• 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:
    Removal of urea, ammonia and carbon dioxide from diluted aqueous solutions, for instance urea process effluent, the solution being led into the top of a reaction column under a pressure of 10-30 bar, in which it flows down in counter-current to a flow of gas, for instance steam. The temperature in the top of the reaction column is 170-220°C; at the bottom, it is 180-230°C. Next, at a pressure of 1-5 bar, ammonia and carbon dioxide are removed from the urea-free bottom solution. The remaining solution contains less than 10 ppm urea and less than 10 ppm ammonia.
    公开号:SU1378781A3
    申请号:SU813363103
    申请日:1981-11-27
    公开日:1988-02-28
    发明作者:Зуидам Ян；Йоханнес Марие Ван Нассау Петрус；Жерар Марие Бернард Брюльс Пьер；Йонкерс Кес
    申请人:Уни Ван Кунстместфабрикен Б.В. (Фирма)；
    IPC主号:
    专利说明:


    cm
    This invention relates to an improved process for the recovery of urea, ammonia and carbon dioxide from dilute aqueous solutions.
    The purpose of the invention is to reduce energy consumption.
    The drawing shows a diagram of the proposed method.
    The process condensate, a dilute aqueous solution containing urea, ammonia and carbon dioxide collected in tank 1, is fed at a pressure of 1-5 atm, for example, 3-4 atm generated by a pump 2, and sent through a heat exchanger 3 to the lower part of the upper half of the pre-desorption column 4. Here, most of the dissolved ammonia and carbon dioxide are emitted due to the effect of desorption of gas streams, the passage w, to the lower half of the reaction column 5 and desorption column b, and also the heat contained in these gas fields otokah. The gas mixture thus separated, which also contains some amount of water vapor, is completely condensed in a reflux condenser 7. A small part of the condensate is returned to the upper part of the pre-desorption column 4, most of it is directed through line 8 to the synthesis of urea, for example 3 condensation and final absorption zones decomposition stages.
    The solution treated in the pre-desorption column 4, which may still contain, in addition to small amounts of ammonia and carbon dioxide, some amount of the initially present urea, is then passed through pump 9 under a pressure of 10-30 atm, for example 12.5 atm, through a heat exchanger 10 in the upper part of the reaction column 5. The reaction column 5 is divided into a number of compartments by filter plates, which serve as an ideal means of washing gas bubbles. In the lower part of this reaction column, steam at a pressure of 15-30 atm, for example 25 atm, is passed through line 11. The temperature of change along the length of the column is set by a device that regulates the amount of steam and pressure in the reaction column, so that the temperature in the upper part of the column 170- 220 С, and in the lower 180-230 С. At a pressure of 12.5 atm, tcm is established
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    peratura 181 ° C at the top and 193 C at the bottom.
    ABOUT
    Then the average temperature is about 185 ° C. The steam provides the heat necessary for the hydrolysis of urea and the evaporation of ammonia and carbon dioxide, resulting in this process. The urea content in the solution flowing down to the bottom of the reaction column 6 decreases markedly, and the faster the higher the temperature. After some time, it has been found that the final urea content is determined by the ends of ammonia and carbon dioxide in liquid. Therefore, pre-desorption of ammonia and carbon dioxide is necessary to achieve the required low urea content in the order of 10 hours per million or less. At an average temperature of 185 ° C, the minimum residence time in the column is 70 minutes. If the average temperature in the reaction column is higher, then a shorter residence time is sufficient.
    The mixture of gases, which is released, and the stripping agent formed in the reaction column 5, is removed from the upper part and, after expansion in the reduction device 12 to a pressure at which the desorption column 4 operates (according to the invention, 3-4 atm), is passed into The pre-desorption column 4 is below the condensate supply of the process and in this column it gives off some of its heat to the liquid that flows down.
    The liquid collecting at the bottom of the reaction column 5 contains almost no urea, gives up heat in the heat exchanger 10 to feed this column, then expands in the reduction device 13 to a pressure of 1-5 atm, for example 3.5 atm, and is passed into the upper part of the desorption column 6. A mixture of ammonia gases, carbon dioxide and water vapor, separated out during expansion, separates immediately in it, and the remaining liquid phase flows in the desorption column downwards in countercurrent with some steam supplied through line 14, whose heat enough d evaporation of ammonia and carbon dioxide and one whose spo - lities for desorbing more or less sufficient to achieve the required ammonia content of 10 ppm or lower. Ammonia and carbon dioxide released in this way and trapped in water vapor.
    test 11) with the mixture separated in the upper part of the desorption column, into the lower part of the pre-adsorption column 4, serve in this column as a heating and desorbing agent for the treated liquid.
