gas removal device and acid gas removal method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1105330A (en) * | 1965-12-31 | 1968-03-06 | Power Gas Ltd | Improvements in or relating to the regeneration of absorbent liquor containing dissolved acidic gases |
| DE2831040A1 (en) * | 1977-07-18 | 1979-02-08 | Elf Aquitaine | PROCESS FOR DE-ACIDIFICATION OF A GAS MIXTURE |
| IT1132170B (en) * | 1980-07-04 | 1986-06-25 | Snam Progetti | SELECTIVE SEPARATION PROCESS OF HYDROGEN SULFURATED FROM GASEOUS MIXTURES CONTAINING ALSO CARBON DIOXIDE |
| US4289738A (en) * | 1980-07-22 | 1981-09-15 | The Dow Chemical Company | Process for removing H2 S from sour gases with generation of a Claus feed gas |
| US4397660A (en) * | 1981-06-15 | 1983-08-09 | Shell Oil Company | Process for the removal of H2 S and CO2 from a gas mixture |
-
1984
- 1984-11-26 IT IT23740/84A patent/IT1177325B/en active
-
1985
- 1985-11-19 SE SE8505462A patent/SE8505462L/en not_active Application Discontinuation
- 1985-11-19 AU AU50050/85A patent/AU5005085A/en not_active Abandoned
- 1985-11-19 GB GB08528410A patent/GB2167738A/en not_active Withdrawn
- 1985-11-22 ES ES549799A patent/ES8607182A1/en not_active Expired
- 1985-11-22 NO NO854681A patent/NO854681L/en unknown
- 1985-11-25 FR FR8517403A patent/FR2573672A1/en not_active Withdrawn
- 1985-11-25 BR BR8506066A patent/BR8506066A/en unknown
- 1985-11-25 HU HU854487A patent/HUT41996A/en unknown
- 1985-11-25 DK DK544285A patent/DK544285A/en not_active Application Discontinuation
- 1985-11-25 DD DD85283214A patent/DD239728A5/en unknown
- 1985-11-26 DE DE19853541797 patent/DE3541797A1/en not_active Ceased
- 1985-11-26 JP JP60263924A patent/JPS61136422A/en active Pending
- 1985-11-26 PL PL25645185A patent/PL256451A1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| AU5005085A (en) | 1986-06-05 |
| GB2167738A (en) | 1986-06-04 |
| BR8506066A (en) | 1986-08-19 |
| HUT41996A (en) | 1987-06-29 |
| IT8423740A0 (en) | 1984-11-26 |
| PL256451A1 (en) | 1986-09-23 |
| ES8607182A1 (en) | 1986-05-16 |
| SE8505462L (en) | 1986-05-27 |
| GB8528410D0 (en) | 1985-12-24 |
| FR2573672A1 (en) | 1986-05-30 |
| IT1177325B (en) | 1987-08-26 |
| DK544285D0 (en) | 1985-11-25 |
| DD239728A5 (en) | 1986-10-08 |
| JPS61136422A (en) | 1986-06-24 |
| SE8505462D0 (en) | 1985-11-19 |
| ES549799A0 (en) | 1986-05-16 |
| DE3541797A1 (en) | 1986-05-28 |
| DK544285A (en) | 1986-05-27 |
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