• 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:
    Disclosed is a process for concentrating aqueous urea solutions in which an aqueous urea solution is allowed to flow as a falling film in countercurrent contact with a stream of hot inert gas to concentrate it to 95-99% by weight and the aqueous urea solution so concentrated is then passed through a packed zone in cocurrent contact with a stream of hot inert gas to concentrate it to not less than 99.5% by weight.
    公开号:SU1155155A3
    申请号:SU802981965
    申请日:1980-09-12
    公开日:1985-05-07
    发明作者:Саида Тойоясу；Симокава Такатацу；Янагисава Юзуру；Нагахама Такаси；Исида Кодзи
    申请人:Тойо Инджиниринг Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    ate j
    The invention of OTIIOCHTCH to a method for the concentration of aqueous solutions of urea. The aqueous solution of the urea, obtained by reacting ammonia and carbon dioxide at high temperature and pressure and carrying out the usual procedure on the resulting effluent of the synthesized urea, has a concentration of 7090% by weight. To obtain granulated urea for practical use, an aqueous solution of urea must be concentrated to at least 99.5 wt.%. To achieve such a concentration. Several processes have been proposed. The closest in technical essence to the present invention is a two-step method of concentrating aqueous solutions of urea. In the first stage of this process, an aqueous solution of urea, having a concentration of 65-95 wt.% In the form of a falling film, is passed along the inner J surface of the heated outside tubes and is in contact with countercurrent air flow with a temperature of 105-120 C in the amount of 300 km / h, resulting in its concentration reaches 97.5-99 wt.%. In the subsequent second stage, the urea water solution leaving after the first stage is passed through a zone filled in with a nozzle. In countercurrent contact with a stream of hot air at the parameters of the first stage of concentration (a stream of hot inert gas coming out of the zone filled with a nozzle, serves as a stream of hot air used in the first stage) 2. The disadvantage of this method is poor quality, blowing, due to the presence of large amounts of biuret (1%), therefore, when countercurrent contact with a stream of hot air in the second stage occurs, the solution is flushed and the solution is returned. flow. Thus, the concentration of the aqueous solution of urea deviates from the regime, the evaporation rate decreases, the quality of the product deteriorates. The effect of this reverse mixing becomes more noticeable at a concentration of about 99% or more, when the supply of water vapor above the aqueous solution of urea decreases sharply with increasing concentration. Such a decrease in the rate of evaporation usually lengthens the prem of being in the apparatus (or the area filled with the nozzle). Consequently, the conversion of urea into the biuret cannot be prevented and the size of the device (or the zone filled with the packing) must be increased proportionally to the increased residence time. The purpose of the invention is to improve the quality of the target product by reducing the formation of biuret. The goal is achieved by the method of concentrating aqueous solutions of urea by two-stage blowing with a stream of hot air, in the first stage by countercurrent contact with a falling film of an aqueous solution of urea with a concentration up to 95-99%, and in the second stage by passing a solution through the nozzle urea concentration up to 99.599, the second stage, the flow of hot air with a temperature of 150-195 0 in the amount of 7L0-MO nm / h per 1 ton of an aqueous solution of urea is passed through direct contact with the urea solution leaving the first stage. FIG. 1 shows a diagram of an apparatus for implementing the proposed method; in fig. 2 - the same for the implementation of the known method. The first stage of the process is carried out using a film evaporator. For this purpose, any film evaporator and known operating conditions can be used. In the first stage, the aqueous solution of urea is concentrated from 70-90 to 95-99 wt.%. The aqueous solution of urea, which is concentrated in the first stage, is then introduced into a concentrator, including a packed layer, through which the aqueous solution of urea is passed from top to bottom in direct contact with a stream of hot air and thereby concentrated to no less than 99.5 wt.% . The temperature of the stream of hot air introduced into the second stage is preferably in the range of 150-195 ° C, and the temperature of the aqueous solution of urea introduced at this stage is within 135-160 ° C. Most preferably, the concentration of the aqueous solution of urea introduced in the second stage, was in the range of 98-99 wt.%. The nozzle layer can be any of the known types of nozzle. The nozzle can be loaded either randomly or correctly, but a properly located tower nozzle is most preferable due to the higher rate of evaporation of water. An aqueous solution of urea (figure 1) with a concentration of 70-90 wt.% And a temperature of 90-120 With served from the cleaning system of urea through pipeline 1 to the upper part of the concentrated apparatus. The aqueous solution of urea introduced in this way is evenly distributed between the heat exchange tubes 2 via the inlet drain. Since the aqueous solution of urea passes as a falling film along the inner walls of the heat exchange tubes 2, it is heated with water vapor (having a pressure of 3.6-6.0 kgf / cm ) introduced through conduit 3 and discharged as condensate via conduit 4, and brought into countercurrent contact with the flow of the inert gas (for example, air) introduced through conduit 5, resulting in an aqueous solution of ureas concentrated to 95-99. The temperature of the urea water solution leaving the heat exchange tubes 2 is 135-160 ° C, preferably 135-150 ° C. The flow rate of the hot inert gas introduced through conduit 5 is preferably 300-900 nm / h at 1 ton / h When a solution of urea is supplied through conduit 1, the temperature is preferably 150-170 ° C. The flow of hot inert gas along with the formations of water "| | steam is released through pipeline 6 and clap pan. If necessary, a very small amount of urea contained in it can be removed from the stream of hot inert gas and the very small amount of ammonia contained in it can be removed before it is released into the atmosphere. 