     From the bottom of the desorption column 6, the effluent is discharged with urea and ammonia concentrations of 10 ppm or less. Part of the heat from this stream is used in heat exchanger 3 to pre-heat the treated liquid in pre-desorb ion column 4. The waste water stream is then, if necessary, cooled in refrigerator 15 with cooling water and released through line 16.
    PRI me R. 1. The condensate of the process obtained in a urea production plant with a capacity of 1500 tons per day is treated according to the scheme shown in the drawing. Material flows are expressed in kilograms per hour.
    .-
    The condensate process, 28333 kg, containing, wt.%: Ammonia 4,28; carbon dioxide 2.95, urea 1.09, heated in heat exchanger 3 from 42 to. In the pre-desorption column 4, this solution at a pressure of 3.43 bar is introduced in countercurrent into contact with 1147 kg of the gas mixture from the reaction column 5, which contains, kg: ammonia 66; carbon dioxide 252; water vapor 829 and which has a temperature of 181 ° C, and then with 5562 kg of the gas mixture of the desorption column 6, whose composition, kg: ammonia 421, carbon dioxide 5; water vapor 5136 and a temperature of 136 ° C. Through the upper part of the column 4, the following is withdrawn, kg: ammonia 2293; carbon dioxide 1720; water vapor 2528. This gas mixture is completely condensed and from the solution thus obtained, which has a temperature of 54 ° C, containing, kg: ammonia 876; carbon dioxide 657; water 966, return as reflux in the desorption column. The rest, which contains, kg: water 1562; ammonia 1417; carbon dioxide 1063, return to the installation for the production of urea.
    Thus, in the pre-desorption stage, already 75% of the initial amount of ammonia is removed.
    - - 10 15 20 25
    35 j
    ZO Q 5 ,,.
    In addition to 30349 kg of water, a stripping solution containing, kg / h: ammonia 310; carbon dioxide 31; urea 319 is brought to a pressure of 12.26 atm by means of pump 9 and, after heating in heat exchanger 10, is sent at a temperature of 135-183 ° C to the upper part of the reaction column 5. The amount of vapor passing to the lower part of this reaction column is 1700 kg its temperature is 225 C and pressure is 24.5 atm. Urea present in the feed solution is hydrolyzed almost completely to ammonia and carbon dioxide. The gas mixture of the composition indicated is withdrawn to a pressure reduction zone from 14.7 to 3.43 atm.
    The bottom product from the reaction column, containing, kg: water 31127; ammonia 419; carbon dioxide 6 is used to pre-heat the feed stream to the reaction column and at this stage the temperature drops from 193 to 146 C. As a result of expansion in the upper part of the desorption column 6, the pressure also drops to 3.43 atm and 136 ° C. In the desorption column, this solution is stripped using 5000 kg of steam at a temperature of 147 C. At this stage, 5562 kg of a gas mixture is formed, which is sent to the bottom of the pre-desorption column. The water withdrawn from the bottom of the desorption column 6 is used to preheat the process condensate to be treated, and during this treatment the temperature drops from 139 to 8 ° C, and then cooled with cooling water to 40 ° C, after which it is discharged to the drain. It contains 6 hours per million ammonia and 8 hours per million urea.
    Example 2. The process is carried out analogously to example 1.
    From the pre-desorption column 4, process condensate in the amount of 310009 kg, containing, kg: NHj 310; COj 31; Urea 319, which is compressed with a pump of 9 to 30 bar, is fed to the upper part of the reaction column 5. The temperature of the raw material supplied to the upper part of columns 1 is approximately 220 ° C and the temperature of the base of the columns. In this reaction column, 1553 kg of water vapor are fed under pressure.
    513
    34.3 atm with temperature (..,. Average residence time in the column is 6 minutes.
    Urea present in the process condensate is almost completely hydrolyzed, and at the same time decomposition products are largely distilled off from the solution. The vapor phase removed from the top of the reaction column is fed to the pre-desorption column 4. The liquid phase removed from the bottom of the reaction column (31703 kg), containing, in addition, 10 ppm of ureaNH
    J - is expanded at the top of the desorption column 6 to 5 bar and distilled from 5275 kg of steam having 5.88 atm and 158 C. The liquid removed from the bottom of the desorption column contains, in addition, 10 hours million urea, 10h. on shn
    , 1, AZ wt.% NH and about
    0.01 wt.% WITH,
    NHj and less than 10 hours per million CO. If desorption is carried out in column 6 under a pressure of 1 bar, then in the liquid to be removed there is the same content of NH, 10 ppm and less than 10 ppm CO, a quantity of 3510 kg is required at 5.88 atm
    Example 3. The process is carried out analogously to example 1.
