[go: up one dir, main page]

WO2003013699A1 - Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides - Google Patents

Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides Download PDF

Info

Publication number
WO2003013699A1
WO2003013699A1 PCT/EP2002/008935 EP0208935W WO03013699A1 WO 2003013699 A1 WO2003013699 A1 WO 2003013699A1 EP 0208935 W EP0208935 W EP 0208935W WO 03013699 A1 WO03013699 A1 WO 03013699A1
Authority
WO
WIPO (PCT)
Prior art keywords
absorbent
gas
piperazine
gases
absorption
Prior art date
Application number
PCT/EP2002/008935
Other languages
German (de)
English (en)
Inventor
Christoph Grossmann
Rupert Wagner
Randolf Hugo
Original Assignee
Basf Aktiengesellschaft
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Basf Aktiengesellschaft filed Critical Basf Aktiengesellschaft
Publication of WO2003013699A1 publication Critical patent/WO2003013699A1/fr

Links

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
    • B01D53/1456—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
    • B01D53/1456—Removing acid components
    • 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

Definitions

  • the present invention relates to a method for removing acid gases from fluids.
  • the present invention further relates to the absorbent itself and its use.
  • fluid flows occur which contain acid gases, such as C0 2 , H 2 S, S0 2 , CS 2 , HCN, COS or mercaptans, as impurities.
  • These fluid streams can be, for example, gas streams (such as natural gas, synthesis gas from heavy oil or heavy residues, refinery gas or the partial oxidation of organic materials such as coal or petroleum, resulting reaction gases) or liquid or liquefied hydrocarbon streams (such as LPG (liquified petroleum gas) or NGL (natural gas liquids)).
  • LPG liquid petroleum gas
  • NGL natural gas liquids
  • the chemical solvents include, in particular, the aqueous solutions of primary, secondary and tertiary aliphatic amines or alkanolamines such as monoethanolamine (MEA), diethanolamine (DEA), monomethylethanolamine (MMEA), diethylethanolamine (DEEA), triethanolamine (TEA), diisopropanolamine (DIPA) and methyldiethanolamine (MDEA) technically proven.
  • Primary and secondary amines can react with CO 2 to form carbamates.
  • C0 2 with water can also form carbonates and bicarbonates and H 2 S with water sulfides and bisulfides. Due to the presence of primary or secondary amines, the equilibria are significantly shifted to the side of the ionic products, ie more C0 2 can be taken up in chemically bound form than in water.
  • tertiary alkanolamines do not react directly with CO 2 since the amine is fully substituted. Rather, C0 2 is converted into bicarbonate in a slow reaction with water.
  • EP 202 600 (CA 1,295,810), EP 190 434 (CA 1,290,553) and EP 159 495 disclose absorbents with 20 to 70% by weight, preferably 30 to 65% by weight, particularly preferably 40 to 60% by weight of MDEA and 0.05 to 1 mol / 1, preferably 0.1 to 0.8 mol / 1, particularly preferably 0.1 to 0.6 mol / 1 piperazine.
  • EP 359 991 (US 4,999,031) discloses absorbents with 20 to 70 wt.%, Preferably 30 to 65 wt.%, Particularly preferably 35 to 60 wt.% MDEA and 0.05 to 3 mol / 1, preferably 0. 1 to 2 mol / 1, particularly preferably 0.1 to 1 mol / 1, perazine.
  • the application DE 198 28 977 (WO 00/00271) relates to an absorbent containing 0.1 to 50% by weight of nitrogen heterocycles, such as piperazine, 1 to 60% by weight of an alcohol, 0 to 60% by weight. -% of an aliphatic alkanolamine, such as MDEA, 0 to 98.9 wt .-% water and 0 to 35 wt .-% K 2 C0 3 contains.
  • the absorbent has a high absorption rate and a high capacity for acidic gas components.
  • the absorbents given by way of example necessarily contain glycerol.
  • the present invention therefore relates to a process for removing acid gases from fluids, in which, in one absorption step, a fluid stream containing the acid gases is brought into contact with an aqueous absorption medium which contains methyldiethanolamine and piperazine, the total amount of amines being in the range from 20 to 70 %
  • an aqueous absorption medium which contains methyldiethanolamine and piperazine
  • the total amount of amines being in the range from 20 to 70 %
  • By weight of the absorbent and the weight ratio of methyldiethanolamine to piperazine is in the range from 9 to 15, a fluid stream depleted in acid gases and an absorbent loaded with acid gases being obtained.