5. 4 A solid urea solution, which is concentrated in heat exchange tubes 2, exits from the underside of the latter, passes through a wire mesh (which is preferably chosen such that it holds a small amount of an aqueous solution of urea; the wire mesh can be eliminated) and falls on packing layer 7. In the packing layer, an aqueous solution of urea is brought into direct contact with a stream of hot inert gas introduced through the pipeline, thereby co-activating it to at least 99.5 wt.%. the hot inert gas introduced through the pipeline preferably has a dew point temperature of 5 ° C or less. In addition, its flow rate is preferably equal to 240-600 per 1 ton / h of an aqueous solution of urea entering through conduit 1, and the temperature is preferably in the range of 150-195 ° C. The resulting concentrate, which has a temperature of 135-145 ° C, is withdrawn through conduit 8 and sent to a granulation tower. The inert gas that has passed through the packed layer 7 is discharged through the pipeline 9 and the valve. Valves 10 and 11 serve to regulate the flow rate of the hot inert gas flowing through the heat exchange tubes 2 and the packed layer, respectively. According to the invention, the reverse mixing of the aqueous solution of urea in the second stage is minimized, so that the formation of biourate is significantly reduced. This result was obtained by replacing the countercurrent contact of the urea aqueous solution with a stream of hot inert gas in the second stage (as in the well-known method) with direct contact and by using a packing layer filled with a properly positioned tower packing. Example 1. A test for determining the concentration of an aqueous solution of urea is carried out in the device shown in FIG. 1. As a heat exchange pipe 2 of the device .12, for concentrating, use 140 tubes of circular cross section with an outer diameter of 51 mm, a wall thickness of 2 mm and a length of 7.5 m each. The casing layer 7 is filled with Raschig 1B rings, which are arranged in order to the height O, 3m Water solution of urea, which contains 83% by weight of urea and 0.52% w / v biuret, calculated on the weight of urea, through line 1 to the top of apparatus 12 and through drain 13 is fed to heat exchange tubes 2 with a flow rate of 6 tons / h The urea aqueous solution flows as a falling film along the inner wall of the heat exchange tubes 2 and is heated by water vapor, which is fed under a pressure of 3.5 kgf / cm along line 3 and withdrawn along line 4, and is brought into contact with the flow according to the counterflow principle hot air, which is injected at an inlet temperature of 150 ° C through line 5 at a flow rate of 3000 im / h, as a result of which the solution is concentrated to 99.0 wt%. The flow of hot air is discharged through line 6 through valve 10. Concentrated urea solution, discharged from the lower ends of heat exchange tubes 2, fall through wire mesh 14 onto packing layer 7. In head pack 7, urea aqueous solution is introduced into contact with the hot air flow, which is injected at an inlet temperature of 150 ° C through line 15 with a flow ratio of 400 per 1 ton of urea solution, as a result of which the concentration of the latter rises to 99.7% by weight. The hot air flow is diverted through line 8. The content of biuret in a concentrated urea solution is 0.68% by weight, calculated on the total. weight amount of urea. Example 2 The process is carried out analogously to example 1 except that the packed layer 7 is filled with Raschig rings 1B, which are continuously filled to a height of 0.6 m. A solution in which the urea content is 98.7 weight is obtained as a result. .% whichever ;. the solution also contains 0.70 8es,% biuret of the total weight of the total amount of urea. Example 3, Process wire is analogous to Example 1 with the exception of 5S in that the inlet temperature is 142 ° C and the flow rate of hot air introduced into the packed layer 7 is PSO per ton of urea solution. The result is a concentrated solution with a urea concentration of 99.6% by weight, where the biuret content is 0.66% by weight of the weight of urea. Example 4. The process is repeated as in Example 1, except that the inlet temperature and the flow rate of hot air introduced into the packed bed 7, 240 nm / h per 1 ton of urea solution. The resulting solution contains 99.5 wt.% Of urea and 0.74 wt.% Of biuret, calculated on the weight quantity of urea. Examples 5 and 6 (comparative). The tests were carried out in a concentration device shown in FIG. 2 (units and parts are indicated by the same reference numerals as in Fig. 1). The urea solution subjected to concentration, as well as the parameters of heat-exchange tubes 2 and Raschig rings used in examples 5 and 6, are similar to those described in examples 1 and 2, respectively. Hot air flow, which is fed through line 5 to the bottom of the evaporator with the flow rate; 4100 at an inlet temperature of 150 ° C, passed through a nozzle layer 7, and then through heat exchange tubes 2 to ensure countercurrent contact with an aqueous solution of urea, enter into heat exchange tubes 2. After this, it is discharged from the top of the evaporator via line 6 Heat exchange tubes 2 are heated with steam, which is fed under pressure. 3.5 kgf / cm through line 3 and discharged through line 4. The concentration of urea solutions, which are discharged from the bottom of the evaporator, is 99.7%. The biuret content of the solution, based on the weight of urea, is 0.80 weight ,% for comparative winner 5 and 0.83% for comparative example 6, Conditions and results of the tests are summarized in table. one,
    . . ZG a b l and c a t
    The height of the nozzle layer is 0.3 m. The outflow of aqueous pacTBOjpa is urinary and the inert of mono gas can be used. The exact flow condition.
