• 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 process for the preparation of urea in which a carbamate- and free ammonia-containing urea synthesis solution is formed from carbon dioxide and excess ammonia in a synthesis zone at a pressure of 125-350 bar, at least a portion of the carbamate present in the urea synthesis solution is decomposed in a stripping zone at the pressure of the synthesis zone or at lower pressure by heat supply and countercurrent contact with a stripping gas, the carbamate decomposition products, together with a portion of the excess ammonia and the stripping gas, are removed from the stripping zone as a gas mixture, at least a portion of the gas mixture obtained is condensed in a condensation zone and the stripped urea synthesis solution is processed into a urea solution or solid urea. The process is characterized in that in the condensation zone also at least 30% of the equilibrium amount of urea achievable under the reaction conditions is allowed to form and the carbamate- and urea-containing mixture is supplied to the synthesis zone. By preference, urea formation is continued until 50-80 %, of the way to the equilibrium has been covered.
    公开号:SU1456009A3
    申请号:SU853873452
    申请日:1985-03-15
    公开日:1989-01-30
    发明作者:Йонкерс Кис
    申请人:Уни Ван Кунстместфабрикен Б.В. (Фирма)；
    IPC主号:
    专利说明:

    one -
    This invention relates to a process for producing urea from ammonia and carbon dioxide.
    The purpose of the invention is to simplify the process. .,five
    The drawing shows the implementation of the method.
    In the drawing, the following notation is accepted: A — synthesis zones, B — desorption zone, C — condensation zone, D — steam reservoir, E — pump, and F — ejector.
    Through line 1, an ejector F, which is set in motion using compressed liquid ammonia through line 2, sucks the carbamate solution obtained by treating the solution containing urea. The mixture of liquid ammonia and carbamate solution enters the condensation zone C via line 3. Via line 4, which has holes containing ammonia and carbon dioxide, the gas mixture is introduced into. liquid. This gas mixture n.onjnieHa during desorption
    WITH
     CM
    to the treatment of the urea synthesis solution formed in the synthesis zone A in the desorption zone B, the desorption treatment is carried out in countercurrent to the desorbing gas, for example, carbon dioxide, when heat is applied. According to the proposed method, the pressures in the synthesis zone A, the desorption zone B and the condensation zone C are, for example, 140 atm. However, the pressures in these zones may vary. The dimensions of the condensation zone C are chosen in such a way that
    ten
    33417 kg of liquid and 45833 kg of gas-rich CO, containing also 286 kg of water vapor and 1533 kg of inert components, are injected into the high pressure unit. The pressure in the reaction zone, in the desorption zone and in the condensation zone is 141.2 a. A gas mixture consisting of 43742 kg NH 65795 kg CO, 2578 kg and 1533 inert components is introduced into the condensation zone, most of which is condensed and absorbed. in carbamate solution containing
    iJ | 3HJH CltV 1 V-l 1 S1LG11 D, - --- W — at least 30% of theoretic, 5 Sch 50964 kg NHg, 17957 kg CO and
    the possible amount of urea. The heat generated in the condensation zone C is removed by water flowing through line 5, which passes through lineo 6 and through the cooling of element 7 in the condensation zone with the aid of pump E and then converted into low pressure steam. The resulting steam passes through line 8 to steam tank D and through line 9 leaves the specified tank to an aggregate consuming low dashgen steam (not shown). Instead of removing heat by generating steam, process streams, such as a liquid urea solution, can be heated, which is then concentrated and passed through cooling elements. The solution of urea and carbamate and the unfused portion of the gas mixture that have passed through the con zone are passed through line 10 to synthesis zone A, where the further formation of urea occurs.
    From synthesis zone A, the urea synthesis solution passes through line 11 to desorption zone B, while gas mixture containing inert gases passes through line 12. The desorption solution for the synthesis of urea is obtained through line 13, is converted into urea solution in a known manner and is concentrated, after which the concentrated solution can be converted to solid urea.
    The invention is illustrated by the following examples.
    Example 1 (comparative).
    Urea is prepared by the method described in European Chemical Chemical, with a plant capacity of 1,500 tons per day.
    20
    9231 kg. The solution of bamate, which consists of 78108 67706 kg of CO and 1029 kg and a temperature of 168 ° C, is formed, while the gas mixture with 18598 kg of NHj, 16046 kg of COj, 980 kg and 1533 kg of inert content of carbamate remaining and the solid mixture is introduced into the reaction zone.
