• 专利附录
  • 专利说明
  • 权利要求
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    • 专利摘要:
    1501038 Urea synthesis MITSUI TOATSU CHEMICALS Inc 20 Sept 1976 [22 Sept 1975] 38714/76 Heading C2C Urea is synthesized from ammonia and carbon dioxide using a molar ratio of ammonia to carbon dioxide of from 5 : 1 to 12 : 1, in a process in which the urea-synthesis effluent is pressurized and then heated in a separation zone to separate therefrom unreacted ammonium carbamate and excess ammonia in the form of a mixed gas of ammonia and carbon dioxide, and this mixed gas is recycled to the urea-synthesis zone.
    公开号:SU971093A3
    申请号:SU762402956
    申请日:1976-09-22
    公开日:1982-10-30
    发明作者:Оно Хироси；Иноуэ Сигеру
    申请人:Мицуи Тоацу Кемикалз Инкорпорейтед(Фирма)；
    IPC主号:
    专利说明:

    (54) METHOD OF OBTAINING UREA
    The invention relates to a method for producing urea from carbon dioxide and ammonia, in particular to improving the stage of separating unreacted components from the stream of synthesized urea and subsequent g. To return them to the synthesis stage.
    A known method for producing urea from carbon dioxide and ammonia, according to which the process is carried out at 180-210 ° C and a pressure of 150-400 kg / cm, followed by separation and re-cycling of the unreacted components to the synthesis stage. Usually, unreacted components containing an excess of ammonia, carbon dioxide and water are recycled or in the form of a gas phase, for which unreacted components are compressed, in the form of a solution, which is obtained by condensation or adsorption with an aqueous adsorbent 1.
    Recycling unreacted components in the form of a gas has several advantages: the heat loss at the stage of extraction of unreacted components is reduced and the heat necessary for this is obtained in the form of; foot steam from the urea synthesis zone, where jg
    an elevated temperature is maintained, since unreacted materials are recycled to the urea synthesis zone as a gas mixture having a high temperature. At the same time, this method of decirculating has significant drawbacks, the main of which is the significant energy demand for compression of the gas mixture and structural difficulties, since the gas mixture is subjected to compression is very corrosive and has a high temperature. It is not possible to lower the temperature of the gas mixture when it is compressed, since as the temperature decreases, ammonia carbamate may begin to condense and solidify, which may cause the equipment to fail.
    When recirculating the solution, significantly less energy is spent on compressing the solution to the pressure of urea synthesis, but in this case there is a significant loss of thermal energy. The latter are due to the fact that the condensation or absorption of a highly heated gas mixture requires efficient cooling. The heat of condensation or the waste of unreacted components can be used 397 in a heat exchanger, but the efficiency of the heat used is very low. The purpose of the invention is to reduce energy costs. The goal is achieved by the method according to the method of producing urea from ammonia and carbon dioxide at 180-185 ° C and a pressure of 160-180 kg / cm with subsequent separation of unreacted components by recycling at the molar ratio of ammonia to carbon dioxide. 5: 1 - 12: 1 with the subsequent separation of unreacted components at a temperature of 5-25 C and a pressure of 0.5-5 kg / cm, exceeding those of jj OepaTypy and the pressure in the synthesis zone, and the condensation of 20-90% of the separated gas mixture with subsequent separate recycling of gas mixture and condensate to the synthesis zone. The drawing is a diagram explaining the proposed method. Initial ammonia and carbon dioxide are fed to the recovery zone 1, heat is supplied via pipelines 2 and 3, respectively. In the heat recovery zone 1, the pressure is maintained at 0.1 kg / cm or more than the pressure in the urea synthesis zone 4, and the temperature of the urea synthesis. In the heat recovery zone 1, the initial ammonia and carbon dioxide react with each other to form ammonium carbamate, during which heat is released, part of this heat is used for the operation in zone 4 of urea synthesis, and the other part is removed ferry. Heat recovery zone 1 is connected by pipeline 5 to urea synthesis zone 4, in which the temperature is maintained at 180-185 ° C and a pressure of 160-180 kg / cm. The flow of synthesized urea from zone 4 synthesis of urea through the outlet through the