• 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:
    1532659 Absorbent regeneration G GIAMMARCO and P GIAMMARCO 28 Nov 1975 [28 Nov 1974] 49121/75 Heading B1L [Also in Division C1] In the removal of acidic impurities, e.g. CO 2 , H 2 S, HCN, SO 2 , from a gaseous mixture by an absorption stage at 40-135‹C using an aqueous absorbent solution of alkali metal carbonates (alone or activated by amino acids, ethanolamines or arsenic trioxide), ethanolamines, amino acids, or alkali metal phosphates, sulphites, bisulphites or borates, followed by a regeneration stage wherein the impurities are stripped by steam from the absorbent, and the absorbent is then recycled (a) the regeneration stage comprises a principal regeneration column and a secondary regeneration column, the principal column operating at a higher pressure than the secondary column; (b) the spent absorbent solution is partially regenerated in one column after which at least part of the partially regenerated solution is fed to the other column for further regeneration; (c) the regeneration in the principal column is effected by steam introduced directly from outside or produced by boiling the solution present in that column, and the pressure in that column is controlled such that steam issuing from the top thereof is produced in quantities from 1.5 to 3 times the quantity corresponding to equilibrium conditions at the top of said column; and (d) the regeneration in the secondary column is effected predominantly by steam evolved by utilising the heat contained in the regenerated solution issuing from the principal regeneration column, e.g. by expansion of that solution to the secondary column pressure. A further secondary column may be provided which is fed by steam issuing from the main secondary column and through which is passed an absorbent fraction extracted from the upper portion of the principal column, this fraction then being returned to the principal column or passed through the main secondary column. The absorption stage may comprise an initial impurity absorption stage and a secondary heat absorption stage, part of the absorbent passing through both stages and part through the second stage only. The regeneration columns may also be multi-stage.
    公开号:SU940633A3
    申请号:SU752196610
    申请日:1975-11-27
    公开日:1982-06-30
    发明作者:Джаммарко Джузеппе；Джаммарко Паоло
    申请人:за вители К ПАТЕНТУ；
    IPC主号:
    专利说明:

    (St) METHOD FOR REGENERATING THE ABSORBENT PROCESS OF GAS CLEANING FROM ACIDIC COMPONENTS
    I
    The invention relates to the processes of absorption purification of gas mixtures from acid components and may find its application in the chemical and gas industries. five
    A known method for regeneration of two saturated absorbents of the process of purifying gases from acid components takes place in two regeneration columns, and two different streams of regenerated absorbent with different degrees of carbonization tl are obtained.
    The main disadvantage of this method is the increased steam consumption for 15 regeneration and considerable energy consumption.
    The closest to the invention in its technical essence and the achieved result is a method for regenerating the absorbent of the process of purifying gases from acidic components by two-step contact with steam at a temperature above the boiling point of the absorption solution, and
    After the purification, the saturated absorbent is taken out, divided into two streams, and each of them is separately subjected to regeneration in two regeneration columns 2.
    The main disadvantage of this method is also the increased steam consumption of 1.5 kg of steam / m CO.
    The purpose of the invention is to reduce steam consumption.
    The goal is achieved by the method of regenerating the absorbent pro-, gas purification process from acidic components by two-stage contact with steam at elevated temperatures, in which the absorbent is completely fed to the first contact stage, the temperature difference between the top and bottom of the column is maintained at 10-5C and 1 , 3-3.5 atm, respectively, after which the absorbent is directed to the second stage of contact.
    This method allows to reduce steam consumption from 1.5 kg to 0.6 kg of steamA
    / m, i.e. almost 3 times
    In addition, the degree of regeneration is 40.9. Using this method, it is possible to increase the degree of extraction of the acidic components in the first stage of the regeneration process, from 60 to 90. The degree of regeneration is 10 kO% t due to which the energy consumption for the process is reduced at the second stage. The choice of ranges of numerical values of temperatures and pressures is due to the fact that when the value exceeds these values, steam consumption increases and energy consumption increases, and a decrease in temperature leads to a decrease in the degree of carbonization. Example. In a two-stage cleaning cycle, the treated gas (151000, 28 at, 18 COg,) is fed to the first reboiler, where it releases 139 1O kcal / h, leaves at Itl-C, and enters the second reboiler, where it releases 61-10 kcal / The gas is then withdrawn at 120 ° C and at this temperature it is fed to the first absorber stage.The gas leaves the absorber at 108 ° C and the solution flow rate is 1040 (250 g / l and 50 g / l glycine). The pressure is set at 1.55 Ata in the upper part and the amount of steam consumption is reduced to 0.6 kg of steam / m SOP in terms of normal conditions. Regenerated f The stock of the abbrbent in the lower part of the second regeneration column has a temperature of 119 ° C, a consumption of 2bO and a degree of regeneration of 23.5%. It is expanded, after which it is cooled to 108 ° C and 937 kg of steam / h are recovered. The regenerated fraction of the solution the column has a temperature of 11b, 2 ° C, flow 312
    权利要求:
    Claims (2)
    [1]
    The ESPZZ4 is expanded, cooled to, and produces kg of steam / h. The degree of regeneration is the regenerated fraction at the outlet of the first column of 23.5 ° C, the regenerated fraction at the exit of the second column 16. Therefore, in addition to a significant reduction in heat consumption, a significant improvement in the degree of regeneration of the solutions is achieved. The use of this method makes it possible to carry out more efficiently the process of regeneration and purification of gases from acidic components, reducing the cost of steam for regeneration by 3 times. DETAILED DESCRIPTION A method for regenerating an absorbent gas purification process from acidic components by two-stage contact with steam at elevated temperatures, characterized in that, in order to reduce steam consumption, the absorbent is completely directed to the first step of contact, and the temperature difference between the top and bottom of the column is maintained equal to 10-45 ° C and 1.33, 3 atm, respectively, after which the absorbent is directed to the second stage of contact. Sources of information taken into account in the examination 1. US patent number 35bZb95, cl. 23-2, pub. 1971
    [2]
