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GB2191419A - Process for the selective removal of hydrogen sulphide - Google Patents

Process for the selective removal of hydrogen sulphide Download PDF

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Publication number
GB2191419A
GB2191419A GB08712025A GB8712025A GB2191419A GB 2191419 A GB2191419 A GB 2191419A GB 08712025 A GB08712025 A GB 08712025A GB 8712025 A GB8712025 A GB 8712025A GB 2191419 A GB2191419 A GB 2191419A
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Prior art keywords
process according
tert
bis
ethane
solution
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GB08712025A
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GB8712025D0 (en
GB2191419B (en
Inventor
Luigi Gazzi
Carlo Rescalli
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SnamProgetti SpA
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SnamProgetti SpA
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    • 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
    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
    • C10K1/14—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic
    • C10K1/143—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic containing amino groups
    • 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
    • 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
    • B01D53/1487—Removing organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/16—Hydrogen sulfides
    • C01B17/167—Separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Gas Separation By Absorption (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Treating Waste Gases (AREA)

Description

GB 2 191 419A 1
SPECIFICATION
Process for the selective removal of hydrogen sulphide The present invention relates to a process for the selective removal of acidic gases from natural 5 gases, or synthesis gases.
More particularly, the present invention relates to a process for the selective removal of H2S and of other sulphur compounds (COS, CS2, mercaptans, sulphides) from natural gases or synthesis gases, which contain also Co'.
The problem of the selective removal of hydrogen sulphide and of other sulphur compounds 10 (COS, CS,, mercaptans) from natural gases or synthesis gases also containing CO, has been felt in the industry for a long time. Many situations exist in fact, in which it is desirable to remove as completely as possible the hydrogen sulphide, and other sulphur compounds, leaving most of C02 in the processed gas.
Here is a list of the most frequent cases:. 15 -In the gas natural industry, specifications are in force, which are very restrictive (2-5 ppm) for H2S, which is a poison, and are, on the contrary, rather wide (0.5-3%) for C02, which is an inert substance only.
When the content Of C02 in the processed gas is low, it is expedient to remove H2S only, with the C02 removal costs being saved. 20 -Some natural gases and some raw synthesis gases contain a small amount of H2S and a large amount Of C021 so that, by using a non-selective de-acidification process, the stream of sepa rated acidic gases would contain, as a result, very diluted H2S, generating problems in the downstream Claus unit for sulphur production. All this can be avoided by the adoption of a selective process. 25 -One of the methods for the purification of the off-gas from the Claus unit consists in the reduction of the residual sulphur compounds into H2S, in the separation of H2S from inerts and C02, and in the recycle of the concentrated HS stream to the Claus unit. In this case, a selective process is essential, otherways making C02 leave the sstern would not be possible.
The selective separation of hydrogen sulphide from carbon dioxide is a rather difficult problem, 30 in as much as both of these components are, as such, and potentially acidic.
The process routes of the prior art consist of an absorption step and of a regeneration step.