  • Fig. 1 shows schematically an apparatus for performing the method according to the invention with single-stage absorption and flash regeneration of the absorbent.
  • FIG. 2 schematically shows a device for carrying out the method according to the invention with two-stage absorption and flash regeneration of the absorbent.
  • the invention further relates to an absorbent containing methyldiethanolamine, piperazine, water and optionally a physically active solvent, the total amount of amine being in the range from 20 to 70% by weight of the absorbent and the weight ratio of methyldiethanolamine to piperazine being in the range 9 up to 15.
  • the invention also relates to the use of the absorbent for removing acid gases from fluids, in particular gases.
  • MDEA acts as a chemical absorbent and piperazine as an activator.
  • the absorbent can contain physically active solvents, such as cyclotetramethylene sulfone (sulfolane) and its derivatives, aliphatic acid amides, NMP (N-methylpyrrolidone), N-alkylated pyrrolidones and corresponding piperidones, methanol and mixtures of dialkyl ethers of polyethylene glycols (selexol , Union Carbide, Danbury, Connecticut, USA).
  • the physical solvent is preferably contained in an amount of up to 30% by weight, in particular 0.1 to 20% by weight.
  • the absorbent according to the invention particularly preferably contains no physical solvents.
  • the total amount of amine is preferably at least 40% by weight, particularly 40 to 60% by weight, very particularly 45 to 55% by weight, of the absorbent.
  • the weight ratio of MDEA to piperazine is in the range from 9 to 15, preferably in the range from 11 to 15, particularly preferably from 13 to 15. These ranges (like all the other ranges specified in the present application) also disclose all integer and decimal numbers. Intermediate values, such as 9; 9.1; 9.2; 9.3; ... 10; 10.1; 10.2; Etc.
  • MDEA other C 1 -C 4 -alkyl-di (hydroxy-C 2 -C -alkyl) amines or tri (hydroxy-C 2 -C 4 -alkyl) amines can also be used. Examples are ethyl diethanolamine, triethanolamine and triisopropanolamine.
  • piperazine instead of piperazine, other primary and secondary amines, such as monoethanolamine, diethanolamine or diisopropanolamine, can also be used.
  • the absorbent according to the invention or the method according to the invention is suitable for removing acid gases from fluid streams.
  • the acidic gases are, in particular, C0 2 , H 2 S, COS and mercaptans. S0 3 , S0 2 , CS 2 and HCN can also be removed.
  • Fluids containing the acidic gases are on the one hand gases such as natural gas, synthesis gas, coke oven gas, coal gasification gas, cycle gas and combustion gases and on the other hand liquids that are essentially immiscible with the absorption medium, such as LPG (liquefied petroleum gas) or NGL (natural gas liquids).
  • the gas streams can contain further inert gas constituents which are not absorbed to any appreciable extent by the absorbent.
  • volatile hydrocarbons preferably C 1 -C 4 -hydrocarbons, such as methane, also nitrogen and hydrogen.
  • the method according to the invention is particularly suitable for removing C0 2 and H 2 S.
  • the absorbent according to the invention is generally suitable for removing acidic gas components from gases which are not absorbed by the absorbent itself and for extracting acidic gases from liquids which are essentially immiscible with the absorbent.
  • the basic process sequence for a gas scrubber and possible variants as they lie within the scope of the present invention are described below. However, the process can easily be transferred to liquids by a person skilled in the art.
  • the regeneration of the absorbent is identical for liquids and gases.
  • the starting gas which is rich in acidic gas components, is brought into contact with the absorption medium according to the invention in an absorption step in an absorber, as a result of which the acidic gas-containing gas is at least partially washed out.
  • a washing device used in conventional gas scrubbing processes preferably acts as the absorber.
  • Suitable washing devices are, for example, packing, packing and tray columns, radial flow washers, jet washers, Venturi washers and rotary tion spray washer, preferably packed, packed and tray columns, particularly preferably packed and packed columns.