pipeline 6 passes to the pump 7, in which its pressure increases by 0.2 kg / cm or more. The solution compressed in this way enters the high pressure separator 8: through Tpy6orfpo-water 9. The high pressure separator 8 operates under pressure by 0.5 kg / cm or more than the pressure in the heat recovery zone 1 and is heated by a hot liquid flowing through pipeline 10 and discharged through pipeline 11. Unreacted materials are separated in high pressure steam generator 8 from the flow of the synthesized urea in the form of gS of ammonia, carbon dioxide and water vapor and are fed to zone I of heat recovery through pipeline 12. At the same time rem stream of sterilized urea, from which unreacted i ateriapes were isolated. sequentially enters the pipeline 13 first into the separator 14 of the pressurized J and then into the low pressure separator 15 to separate small amounts of unreacted components from it and finally discharged through the pipeline 16 as an aqueous solution of urea containing a trace of unreacted components. Thus, in the medium pressure separator 14, in which the pressure is maintained at 14–18 kg / cm and the temperature is 140–170 ° C, 20–90% of unreacted substances are separated from the stream of synthesized urea and passed through pipeline 17 as a carbon dioxide gas mixture. aza, ammonia and water vapor. A stream of synthesized urea, from which unreacted products are thus separated, is fed via conduit 18 to a low pressure separator 15, in which all unreacted components are separated from the stream of synthesized urea. The resulting aqueous solution of urea is discharged through line 16. In a low pressure separator, the temperature is maintained at 110-145 ° C and the pressure is within 0.05-3.5 kg / cm, while the mixed gas from carbon dioxide, ammonia and water vapor is separated. in the manner described above. The gas mixture separated in the low-pressure separator is then fed via conduit 19 to a low-pressure condenser 20, in which the gas is cooled to 30-60 ° C to condense and form an aqueous solution containing ammonium carbamate: Water-1PSh solution is compressed and fed to a condenser 21 moderate pressure using a pump 22. In a moderate pressure condenser 21, the mixed gas entering through conduit 17 and consisting of carbon dioxide, ammonia and water vapor is absorbed at 50-120 ° C. The resulting solution is then returned to heat recovery zone 1 via pipeline 23 using a pump 24. Example 1. Ammonia and carbon dioxide are fed to heat recovery zone 1 via pipelines 3 and 2 at a feed rate of 56.8 tons / day and 74.0 tons / day, respectively, and then via pipeline 5 to zone 4 of urea synthesis, along with unreacted materials through pipelines 12 and 23. In the zone of urea synthesis, a temperature of 185 ° C and a pressure of 180 kg / cm are set. The flow of the synthesized urea from the synthesis zone has the following composition, weight. including: urea 102.1; ammonium carbamate 43.4; ammonia (NH3: CO2 5.05) 117.1; water 47.1; biuret 0.4. The flow of the synthesized urea enters through conduit 6 to pump 7, where exhb pressure increases to 183 kg / cm, and then to the high pressure separator through conduit 9. The high pressure separator maintains a temperature of 195 ° C and a pressure of 188 kg / cm. It separates 107.2 tons / day of ammonia, 6.7 tons / day of carbon dioxide and 5.5 tons / day of water from the synthesized urea stream and returns it to the heat recovery zone 1 via the duct 12. The degree of condensation of the mixed gas containing ammonia, carbon dioxide and water, is about 80 wt.% in the heat recovery zone 1, and the resulting condensate and the remaining mixed gas are recycled to the urea synthesis zone 4 via pipeline 5. The separator 8 is kept warm by means of steam with a pressure of 20 kg. /cm. The flow of the synthesized urea at the base of the high pressure separator 8 has the following composition, weight. including: urea 100.4; ammonia 14.9; water 41.2; ammonium carbamate 33.5; biu ret 0.6. The flow of the synthesized urea enters the medium pressure separator 14, in which the temperature is maintained at 170 ° C and the pressure of 18 kg / cm to separate most of the remaining unreacted materials from the stream entering the low pressure separator 15, in which the temperature is maintained at 140 ° C and a pressure of 0.5 kg / cm to separate all residual unreacted components. The resulting 76% urea aqueous solution is discharged through water pipe 16. At the same time, the separated unreacted components are condensed in a