The raw gas is purified from H2S and from the sulphur compounds in the absorption section, by washing by means of the regenerated solution. The rich solution exiting the absorpion section is regenerated by stripping with steam or with an inert gas in the regeneration section. 35 Whilst the regeneration section does not involve problems, the absorption section was found to pose some problems. In fact, the removal of the undesired compounds is accompanied by the evolution of heat, which heats the solution, decreasing the acidic load which can be achieved. The circulation of absorber solution results large.
It is known, even if scarcely practiced, that one of the means for decreasing the circulation of 40 the absorber solution of the aminic plants, is that of cooling once, or more times, the absorber solution during the absorption, by drawing it from a suitable plate of the absorber tower, and reintroducing it, after cooling, to the immediately lower plate.
In case of a packed absorber tower, the constructive accomplishment of the cooling is more complex, in that for each cooling, it is necessary to insert in the tower a stack-plate, to be able 45 to collect and draw the absorber solution. Very often, this complication, and the related cost are accepted, because many times-the packed absorber tower results cheaper than the plate absorber tower.
We have found now that by using determined tertiary amines, and/or sterically hindered primary and/or secondary amines, according to the hereunder disclosed scheme, it is possible to 50 solve the problem posed by the selective spearation of hydrogen sulphide, and/or of the other sulphur compounds (COS, CS2, mercaptans) from carbon dioxide. The solvents of the process according to the invention are tertiary amines and/or sterically hindered primary and/or secondary amines in solution in water and/or in an organic solvent. 55 The tertiary amines are seicted from those wherein the three hydrogen atoms of ammonia are 55 substituted by alkyl or alkanol groups. The alkyl groups must have from one to four carbon atoms, arranged in either a linear or branched chain. The alkanol groups must have from two to five carbon atoms, they too in a linear or branched chain. The hydroxy functions of the alkanol groups must be not more than two, and may be bonded to any carbon atoms. At least one of the three groups must be an alkanol group. 60 The preferred tertiary amines are: methyidiethanolamine, dimethylethanolamine, ethyidiethano lamine, diethylethanolamine, methyidiisopropyla mine, diisopropylethanolamine, N,N-dimethyl nolamine, 2-dimethylamino-2-methyi-1,3-propanediol, 2-methyi-2-(methyl-,8- hydroxyethylami- no)-1-propanol, N,N-dimethy]-2-amino-propan-l-ol. 65 2 GB 2 191 419A 2 Among the sterically hindered primary and secondary amines which can be advantageously used in the present invention, we remind the diamino-ethers, in which either one or both of the amino-groups can be also tertiary, as well as the amino-alcohols, which may possibly contain ether groups.
The preferred sterically hindered amines are: 1,2-bis-(tertbutylaminoethoxy)-ethane, 1-(pyrro- 5 lidinylethoxy)-2(tert-butylaminoethyoxy)-ethane, tertbutylaminoethoxyethanol, 2-(2-tert-buty [amino)-propoxyethanol, 2-(2-isopropylamino)-propoxyethanol, tert- amyiaminoethoxyethanol, (1 -methy]- 1 -ethylpropylamino)-ethoxyethanol, N-methyi-N-tertbutylaminoethoxyethanol, 2-(N-isopropyi-N-methylamino)-propoxyethanol, 3-aza-2,2,3-trimethyi-1,6- hexanediol, tert--- butylaminoethanol, 2-tert-butylamino-l-propanol, 2-isopropylamino-l- propanol, (3-tert-buty10 [amino)-n-butanol, 3-aza-2,2-dimethy]-1,6-hexanediol, 3-tertbutylamino-l- propanol, bis(tert-butylaminoethyi)-ether, 1,2-bis(tert-butylaminoethoxy)- ethane, bis-(2-isopropylaminopropyi) -ether, 1,2-bis- (pyrrolidinylethoxy)ethane, 1,2-bis-(3-pyrrolidinyi-n-propoxy)-ethane, bis-(Npyrrolidinylethyi)-ether, 1,2-bis-(pyperidinylethoxy)-ethane, 1- (pyrrolidinylethoxy)-2(tert-butylaminoethoxy)-ethane. 15 The amines can be used alone, or mixed with each other.
The organic solvent can be selected from N-methyl-3morpholone, sulpholane, N-methyl-pyrrolidone, N-phenyimorpholine, N,N-dimethylimidazolydin-2-one, methanol, N-methyl-imidazole, n-butanol. These organic solvents can be used alone, or mixed with each other.
