EP1902118A2 - Method and device for the absorption of acid gas from natural gas - Google Patents
Method and device for the absorption of acid gas from natural gasInfo
- Publication number
- EP1902118A2 EP1902118A2 EP06753798A EP06753798A EP1902118A2 EP 1902118 A2 EP1902118 A2 EP 1902118A2 EP 06753798 A EP06753798 A EP 06753798A EP 06753798 A EP06753798 A EP 06753798A EP 1902118 A2 EP1902118 A2 EP 1902118A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- separator
- detergent
- column
- stripping
- gas
- Prior art date
- Legal status (The legal status 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 status listed.)
- Withdrawn
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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
Definitions
- the invention relates to a method and apparatus for the absorption of sour gas from crude natural gas by means of physically acting solvents.
- Corresponding absorption devices are used for raw natural gases which, in addition to valuable components such as methane, higher hydrocarbons, hydrogen, carbon dioxide and impurities such as hydrogen sulphide, organic sulfur components, such as. Mercaptan and carbon dioxide sulfide, as well as carbon dioxide - where undesirable - and contained small amounts of water vapor in different proportions used.
- the e.g. sulfur components contained in the raw natural gas for further technical use up to ppm levels from the natural gas to remove.
- the removal of hydrogen sulphide, mercaptans, carbon dioxide and other sour gas constituents from natural gas is generally accomplished by means of chemically acting absorbents, such as e.g. Amine solutions, alkali salt solutions, etc., or physically acting absorbents, e.g. Selexol, propylene carbonate, N-methyl-pyrrolidone, morphysorb, methanol and the like, in circulatory systems, wherein physically acting absorbents, in contrast to chemically acting detergents, are also able to remove organic sulfur components.
- the carbon dioxide contained in the gas is either completely, partly or as little as possible removed.
- the invention solves the problem by
- the natural gas containing sour gas is first passed into an absorption column, where it is brought into direct contact with the physical detergent, and the physical detergent absorbs the sour gas to a residue, • the loaded detergent is passed under lowering of the working pressure in a first separator in that a part of the dissolved acid gas out of the detergent,
- the at least one part of the loaded detergent is passed, while the working pressure is lowered again, to a stripping column in which the remainder of the dissolved acid gas is expelled from the detergent,
- the sour gas leaving the first separator is passed into a further absorption column in which regenerated detergent is used to re-absorb a portion of the outgassed sour gas containing predominantly hydrogen sulfide and to admix it with the laden detergent of the first separator,
- This stripping gas is used in the stripping column to remove the hydrogen sulfide in the detergent supplied to the stripping column, and
- the finely regenerated solvent is divided into two sub-streams, one of which is at the downstream of the first separator stage absorption column and the other is passed to the absorption column located in the natural gas stream.
- the detergent leaving the first separator is passed in lowering the working pressure in a second separator before the still partially loaded detergent is passed to the stripping column.
- the individual pressure stages are designed so that • the pressure of acid gas absorption above 50 bar, preferably 70 bar is selected,
- the pressure of the first separator is between 6 and 30 bar, preferably 15 bar
- the pressure of the stripping column is selected between 0.2 and 3 bar. If a second separator is provided, the pressure of the second separator should be between 1 and 3 bar, preferably 1 bar, but always above the pressure of the stripping column.
- the fact is taken into account that the physical solvent used has also mitabsorbiert valuable hydrocarbon compounds, which should not be deposited.
- the first separator is therefore preceded by a recycle gas flash stage, in which a pressure drop of the loaded solvent takes place to a pressure which lies between the pressure of the absorption and that of the first separator, whereby the flash gas released by depressurization and containing absorbed, valuable gas constituents is recycled back to the absorption column by means of a recycle compressor.
- the loaded solution is preheated by means of a preheater before entering the stripping and leaving the stripping, warm, regenerated solvent in heat exchange with the guided to the preheater, loaded solvent, and then further cooled before This cooled, regenerated solution is used for absorption.
- the solvent used is a mixture of N-formylmorpholine and N-acetylmorpholine. applies.
- the invention also includes suitable devices for carrying out the method.
- the first separator and the absorption column arranged downstream of it on the oxygen gas side form a constructional unit in which the first separator is integrated into the column sump of the absorption column.
- the second separator and the stripping column form a structural unit in which the second separator is arranged at the top of the stripping column and has a liquid outlet with a device for reducing pressure, further a distributor for liquid in the head region of the stripping column, an inlet for loaded detergent in the bottom region of the column bottom of the stripping column as well as removal devices for sour gas in the top region of the stripping column and in the second separator.
- Fig. 1 shows the inventive method consisting of an absorption column 2, a first separator 7 with attached absorption column 7a, a second separator 12 and a stripping column 15 and the main process streams.
- the crude natural gas 1 is passed into the absorption column 2, where it is washed at a pressure of 91 bar with the solvent 3 and leaves it as purified natural gas 4 again.
- the loaded solvent 5 is depressurized in the pressure relief device 6 to 13 bar and then introduced directly into the bottom of the first separator 7 with attached absorption column 7a. There, a portion of the sour gas is discharged from the loaded solvent and flows into the absorption column arranged above it, where a portion thereof is re-absorbed with fresh solvent 8. In this way, a stripping gas 9 which is poor in H 2 S is formed.
- the added solvent mixes in the sump with the loaded solvent 5 from the absorption column 2.
- the withdrawn loaded solvent 10 is relaxed in a further pressure relief device 11 to 1, 1 bar and passed into the second separator 12, where the major part of the acid gas out of the solvent.