    25
    The water liberated during condensation is removed with the help of water, which is detrimental to the formation of 60000 kg of vapor pressure (4.4 atm, T 3Q Heat transfer surface 1694 m
    Example 2. According to the proposed method, the same quality of urea is obtained as in example 1. The flow in the high pressure section of the unit is 141.2 atm. Condensation of gas from that obtained by desorption is carried out in a horizontally arranged refrigerator with suction. Condensation is accompanied by the formation of 50% of the theoretically possible amount of urea. Formed a carbamate containing 30,839 kg m of guilt, 60,871 kg of W, 50,553 kg of CO j and 20521 kg. Its temperature
    35
    40
    45
    . In addition, a gas mixture remains, which consists of 18171
    NH
    3
    10706 kg C02, 505 kg
    50
    55
    And 1533 kg of inert components. With the power of heat released in the heat congress zone, 60000 kg of low pressure (4.4 atm) is formed. Some heat transfer surface 66 Example D0 Similarly, Straight 2 is produced with the same amount of urea. But now, 75% of a balanced amount of urea is formed in the condation zone. no condensation is obtained solution which contains in addition to 56188 kg
    0
    33417 kg of liquid and 45833 kg of gas-rich CO containing also 286 kg of water vapor and 1533 kg of inert components are introduced into the high pressure unit. The pressure in the reaction zone, in the desorption zone and in the condensation zone is 141.2 atm. A gas mixture consisting of 43,742 kg of NH, 65,795 kg of CO, 2,578 kg and 1,533 kg of inert components is introduced into the condensation zone, most of which is condensed and absorbed into the carbamate solution containing W-SCH 50,964 kg NHg, 17957 kg WITH and
    9231 kg. A carbamate solution is formed, which consists of 78108 NH, 67706 kg CO and 1029 kg and has a temperature of 168 ° C, while the gas that remains with the clean gas contains 18598 kg NHj, 16046 kg COj, 980 kg and 1533 kg of inert components Carbamate solution and the gas mixture is introduced into the reaction zone.
    five
    The heat released during condensation is removed with water, which leads to the formation of 60,000 kg of low-pressure steam (4.4 atm, T). Q Heat transfer surface 1694 m.
    Example 2. According to the proposed method, the same amount of urea is obtained as in Example 1. The pressure in the high pressure section of the installation is 141.2 atm. The condensation of the gas mixture obtained by desorbing is carried out in a horizontally located refrigerator with suction. Condensation is accompanied by the formation of 50% of the theoretically possible amount of urea. Formed a carbamate solution containing 30839 kg of urea, 60871 kg of W, 50553 kg of CO j and 20521 kg. Its temperature
    five
    0
    five
    . In addition, there remains a gas mixture, which consists of 18171 kg
    NH
    3
    10706 kg C02, 505 kg
    0
    five
    And 1533 kg of inert components. With the help of heat released in the condensation zone, 60000 kg of low-pressure steam (4.4 atm) is formed. The required heat exchange surface is 667 m. Example 3 Analogously to example 2, an identical amount of urea is obtained. But now, in the condensation zone, 75% of the balanced available amount of urea is formed. In the condensation zone, a solution is obtained which contains, in addition to 56188 kg NH
    and 40203 kg COj, also 47930 kg of urea and 25649 kg.
    In addition, there remains a gas mixture consisting of 14,825 kg NH 8400 kg CO 605 kg H20 and 1533 kg of inert components. The temperature of the liquid and gas components released from the condensation zone, The released heat is used to form 60000 kg of low pressure steam (6.8 atm). A heat transfer surface of 1694 m is required.
    Example 4. At the plant, according to the technological scheme, the method for producing urea according to the invention is used to synthesize the same amount of urea as described in Example 1. The pressure in the high pressure section, including synthesis, evaporation and condensation zones, is maintained at 122.6 atm. The condensation of the gas mixture obtained at the stage of evaporation is carried out in the annular zone of a vertically placed condenser with a submerged coil, the average residence time of condensate in which was about 22.7 minutes, which leads to the formation of 50% of urea from the theoretically possible x reaction. The resulting ammonium carbamate solution contains 29291 kg of urea, 62667 kg of ammonia, 52656 kg of carbon dioxide and 18997 kg of water. Solution temperature In addition, a gas mixture containing 18,665 kg of ammonia, 9553 kg of carbon dioxide, 543 kg of water and 1710 kg of an inert component remains. With the help of heat in the condensation zone, 66970 kg of low pressure steam (4.4 atm) is formed. A heat transfer surface of 850 m is required.
    Example 5. Similarly to Example 2, an identical amount of urea is obtained, but now 73% of the achievable equilibrium amount is formed in the condensation zone with an average residence time of condensate of about 21.5 minutes. The pressure in the condensation zone is 156.9 atm. The solution obtained in the condensation zone contains, in addition to 56967 kg of ammonia and 42429 kg of carbon dioxide, also 43818 kg of urea and 25782 kg of water. In addition, a gas mixture containing 14344 kg of ammonia, 10157 kg of carbon dioxide, 671 kg of water and 1711 kg remains.