    83
    83
    0.43
    0.43 6 6 Air flow rate: through the tag-shaped tubes, through the nozzle,. and 1 t of urea solution. Air flow temperature. C, at the entrance: to the heploexchange tubes 150 packed layer 150 Water vapor pressure, kgf / cm
    83
    83
    83
    0.43
    0.43
    0.43 6 6 6 Prstivo-ProtivRo my exact exact 000 3000 150 150 150 150 150 142 195 150. 150 Concentration of urea water solution discharged from heat exchange tubes,% 99, Concentrate discharged from the outlet of the evaporator: concentration, wt.% 99, biuret content, wt.% (By weight of urea) 0
    increase in the content of bio, 25 ureth, wt.%
    In tab. Figure 2 shows the relationship 35 between the flow rate of air passing through the packed layer and the increase in biuret content.
    Table 2
    Continued tabl, 1
    0.37 0.40
    0.31
    0.23
    0.27
    Continuation of table 2
    Thus, from the above results it can be seen that in the case of direct contact, in accordance with the invention, the urea solution; the concentration of which is over 971% by weight can be concentrated to a urea content of not less than 99.5% by weight with a reduced increase in biuret content due to passing air at a flow rate of more than 200 nm / h per ton of urea solution through a packed column. 9,098,998,7 9,599,799,7 0,740,800,83
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    权利要求:
    Claims (1)
    [1]
    METHOD FOR CONCENTRATION OF UREA AQUEOUS SOLUTIONS by two-stage flushing with a stream of hot air, in the first stage - by means of countercurrent contact with a falling film of an aqueous urea solution with a concentration of up to 95-99%, and in the second stage - by passing through a nozzle zone a urea solution with a concentration of up to 99.599.7%, characterized in that, in order to improve the quality of the product for the second stage, the flow of hot air with a temperature of ISO195 0 C in an amount of 240-600 nm e / h on. 1 t of an aqueous urea solution is passed through direct-contacting with a urea solution leaving the first stage.
    SU-1155155>
    1 11551
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    同族专利:
    公开号 | 公开日
    US4316767A|1982-02-23|
    IN151544B|1983-05-14|
    JPS5643256A|1981-04-21|
    GB2058764A|1981-04-15|
    BR8005864A|1981-03-24|
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    JPS5826909B2|1983-06-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2367695A|1940-10-03|1945-01-23|Research Corp|Concentration of hygroscopic solutions|
    US2933527A|1956-04-13|1960-04-19|Lonza Electric & Chem Works|Process for the manufacture of urea in granular form|
    US3147174A|1959-10-14|1964-09-01|Chemical Construction Corp|Low moisture urea melt|
    NL141179B|1967-01-20|1974-02-15|Whitlock Mfg Co|METHOD AND EQUIPMENT FOR THE PREPARATION OF UREA.|
    US3405689A|1967-05-29|1968-10-15|Stauffer Chemical Co|Apparatus for boiling liquids by falling film heating|
    US3822192A|1971-12-08|1974-07-02|Aluminum Co Of America|Evaporative method|NL8006477A|1980-11-28|1982-06-16|Unie Van Kunstmestfab Bv|METHOD FOR REMOVING UREA, AMMONIA AND CARBON DIOXIDE FROM DILUTED AQUEOUS SOLUTION.|
    IT1163795B|1983-07-18|1987-04-08|Montedison Spa|APPARATUS FOR THE STRIPPING OF AMMONIA FROM SOLUTIONS COMING FROM THE SYNTHESIS OF UREA|
    US4654124A|1985-09-27|1987-03-31|Aristech Chemical Corporation|Purifying cumene hydroperoxide|
    NL8602769A|1986-11-03|1988-06-01|Stamicarbon|METHOD FOR CONCENTRATING A UREA SOLUTION AND APPARATUS FOR CARRYING OUT THE METHOD|
    US5597454A|1995-04-06|1997-01-28|Lee; Jing M.|Process for producing urea|
    EP0891968B1|1997-06-26|2003-06-04|Urea Casale S.A.|Process for reducing the residual free ammonia emissions from an urea production plant|
    EP3452212B1|2016-05-03|2020-02-12|Stamicarbon B.V.|Urea production with controlled biuret|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    JP54117370A|JPS5826909B2|1979-09-14|1979-09-14|
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