low pressure condenser 20 and then in a moderate pressure condenser 21 and the condensate is recycled through conduit 23 to the heat recovery zone 1 as an aqueous solution. consisting of 33.7 wt. including ammonium carbamate, 15.4 wt. am ammonia and 10.8 wt. h of water. Example 2. Ammonia and carbon dioxide are supplied to heat recovery zone 1 via pipelines 3 and 2 at a feed rate of 57.2 tons / day and 74 tons / day, respectively, and then fed through pipeline 5 to zone 4 of urea synthesis together with unreacted materials. pipelines 12 and 23. In the area of the synthesis of urea set the temperature of 180 ° C and a pressure of 169 kg / cm. The flow of the synthesized urea from the synthesis zone has the following composition, weight. including: urea 102; ammonium carbamate 16.3; ammonia (NHaiCOj 11.5) 308.5; water 65.0; biuret 0.1. The flow of synthesized urea enters through conduit 6 to pump 7, where its pressure increases to 171 kg / cm, then the flow enters high-pressure separator 8 through conduit 9. In high-pressure separator 8, the temperature is maintained at 200 ° C and pressure 171 kg / cm. It separates 297.7 tons / day of ammonia, 6.0 tons / day of carbon dioxide and 25.9 tons / day of WATER from the stream of synthesized urea and returns to the heat-recovery zone 1 via pipeline 12. The separator 8 is kept warm. by means of steam with a pressure of 25 kg / cm. The flow of the synthesized urea at the base of the high pressure separator 8 has the following composition, weight. including: urea 101.3; ammonia 15.4; water 39.0; ammonium carbamate 6.4; biuret 0,2. The flow of the synthesized urea enters the cenapafop 14 medium pressure, in which the temperature is maintained at 170 ° C and the pressure of 18 kg / cm to separate most of the remaining unreacted components from the I stream, then to the low pressure separator 15, in which the temperature is maintained at 140 ° C and a pressure of 0.5 kg / cm to remove all residual unreacted materials. The resulting 77% urea aqueous solution is discharged through conduit 16. At the same time, the separated unreacted materials are condensed in a low pressure condenser 20 and then in a moderate pressure condenser 21 and the condensate is recycled through conduit 23 to the heat recovery zone 1 as an aqueous solution, consisting of 6.9 wt. including ammonium carbamate, 15.5 wt. am ammonia and 8.5 wt. h of water. Amount. The condensate in the gas mixture, containing ammonia, carbon dioxide and water, in the reduction zone 1 is about 90% by weight. The resulting condensate and the remaining mixed gas are recycled to zone 4 of urea synthesis via pipeline 5. Example 3. Ammonia and carbon dioxide are supplied to zone 1 by heat recovery via pipelines 3 and 2 at a feed rate of 56.8 tons / day and 74 tons / day, respectively, and The pipeline is fed through pipeline 5 to zone 4 of urea synthesis together with unreacted components via pipelines 12 and 23. In the zone of the urea resin, a temperature of 185 ° C and a pressure of 180 kg / cm is set. The flow of the synthesized urea from the urea synthesis zone has the following composition, parts by weight: urea 101.5; ammonium carbamate 45.6; ammonia (NH3: COi 5.07) 118.4; water 50.9; biuret 0.1. The flow of synthesized urea flows through conduit 6 to pump 7, where its pressure increases to 180.5 kg / cm, then the flow enters high-pressure separator 8 through conduit 9. In high-pressure separator 8, the temperature is maintained at 190 ° C and the pressure is 180.5 kg / cm. It is separated from a stream of synthesized urea with 63 tons / day of ammonia, 4.9 tons / day of carbon dioxide and 4.3 tons / day of iodine and returned to zone 1 to recover heat through pipeline 12. The separator 8 is kept warm. by means of 25 kg / cm steam. 79 The flow of the synthesized urea in the base of the high pressure separator 8 has the following; weight including: urea 100.4; ammonia / 59.2; water 46.3; ammonium carbamate 383; biuret 0.1. The flow of synthesized urea enters the medium pressure separator 14, in which the temperature and pressure are maintained at 18 kg / cm to separate most of the remaining unreacted materials from the stream entering aaievr in the low pressure separator 15, in which the temperature is maintained at 140 ° C and pressure 0 kg / cm to separate all residual unreacted components. The resulting 77% urea water solution is withdrawn through conduit 16. At the same time, the separated unreacted components are condensed in a low pressure condenser 20 and then / j in a