    5 o Q
    g g with
    five
    inert component. The temperature of the liquid and gaseous components leaving the condensation zone,. The released heat is used to produce 52,450 kg of low-pressure steam (6.33 atm). This requires a heat exchange surface area of 850 m.
    Example 6. The preparation of urea in an amount of 1500 tons / day is carried out in the installation shown in the drawing. The pressure in the high pressure zone, including the synthesis, desorption and condensation zones, was 196 atm. The condensation of the gas mixture formed during desorption occurs on the side of the casing of the submerged condenser. The average residence time of condensate in it was 16.9 minutes. Under these conditions, the urea yield was 69% of the theoretical. The resulting carbamate solution contains 46.958 kg of urea, 57.510 kg NHj, 40.656 kg COi and 28.206 kg. Its temperature is 188.5 ° C. In addition, a gas mixture consisting of 7.523 kg of NH, 6.053 kg of CO, 414 kg and 1.533 kg of inert components is obtained. Due to the heat generated in the condensation zone, 52.970 kg of low pressure steam (6.8 atm) is formed. The heat exchange surface required for this is 667 m.
    The table shows examples of the implementation of the known and proposed methods.
    As can be seen from the table, the proposed method allows to reduce the required heat exchange surface in the condenser and increase the parameters of the low-pressure steam to 6.9 atm.
    权利要求:
    Claims (1)
    [1]
    The invention of the method of obtaining urea by the interaction of carbon dioxide and excess ammonia at a pressure of 125-200 atm in the synthesis zone with obtaining a solution containing ammonium carbamate and free ammonia with subsequent decomposition of ammonium carbamate in the desorption zone at the pressure of the synthesis zone, heating and countercurrent interaction with the desorbing gas to obtain a desorbed solution, from which mercury concentrated urea or solid urea has passed, and a gas mixture containing decomposition products of carbamate a mmoni with part
    7, 14560098
    an excess of ammonia and a stripping gas for the stay of the gas mixture into the zone, a part of which condenses in the non-zone, which provides for the formation of 50-condensation to produce condensate, characterized in that, in order to simplify the process, the condensation is carried out with a time of 75% urea of an equilibrium amount achieved under synthesis conditions, to produce a condensate containing ammonium carbamate and urea, which is sent to the synthesis zone.
    we change the stay of the gas mixture in the zone providing the formation of 50-
    75% of the urea is from the equilibrium amount achieved under the synthesis conditions to produce a condensate containing ammonium carbamate and urea, which is sent to the synthesis zone.
    3 4 5 6
    eleven
    About 5.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1456009A3|1989-01-30|Method of producing carbamide
    SU1378781A3|1988-02-28|Method of separating carbamide,ammonia and carbon dioxide from diluted water solutions
    US4308385A|1981-12-29|Process for purifying urea-containing waste water and process for preparing melamine
    SU1494865A3|1989-07-15|Method of producing urea
    US4801746A|1989-01-31|Process for the preparation of urea
    CN1980887B|2012-03-14|Process for the preparation of urea
    CA1053701A|1979-05-01|Integrated urea-ammonia process
    NL8201652A|1983-11-16|METHOD FOR THE PREPARATION OF UREA.
    US3120563A|1964-02-04|Urea preparation
    SU1064863A3|1983-12-30|Process for producing urea
    SU459887A3|1975-02-05|Urea production method
    EP0266840A1|1988-05-11|Process for preparing urea
    EP0145054B1|1988-03-23|Process for preparing urea
    CA1049556A|1979-02-27|Urea manufacture
    US4311856A|1982-01-19|Process for synthesizing urea
    US3232983A|1966-02-01|Urea synthesis
    US3107149A|1963-10-15|Method of separating ammonia from carbon dioxide
    KR870000807B1|1987-04-20|Synthesis method of urea
    UA67718C2|2004-07-15|A method for the preparation of urea, condenser and plant for realizing this method
    IE45825B1|1982-12-01|Process for preparing a urea solution from nh3 and co2