In the circulating solutions, the content of the constituents is preferably as follows: 20 -the amine, or the amines, in the proportion of from 20 to 96% by weight, more preferably of from 20 to 90% by weight, still more preferably of from 30 to 50% by weight; -water, in the proportion of from 2 to 70% by weight, more preferably of from 4 to 22% by weight; -the possible organic solvents, in such a proportion as to constitute the balance to 100%. 25 The process according to the invention comprises an absorption section, inside the absorber unit of which the sulphur compounds contained in the natural gas or in the synthesis gas are absorbed by means of an absorber solution, and a regeneration section, wherein the absorber solution is regenerated by means of stripping by steam or by an inert gas, in the regeneration unit. 30 The other basic characteristics of the present process consists in mixing the gas leaving the absorber unit with the regenerated solution, then cooling in a heat exchanger the so-formed mixture, and finally separating the purified gas from the absorber solution, which is fed to the top of the absorber tower.
The absorber tower can be of the plate-type, or of the packed-type: in fact, by such a 35 refrigerator, also the advantage is achieved that the use of a packed absorber does not require the above mentioned constructive complications.
In order to obtain a good mixing of the absorber solution with the gas leaving the absorber tower top, the absorber solution can be nebulized before being introduced into the overhead gas stream, or the overhead gas stream can be intaken by means of an ejector, the drive fluid of 40 which is constituted by the absorber solution, or, according to a further variant, by using a Venturi scrubber.
The subject process of the present invention is recommended in particular in case of selective removal of H,S and of at least one further sulphur compound (COS, CS,, mercaptans).
Some Examples are now given to the purpose of better illustrating the invention, which 45 Examples are not to be regarded as being limitative of the same invention.
Examples 1-2
A raw gas, having the following composition:
50 H2S 1.600% by volume C02 12.500% by volume CH, 85.864% by volume COS 0.017% by volume - CH,SH 0.019% by volume 55 100.000% by volume available under the pressure of 63.8 kg/CM2, and at the temperature of 2M, and flowing at a flowrate of 19,289.5 kmol/h was treated according to the present process: in Example 1, with 60 an aqueous solution of tertiary amines; and in Example 2, with a prevailingly organic solution of tertiary amines, with in both of the Examples a refrigerator being used for refrigerating the regenerated solution mixed with the overhead gas absorber, plus a 7- theoretical-plate absorber, with the results as shown in Table 1 (wherein also the operating conditions are reported) being obtained. 65 3 GB 2 191 419A 3 Examples 34 (Comparative Examples) The same raw gas as specified above was treated: in Example 3, with the same aqueous solution of Example 1; and, in Example 4: with the same previalingly organic solution of tertiary amines of Example 2, with an 8-theoretical-plate absorber tower and two intercoolers being 5 used, without the gas exiting the absorber unit being mixed with the regenerated absorber solution, with the results as reported in Table 1 being obtained.
From a reading of said Table, we can observe that, by adopting the process according to the present patent application, a descrease is obtained in the circulation stream of the absorber solution, with a consequent reduction in costs. 10 Table 1
Examples 1 2 3 4 -Absorber solution MDEA, % by weight 50 - 50 - 15 H,O, % by weight 50 10 50 10 NIVIP, % by weight - 50 - 50 DMEA, % by weight 40 40 -Treated gas H2S, ppm by vol. 4 4 4 4 20 C021 % by vol. 5.4 9.8 5.5 9.4 COS, ppm by vol. 166 1 165 1 CH3SH, ppm by vol 1 1 2 1 -Duties, MIVIKcal/h Pre-saturator 18.7 7.2 - 25 1 st Intercooler - 4.5 3.7 2nd Intercooler 8.5 1.6 Refrigerating gas - - 5.8 2.8 -Absorber bottom temp., 'C 43 41 - 47 42 -Solution circulation, t/h 572 483 605 559 30 -Circulation decrease, % 5.45 13.6 - - wherein:
MDEA = Methyidiethanolamine, NIVIP = N-methylpyrrolidone, 35 DMEA = Dimethyiethanolamine.