- the still charged with sour gas residues solvent 13 is relaxed in another pressure relief device 14 to 0.6 bar and passed into the stripping column 15, where with the H 2 S-poor stripping gas 9, the remaining sour gas is expelled from the solvent.
- the thus regenerated solvent 16 is promoted by the solvent pump 17 to the first separator 7 with attached absorption column 7a and the branch to the absorption column 2, and promoted by the latter after further pressure increase in the solvent pump 18 to the top of the absorption column 2.
- the second separator 12 taken sour gas 19 is combined with the withdrawn from the vacuum pump 21 from the stripping column 15 sour gas stream 20 and fed by means of the conveyor compressor 22 another acid gas utilization 23.
- Pressure relaxation device first separator a patch absorption column regenerated solvent
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102005030028A DE102005030028A1 (en) | 2005-06-27 | 2005-06-27 | Absorption of hydrogen sulfide and carbon dioxide from compressed natural gas uses two absorption columns, hydrogen sulfide being removed in second column using regenerated solvent |
PCT/EP2006/004872 WO2007000217A2 (en) | 2005-06-27 | 2006-05-23 | Method and device for the absorption of acid gas from natural gas |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1902118A2 true EP1902118A2 (en) | 2008-03-26 |
Family
ID=37074432
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP06753798A Withdrawn EP1902118A2 (en) | 2005-06-27 | 2006-05-23 | Method and device for the absorption of acid gas from natural gas |
Country Status (6)
Country | Link |
---|---|
US (1) | US20090199712A1 (en) |
EP (1) | EP1902118A2 (en) |
CA (1) | CA2611600C (en) |
DE (1) | DE102005030028A1 (en) |
NO (1) | NO20080448L (en) |
WO (1) | WO2007000217A2 (en) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102008062387A1 (en) * | 2008-12-17 | 2010-07-01 | Uhde Gmbh | Process for the purification of industrial gases and production of sour gases |
US20100219061A1 (en) * | 2009-03-02 | 2010-09-02 | Saudi Arabian Oil Company | Enhancement of acid gas enrichment process |
DE102009018444A1 (en) * | 2009-04-22 | 2010-10-28 | Uhde Gmbh | Process for removing acidic gas components from a gas mixture |
DE102009042365A1 (en) | 2009-09-23 | 2011-04-07 | Uhde Gmbh | Process and apparatus for removing water from natural gas or industrial gases with physical solvents |
DE102011108749A1 (en) | 2011-07-28 | 2013-01-31 | Thyssenkrupp Uhde Gmbh | Heat recovery in absorption and desorption processes |
US8790452B2 (en) | 2012-02-22 | 2014-07-29 | Richard Paul Posa | Method and system for separating and destroying sour and acid gas |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2685941A (en) * | 1951-01-31 | 1954-08-10 | Universal Oil Prod Co | Method for concentrating hydrogen |
US3362133A (en) * | 1965-10-25 | 1968-01-09 | Allied Chem | Process for hydrogen sulfide removal from gas mixtures containing h2s and co2 |
US3594985A (en) * | 1969-06-11 | 1971-07-27 | Allied Chem | Acid gas removal from gas mixtures |
US4359450A (en) * | 1981-05-26 | 1982-11-16 | Shell Oil Company | Process for the removal of acid gases from gaseous streams |
US4397660A (en) * | 1981-06-15 | 1983-08-09 | Shell Oil Company | Process for the removal of H2 S and CO2 from a gas mixture |
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 |
DE19945326B4 (en) * | 1999-01-22 | 2008-03-27 | Uhde Gmbh | Process for the removal of carbon dioxide, sulfur compounds, water and aromatic and higher aliphatic hydrocarbons from industrial gases |
US7192468B2 (en) * | 2002-04-15 | 2007-03-20 | Fluor Technologies Corporation | Configurations and method for improved gas removal |
ATE505254T1 (en) * | 2002-12-12 | 2011-04-15 | Fluor Corp | METHOD FOR REMOVING ACID GAS |
DE10313438A1 (en) * | 2003-03-26 | 2004-11-04 | Uhde Gmbh | Process for the selective removal of hydrogen sulfide and CO2 from raw gas |
DE10324694A1 (en) * | 2003-05-28 | 2004-12-23 | Uhde Gmbh | Process for the removal of acid gases from pressurized natural gas contaminated with acid gas compounds and recovery of the removed acid gases at an elevated pressure level |
-
2005
- 2005-06-27 DE DE102005030028A patent/DE102005030028A1/en not_active Ceased
-
2006
- 2006-05-23 WO PCT/EP2006/004872 patent/WO2007000217A2/en not_active Application Discontinuation
- 2006-05-23 CA CA2611600A patent/CA2611600C/en not_active Expired - Fee Related
- 2006-05-23 EP EP06753798A patent/EP1902118A2/en not_active Withdrawn
- 2006-05-23 US US11/922,170 patent/US20090199712A1/en not_active Abandoned
-
2008
- 2008-01-23 NO NO20080448A patent/NO20080448L/en not_active Application Discontinuation
Non-Patent Citations (1)
Title |
---|
See references of WO2007000217A2 * |
Also Published As
Publication number | Publication date |
---|---|
US20090199712A1 (en) | 2009-08-13 |
CA2611600A1 (en) | 2007-01-04 |
CA2611600C (en) | 2013-09-24 |
WO2007000217A2 (en) | 2007-01-04 |
NO20080448L (en) | 2008-01-23 |
DE102005030028A1 (en) | 2006-12-28 |
WO2007000217A3 (en) | 2007-03-15 |
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RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: THYSSENKRUPP UHDE GMBH |
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RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: THYSSENKRUPP INDUSTRIAL SOLUTIONS AG |
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