• 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:
    An improved process for the separate recovery of substantially pure ammonia and substantially pure carbon dioxide from mixtures containing ammonia and carbon dioxide, and possibly water, such as are obtained as by-products in the manufacture of melamine from urea or the synthesis of urea from ammonia and carbon dioxide. The by-product mixture is introduced into a process loup having an ammonia separation zone (1) with a NH3- rectifying column (3), a carbon dioxide separation zone (2) with a CO2- rectifying column (18). and a desorption zone (3) where virtually all NH3 and C02 are removed in desorber (10), the zone to which the mixture is initially fed being dependent upon its composition. The separation is effected by maintaining a system pressure differential between the ammonia and carbon dioxide separation zones, or adding diluting water to the carbon dioxide separation zone. The efficiency of the separation is enhanced by introducing an ammonia containing gaseous phase into the bottom of the carbon dioxide separation zone.
    公开号:SU973012A3
    申请号:SU792762791
    申请日:1979-04-28
    公开日:1982-11-07
    发明作者:Йоханнес Берманс Андреас
    申请人:Стамикарбон Б.В. (Фирма)；
    IPC主号:
    专利说明:

    (54)
    SPREAD OF AMMONIA AND CARBON DIOXIDE.
    ; This invention relates to methods for separating NHj and CO2 from their mixture.
    The cnoct is known in which the gas mixture of ammonia and carbon dioxide, in which the ammonia content is higher than in the azeotrope, is absorbed by water or aqueous paci thief. At atmospheric pressure (ammonia pressure is discharged from the solution, and the remainder of the solution is subjected to fractional distillation at a pressure of 5-ZO ata and: heated to distill | carbon dioxide Q 13.
    The disadvantage of this method is that the pressure of the processed mixture should be reduced to 1 at.
    The closest to the proposed technical x 15; and the achieved result is a method of separating ammonia and carbon dioxide from their mixture by fractional distortion when heated in the ammonia discharge zone and in the carbon dioxide separation zone, and carbon dioxide is liberated in the presence of 0, 2-6 edges + total amount of added water to the weight of the initial mixture in the zone of carbon dioxide 2.
    The disadvantage of this method is quite high energy costs.
    The purpose of the invention is to reduce energy consumption.
    This goal is achieved in that, according to the method of separation of ammonia and carbon dioxide from a mixture containing ammonia, carbon dioxide and water, in a technological circuit having an ammonia separation zone, a separation zone / hvooxyrode and a desorption zone, including the release of ammonia in the zone ode (ammonium sludge with the supply of the remaining liquid phase to the carbon dioxide separation zone and the release of carbon dioxide in the presence of water in the carbon dioxide separation zone, removal of the remaining liquid phase from it, the remaining liquid phase from zone (separation of carbon dioxide ,, vvrd into a desorption zone where Ammian was separated | soderzhaschivg gas 1-5O% of which is introduced into the carbon dioxide separation zone.
    Energy consumption (%) depending on the amount of ammax-containing gas (desorber) fed to the carbon dioxide release zone is presented in the table.
     t, -, r, im - Г - ГГ, i, j ii ij-ц / V-iii-ii М Desorber .Ч О 2 lО 2О 45 55 5 (prototype)
    Energy flow
    % 10O 92 89-89 93 1О2 reduction
    i - “About
    The drawing shows the scheme of the proposed method.