    2. US patent No. 35bZb9b CL, 23-2, published. 1971 (prototype).
    类似技术:
    公开号 | 公开日 | 专利标题
    SU940633A3|1982-06-30|Method for regenerating absorbent in the process of gas purification from acid components
    US4702898A|1987-10-27|Process for the removal of acid gases from gas mixtures
    US4847057A|1989-07-11|Process and installation for ammonia treatment of a gas
    SU1134113A3|1985-01-07|Method of regenerating absorption solution saturated with hydrogen sulfide and/or carbon dioxide
    US4082835A|1978-04-04|Removal of SO2 from gases
    US4146569A|1979-03-27|Process for removing gaseous impurities from a gaseous mixture containing the same
    GB1467027A|1977-03-16|Removal of impurities from gaseous mixtures and the regeneratioof absorbent solutions used therefor
    US4421536A|1983-12-20|Process for producing krypton and xenon
    CA1176824A|1984-10-30|Integrated cyclic scrubbing and condensate strippingprocess for the removal of gaseous impurities fromgaseous mixtures
    US4412977A|1983-11-01|Selective acid gas removal
    SU1378781A3|1988-02-28|Method of separating carbamide,ammonia and carbon dioxide from diluted water solutions
    GB1501195A|1978-02-15|Method of removing co2 and/or h2s from a gaseous mixture containing same
    US3155722A|1964-11-03|Recovery of residual ammonia and carbon dioxide in the synthesis of urea
    US4213958A|1980-07-22|Production of sulphur trioxide, sulphuric acid and oleum
    CA1068638A|1979-12-25|Regeneration of regenerable aqueous scrubbing solutions used for removing acidic gases from gas mixture
    US4293531A|1981-10-06|Selective removal of H2 S from gas mixtures containing CO2 and H2 S
    US3725210A|1973-04-03|Method of removing unreacted materials remaining in urea synthesis effluent by plural stage distillation and co2 stripping
    US4562052A|1985-12-31|Process for the removal of nitrogen oxides from nitric acid plant tail gas
    US3742016A|1973-06-26|Production and purification of acetone cyanohydrin by multiple stage distillation and condensation steps
    GB1455204A|1976-11-10|Process for purifying coke oven gas
    Salkind et al.1959|Acrylates Methacrylates. Raw Materials, Intermediates, Plant Integration
    US3470247A|1969-09-30|Process for the production of urea by synthesis of ammonia and carbon dioxide,with total recycling of the portion which has not been converted into urea
    US4174383A|1979-11-13|Process for purifying a sulfur dioxide containing gas with production of elemental sulfur
    US2930672A|1960-03-29|Method of regenerating ammoniacal copper solutions utilized to remove carbon monoxide from gases
    US4205050A|1980-05-27|Method of reducing corrosion in sour gas sweetening systems
    同族专利:
    公开号 | 公开日
    US4073863A|1978-02-14|
    IN145648B|1978-11-25|
    ES442977A2|1977-07-01|
    FR2292511A2|1976-06-25|
    DE2553400A1|1976-06-16|
    FR2292511B2|1979-01-05|
    ZA757108B|1976-10-27|
    JPS5177580A|1976-07-05|
    CA1068473A|1979-12-25|
    AU8699275A|1977-11-24|
    BE836122R|1976-05-28|
    NL7513878A|1976-06-01|
    IT1046519B|1980-07-31|
    GB1532659A|1978-11-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3563695A|1968-03-22|1971-02-16|Field And Epes|Separation of co2 and h2s from gas mixtures|
    GB1281571A|1968-07-13|1972-07-12|Vetrocoke Cokapuania Spa|Improvements in or relating to the removal of CO2 and/or H2S from gaseous mixtures|
    US3563696A|1969-06-17|1971-02-16|Field And Epes|Separation of co2 and h2s from gas mixtures|
    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|
    US3714327A|1969-10-13|1973-01-30|G Giammarco|Gas purification process|
    NL7402037A|1973-02-16|1974-08-20|US4094957A|1976-12-14|1978-06-13|Exxon Research & Engineering Co.|Process for removing acid gases with hindered amines and amino acids|
    US4160810A|1978-03-07|1979-07-10|Benfield Corporation|Removal of acid gases from hot gas mixtures|
    IT1156991B|1978-04-27|1987-02-04|Giuseppe Giammarco|IMPROVED PROCEDURE FOR THE PURIFICATION OF LIQUIDS AND OR FOR THE REGENERATION OF ABSORBENT SOLUTIONS|
