• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    METHOD OF REGENERATION OF A SATISFATED HYDROGEN AND OTHER DUAL CARBON OF ABSORV1 SCENE SOLUTION, INCLUDED COLLECTIONS OCRAPS OASERS COURT OI OECESS OFFICERS WITH A saturated solution to a regeneration zone the lower part of the zone and the multistage sequential Drosheshfov non-regenerated absorption solution with obtaining several vapor phases with the subsequent return to the regeneration zone, characterized in o, in order to reduce steam consumption and increase the degree of regeneration, the resulting vapor phases are pre-combined and ejected into the lower regeneration zone under a pressure equal to the pressure in this zone.
    公开号:SU1134113A3
    申请号:SU813269601
    申请日:1981-03-30
    公开日:1985-01-07
    发明作者:Батто Жак；Годард Ален
    申请人:Сосьете Насьональ Елф Акитэн /Продюксьон/ (Фирма)；
    IPC主号:
    专利说明:

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    1 The invention relates to processes for the absorption of gases from acid components and can be used in the chemical industry. A known method of purifying gases from hydrogen sulfide and carbon dioxide impurities by absorbing these impurities with an aqueous solution of potassium carbonate, followed by regeneration of the high grade solution by contacting with steam in the regeneration zone, the solution being heated to boiling with water vapor during regeneration and returned to the absorption stage L. The main disadvantage of this method is the high consumption of steam for regeneration, as well as the presence in the scheme of sewage contaminated with hydrogen sulfide. The closest to the invention to the technical essence and the achieved result is the method of regeneration of absorption solution saturated with hydrogen sulfide and / or carbon dioxide, which involves the ejection of a saturated solution into the regeneration zone having a pressure at the bottom of the zone 1.3-5 bar, removal of hydrogen sulfide and / or carbon dioxide from the upper part of the regeneration zone, the selection of the regenerated solution from the lower part of the zone and multistage sequential throttling of the regenerated absorption solution with obtaining ultiple steam phase, then return them to a regeneration zone at a stage at which they were obtained 2 | . The main disadvantage of this method is the increased consumption of steam for regeneration, which is 64 tons / h, and the degree of regeneration is not high enough (residual content of hydrogen sulfide is about 95 g / l). The aim of the invention is to reduce steam consumption and increase the degree of regeneration. The goal is achieved by the method of regeneration of the absorption solution saturated with hydrogen sulfide and / or carbon dioxide, which includes the injection of a saturated solution into the regeneration zone, having a pressure of 1, 3-5 bar, removal of hydrogen sulfide and / or carbon dioxide from the upper part of the regeneration zone, selection of the regenerated solution parts of the zone and multistage sequential throttling of the regenerated absorption solution with the formation of several vapor phases with their last dull return to the regeneration zone Whereby equal pressure in this zone vapor phase obtained previously were combined and ejected into the lower regeneration zone under pressure. The proposed method allows to reduce steam consumption from 64 to 54 t / h and to increase the degree of regeneration by 18% (the residual hydrogen sulfide content decreases from 0.95 to 0.8 g / l). The installation throttling complex according to the proposed method consists of a plurality of throttling chambers, i.e. from the initial throttling chamber (in some cases from one or more intermediate throttling chambers) and from the final throttling chamber. A recompression node connected to it contains the same number of compression stages. Each compression stage may include one or more compressors. In particular, the installation has n throttling chambers and n connected compression stages, where n is an integer between 2 and 4. The method is as follows. The gas to be purified, for example natural gas, containing acidic gaseous compounds H „S and C02 to be removed, is fed to the absorption column through a pipeline and an absorbing solution is fed in countercurrent. The purified gas is withdrawn from the head of the absorption column, while the absorption solution is withdrawn from the bottom of the column. containing acidic absorbed compounds. This absorption component, the acidic component to be regenerated, is fed to a degassing vessel in which the gaseous fraction, containing mainly the hydrocarbons trapped in the absorption solution, is separated. This fraction is removed from the system. The degassed absorption solution is heated and partly 3 is evaporated in the heat exchanger system and fed to a regenerated well column, for example, a plate-type column. In this column, the absorption solution, saturated with absorbed acidic compounds, is boosted at boiling at a pressure above atmospheric (pressure at the bottom of the column is 1.2 bar., Preferably 1.35 bar). The heat required to maintain the boiling of the regenerated absorption solution and to produce steam for stripping light fractions is generated when the indicated solution passes through a boiler with saturated water vapor. Acid gases that are released in the regeneration column are distilled