• 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:
    A continuous process for acid gas removal from process gas streams by contact with an aqueous alkanolamine solution such as MEA wherein the temperature of the MEA solution is controlled by placing an intercooler at the lower end of the absorption column such that the temperature of the down-coming MEA solution is cooled to allow increased mole loading of acid gas in the solution, but is not so cooled that the mass transfer rate of the acid gas from the process gas to the MEA solution is slowed to an unacceptable level. The lower temperature highly loaded MEA solution is then passed to a heat exchanger-flash-heat exchanger arrangement where the temperature is increased to provide satisfactory flash efficiency and then heated again prior to introduction into the stripper to reduce the sensible heat duty in the stripper. The combination of optimally positioned intercooler and flash together with the temperature ranges recited permit the obtainment of a net energy demand lower than can be expected from the addition of the intercooler effect and the flash effect.
    公开号:SU1042603A3
    申请号:SU782704704
    申请日:1978-12-28
    公开日:1983-09-15
    发明作者:Фрэнсиз Батвелл Кеннет；Джон Кьюбек Даниел
    申请人:Юнион Карбид Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    with
    This invention relates to methods for removing acidic impurities from process gases. A known method of purifying gases from carbon dioxide by absorption of covoid acid by alkaline salts of mice}. The disadvantage of this method is the use of toxic reagents as an absorbent, which complicates its operation. The closest to the invention in its technical essence and the achieved result is a method of purifying hydrocarbon gases from acidic components, including heating the gas mixture, contacting it with an aqueous solution of alkanolamine at 0-70 ° C under a pressure of 10-12 these, separating a saturated absorber solution, heating it up to 75-100 ° C, supplying the heated solution to the evaporator, in which instantaneous depressurization takes place and part of the acid is released into the atmosphere, supplying the absorber solution to the stripping column at 93-115 ° C for regeneration from The next step is to return it to the contacting stage 2. The disadvantage of the known method is the increased energy consumption of the process, which is 30.5 kcal / kg mole. The purpose of the invention is to reduce the energy consumption of the process. The goal is achieved by the fact that according to the method of purification of hydrocarbon gases from acidic impurities, including heating the gas mixture, its contacting with an aqueous alkanolamine solution at tO-70 C under pressure, separating the absorber’s saturated solution, heating it to, supplying the heated solution to the evaporator in which instantaneous depressurization and ejection of a part of acidic impurities into the atmosphere occurs, feeding the absorber solution into the stripping column at 93-115 ° C for regeneration, followed by returning it to the contacting stage, after tadii contacting from 50 to 100 saturated scavenger is output from the process is cooled to 57-85 C and recycled to the contacting step. Example, The basic principles of the invention are embodied in a system of the type indicated using 35 weight ,; a solution of MEA (mrnoethanolamine) as an absorbent. The flow rate of the incoming gas is i133 kg-mol / h, of which 1089 kg-mol / h comes from CO, and this gas enters the contactor at 65.6 ° C. The inlet gas stream is saturated with water; contact pressure is 25.3 atm. To facilitate the comparison of the invention with various other systems on an equivalent basis, the approximation of the loading of the enriched solution with steam to the equilibrium is kept constant at a level of about. The flow rate of the solution is 8706 l / min. It is introduced into the contactor at 40.6 ° C when the depleted solution is charged, which is 0.21 mole of CO per mole of amine. The MEA solution, partially loaded with carbon dioxide, is passed through an intermediate cooler at 71.1 ° С, a. then through the contactor in the place where the loading of the enriched solution was increased to 0.5b mol C02 by. 1 mole of amine. The temperature of the solution at the exit of the contactor is 57.2 C, and the content of C02 in the exhaust gas is reduced to LLP h, / million The intermediate cooler requires for cooling a partially loaded solution of the MEA 11.8 ppm, kcal / h with cooling water consumption of about 11920 l / min. The enriched amine solution is passed to the heat exchanger at 57.2 ° C and withdrawn at 800 ° C, respectively. The recycled depleted amine solution enters at 86.7 ° C and exits at 64 ° C. The solution is then passed to an evaporation tank and evaporated to a pressure of 0.0 ati. The temperature of the enriched solution decreases from 80.0 to 73.9 C as a result of flash evaporation, resulting in the separation of 1–7 kg-mol / h CO2, the content of CO2 in the enriched solution thereby decreasing from 157 k) mol / h. The solution is then passed to a second heat exchanger, where the enriched amine solution is heated to 110.0 ° C by recycling the depleted amine, which enters at 121.1 ° C and exits at 86,. The enriched solution is passed into a stripping column at 110.0 ° C. It requires 23 , 9 thousand, kcal / k |-mol CO for stripping the carbonated gas-rich amine stream from 157 to 653 kg-mol CO2 / H. Some improvement can be achieved in terms of both the heat and power supply and the operational
    costs (30.6 thousand kcal / kg-mole, and the ratio of reduced operating costs of 1.0; up to 11.6 thousand kcal / kg-mole and the coefficient OjS). This is achieved by increasing the s loading of the enriched solution by using an intermediate cooler, i.e. at a lower temperature of the enriched solution, it is possible to achieve 10 higher loads of the enriched solution to maintain the same equilibrium. The effect can be further enhanced by increasing the load of the depleted solution and as a result of improving the thermodynamics of the stripping column. For this, 50-100 C02 saturated. monoethanolamine is removed from the process and cooled to, and then returned to the contacting stage.