    Obtained in the pre-desorption column 4 process condensate 310009 kg, containing, kg: NHj 310; COj 31; urea 319 compressed to
    10 bar and served in the upper part of the rack. Ion column 5. On the flow line
    11The water vapor is compressed to high pressure (34.3 atm) in the amount of 1707 kg with a temperature of 242 C.
    The average residence time of the treated liquid in the reaction column is 117 minutes. Urea, containing; uus, in the solution introduced into the reaction column, is almost completely hydrolyzed. The pressure of the liquid removed from the reaction column (31562 kg) containing, kg: NH 421.21; CO 7.42; and 10 parts per million of urea, reduced to 5 atm, with the result that the tempera
    This liquid is reduced to 155 C. This liquid is treated in a desorption column 6 using 5225 kg of low-pressure steam (5.88 atm) with a temperature of 158 C. The liquid removed from the bottom of this column contains 10 ppm of urea, less than 10 hours per million NHj and less than 10 hours per million CO ,. If desorbQ
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    The CRC is inspected under a pressure of 1 atm, then to achieve an MH content. meJ
    10 ppm in the removed liquid requires 3475 kg of steam under a pressure of 5.88 atm.
    Example 4. The process is carried out analogously to example 1.
    From the pre-desorption column 4, 31009 kg / h of condensate containing NH 310; WITH 31;
    urea 319, whose pressure is increased to 30 atm using a pump 9, is supplied to the upper part of the reaction column 5. The temperature of the stream supplied to the upper part of the column is about 220 ° C, and the temperature at the bottom of the column is 230 ° C. kg / h of steam at a pressure of 34.3 atm and at 242 C. The average residence time is 7.68 minutes.
    The liquid discharged from the bottom of the reaction column (31713 kg), which contains 2 parts per million of urea, 1.42% by weight of NH, and about O, 08% by weight
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    CO, is fed to the top of the desorption column 6 at a pressure drop of up to 5 atm and 60,600 kg of steam are desorbed under a pressure of 5.88 atm at 158 s. The liquid that is removed from the bottom of the desorption column contains, in addition to 2 hours. per million of urea 2 h per million of NH and 0.1 h, per million of CQ,
    If the desorption in the desorption column 6 is carried out at 1 atm, in order to achieve that low value of 2 ppm NHg in the withdrawn liquid, 4030 kg of steam will be needed under a pressure of 5.88 bar.
    Example 5. The process is carried out analogously to example 1.
    From column 4 pre-desorption 310009 condensate process containing, kg: NH 310; COj 31; Urea 319 is brought to a pressure of 10 atm and fed to the upper part of the reaction column 5. For 1 hour, line 11 serves 1723 kg of high pressure steam (34.3 atm) with a temperature of 242 ° C.
    The average residence time in the reaction column of the treated liquid is 147.24 minutes. The urea present in the feed solution is almost completely hydrolyzed. The pressure of the liquid withdrawn from the reaction column (31,604 kg) containing 422.25 kg NHj, 6.89 kg CO and 1.8 ppm of urea, is reduced to 5 bar
    71
    and treated in desorption column 6 with 6,000 kg of low-pressure steam at 5.88 atm with a temperature of 158 ° C. The liquid discharged from the bottom of this column contains 1.8 hours, per million of urea, 2.1 hours per million of NH and 0.1 hours per million of COg.
    If desorption is carried out at a pressure of 1 atm, 4000 kg / h of steam under a pressure of 5.88 bar is required to achieve a low value of 2 ppm of NH and urea in the withdrawn liquid.
    Example 6. The process is carried out analogously to example 1, but 1711 kg of high-pressure steam (24.5 atm) with temperature is supplied to the reaction column, and the residence time of the reaction mixture is increased from 1.14 to 1.37 hours. The residual product of the reaction column consists of 31658 kg of liquid containing 1.36% by weight of ammonia, 0.017% by weight of carbon dioxide and 2 parts per million of urea. This residual product is sent to the upper part of the desorption column, in which the pressure is 3.43 bar and the product is desorbed 5350 kg of low pressure steam with a temperature of 147 ° C. The aqueous liquid discharged from the lower part of the desorption column contains 2 ppm of ammonia, 0.1 ppm of carbon bicon and 2 ppm of urea.
    The amount of water vapor for carrying out the process with a total content of urea and ammonia 2 hours per million in examples 4-6 is given in table. one .
    To obtain the same effect (the total content of urea and ammonia is 2 ppm), according to a known method, 35000 kg of steam with a pressure of 12.7 atm must be used.