off with water vapor generated in the boiler from the absorption solution and fed to the condensation system. In this system, the gaseous phase is cooled in a condenser, then it is separated in a separator in the form of a gaseous mixture consisting of acidic gases Hl5 and CO, which is removed from the system, and the condensed liquid phase (condensate) is recycled to a regeneration column. The regenerated absorption solution is withdrawn and sent to the initial throttling chamber. In this chamber, a rapid drop in pressure of the regenerated absorption solution occurs, resulting in the formation of a vapor phase consisting essentially of water vapor. The first cooling of the regenerated absorption solution occurs. From the initial throttling chamber, the absorption solution is then sent to the last throttling chamber, in which the pressure of the absorption solution again drops sharply with the formation of a new vapor phase consisting essentially of water vapor, the pressure of which is lower than the vapor phase pressure. the throttling chamber, and the new cooling of the regenerated absorption solution. The vapor phase exiting the terminal throttling chamber is again compressed by the compressor to a pressure equal to the vapor phase pressure exiting the initial throttling chamber and the vapor phases having the same pressure leaving the compressor and the initial throttling chamber are in the compressor. In this compressor, all the resulting vapor phases are compressed to a pressure equal to the pressure at the bottom of the regeneration column, and the resulting compressed vapor phase is added to the regenerated vapor phase and sent to the regeneration column. The choked regenerated absorption solution removed from the last chamber is choked, which is lost l amount of water corresponding to the amount of water vapor obtained in the throttling chambers during two successive stages of throttling and cooled partly during said steps orifice, is fed to effect indirect heat exchange with the absorption solution containing absorbed acidic compound, supplied from the absorption zone, and said absorption solution is heated before introduction of the latter into regeneratsyonnuyu column. At the outlet of the heat exchanger system, the regenerated absorption solution is sent for cooling to the absorption temperature. The cooled regenerated absorption solution is fed to the collector, from where it is sent to the absorption zone. The evaporation of water, caused by the throttling of the regenerated absorption solution in the throttling chambers, leads to the cooling of the indicated absorption solution. In addition, each stage of the throttling valve is a new distillation zone, which increases the number of theoretical plates of the regeneration column and this allows to reduce the amount of gas for distillation. In addition, the compressed water vapor produced by compressors from a single vapor evaporated in throttling cams is again combined in a steam recovery column obtained by boiling the regenerated absorption solution, which contributes to the distillation of the fractions separated by the acidic gas vapor. . Finally, the lowering of the temperature of the regenerated absorption solution, the result of evaporation of water in the throttling chambers, markedly reduces the flow rate of the cooling fluid in the refrigerator and in the condensation system, the cooling fluid usually being water. Example. In an installation similar to that described, natural gas is purified, containing 002 by washing with an absorption solution, which is an aqueous solution of diethanolamine, containing approximately 30 May. % diethanolamine. The purified natural gas contains by volume 15% H jS and 10% COj, the remaining are hydrocarbons, of which 69% are manganese. Absorption during this purification is carried out under a pressure of 78 bar, with the flow rate of the gas to be purified being fed into the absorption column 1, the flow rate of the absorption solution supplied to the absorption column is 570 tons / hour. Regeneration - with a pressure at the bottom of the column of 2.5 bar, steam consumption for boiling 54 t / h, boiling point 129 ° С. The throttling of the regenerated amine flow rate is carried out at a pressure in the initial throttling chamber 1.6 bar and a pressure in the final throttling chamber 1.05 bar. The use of the invention allows to improve the technical and economic characteristics of the process of absorption purification of gases from acidic components and to reduce the cost of the process by saving steam.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR REGENERATING SATURATED WITH HYDROGEN SULFUR AND / OR TWO
    SUE CARBON OF ABSORPTION SOLUTION, including ejection of a saturated solution into a regeneration zone having a pressure below the 1.35 bar zone, removal of hydrogen sulfide and / or carbon dioxide from the upper part of the regeneration zone, selection of the regenerated solution from the lower part of the zone, and multistage sequential throttling of the regenerated an absorption solution to obtain several vapor phases with their subsequent return to the regeneration zone, characterized in that, in order to reduce steam consumption and increase the degree of regeneration, the resulting vapor phases are previously combined and ejected into the lower regeneration zone under a pressure equal to the pressure in this zone.