    IT1109076B|1978-11-16|1985-12-16|Giammarco Giuseppe|IMPROVED PROCEDURE TO INCREASE THE EFFICIENCY OF THE SOLUTIONS USED FOR THE ABSORPTION OF CO2 AND H2S|
    DE2945675C2|1979-11-12|1984-08-16|Union Rheinische Braunkohlen Kraftstoff AG, 5000 Köln|Process for the production of pure hydrogen sulfide|
    US4299801A|1980-11-18|1981-11-10|Bethlehem Steel Corporation|Regenerating alkanolamine desulfurizer solutions|
    US4406868A|1981-11-13|1983-09-27|Phillips Petroleum Company|Process and apparatus for removing H2 S from gas streams|
    US4741884A|1981-11-13|1988-05-03|Phillips Petroleum Company|Process and apparatus for removing H2 S from gas streams|
    US4409191A|1982-01-04|1983-10-11|Exxon Research & Engineering Co.|Integrated cyclic scrubbing and condensate stripping process for the removal of gaseous impurities from gaseous mixtures|
    US6800120B1|1998-11-23|2004-10-05|Fluor Corporation|Split-flow process and apparatus|
    EP1551532B1|2002-07-03|2008-11-19|Fluor Corporation|Improved split flow apparatus|
    CN100509674C|2002-07-29|2009-07-08|伊万奈特纤维公司|Glass compositions|
    DE102004011429A1|2004-03-09|2005-09-29|Basf Ag|Process for removing carbon dioxide from gas streams with low carbon dioxide partial pressures|
    JP4690659B2|2004-03-15|2011-06-01|三菱重工業株式会社|CO2 recovery device|
    JP4745682B2|2005-02-23|2011-08-10|関西電力株式会社|CO2 recovery apparatus and method|
    WO2006118795A1|2005-04-29|2006-11-09|Fluor Technologies Corporation|Configurations and methods for acid gas absorption and solvent regeneration|
    KR100635698B1|2005-05-24|2006-10-17|한국전력공사|Absorbent for separation of acid gas from mixed gas and process for separating acid gas from mixed gas|
    DE102005050385A1|2005-10-20|2007-04-26|Basf Ag|Absorbent and method for removing carbon dioxide from gas streams|
    PE20071048A1|2005-12-12|2007-10-18|Basf Ag|PROCESS FOR THE RECOVERY OF CARBON DIOXIDE|
    WO2007093615A1|2006-02-14|2007-08-23|Basf Se|Refitting plants for acid gas removal|
    CA2861539C|2006-05-18|2016-01-12|Norbert Asprion|Carbon dioxide absorbent requiring less regeneration energy|
    US7901488B2|2006-10-04|2011-03-08|Board Of Regents, The University Of Texas System|Regeneration of an aqueous solution from an acid gas absorption process by matrix stripping|
    NO336193B1|2007-09-14|2015-06-08|Aker Engineering & Technology|Improved method of absorbent regeneration|
    AU2008322922B2|2007-11-15|2013-05-30|Basf Se|Method for removing carbon dioxide from fluid flows, in particular combustion exhaust gases|
    US8167979B2|2008-06-30|2012-05-01|University Of South Carolina|High efficiency, non-toxic scrubbing system and method for removing carbon dioxide from a gas|
    CH699928A2|2008-11-20|2010-05-31|Lonza Ag|A process for removing hydrogen cyanide from Ethandinitril.|
    CA2750780C|2009-01-28|2016-12-13|Siemens Aktiengesellschaft|Method and device for separating of carbon dioxide from an exhaust gas of a fossil-fired power plant|
    EP2311545A1|2009-10-15|2011-04-20|Nederlandse Organisatie voor toegepast -natuurwetenschappelijk onderzoek TNO|Method for absorption of acid gases|
    EP2536481A4|2010-02-17|2014-02-19|Fluor Tech Corp|Configurations and methods of high pressure acid gas removal in the production of ultra-low sulfur gas|
    JP5174194B2|2011-01-04|2013-04-03|三菱重工業株式会社|CO2 recovery apparatus and method|
    US9259680B2|2011-09-06|2016-02-16|Frank Bela|Claus hydrocarbon destruction via staged solvent regeneration|
    US9671162B2|2012-10-24|2017-06-06|Fluor Technologies Corporation|Integration methods of gas processing plant and nitrogen rejection unit for high nitrogen feed gases|
    WO2015089446A1|2013-12-12|2015-06-18|Fluor Technologies Corporation|Configurations and methods of flexible co2 removal|
    WO2022018832A1|2020-07-21|2022-01-27|株式会社 ユーリカ エンジニアリング|Carbon dioxide gas recovery system|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT7046474A|IT1046519B|1974-11-08|1974-11-08|Removing impurities from gas streams - with two-column absorption appts to improve energy consumption|
    [返回顶部]