  • the treatment of the fluid stream with the absorbent is preferably carried out in a countercurrent column. The fluid is generally fed into the lower region and the absorbent into the upper region of the column.
  • the temperature of the absorbent is generally about 40 to 100 ° C. in the absorption step, for example 40 to 70 ° C. at the top of the column and 50 to 100 ° C. at the bottom of the column when using a column.
  • the total pressure in the absorption step is generally about 1 to 120 bar, preferably about 10 to 100 bar.
  • a low in acidic gas components i.e. receive a product gas depleted of these components (clean gas) and an absorbent loaded with acid gas components.
  • the method according to the invention can comprise one or more, in particular two, successive absorption steps.
  • the absorption can be carried out in several successive substeps, the raw gas containing the acidic gas components being brought into contact with a substream of the absorbent in each of the substeps.
  • the absorbent with which the raw gas is brought into contact may already be partially loaded with acid gases, i.e. it can be, for example, an absorbent that was returned from a subsequent absorption step to the first absorption step, or a partially regenerated absorbent.
  • the two-stage absorption reference is made to the publications EP-A 0 159 495, EP-A 0 190 434, EP-A 0 359 991 and WO 00/00271.
  • the method according to the invention is carried out in such a way that the fluid containing the acid gases is first treated with the absorbent in a first absorption step at a temperature of 40 to 100 ° C., preferably 50 to 90 ° C. and in particular 60 to 90 ° C. becomes.
  • the fluid depleted in acidic gases is then treated in a second absorption step with the absorbent at a temperature of 30 to 90 ° C., preferably 40 to 80 ° C. and in particular 50 to 80 ° C.
  • the temperature is 5 to 20 ° C lower than in the first absorption stage.
  • the acid gas components can be released in a conventional manner (analogously to the publications cited below) from the absorption medium loaded with the acid gas components in a regeneration step, a regenerated absorption onsffen is obtained.
  • the regeneration step the loading of the absorbent is reduced and the regenerated absorbent obtained is preferably subsequently returned to the absorption step.
  • the regeneration step includes at least relieving the pressure of the loaded absorbent from a high pressure, as prevails when the absorption step is carried out, to a lower pressure.
  • the pressure can be released, for example, by means of a throttle valve and / or an expansion turbine. Regeneration with a relaxation stage is described, for example, in US Pat. Nos. 4,537,753 and 4,553,984.
  • the release of the acidic gas components in the regeneration step can, for example, in a relaxation column, e.g. a vertically or horizontally installed flash tank or a counterflow column with internals.
  • a relaxation column e.g. a vertically or horizontally installed flash tank or a counterflow column with internals.
  • Several relaxation columns can be connected in series, in which regeneration takes place at different pressures. For example, in a pre-expansion column at high pressure, which is typically about 1.5 bar above the partial pressure of the acidic gas constituents in the absorption step, and in a main expansion column at low pressure, for example 1 to 2 bar absolute, regeneration can be carried out.
  • the loaded absorption liquid is first expanded to a pressure of 1 to 2 bar (absolute) in a first low-pressure relaxation stage.
  • the partially regenerated absorption liquid is then heated in a heat exchanger and then expanded again to a pressure of 1 to 2 bar (absolute) in a second low-pressure relaxation stage.
  • the last relaxation stage can also be carried out under vacuum, for example by means of a water vapor emitter, possibly in combination with a mechanical generation device. is generated as described in EP-A 0 159 495, EP-A 0 202 600, EP-A 0 190 434 and EP-A 0 121 109 (US 4,551,158).
  • stripping can also be carried out, with further acidic gas components being released from the absorbent. Stripping or stripping can also be done in one or more stages.
  • the stripping can be carried out in a desorption column equipped with packing or packing.