    The table presents the comparative data of the processes according to the method of the prototype and the proposed
    Loading 0, 50 0.50. 0.50 pu of the solution. Loading of the depleted 0,150,150,21 solution 87,587,587,5 Equilibrium, 30.55327.27525.55% kcal / kg-mol Hapitalovlode 5355593-5573 no, thousands of dollars. Heat supply costs, 3520 3159 2396 thousand dollars / year Operating costs, D127 “151 thousand dollars / year Ratio of capital 1.23, 1.27 costs Heat energy ratio, 90 0.85 tic costs Coefficient of operating 0, 97 0, 9 costs
    This method allows to reduce the energy consumption for the process from 30.5 to 23.7 kcal / kg. mole, i.e. by 25-30%.
    The use of the intermediate cooling stage of a saturated absorber contributes to an increase in the effect5 (Q3.
    The ability of the instant evaporation stage to increase the load. Saturated plant absorber by reducing the restriction to the absorber. It is the presence of tension in equilibrium, that the tolerances of property as in the part of intensification
    higher loads at the intermediate stage are cooled down by 1I, so
    the start of the absorber. The use of between and increasing the load on the cannula cooling absorber also reduces the energy consumption of the process.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR CLEANING HYDROCARBON GASES FROM ACID IMPURITIES, including heating the gas mixture, contacting it with an aqueous alkanolamine solution at 40- / 0 ° С under pressure, separating the saturated absorber solution, heating it to 75-10 ° С, supplying the heated solution to the evaporator in which there is an instant pressure release and the release of part of acidic impurities into the atmosphere, the absorber solution is supplied to the stripping column at 93-115 ° С for regeneration, with its subsequent return to the contacting stage, characterized in that, in order to reduce the energy Atrato, after step h kontaktirova- Nia from 50 to 100% saturated absorption g Titel removed from the process is cooled to 57-85 C and recycled to the contacting step.
    g with c>
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    同族专利:
    公开号 | 公开日
    ES476412A1|1979-04-16|
    FR2413117A1|1979-07-27|
    HU180102B|1983-01-28|
    MX150634A|1984-06-13|
    GB2014183A|1979-08-22|
    JPS5496475A|1979-07-30|
    DE2856571A1|1979-07-05|
    IT7831367D0|1978-12-28|
    SE440484B|1985-08-05|
    TR20543A|1981-10-15|
    BR7808557A|1979-08-28|
    BG47650A3|1990-08-15|
    US4184855A|1980-01-22|
    IN150766B|1982-12-11|
    CA1105241A|1981-07-21|
    FR2413117B1|1986-06-20|
    BE873127A|1979-06-28|
    JPS5918092B2|1984-04-25|
    DE2856571C3|1982-06-24|
    SE7812626L|1979-06-30|
    GB2014183B|1982-06-23|
    DE2856571B2|1981-06-25|
    NL7812615A|1979-07-03|
    引用文献:
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    US2477314A|1945-11-27|1949-07-26|Standard Oil Dev Co|Process for purifying gases|
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    US3242644A|1962-12-27|1966-03-29|Union Oil Co|Process for removing acid constituents from gaseous mixtures|
    GB1244176A|1968-02-23|1971-08-25|Foster Wheeler Ltd|Gas treatment process|
    US3961015A|1969-08-21|1976-06-01|Societe Nationale Des Petroles D'aquitaine|Combined hydrolysis and absorption process and apparatus therefor|
    US3808140A|1970-07-13|1974-04-30|B Mago|Antimony-vanadium corrosion inhibitors for alkanolamine gas treating system|US4274841A|1980-03-28|1981-06-23|Union Carbide Corporation|Acetylene recovery process and apparatus|
    US4397660A|1981-06-15|1983-08-09|Shell Oil Company|Process for the removal of H2 S and CO2 from a gas mixture|
    US4590036A|1982-02-02|1986-05-20|Exxon Research And Engineering Co.|Process for corrosion inhibition utilizing an antimony-molybdenum salt corrosion inhibitor composition|
    AT380092B|1983-09-29|1986-04-10|Simmering Graz Pauker Ag|METHOD AND DEVICE FOR RECOVERING HEAT FROM WATER STEAM GASES BY ABSORPTION OR ADSORPTION|
    IN164027B|1984-03-29|1988-12-31|Basf Ag|
    CA1284334C|1985-06-27|1991-05-21|Masayuki Sawada|Method for recovery of ethylene oxide|
    AT385914B|1985-11-26|1988-06-10|Innofinance Altalanos Innovaci|METHOD AND DEVICE FOR DEHUMIDIFYING GASEOUS MEDIA|
    CA1334836C|1987-04-09|1995-03-21|Richard A. Gregory, Jr.|Removal of salts from aqueous alkanolamines using an electrodialysis cell with an ion exchange membrane|
    ES2003265A6|1987-04-21|1988-10-16|Espan Carburos Metal|Method for obtaining CO2 and N2 from internal combustion engine or turbine generated gases|
    ZA899705B|1989-01-26|1990-09-26|Aeci Ltd|Purification of gases|
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    US8535419B2|2009-04-01|2013-09-17|Zephyr Gas Services Llc|Modular amine plant|
    EP2311545A1|2009-10-15|2011-04-20|Nederlandse Organisatie voor toegepast -natuurwetenschappelijk onderzoek TNO|Method for absorption of acid gases|
    DE102009052640A1|2009-11-10|2011-05-12|Linde-Lkca-Dresden Gmbh|Process and apparatus for gas scrubbing|
    JP5665022B2|2010-03-31|2015-02-04|新日鉄住金エンジニアリング株式会社|Carbon dioxide gas recovery device|
    JP5697411B2|2010-11-17|2015-04-08|株式会社東芝|Carbon dioxide recovery device and carbon dioxide recovery method|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/865,732|US4184855A|1977-12-29|1977-12-29|Process for CO2 removal|
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