condenser 21 jTviepeHHoro pressure (88% condensation) and the condensate is recycled through conduit 23 to the zone 1 heat recovery in the form of an aqueous solution consisting of: from 37.6 parts by weight ammonium carbamate, 59.6 parts by weight ammonia and 16.1 wt. h of water. Example 4. Ammonia and carbon dioxide dioxide are supplied to heat recovery zone I via pipelines 3 and 2 at a feed rate of 56.8 tons / day and 74 tons / day, respectively, and then fed through pipeline 5 to zone 4 of urea synthesis together with unreacted components through pipelines 12 and 23. In zone 4 of urea synthesis, temperature is set (180 ° C and pressure of 160 kg / cm). The flow of synthesized urea from the urea synthesis zone has the following composition, parts by weight: urea 102.1; ammonium carbamate 45, 2; ammonia (MNZ: C02 5.5) 135.7; water 55.3; boret 0.1 Flow of synthesized urea p Steps through pipeline 6 to pump 7, where its pressure increases to 165 kg / cm, and then the flow is sent to high pressure separator 8 through pipe 9. In high pressure separator 8, the temperature is maintained at 205 ° C and pressure 165 kg / cm. It separates 122.9 tons / day of ammonia, 20.4 tons / day of carbon dioxide and 12., 9 tons / day of water from the synthesized urea and returns it to the heat recovery zone 1 via pipeline 12. The separator 8 is kept heated condition by 25 kg / cm steam. The flow of the synthesized urine into the bases of the high pressure separator 8 has the following composition, weight. including: urea 100.1; ammonia 28.6; water 41.8; ammonium carbamate 11.5; biuret 0,2. The flow of the synthesized urea enters the separator 14 I) of the same pressure, in which the temperature and pressure of 18 kg / cm are maintained to separate part of the remaining non-recirculating components from the stream which then goes to the low pressure separator 15, in which the temperature is maintained at 140 ° C and pressure 0.5 kg / cm. For separating all residual unreacted materials. The resulting 77% urea aqueous solution is withdrawn through conduit 16. At the same time, the separated unreacted components are condensed in a low pressure condenser 20 and then in a moderate pressure condenser 21 (condensation degree 84%) and the condensate is recycled through conduit 23 heat in the form of an aqueous solution consisting of 10.6 wt. including ammonium carbamate, 29.0 weight. am ammonia and 11.8 wt. h of water. Example 5. Ammonia and carbon dioxide are supplied to heat recovery zone 1 via pipelines 3 and 2 at a feed rate of 57.2 tons / day and 74.1 tons / day, respectively, and then fed through pipe 5 to zone 4 of the urine synthesis 1 together with unreacted materials through pipelines 12 and 23. On the 4th side of urea synthesis, a temperature of 180 ° C and a pressure of 169 kg / cm are established. The flow of the synthesized urea from the urea synthesis zone has the following composition, BeCi h / urea 102.0; ammonium carbamate 16.3; ammonia (NHjiCOz 5.07) 308.5; water 65.0; biuret 0.1. The flow of synthesized urea flows through line 6 to pump 7, where its pressure increases to 171 kg / cm, then the stream goes to high pressure separator 8 to line 9. In high pressure separator 8, the temperature is maintained at 185 ° C and pressure 171 kg / cm B 194.5 tons / day of ammonia, 1.8 tons / day of carbon dioxide and 14.5 tons / day of water are separated from the flow of the synthesized urea and returned to the heat recovery zone 1 via conduit 12. The separator 8 is kept hot. 24 kg / cm of steam. The flow of the synthesized urea at the base of the high pressure separator 8 has the following composition, weight. including: urea 101.9; ammonia 115.4; water 50.5; ammonium carbamate 13.1; biuret 0.1. The flow of the synthesized urea enters the medium pressure separator 14, in which the temperature is maintained at 170 ° C and the pressure of 18 kg / cm to separate most of the remaining unreacted materials from the stream then fed to the low pressure separator 15, in which the temperature and pressure are maintained 0.5 kg / cm for separation. all residual unreacted materials. The resulting 77% aqueous solution of urea is discharged through line 16. At the same time, the separated unreacted materials are condensed in a low-pressure condenser 20 and then in a moderate-pressure condenser 21
    pressure and condensate through conduit 23 are recycled to heat recovery zone 1 as an aqueous solution consisting of 14.4 wt. including ammonium carbamate, 115.4 wt. am ammonia and 19.9 wt. h of water.