  • the pressure is preferably 1 to 3 bar absolute and the temperature 90 to 130 ° C., stripping with hot gas or steam, preferably with steam. Processes in which additional stripping is carried out are described in EP-A 0 159 495, EP-A 0 190 434 and EP-A 0 359 991.
  • water vapor can be supplied, for example at the bottom of a relaxation stage, as described in EP-A 0 159 495 and US 4,551,158 (EP-A 0 121 109).
  • the regeneration step can be carried out in several successive substeps, the absorbent obtained after successive substeps having a decreasing load of acidic gas components.
  • a first part of the acidic gas components can be released from the loaded absorbent in a flash column and then stripped, whereby further acidic gas components are released and the absorbent is largely regenerated. It can also be regenerated in several relaxation columns connected in series or in several relaxation columns and additionally in a stripper.
  • a rough wash can be carried out with a pure relaxation circuit, the loaded absorbent being relaxed via a relaxation turbine and being gradually regenerated in a pre-relaxation column and a main relaxation column.
  • the partial streams of the absorbent used in successive sub-steps of the absorption step have a decreasing load of acidic gas components.
  • a method is particularly preferred in which the starting gas containing the acidic gas constituents is successively mixed with a first partial stream of the absorbent, which after partial regeneration in a flashing column and before stripping, and a second substream of the absorbent obtained after stripping is brought into contact.
  • the absorption step can be carried out in two sub-steps, a coarse and a delicate wash, and the regeneration step can be carried out step by step by depressurization in an expansion turbine, a pre-expansion column and a main expansion column and a subsequent stripping, the partial flow for the coarse washing comes from the main relaxation column and the partial flow of the absorbent for the fine washing comes from the stripping.
  • Processes with multi-stage absorption and regeneration with low-pressure relaxation and strippers are particularly preferred, as are the process variants described in EP-A 0 359 991 with multi-stage absorption, single- or multi-stage relaxation and strippers.
  • the flash gas drawn off at the top of a flash column is compressed in a compressor and added to the starting gas to be purified in the first absorption stage.
  • the absorbent according to the invention has a high loading capacity with acid gases, which can also be easily desorbed again. As a result, energy consumption and solvent circulation can be significantly reduced in the method according to the invention.
  • FIG. 1 schematically shows a device in which the absorption stage is carried out in one stage and the relaxation stage in two stages.
  • the feed gas is fed via line 1 into the lower area of the absorber 2.
  • the absorber 2 is a column which is packed with packing elements in order to effect the mass and heat exchange.
  • the absorbent which is regenerated absorbent with a low residual acid gas content, is fed via line 3 to the top of the absorber 2 in countercurrent to the feed gas.
  • the gas depleted in acidic gases leaves the absorber 2 overhead (line 4).
  • the absorbent enriched with acidic gases leaves the absorber 2 at the bottom via line 5 and is introduced into the upper region of the high-pressure expansion column 6, which is generally operated at a pressure above the C0 2 partial pressure in the the raw gas supplied to the absorber.
  • the relaxation of the absorbent is generally carried out with the aid of Licher devices, such as a level control valve, a hydraulic turbine or a pump running in reverse. During the relaxation, most of the dissolved non-acidic gases and a small part of the acidic gases are released. These gases are discharged via line 7 from the high-pressure expansion column 6 overhead.
  • the absorbent which is still loaded with the majority of the acid gases, leaves the high-pressure expansion column via line 8 and is heated in the heat exchanger 9, a small part of the acid gases being released.
  • the heated absorbent is introduced into the upper region of a low-pressure expansion column 10, which is equipped with a packed packing in order to achieve a large surface area and thus to release the CO 2 and establish the equilibrium.