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    类似技术:
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    同族专利:
    公开号 | 公开日
    DE3112792A1|1981-12-24|
    NO811090L|1981-10-01|
    FR2479021B1|1984-05-18|
    ES500882A0|1982-01-16|
    CA1166596A|1984-05-01|
    US4384875A|1983-05-24|
    GB2074035B|1984-06-13|
    NO164643C|1990-10-31|
    GB2074035A|1981-10-28|
    FR2479021A1|1981-10-02|
    NO164643B|1990-07-23|
    DE3112792C2|1997-02-13|
    ES8201841A1|1982-01-16|
    引用文献:
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    DE2043190C3|1969-09-09|1979-02-15|Benson, Field & Epes, Berwyn, Pa. |Process for the separation of acid gases from hot gas mixtures containing water vapor|
    US4088735A|1974-07-10|1978-05-09|Metallgesellschaft Aktiengesellschaft|Process for purifying gases from the gasification of fossil fuels|
    IT1056904B|1976-03-05|1982-02-20|Snam Progetti|PROCEDURE FOR THE PURIFICATION OF NATURAL GASES WITH HIGH CONTENT OF ACID GASES|
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    US4284423A|1978-02-15|1981-08-18|Exxon Research & Engineering Co.|Separation of carbon dioxide and other acid gas components from hydrocarbon feeds containing admixtures of methane and hydrogen|
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    DE2856078A1|1978-12-23|1980-07-10|Linde Ag|METHOD FOR SEPARATING AND RECOVERING GAS-SHAPED COMPONENTS FROM A GAS MIXTURE BY PHYSICAL LAUNDRY|
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    DE2912761A1|1979-03-30|1980-10-09|Linde Ag|METHOD FOR DISASSEMBLING A GAS MIXTURE|FR2517557B1|1981-12-04|1986-10-17|Elf France|RECOMPRESSION VAPOR REBUILDING PROCESS|
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    US5788843A|1997-07-11|1998-08-04|Larrabee, Jr.; Carl Richard|Method and installation for treating water|
    EP0918049A1|1997-10-27|1999-05-26|Shell Internationale Researchmaatschappij B.V.|Process for the purification of an alkanolamine|
    FR2771020B1|1997-11-19|1999-12-31|Inst Francais Du Petrole|DEVICE AND METHOD FOR TREATING A FLUID BY DIPHASIC COMPRESSION AND FRACTIONATION|
    FR2772373B1|1997-12-17|2001-05-04|Inst Francais Du Petrole|PROCESS FOR THE REMOVAL OF POLAR COMPOUNDS FROM AN ETHERIFICATION UNIT|
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    US7901487B2|2003-03-10|2011-03-08|Board Of Regents, The University Of Texas System|Regeneration of an aqueous solution from an acid gas absorption process by multistage flashing and stripping|
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    WO2011088008A1|2010-01-12|2011-07-21|Board Of Regents, The University Of Texas System|Acidic gas removal by aqueous amine solvents|
    CA2809209C|2010-08-24|2021-10-19|Terrance Trofimuk|Process for recovery of processing liquids|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR8007210A|FR2479021B1|1980-03-31|1980-03-31|
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