    GB2089786A|1982-06-30|Process for synthesizing urea
    WO2016099269A1|2016-06-23|Process for urea production
    US3232982A|1966-02-01|Urea synthesis
    EA007593B1|2006-12-29|Method for the production of an aqueous hydroxylamine solution
    SU1225485A3|1986-04-15|Method of producing urea
    同族专利:
    公开号 | 公开日
    CN85101703A|1987-01-24|
    LT2206B|1993-11-15|
    LV5225A3|1993-10-10|
    EG16600A|1989-01-30|
    BR8501156A|1985-11-12|
    TR22418A|1987-04-30|
    BG60247B2|1994-03-24|
    AT38033T|1988-11-15|
    ZW4185A1|1985-06-26|
    IN164392B|1989-03-11|
    NL8400839A|1985-10-16|
    ES8602622A1|1985-12-01|
    CN1010308B|1990-11-07|
    PT80109B|1986-11-14|
    IL74522D0|1985-06-30|
    AU579614B2|1988-12-01|
    PT80109A|1985-04-01|
    EP0155735B1|1988-10-19|
    CA1330444C|1994-06-28|
    ZA851978B|1985-11-27|
    RO91349A|1987-08-31|
    FI851046A0|1985-03-15|
    CN85100951A|1987-01-10|
    MX7357E|1988-07-19|
    ES541294A0|1985-12-01|
    GR850639B|1985-07-02|
    YU41685A|1987-12-31|
    KR850006930A|1985-10-25|
    KR870001692B1|1987-09-24|
    NZ211460A|1987-10-30|
    RO91349B|1987-09-01|
    FI851046L|1985-09-17|
    AU3989385A|1985-09-19|
    EP0155735A1|1985-09-25|
    NO851044L|1985-09-17|
    DD232038A1|1986-01-15|
    HUT39721A|1986-10-29|
    JPS60209555A|1985-10-22|
    DE3565680D1|1988-11-24|
    MA20372A1|1985-10-01|
    PL252389A1|1985-10-22|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    NL101446C|1960-04-08|
    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.|
    US4013718A|1970-09-03|1977-03-22|Snam Progetti S.P.A.|Integrated process for the production of urea|
    AU8825782A|1981-09-01|1983-03-28|Unie Van Kunstmestfabrieken B.V.|Process for the preparation of urea|NL8303888A|1983-11-13|1985-06-03|Unie Van Kunstmestfab Bv|METHOD FOR THE PREPARATION OF UREA.|
    NL8800284A|1988-02-08|1989-09-01|Stamicarbon|METHOD FOR THE PREPARATION OF UREA.|
    US6274767B1|1992-11-19|2001-08-14|Urea Casale, S.A.|Process for the revamping of urea synthesis plants consisting of a stripper with ammonia|
    US5767313A|1995-05-23|1998-06-16|Dsm N.V.|Method for the preparation of urea|
    NL1000416C2|1995-05-23|1996-11-25|Dsm Nv|Process for the preparation of urea.|
    JP3987607B2|1996-10-07|2007-10-10|東洋エンジニアリング株式会社|Improved urea synthesis method and apparatus|
    IT1290423B1|1996-10-17|1998-12-03|Eurotecnica Contractors And En|PROCEDURE FOR THE SYNTHESIS OF UREA FROM CARBON DIOXIDE AND AMMONIA|
    NL1004977C2|1997-01-13|1998-07-15|Dsm Nv|Method to increase the capacity of an existing urea process.|
    NL1005118C2|1997-01-29|1998-07-30|Dsm Nv|Process for the preparation of urea.|
    NL1009516C2|1998-06-29|2000-01-04|Dsm Nv|Process for the preparation of urea.|
    NL1016643C2|2000-11-17|2002-05-22|Dsm Nv|Process for the preparation of urea.|
    NL1019081C2|2001-10-01|2003-04-02|Dsm Nv|Process for the preparation of urea.|
    JP4426415B2|2004-10-01|2010-03-03|東洋エンジニアリング株式会社|Reactor|
    US7582795B2|2005-04-27|2009-09-01|Toyo Engineering Corporation|Apparatus for synthesizing urea and method for revamping the same|
    EP2107051A1|2008-04-02|2009-10-07|DSM IP Assets B.V.|Process for inreasing the capacity of an existing urea plant|
    EP2123634A1|2008-05-19|2009-11-25|DSM IP Assets B.V.|Process for the production of urea from ammonia and carbon dioxide|
    EP2123633A1|2008-05-19|2009-11-25|DSM IP Assets B.V.|Process for the production of urea from ammonia and carbon dioxide|
    EP3190101B1|2012-05-03|2019-09-25|Stamicarbon B.V.|Method and apparatus for the production of urea from ammonia and carbon dioxide|
    CN105246874B|2013-05-28|2018-06-12|东洋工程株式会社|Urea synthesis method|
    EP2843304A1|2013-08-29|2015-03-04|Casale SA|A shell-and-tube apparatus for heat recovery from a hot process stream|
    USD843660S1|2017-11-27|2019-03-19|Mary Kay Inc.|Cosmetic compact|
    USD850006S1|2017-11-27|2019-05-28|Mary Kay Inc.|Cosmetic compact|
    USD863685S1|2017-11-27|2019-10-15|Mary Kay Inc.|Cosmetic compact|
    JP2020147534A|2019-03-14|2020-09-17|東洋エンジニアリング株式会社|Urea manufacturing method and apparatus|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL8400839A|NL8400839A|1984-03-16|1984-03-16|METHOD FOR THE PREPARATION OF UREA.|
    [返回顶部]