  • the low-pressure expansion column 10 the major part of the C0 2 and the H 2 S are released almost completely by flashing. In this way, the absorbent is regenerated and cooled at the same time.
  • a reflux condenser 11 with a collecting container 12 is provided in order to cool the released acid gases and to condense some of the steam.
  • the majority of the acidic gas leaves the reflux condenser 11 via line 13.
  • the condensate is pumped back to the top of the low-pressure expansion column 10 by means of a pump 14.
  • the regenerated absorbent which still contains a small part of the CO 2 , leaves the low-pressure expansion column 10 at the bottom via line 15 and is applied to the top of the absorber 2 by means of pump 16 via line 3.
  • Fresh water can be fed in via line 17 to compensate for the water discharged with the gases.
  • FIG 2 shows schematically an apparatus for performing the method according to the invention using a two-stage absorber and a two-stage relaxation.
  • the absorber comprises the raw absorber 1 and the pure absorber 2.
  • the feed gas is fed via line 3 into the lower region of the raw absorber 1 and treated in countercurrent with regenerated absorbent, which is applied to the top of the raw absorber 1 via line 4 and still contains some acidic gases.
  • regenerated absorbent is added via line 5, which essentially no longer contains acid gases.
  • Both parts of the absorber contain a packing to effect the mass and heat exchange between raw gas and absorbent.
  • the treated gas leaves the pure absorber 2 overhead (line 6).
  • the absorbent loaded with acid gases is discharged at the bottom of the raw absorber 1 and via line 7 fed into the upper region of the high-pressure expansion column 8.
  • the column 8 is equipped with a packing and is operated at a pressure which is between the pressure in the absorber and the subsequent low-pressure expansion column 11.
  • the absorption medium, which is loaded with acidic gases is expanded with the aid of conventional devices, for example a level control valve, a hydraulic turbine or a pump running in reverse.
  • the high pressure release releases most of the dissolved non-acidic gases as well as a small part of the acidic gases. These gases are discharged via line 9 from the high-pressure expansion column 8 overhead.
  • the absorbent which is still loaded with the majority of the acid gases, leaves the high-pressure expansion column 8 via line 10 and is fed into the upper region of the low-pressure expansion column 11, where most of the C0 2 and H 2 S through Flashes are released.
  • the absorbent is regenerated in this way.
  • the low pressure expansion column 11 is equipped with a packing in order to provide a large surface for the heat and mass transfer.
  • a reflux condenser 12 with a condensate tank 13 is provided in order to cool the acid gases emerging from the top of the low-pressure expansion column 11 and to condense some of the steam.
  • the uncondensed gas which contains the majority of the acid gases, is discharged via line 14.
  • the condensate from the condensate tank 13 is fed via pump 15 to the top of the low-pressure expansion column 11.
  • the partially regenerated absorbent which still contains some of the acid gases, leaves the low-pressure expansion column 11 at the bottom via line 16 and is split into two partial streams.
  • the larger partial flow is fed via pump 17 and line 4 to the top of the raw absorber 1, whereas the smaller part is heated via line 18 by means of pump 19 in the heat exchanger 20.
  • the heated absorbent is then fed into the upper region of the stripper 21, which is equipped with a pack.
  • the majority of the absorbed CO 2 and H 2 S is stripped out by means of steam, which is generated in the reboiler 22 and fed into the lower region of the stripper 21.
  • the absorbent leaving the stripper 21 at the bottom via line 23 has only a low residual content of acid gases.
  • An absorbent is suitable for carrying out the process according to the invention which, based on the total weight of the composition, contains 40% by weight of methyldiethanolamine and so much piperazine that the weight ratio of methyldiethanolamine to piperazine is 12.5.
  • the absorbent according to the invention has a reduced energy requirement and solvent circulation in comparison to an absorbent which, however, contains the same amount of piperazine for the same methyldiethanolamine content that the methyldiethanolamine-piperazine weight ratio is 16.