    The amount of condensate in a mixture of gas containing ammonia, carbon dioxide and water,
    Way
    Mitsui-Toatsu TR-C (improved.)
    STAMI (removal of CO2)
    SNAM (NHj removal)
    权利要求:
    Claims (1)
    [1]
    Method according to the invention From these tables it can be seen that the proposed method has an advantage over known methods not only in relation to the quality of urea, determined by the content of agglomerates, but also in terms of water vapor savings. The invention of the method for producing urea from ammonia and carbon dioxide at a temperature of 180-185 ° C and a pressure of 160-180 kg / cm, followed by separation and recycling of unreconstructed components to the synthesis stage, characterized in that in order to remove the energy from the heat recovery zone I, , about 23 wt.%. The resulting covdensate and the remaining shifted gas are recycled to line 4 of the urea synthesis via line 5. To the table; 1 and 2 shows the comparative data characterizing the proposed and known methods.
    Table 1
    I
    The content of agglomerates,% Less than 0.8
    Less than 0.9
    0.75
    Less than 0.6 Table 2, tic costs, the latter is carried out at a molar ratio of ammonia to carbon dioxide 5: 1-12: 1, followed by the separation of unproof components at a temperature of 5-25 ° C and pressure per kg / cm exceeding temperature and pressure in the zone of urea synthesis, and by condensation of 20–90% of the separated pelvic mixture with the POTSI (separate recycling of the j-ae mixture and condensate into the synthesis zone. Sources of information taken into account during the examination 1. K) chery V. I., Lebedev V.V. Synthesis of carbamide. L., Khimi, 1970. p. 187-208.
    7.x
    / g
    4h
    T
    l
    NJ
    / i
    /five
    g

    25
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    US3107149A|1963-10-15|Method of separating ammonia from carbon dioxide
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    同族专利:
    公开号 | 公开日
    NO150556C|1984-11-07|
    PH13079A|1979-11-23|
    FR2324622A1|1977-04-15|
    DE2642429A1|1977-03-31|
    JPS585190B2|1983-01-29|
    NO763240L|1977-03-23|
    BR7606033A|1977-08-23|
    NL7610490A|1977-03-24|
    IT1070815B|1985-04-02|
    NO150556B|1984-07-30|
    JPS5239626A|1977-03-28|
    FR2324622B3|1979-06-01|
    GB1501038A|1978-02-15|
    CA1059145A|1979-07-24|
    PT65594B|1978-03-28|
    PT65594A|1976-10-01|
    US4081469A|1978-03-28|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2848493A|1955-06-27|1958-08-19|Allied Chem|Process for synthesis of urea|
    US3049563A|1957-04-05|1962-08-14|Sxpaf |
    US3573173A|1968-07-24|1971-03-30|Mitsui Toatsu Chemicals|Process for recovering excess ammonia in urea synthesis by direct contact condensation with liquid ammonia|
    US3876696A|1968-09-03|1975-04-08|Snam Progetti|Process for the production of urea having a low carbamate content|
    US3984469A|1969-10-16|1976-10-05|Snam Progetti S.P.A.|Process for the production of urea|
    BE790015A|1971-10-19|1973-04-12|Mavrovic Ivo|UREA SYNTHESIS WITH IMPROVED CONVERSION AND HEAT RECOVERY|
    JPS5535378B2|1973-02-14|1980-09-12|JPS5715832B2|1978-11-30|1982-04-01|
    JPS5746954A|1980-09-05|1982-03-17|Mitsui Toatsu Chem Inc|Synthesis of urea|
    JPS6116384B2|1980-09-12|1986-04-30|Mitsui Toatsu Kagaku Kk|
    JPS6215070B2|1981-10-16|1987-04-06|Mitsui Toatsu Chemicals|
    JPH0241751Y2|1984-11-16|1990-11-07|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP50113709A|JPS585190B2|1975-09-22|1975-09-22|
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