    Example 1. Essentially pure NHj and substantially pure CO are separated from the mixture NH, in a plant using a process of dilution, o; Type 1
    At a pressure of 18OO kPa and, in, the KH-distillation column 1 is added, 20 liters of 44348 kg / h of a solution of NHg and CO in water, which had the composition,%: ННс38.3} COj 21.1 {water 4О, 6. With the help of a com- pressor 2, 635 kg / h of air was introduced, and 248 kg / h were introduced into NH3-rectification-shonnaya column 1 and 387 kg / h - into a desorber of 3,227O kg / h gas mixture containing,%: NH 3 55.4; CO29.6; 33, B, inert gas 1.5, from desrrber 3, 184 ,, are expanded to 18OO kPa 30 through the valve and after that also I feed to the LV-Rafikion ion column 1, 37246 kg / h of gas mixture containing,,%: NH e 98.0; H2O O, 3; an inert gas 1 | 7, is discharged from the top of this column, jj Part of this gas mixture is liquefied by cooling in a condenser 4, 17824 kg / h. This mixture is returned to column 1 as reflux, 16959 kg / h of liquid ammonia is obtained at the outlet. From kond-40 of the sator 4 comes 2464 kg / h of the pelvic mix, containing,%: MH 74.2; iyer-shchly gay 25,8O, This mixture is washed in a scrubber 5 with water (2000 kg / h). Heat is removed from the scrubber using a radirku-; 45 p dione condenser 6. In an hour in the N N, return the rectifying column. 3829 kg of a solution containing,%: NHj 47.8; 52.2. The temperature at the top of this column is 5–5 ° C.
    63 S kg / h of inert gas is passed through pipelines 7 and 8 into the cpjj distillation column 9, which operates at a pressure in the ZOOO kPa system. 54273 kg / h of a liquid with a temperature of 131 ° C and a composition,%: NH j 25.8; CO 21.8; 52.4 is passed from the bottom of the HHhHyrsting column 1
    through the pipeline 1O and through the pump to the CO-rectifying column 9.
    In this column 9, in which the pressure ZOOO kPa, is supplied 72OO kg / h of the gas mixture from stripper 3 through line 11. This amount is 22.4% of the total amount of gas mixture leaving the stripper 3. In column 9 also serves 12 46313 kg / h of diluent through the pipeline, consisting of water and traces
    NH and CO2, which are at the outlet of the desorier. Some of this heat is released in the lower part of the capped dow column 9. In total, 7,227 kg / h of liquid is discharged from the stripper, so that 25,914 kg / h of water, after cooling in the condenser 13, are drained from the system, and desorbton water can be used, for example, for absorption
    NH 3 and CO ;.
    5,951 kg / h of wash water is fed to a portion of the CO2 distillation column to wash out the last traces of NHj.
    The temperature at the bottom of the CO-distillation column is kept at a level with steam. The temperature in the upper part is 55 ° C. From the top, the gas mixture is 1006-1 kg / h and contains 93.2% CO2 and less than 100 h / min NHj. From the bottom of the column 9, 10431 kg / h of solution having 180 ° C and containing,%: HO 79.9; # 17.3,3; COj 3.0. The composition of this liquid is located on the side of the boundary line that corresponds to the enrichment of ammonia. In this desorber, the solution is practically free of NHi and COj as a result of steam treatment, so that 72227 kg / h of water containing only traces of NHj and ISO can be discharged. The relative power consumption is 89% of the power consumption of the prototype.
    Formulaobretenov
    The method of separating ammonia and carbon dioxide in a mixture containing ammonia, carbon dioxide and water in a technological circuit with an ammonia separation zone, a bauxite separation zone; in carbon and a desorption zone, including the emission of ammonia in the ammawa separation zone with the flow of the remaining liquid phase carbon dioxide separation zone in the release of carbon dioxide in the presence of water in the call of carbon dioxide separation
    权利要求:
    Claims (1)
    [1]
    Claim
    A method for separating ammonia and carbon dioxide 1 from a mixture containing ammonia, carbon dioxide and water in a process circuit having an ammonia separation zone, a carbon dioxide separation aeration zone and a desorption zone ( including the separation of ammonia in the ammonia separation aeon with the remaining liquid phase being fed into the zone separation of carbon dioxide and the release of carbon dioxide in the presence of water in the zone of separation of carbon dioxide 973012 and with the conclusion of the remaining liquid phase, characterized in that, in order to reduce energy consumption, the remaining liquid phase, conductivity of the carbon dioxide separation zone, administered 5 dates in a desorption zone, where gas is separated ammiaksoderzhafy, 1 - 50% of which is introduced into the zone of separation of carbon dioxide.