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)

Abstract

L'invention concerne un procédé d'extraction de gaz acides dans des fluides consistant à mettre en contact dans une étape d'absorption un courant fluidique contenant les gaz acides et un agent d'absorption aqueux contenant méthyldiéthanolamine et pipérazine. Selon l'invention, la quantité totale d'amine est de 20 à 70 % en poids de l'agent d'absorption, et le rapport massique de méthyldiéthanolamine sur pipérazine est de 9 à 15. Par ailleurs, on obtient un courant fluidique à teneur réduite en gaz acides, et un agent d'absorption chargé de gaz acides.
PCT/EP2002/008935 2001-08-10 2002-08-09 Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides WO2003013699A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE10139453.5 2001-08-10
DE2001139453 DE10139453A1 (de) 2001-08-10 2001-08-10 Verfahren und Absorptionsmittel zur Entfernung saurer Gase aus Fluiden

Publications (1)

Publication Number Publication Date
WO2003013699A1 true WO2003013699A1 (fr) 2003-02-20

Family

ID=7695115

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2002/008935 WO2003013699A1 (fr) 2001-08-10 2002-08-09 Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides

Country Status (3)

Country Link
AR (1) AR034976A1 (fr)
DE (1) DE10139453A1 (fr)
WO (1) WO2003013699A1 (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012068327A1 (fr) 2010-11-19 2012-05-24 Nalco Company Composition absorbant les gaz acides
US8192530B2 (en) 2007-12-13 2012-06-05 Alstom Technology Ltd System and method for regeneration of an absorbent solution
US8318114B2 (en) 2010-04-16 2012-11-27 Nalco Company Composition for treating acid gas
WO2013079116A1 (fr) * 2011-12-01 2013-06-06 Statoil Petroleum As Procédé comportant un absorbant dans un réacteur à cuve agitée en continu et un dispositif d'épuisement instantané à cuve
US8461335B2 (en) 2009-06-30 2013-06-11 Nalco Company Acid gas scrubbing composition
US8541622B2 (en) 2009-06-30 2013-09-24 Nalco Company Acid gas scrubbing composition
US8864878B2 (en) 2011-09-23 2014-10-21 Alstom Technology Ltd Heat integration of a cement manufacturing plant with an absorption based carbon dioxide capture process
US8911538B2 (en) 2011-12-22 2014-12-16 Alstom Technology Ltd Method and system for treating an effluent stream generated by a carbon capture system
US9028654B2 (en) 2012-02-29 2015-05-12 Alstom Technology Ltd Method of treatment of amine waste water and a system for accomplishing the same
US9101912B2 (en) 2012-11-05 2015-08-11 Alstom Technology Ltd Method for regeneration of solid amine CO2 capture beds
US9133407B2 (en) 2011-02-25 2015-09-15 Alstom Technology Ltd Systems and processes for removing volatile degradation products produced in gas purification
US9555364B2 (en) 2009-06-30 2017-01-31 Nalco Company Acid gas scrubbing composition

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2519763C (fr) * 2003-03-21 2012-07-10 Dow Global Technologies Inc. Composition amelioree et methode d'elimination du sulfure de carbonyle present dans des gaz acides
FR2860442B1 (fr) * 2003-10-01 2006-01-27 Inst Francais Du Petrole Utilisation d'une turbine diphasique dans un procede de traitement de gaz
JP2007533431A (ja) 2003-11-10 2007-11-22 ビーエーエスエフ　アクチェンゲゼルシャフト 酸性ガスを流体の流れから除去することによって高い圧力下にある酸性ガス流を取得する方法
EP4427835A1 (fr) * 2013-01-31 2024-09-11 Carbon Clean Solutions Limited Solvants de captage du carbone et procédés d'utilisation de ces solvants
CN116351213A (zh) * 2021-12-27 2023-06-30 中国石油天然气股份有限公司 一种脱除乙烯裂解气中酸性气的方法和系统

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4336233A (en) * 1975-11-18 1982-06-22 Basf Aktiengesellschaft Removal of CO2 and/or H2 S and/or COS from gases containing these constituents
EP0107783A1 (fr) * 1982-10-02 1984-05-09 BASF Aktiengesellschaft Procédé d'élimination de CO2 et/ou de H2S de gaz
EP0331788A1 (fr) * 1987-02-05 1989-09-13 Uop Absorbant de tertiaire alcanol-amine contenant de l'éthylène-amine comme promoteur et son procédé d'utilisation
WO2000000271A1 (fr) * 1998-06-29 2000-01-06 Basf Aktiengesellschaft Procede permettant d'eliminer d'un gaz ses composants acides
EP1016445A1 (fr) * 1998-04-06 2000-07-05 Nippon Nyukazai Co., Ltd. Procede de recyclage d'absorbant liquide pour vapeur d'acide, qui comprend de la methyldiethanolamine et une alkylpiperazine inferieure
DE19947845A1 (de) * 1999-10-05 2001-04-12 Basf Ag Verfahren zum Entfernen von COS aus einem Kohlenwasserstoff-Fluidstrom und Waschflüssikgkeit zur Verwendung in derartigen Verfahren
WO2002009849A2 (fr) * 2000-07-27 2002-02-07 Continental Engineering B.V. Recuperation de co2 tres pur dans des fumees