    Example 7. Technological condensate obtained at a urea plant with a capacity of 1500 tons / day, in the amount of 28333 kg, is treated according to the described method.
    Technological condensate containing, wt.%: 4,38; CO., 2.95; Urea 1.09, is treated in a heat exchanger 3 at 42-90 ° C. In pre-desorb-ion column 4, this solution is first contacted at 1 atm in countercurrent with a 1128 kg gas mixture from a reactive column 5, which contains 68 kg NHj, 258 kg COg and 802 kg of vapor
    787818
    water and has a temperature of 172 ° C and thereafter with 4857 kg of the gas mixture from the desorption column 6, the composition
     which is 422 kg NH, 7 kg CO and
    4428 kg of water vapor and a temperature of 97 C. Through the upper part of the column 4, a gas mixture is released in the amount of 6143 kg, containing 2725 kg of NH,
    10 1960 kg CO and 1458 kg of water vapor. This gas mixture is completely condensed and from the solution obtained in this way, which has a temperature of 1 C, part in the amount of 2810 kg, so15
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    costing 1247 kg of NHj, 896 kg of COj, and 667 kg are recirculated to the pre-desorption column. The remainder is returned to the urea plant or processed at the NH NOj plant.
    The desorbed solution, which in addition to 30386 kg of water contains 253 kg of NH, 37 kg of COg and 309 kg of urea, is brought to a pressure of 10 bar with a pump 9 and sent after heating from 97 to in a heat exchanger 10 to the upper part of the reaction column 5. Amount steam sent to the bottom of this reaction column is 1723 kg, its temperature is 242 C and pressure is 34., 3 atm. The urea present in the feed is almost completely hydrolyzed to NH and CO. The gas mixture having the specified composition is discharged from the reaction column, expanded in the expansion valve from 12-10 to 1 atm and passed into the pre-desorption column 4.
    The product from the bottom of the reaction column, consisting of 31604 kg of liquid, containing 31175 kg of water, 422 kg of NHj and 7 kg of CO, and having a temperature is used to preheat the make-up stream of the reaction column. Due to the expansion in the upper part of the desorption column 6, the pressure is again reduced to 1 atm, with the result that
    The temperature is reduced to 110 ° C. In this desorption column, which is equipped with 25 plates, this solution is desorbed with .4000 kg of steam with a temperature of 158 ° C (vapor pressure 5 5.88 atm). The temperature in the desorption column is from 96 (top) to 100 ° C (bottom). In this process, 4857 kg of the indicated
    gas mixture, which is directed to the bottom of the pre-desorption column. Water is taken from the bottom of the desorption column 6 at 100 ° C and is used to preheat the process streams. It contains 2 parts per million NHj and 2 parts per million urea.
    Example 8. The process is carried out analogously to example 7. In the heat exchanger 3, the temperature of the process condensate is increased from 42 to 142 C. In the pre-desorption column 4, the solution is first contacted under pressure of 5 atm in countercurrent with 848 kg of gas mixture from the reaction column 5, the composition of which is 36 kg MN , 262 kg SOD and 550 kg of water vapor and which
    flow of the reaction column. By expanding in the upper part of the desorption column 6, the pressure is reduced to 5 atm. As a result, the temperature drops to 155 C. In this desorption column, equipped with 32 plates, this solution is desorbed with 5275 kg of steam at 158 C
    (vapor pressure 5.88 atm). The temperature in the desorption column is from 148 (top) to 152 ° C (bottom). In this process, 5620 kg of the specified gas mixture is formed,
    which is directed to the bottom of the pre-desorption column. Water withdrawn from the bottom of the desorption column 6 and having a temperature of 152 ° C is used for preliminary
    has a temperature of 219 ° C, and after that it is -20 heating of the process condensate.
    with 5620 kg of gas mixture from the desorption column 6, which consists of 455 kg NH, 2 kg CO and 5163 kg of water vapor with a temperature of 149 C. Through the upper part of the column 4 they release 2467 kg 25 NHj, 1893 kg CO., and 2232 kg of water vapor . This gas mixture is completely condensed and from the solution obtained in this way, which has a temperature part of the amount, composition 30
    intended for processing. It contains less than 2 ppm NH3 and less than 2 ppm Urea.
    To carry out the process according to Examples 7 and 8, for example 7, 1723 kg of steam at a pressure of 34.3 atm and 4000 kg of steam at a pressure of 5.88 atm for example 8 are 1552 kg of steam at a pressure of 34.3 atm and 5275 kg of steam at pressure of 5.88 atm.
    2800 kg and consisting of 1048 kg, .804 kg of COg and 948 kg are returned to the urea plant or processed at the plant.