Claims (13)

1. A process for the selective removal of a sulphur compound from a natural or synthesis gas which additionally contains carbon dioxide, in an apparatus comprising an absorption section 40 in which the sulphur compound contained in the natural or synthesis gas is absorbed by means of an absorber solution and a regeneration section in which the absorber solution is regenerated; at least part of the gas leaving the absorption section being mixed with at least part of the regenerated solution and the resulting mixture then being separated, after being cooled, so that the purified gas and the absorber solution are obtained, at least part of the absorber solution 45 being fed to the absorption section; and the absorber solution comprising:
(1) one or more amines selected from tertiary amines wherein the nitrogen atom is bonded to three groups, namely (a) an alkyl group, (b) an alkanol group, and (c) a (same or different) alkyl or alkanol group, the alkyl groups being linear or branched groups having from 1 to 4 carbon atoms, and the alkanol groups being linear or branched groups having from 2 to 5 carbon atoms 50 and not more than two hydroxy groups bonded to any one of the carbon atoms, and/or from sterically hindered primary and/or secondary amines selected from diaminoethers and aminoalco hols the latter optionally containining one or more ether groups; and (2) one or more organic solvents and/or water, said organic solvents being selected from compounds able to keep in solution, in one single liquid phase, both the amine or arnines and 55 water.
2. A process according to claim 1, wherein the tertiary amine is one or more of methyidieth anolamine; dimethylethanolamine; ethyldiethanolamine; diethylethanolamine; methyidiisopropylam ine; diisopropylethanolamine; N,N-dimethy]-2-amino-2-methylpropan- 1 -ol; N,N-dimethyl -2-amino2-methylbutan-l-ol; propyidiisopropanolamine; 2-dimethylamino-2methyi-1,3-pro- 60 panediol; 2-methyi-2-(methyi-p-hydroxyethylamino)-1-propanol; and N,Ndimethyl-2-amino propan- 1 -ol.
3. A process according to claim 1 or 2, wherein the sterically hindered amine is one or more of 1,2-bis-(tertbutylaminoethoxy)-ethane; 1-(pyrrolidinylethoxy)-2-(tert- butylaminoethoxy)-eth- ane; tert-butylaminoethoxyethanol; 2-(2-tert-butylamino)-propoxyethanol; 2-(2-isopropylami- 65 4 GB 2 191 419A 4 no)-propoxyethanol; tert-amyiaminoethanoxyethanol; (1 -methyl- 1 ethylpropylamino)-ethoxyethanol; N-methy]-N-tert-butylaminoethoxyethanol; 2-(N-isopropyi-N-methylamino)-propoxyethanol; 3-aza2,2,3-trimethyi1,6hexanediol; tert-butylaminethanol; 2-tert-butylamino-l-propanol; 2-isopropylamino-lpropanol; (3-tertbutylamino)-n-butanol; 3-aza-2,2-dimethyi-l, 6-hex- andiol; 3tert-butylamino-l-propanol; bis(tert-butylaminoethyl)-ether; 1,2- bis-(tert-butylaminoe- 5 thoxy)-ethane; bis-(2-isopropylaminopropyi)- ether; 1,2-bis-(pyrrolidinylethoxy)ethane; 1,2-bis-(3-pyrrolidinyl-npropoxy)-ethane; bis(N-pyrrolidinylethyi)-ether; 1,2-bis(pyperidinylethoxy)-ethane; and 1(pyrrolidinylethoxy)-2-(tertbutylaminoethoxy)-ethane.
4. A process according to any of claims 1 to 3, wherein the organic solvent is one or more of N-methyl-3-morpholone; sulpholane; N-methyl-pyrrolidone; N,N- dimethylimidazolydin-2-one; 10 methanol; N-methylimidazole; and n-butanol.
5. A process according to any of claims 1 to 4, wherein the absorber solution comprises said amine or amines in an amount of from 20 to 90% by weight, water in an amount of from 2 to 70% by weight, and optionally said organic solvent or solvents forming the balance to 100% by weight. 15
6. A process according to claim 5, wherein the water is present in an amount of from 4 to 22% by weight.
7. A process according to any of claims 1 to 6, wherein the mixing of the gas leaving the absorption section with the regenerated solution is effected by nebulizing the regenerated solu tion before introducing it into a referigerator unit together with said gas. 20
8. A process according to claim 7, wherein the mixing is carried out by means of an ejector the drive fluid of which is the regenerated solution.
9. A process according to claim 7, wherein the mixing is carried out by means of a Venturi scrubber.
10. A process according to any of claims 1 to 9, wherein the absorber solution comprises at 25 least one of said tertiary amines and at least one of said sterically hindered primary and/or secondary amines.
11. A process according to any of claims 1 to 10, wherein the absorber solution comprises said amine or amines in an amount of from 20 to 96% by weight.
12. A process according to any of claims 1 to 11, wherein said sulphur compound is H2S, 30 COS, CS, or a mercaptan.
13. A process according to claim 1, substantially as described in any of the Examples.
Printed for Her Majesty's Stationery Office by Burgess & Son (Abingdon) Ltd, Dd 8991685, 1987. Published at The Patent Office, 25 Southampton Buildings, London, WC2A 1 AY, from which copies may be obtained.
GB8712025A 1986-06-11 1987-05-21 Process for the selective removal of hydrogen sulphide Expired - Fee Related GB2191419B (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
IT20757/86A IT1191805B (en) 1986-06-11 1986-06-11 PROCESS FOR SELECTIVE REMOVAL OF SULPHIDIC ACID

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GB8712025D0 GB8712025D0 (en) 1987-06-24
GB2191419A true GB2191419A (en) 1987-12-16
GB2191419B GB2191419B (en) 1990-04-25

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GB8712025A Expired - Fee Related GB2191419B (en) 1986-06-11 1987-05-21 Process for the selective removal of hydrogen sulphide