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4336233A (en) * 1975-11-18 1982-06-22 Basf Aktiengesellschaft Removal of CO2 and/or H2 S and/or COS from gases containing these constituents
EP0107783A1 (fr) * 1982-10-02 1984-05-09 BASF Aktiengesellschaft Procédé d'élimination de CO2 et/ou de H2S de gaz
EP0331788A1 (fr) * 1987-02-05 1989-09-13 Uop Absorbant de tertiaire alcanol-amine contenant de l'éthylène-amine comme promoteur et son procédé d'utilisation
EP1016445A1 (fr) * 1998-04-06 2000-07-05 Nippon Nyukazai Co., Ltd. Procede de recyclage d'absorbant liquide pour vapeur d'acide, qui comprend de la methyldiethanolamine et une alkylpiperazine inferieure
WO2000000271A1 (fr) * 1998-06-29 2000-01-06 Basf Aktiengesellschaft Procede permettant d'eliminer d'un gaz ses composants acides
DE19947845A1 (de) * 1999-10-05 2001-04-12 Basf Ag Verfahren zum Entfernen von COS aus einem Kohlenwasserstoff-Fluidstrom und Waschflüssikgkeit zur Verwendung in derartigen Verfahren
WO2002009849A2 (fr) * 2000-07-27 2002-02-07 Continental Engineering B.V. Recuperation de co2 tres pur dans des fumees

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8192530B2 (en) 2007-12-13 2012-06-05 Alstom Technology Ltd System and method for regeneration of an absorbent solution
US8551435B2 (en) 2009-06-30 2013-10-08 Nalco Company Process for reducing contaminants in an industrial fluid stream
US9555364B2 (en) 2009-06-30 2017-01-31 Nalco Company Acid gas scrubbing composition
US8461335B2 (en) 2009-06-30 2013-06-11 Nalco Company Acid gas scrubbing composition
US8541622B2 (en) 2009-06-30 2013-09-24 Nalco Company Acid gas scrubbing composition
US8318114B2 (en) 2010-04-16 2012-11-27 Nalco Company Composition for treating acid gas
US8765951B2 (en) 2010-11-19 2014-07-01 Nalco Company Acid gas absorbent composition
US8765083B2 (en) 2010-11-19 2014-07-01 Nalco Company Acid gas absorbent composition
WO2012068327A1 (fr) 2010-11-19 2012-05-24 Nalco Company Composition absorbant les gaz acides
US9133407B2 (en) 2011-02-25 2015-09-15 Alstom Technology Ltd Systems and processes for removing volatile degradation products produced in gas purification
US8864878B2 (en) 2011-09-23 2014-10-21 Alstom Technology Ltd Heat integration of a cement manufacturing plant with an absorption based carbon dioxide capture process
US9545597B2 (en) 2011-12-01 2017-01-17 Statoil Petroleum As Continuously stirred tank reactor absorber and flash tank stripper system
WO2013079116A1 (fr) * 2011-12-01 2013-06-06 Statoil Petroleum As Procédé comportant un absorbant dans un réacteur à cuve agitée en continu et un dispositif d'épuisement instantané à cuve
US8911538B2 (en) 2011-12-22 2014-12-16 Alstom Technology Ltd Method and system for treating an effluent stream generated by a carbon capture system
US9028654B2 (en) 2012-02-29 2015-05-12 Alstom Technology Ltd Method of treatment of amine waste water and a system for accomplishing the same
US9101912B2 (en) 2012-11-05 2015-08-11 Alstom Technology Ltd Method for regeneration of solid amine CO2 capture beds