    类似技术:
    公开号 | 公开日 | 专利标题
    EP0019326B1|1983-08-24|Process for purifying urea-containing waste water and process for preparing melamine
    SU973012A3|1982-11-07|Process for separating ammonia and carbon dioxide
    EP0093466B1|1985-08-07|Process for the preparation of urea
    US4801745A|1989-01-31|Improved process for the preparation of urea
    US4801746A|1989-01-31|Process for the preparation of urea
    US4163648A|1979-08-07|Process for separation of ammonia and carbon dioxide
    US3759992A|1973-09-18|Urea synthesis
    EP0145054B1|1988-03-23|Process for preparing urea
    US3114681A|1963-12-17|Process of recovering unreacted ammonia from a urea synthesis melt by a two stage rectification operation
    EP0088478B1|1986-06-11|Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water
    EP0266840A1|1988-05-11|Process for preparing urea
    SU1153825A3|1985-04-30|Method of obtaining urea
    US4256471A|1981-03-17|Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water
    US3193353A|1965-07-06|Method of removing carbon dioxide from ammonia
    US4207256A|1980-06-10|Treatment of water vapor generated in concentrating an aqueous urea solution
    US3107149A|1963-10-15|Method of separating ammonia from carbon dioxide
    US3711479A|1973-01-16|Process for separating melamine from a hot synthesis gas mixture which contains melamine vapor
    KR800001159B1|1980-10-18|Process of separating substantially pure nh3 and substantially pure co2 from a composition containing nh3 and co2
    AU2006244735A1|2006-11-16|Method for concentrating an aqueous ammonium carbamate stream
    US3808271A|1974-04-30|Urea synthesis
    US4053508A|1977-10-11|Process and installation for preparing urea from ammonia and carbon dioxide
    KR820001898B1|1982-10-19|Process for separation of nh3 and co2 from mixtures of nh3 co2 and water
    KR830001019B1|1983-05-25|How to separate ammonia and carbon dioxide from a mixture of ammonia and carbon dioxide and water
    KR790001171B1|1979-09-10|Method of recovering unreacted materials and heat in urea synthesis
    CS213330B2|1982-04-09|Method of separating the ammonia and carbon dioxide from the mixture containing the ammonia and carbon dioxide
    同族专利:
    公开号 | 公开日
    NL7804668A|1979-10-31|
    AT371738B|1983-07-25|
    NO791441L|1979-10-30|
    IL57169A|1982-07-30|
    DE2960975D1|1981-12-24|
    JPS6210924B2|1987-03-09|
    NO151117C|1985-02-13|
    ES479903A1|1980-06-16|
    NO151117B|1984-11-05|
    EP0005292B1|1981-10-14|
    CA1131885A|1982-09-21|
    MX5686E|1983-12-09|
    BR7902619A|1979-11-20|
    ZA791801B|1980-04-30|
    PL215241A1|1980-02-25|
    AR222654A1|1981-06-15|
    IN151692B|1983-07-02|
    US4251235A|1981-02-17|
    RO77950A|1982-03-24|
    ATA306179A|1982-12-15|
    AU526062B2|1982-12-16|
    AU4632579A|1979-11-01|
    PL114967B1|1981-03-31|
    EP0005292A1|1979-11-14|
    JPS54143800A|1979-11-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE669319C|1937-07-21|1938-12-22|Julius Pintsch Kom Ges|Device for filling containers with propane, butane or similar liquefied gases|
    GB664375A|1954-07-27|1952-01-02|
    DE1067014B|1957-05-18|
    US2992703A|1958-06-05|1961-07-18|Vasan Srini|Separation of carbon dioxide from ammonia|