    The desorbed solution, which contains, in addition to 30349 kg of water, 310 kg NH, 31 kg C0.2, and 319 kg of urea, is brought to a pressure of 30 bar with a pump 9 and sent after heating 149 to the heat exchanger 10 in the upper part of the reaction column 5. Amount sent to the bottom
    part of this steam reaction column
    1,552 kg, its desorption pressure temperature, varies in
    9445 kg / h (18 atm) up to 18890 kg / h
    The proposed method allows energy costs for the process. T for the implementation of the process according to the iznomu method, the amount of steam, and used in the stages of hydrolysis
    the limits
    34.3 atm. The urea present in the feed is almost completely hydrolyzed to NH and CO. The gas mixture having the specified composition is discharged and expanded in the expansion valve 12 from 30 to 5 atm, and sent to a preci- ditional column 4.
    The product from the bottom of the reaction column, consisting of 31713 kg of liquid containing 31255 kg of water, 455 kg of NHj and 2 kg of CO and having a temperature of 230 ° C, is used to pre-heat the pre-heating feed
    50
    55
    (24 atm). This method allows to reduce the amount of steam in these two stages to 6,700 kg / h and to use for this purpose steam more than a pressure (4 atm).
    权利要求:
    Claims (1)
    [1]
    Formula invented
    The method of separating urea, ammonia and carbon dioxide from dilute aqueous solutions by hydrolysis of the reaction column of urea and sorption of ammonia and carbon dioxide
    desorption, changes in
    intended for processing. It contains less than 2 ppm NH3 and less than 2 ppm million urea.
    To carry out the process according to examples 7 and 8, for example 7, 1723 kg of steam at a pressure of 34.3 atm and 4000 kg of steam at a pressure of 5.88 atm; for example 8, 1552 kg of steam at a pressure of 34.3 atm and 5275 kg of steam at a pressure of 5.88 atm.
    Table 2 shows the values of the amount of water vapor of high (HP) and low (LP) pressures at different operating parameters of the hydrolyser and desorber and at different residual urea and ammonia contents (this is compared with the one-column variant by a known method) .
    The proposed method allows to reduce the energy consumption for the process. Thus, for carrying out the process according to a known method, the amount of steam used in the hydrolysis and
    the limits
    (24 atm). This method allows reducing the amount of steam in these two stages to 6,700 kg / h and using lower pressure steam (4 atm) for this purpose.
    Invention Formula
    A process for the separation of urea, ammonia and carbon dioxide from dilute aqueous solutions by hydrolysis and in the reaction column of urea and desorption of ammonia and carbon dioxide.
    II137878112
    different VeM that, with a temperature of 170-220 C, and in the lower
    in order to reduce energy consumption, the initial solution is sent to a pre-desorption column, in which at least 1–4 atm and at 1–149 ° C at least part of the dissolved ammonia and carbon dioxide together with water vapor is removed as gas mixture,
    which is condensed, and at least under a pressure of 1-5 atm and at
    as far as part of the condensate obtained, 96-152 seconds in the desorption column is recycled into the process, after chemiomyak and carbon dioxide are removed from
    the remaining solution is passed under this solution by countercurrent desorption with a pressure of 10-30 atm to the upper part with steam, this solution is directed
    of the reaction column and force the flow to the runoff, and gaseous impurities, get down in countercurrent with floor vapors in the reaction and desorption
    at a pressure of 15-42 atm, and in the top of the columns, they are sent to the pre-desorption part of this column and support an ion column.
    Table 1
    1553 BD34.3 bar
    5275 ND5,88 bar
    1553 VD34.3. Bar
    3510 НД5.88 bar
    1707 BD34.3 bar.
    5225 НД5.88 bar
    1707 BD43.3 bar
    3475 ND5,88 bar.
    parts - temperature 180-230 ° C, containing ammonia, carbon dioxide and water vapor, the gas mixture is removed from the upper part of the column, and from the lower part of the column, an aqueous solution of ammonia and carbon dioxide, which does not contain urea, is discharged
    34.3 bar
    5.88 bar
    34.3 bar
    5.88 bar
    34.3 bar
    5.88 bar
    34.3 bar
    5.88 bar
    desorb (1 to 9020 DB 34.3 bar
    desorb (1 cal 7700 34.3 bar
    7
    1 2/5
    Continued not tlbJT. 2
    9800 DB 34.3 bar
    8500 DB 34.3 bar
    / 2
    /
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    同族专利:
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    YU274181A|1983-02-28|
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    JPS57118011A|1982-07-22|
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    引用文献:
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    申请号 | 申请日 | 专利标题
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