Also Published As

Publication number Publication date
DE10139453A1 (de) 2003-02-20
AR034976A1 (es) 2004-03-24

Similar Documents

Publication Publication Date Title
EP1599274B1 (fr) Agent absorbant et procede pour eliminer des gaz acides presents dans des fluides
EP1682638B1 (fr) Procede d'extraction d'un flux de gaz acide sous haute pression par extraction des gaz acides contenus dans un flux fluidique
EP1485190B1 (fr) Procede de desacidification d'un courant fluidique et liquide laveur utilise dans ce procede
EP1303345B1 (fr) Procede de desacidification d'un courant de fluide et liquide de lavage destine a un tel procede
EP1412056B1 (fr) Procede d'elimination de gaz acides dans un courant gazeux
EP1289625B1 (fr) Procede de desacidification d'un courant fluidique d'hydrocarbure
WO2003013699A1 (fr) Procede et agent d'absorption destines a l'extraction de gaz acides dans des fluides
DE102007056625B3 (de) Verfahren zur Behandlung eines CO2 enthaltenden Prozessgasstrom
EP1196233B1 (fr) Procede permettant de supprimer des mercaptans de courants de flux
EP3903909B1 (fr) Élimination du sulfure d'hydrogène et du dioxyde de carbone d'un écoulement de fluide
DE19947845A1 (de) Verfahren zum Entfernen von COS aus einem Kohlenwasserstoff-Fluidstrom und Waschflüssikgkeit zur Verwendung in derartigen Verfahren
WO2009156273A1 (fr) Agent absorbant et procédé pour éliminer des gaz acides contenus dans des flux de fluide, en particulier des gaz de fumée
EP1633458A2 (fr) Procede de desacidification d'un flux de fluide a l'aide d'une colonne de lavage inerte et dispositif correspondant
WO2017055087A1 (fr) Agent absorbant et procédé d'élimination sélective d'hydrogène sulfuré
WO2018024598A1 (fr) Procédé en deux étapes permettant d'extraire su co2 présent dans du gaz de synthèse
DD202129A5 (de) Verfahren zum entfernen von kohlendioxid und, sofern vorhanden, schwefelwasserstoff aus einem gasgemisch
DE19945326A1 (de) Verfahren zur Entfernung von Kohlendioxid, Schwefelverbindungen, Wasser und aromatischen und höheren aliphatischen Kohlenwasserstoffen aus technischen Gasen
DE10338563A1 (de) Verfahren zum Entsäuern eines Fluidstroms mittels Membraneinheiten aus inerten Gehäusen
DE10352878A1 (de) Verfahren zur Gewinnung eines unter hohem Druck stehenden Sauergasstroms durch Entfernung der Sauergase aus einem Fluidstrom
DE10325358A1 (de) Verfahren zum Entsäuern eines Fluidstroms mittels einer inerten Waschkolonne und Vorrichtung hierzu
DE102004031051A1 (de) Verfahren zur Gewinnung eines unter hohem Druck stehenden Sauergasstroms durch Entfernung der Sauergase aus einem Fluidstrom
DE102004050936A1 (de) Verfahren zur Gewinnung eines unter hohem Druck stehenden Sauergasstroms durch Entfernung der Sauergase aus einem Fluidstrom
DE10334002A1 (de) Verfahren zum Entsäuern eines Fluidstroms mittels einer inerten Waschkolonne und Vorrichtung hierzu
WO2024008248A1 (fr) Procédé pour séparer du méthane et du dioxyde de carbone de biogaz et installation de préparation
DE102010008846A1 (de) Absorptionsmittel zum Entsäuern eines Fluidstroms und Verfahren zur Verwendung desselben

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): JP

Kind code of ref document: A1

Designated state(s): JP US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FR GB GR IE IT LU MC NL PT SE SK TR

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LU MC NL PT SE SK TR

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP

WWW Wipo information: withdrawn in national office

Country of ref document: JP