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JP (1) JPS62292888A (en)
DE (1) DE3717556C2 (en)
GB (1) GB2191419B (en)
IT (1) IT1191805B (en)
NO (1) NO872369L (en)
NZ (1) NZ220366A (en)
SE (1) SE8702301L (en)

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EP0588178A2 (en) * 1992-09-16 1994-03-23 The Kansai Electric Power Co., Inc. Process for removing carbon dioxide from combustion gases
EP0672446A2 (en) * 1994-03-18 1995-09-20 The Kansai Electric Power Co., Inc. Method for the removal of hydrogen sulfide present in gases
US5861051A (en) * 1996-03-06 1999-01-19 Huntsman Petrochemical Corporation Process for removing carbon dioxide from gas mixture
US6051056A (en) * 1998-03-20 2000-04-18 Air Products And Chemicals, Inc. Alkylated aminoether surfactants
US6689332B1 (en) 1992-09-16 2004-02-10 The Kansai Electric Power Co, Inc. Process for removing carbon dioxide from combustion gases
US6740230B1 (en) 1999-07-15 2004-05-25 Basf Aktiengesellschaft Method for removing mercaptans from fluid fluxes
US7175820B2 (en) 2002-12-10 2007-02-13 Institut Francais Du Petrole Natural gas deacidizing and dehydration method
US7857891B2 (en) 2003-03-21 2010-12-28 Dow Global Technologies Inc. Composition and method for removal of carbonylsulfide from acid gas containing same
FR2961114A1 (en) * 2010-06-09 2011-12-16 Inst Francais Du Petrole Removing carbon dioxide from flue gases, comprises a absorption step of contacting flue gases with an absorbent solution comprising water and diamine e.g. 1,2-bis(2-dimethylaminoethoxy)ethane and 1,2-bis(2-pyrolidinoethoxy)ethane
FR2982170A1 (en) * 2011-11-09 2013-05-10 IFP Energies Nouvelles PROCESS FOR REMOVING ACIDIC COMPOUNDS FROM A GASEOUS EFFLUENT WITH AN ABSORBENT SOLUTION BASED ON DIHYDROXYALKYLAMINES HAVING A SEVERE STERIC SIZE OF THE NITROGEN ATOM
WO2014001664A1 (en) 2012-06-26 2014-01-03 IFP Energies Nouvelles Absorbent solution made from tertiary diamines belonging to the hindered aminoethyl morpholine family and method for eliminating acid compounds from a gaseous effluent
WO2017055087A1 (en) * 2015-09-29 2017-04-06 Basf Se Absorption agent and a method for selectively removing hydrogen sulphide
WO2019043099A1 (en) * 2017-09-04 2019-03-07 Basf Se Absorbent and process for selectively removing hydrogen sulfide
CN109499335A (en) * 2018-11-14 2019-03-22 江苏科创石化有限公司 A kind of bulky amine composite desulfurizing agent
CN110876878A (en) * 2018-09-06 2020-03-13 中国石油化工股份有限公司 SO2Absorbent and absorption of SO2Method (2)

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CN103201014B (en) * 2010-10-29 2017-02-08 亨斯迈石油化学有限责任公司 Use of 2-(3-aminopropoxy)ethan-1-ol as an absorbent to remove acidic gazes
WO2012135178A1 (en) * 2011-03-28 2012-10-04 The Board Of Trustees Of The University Of Alabama N-functionalized imidazole-containing systems and methods of use
AU2016330648A1 (en) 2015-09-29 2018-03-29 Basf Se Method for the selective removal of hydrogen sulfide
CN111744350A (en) * 2019-03-29 2020-10-09 中国石油天然气股份有限公司 Desulfurizing agent and preparation method thereof
CN116550100A (en) * 2023-05-30 2023-08-08 江苏太湖新材料控股有限公司 Desulfurizing agent and preparation method thereof

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SE8702301D0 (en) 1987-06-02
DE3717556C2 (en) 1994-04-28
GB2191419B (en) 1990-04-25
IT8620757A1 (en) 1987-12-11
JPS62292888A (en) 1987-12-19
NO872369D0 (en) 1987-06-05
NZ220366A (en) 1990-07-26
NO872369L (en) 1987-12-14
SE8702301L (en) 1987-12-12
IT8620757A0 (en) 1986-06-11
DE3717556A1 (en) 1987-12-17
IT1191805B (en) 1988-03-23

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