    US3112177A|1959-11-11|1963-11-26|Toyo Koatsu Ind Inc|Method of separating ammonia from hydrogen cyanide|
    NL264624A|1960-05-10|
    US3315442A|1964-10-05|1967-04-25|American Cyanamid Co|Quenching of crude melamine gases|
    FR1457776A|1964-10-16|1966-01-24|Allied Chem|Process for reducing corrosion in a gas scrubber during the separation of carbon dioxide and ammonia from their mixtures with water vapor|
    AT261638B|1966-05-02|1968-05-10|Chemie Linz Ag|Process for processing an ammonia-carbonic acid gas mixture|
    DE1670290A1|1967-12-01|1971-01-14|Basf Ag|Process for the separation of ammonia from the waste gases resulting from melamine synthesis|
    NL165712C|1970-05-30|1981-05-15|Stamicarbon|METHOD AND APPARATUS FOR RECOVERY OF AMMONIA AND CARBON DIOXIDE FROM THE SPRAY GAS OF A UREUM SYNTHESIS IN SYNTHESIS PRESSURE.|
    DE2229213C2|1972-06-15|1982-12-02|Metallgesellschaft Ag, 6000 Frankfurt|Process for the processing of waste water resulting from the degassing or gasification of coal|
    DE2317603C3|1973-04-07|1982-03-25|Basf Ag, 6700 Ludwigshafen|Process for at least partial separation of gas mixtures containing ammonia and carbon dioxide|
    DE2527985C3|1975-06-24|1981-04-16|Metallgesellschaft Ag, 6000 Frankfurt|Continuous process for the production of pure ammonia|
    DE2646804C3|1976-10-16|1982-03-11|Basf Ag, 6700 Ludwigshafen|Process for the production of pure ammonia from gas mixtures containing ammonia and carbon dioxide|
    NL168196C|1976-11-03|1982-03-16|Stamicarbon|METHOD FOR SEPARATING NH & 013 AND CO & 012 FROM A MIXTURE OF NH & 013, CO & 012 AND H & 012O.|US4256471A|1979-04-16|1981-03-17|Stamicarbon, B.V.|Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water|
    NL8200905A|1982-03-05|1983-10-03|Stamicarbon|METHOD FOR SEPARATING AMMONIA AND CARBON DIOXIDE FROM AMMONIA, CARBON DIOXIDE AND WATER MIXTURES|
    US4502997A|1983-03-04|1985-03-05|The Lummus Company|Treatment of purge gas|
    US4801356A|1987-10-15|1989-01-31|International Fuel Cells Corporation|Removal of ammonia from fuel cell power plant water system|
    JP4975205B2|2000-04-28|2012-07-11|日揮株式会社|Method for recovering ammonia from gaseous mixtures|
    US6706093B2|2000-05-23|2004-03-16|Rohm And Haas Company|Method and apparatus for preventing iron contamination in corrosive service|
    AT500297B8|2000-11-08|2007-02-15|Agrolinz Melamin Gmbh|PROCESS FOR CLEANING MELAMINE AMMONIA|
    NL1022526C2|2003-01-30|2004-08-04|Dsm Nv|Process for separating NH3, and optionally also CO2 and H2O, from a mixture containing NH3, CO2 and H2O.|
    CN102688651A|2012-06-13|2012-09-26|北京烨晶科技有限公司|Separation method of mixed gas of ammonia and carbon dioxide|
    CN105148682B|2015-08-22|2017-07-04|安徽金禾实业股份有限公司|A kind of method of melamine tail gas coproduction ammoniacal liquor|
    CN106395858B|2016-10-15|2018-09-28|上海国际化建工程咨询有限公司|A kind of method and device converting lime set waste water making pure liquefied ammonia containing ammonia|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL7804668A|NL7804668A|1978-04-29|1978-04-29|METHOD FOR SEPARATING NH3 AND CO2 FROM MIXTURES OF NH3, CO2 AND WATER.|
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