• 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:
    In producing ammonium nitrate by neutralisation of nitric acid with ammonia in a reactor 1 under superatmospheric pressure, the hot ammonium nitrate solution is discharged through a conduit 7 and depressurised in a valve 8 to a pressure at which its boiling temperature is less than the temperature of the solution in the reactor. The solution is then passed through a heat exchanger/evaporator 9 where it is concentrated by evaporation by the heat transferred to it by a circulated ammonium nitrate solution which is discharged from the reactor 1 through a conduit 11 and passed through the heat exchanger 9 and returned to the reactor 1. The vapours and concentrated ammonium nitrate solution are then separated in a vapour separator 10. <IMAGE>
    公开号:SU1367853A3
    申请号:SU823416147
    申请日:1982-03-29
    公开日:1988-01-15
    发明作者:Хаген Курт；Хайнрих Лауе Карл；Бихтеманн Клаус
    申请人:Дидиер Энжинееринг Гмбх (Фирма)；
    IPC主号:
    专利说明:

    Ltd
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    The invention relates to the production of ammonium nitrate by neutralizing nitric acid with ammonia and can be used in the technology of mineral fertilizers.
    The aim of the invention is to increase the concentration of ammonium nitrate solution.
    The drawing shows the scheme for ammonium nitrate, which is connected through a water seal 16 with a capacity of 17 for storage. From the latter, an ammonium nitrate solution can be directed using a feed pump 18 for further
    implementation of the method.
    In the neutralization reactor 1, which is made in the form of a one-piece apparatus with an internal overflow device, nitric acid, acid, and ammonia are supplied through conduit 2. The upper space of the reactor is connected to a pressure control device 4, which consists of a pipe 5 and a cooler 6 connected to it. Through a pipe
    5 output steam generated in the upper part of the reactor 1, which is cooled in the refrigerator 6 with cold water so that the pressure of the desired value is maintained in the reactor 1. From the upper part of the reactor 1, the formed ammonium nitrate solution is removed through pipe 7 to the evaporator 9 through the reduction valve 8 and further in the separator 10 pair. The evaporator 9 is connected by a feed pipe 1 1 and a discharge pipe 12 of the circuit through a supercharger pump 13 with a neutralization reactor. Feed line 11 starts in reactor 1 at the bottom of its upper part. The discharge pipe 12 is connected to the reactor 1 from below. The solution of ammonium nitrate circulates around the contour 11, 12, 13.
    The pressure in the reactor 1 with the aid of the pressure control device 4 is set such that the boiling point of the ammonium nitrate solution in the reactor 1 is 180-185 ° C. The pressure here is 5 6 abs. Bar. The ammonium nitrate solution formed by neutralization with a concentration of 70% by weight through the pipeline
    7 moves under its own pressure. In the reduction valve 8, the pressure of the ammonium nitrate solution is reduced to evaporation pressure, at which the temperature of the ammonium nitrate solution is approximately 105 ° C. After that, the evaporator 9 evaporates the ammonium nitrate solution using the heat of another stream, ic at 180 ° C circulating
    13678532
    from the neutralization stage. In the vapor separator 10, the phases are separated into an ammonium nitrate solution with a concentration of 98% by weight, which is withdrawn through conduit 14, and the secondary vapor is withdrawn through conduit 15. The conduit 14, through which the highly concentrated solution moves
    Ammonium nitrate is bound through a water seal 16 with a storage capacity of 17. From the latter, an ammonium nitrate solution can be directed using a feed pump 18 for further
    processing, e.g., into a pelletizer.
    Secondary vapors passing through conduit 15 are fed to condenser 19. Condensate through a water seal
    20 enters collector 21, from where it is removed by pump 22. Condensate as process water is suitable for the production of nitric acid. For supplying secondary steam
    A vacuum pump 23 is provided through the pipeline 15 to the condenser 19.
    The evaporator 9 can be used single or multiple. If it is performed by a multistage, it is required
    lower heat consumption. Excess heat can be used in a heat exchanger 24 connected to the discharge pipe 12 to produce heating steam.
    With preheating of nitric acid and / or ammonia, prior to entering reactor 1, heat exchangers 25, 26 are connected to corresponding pipelines 2, 3. These heat exchangers can be supplied with secondary steam passing through pipeline 15 with a temperature of 17 ° C. - EU in passing through pipelines
    secondary pairs, single or multistage washing 27 is connected to the pipeline 15.
    Example 1. Entering into the reactor 1, t / h: nitric acid (65 wt.% At
    30 C) 50.48; ammonia gas (at 10 ° C) 8.88.
    The output of the reactor 1: a solution of ammonium nitrate (70.2 wt.% At and 5 abs.bar) 59., 36 t / h; 32.24
    10 MJ / h for heating in the evaporator 9.
    Enter into the evaporator 9: a solution of ammonium nitrate (70.2 wt.% At) 59.36 t / h; 32.24-103 MJ / h.
    Exit from the separator, t / h: ammonium nitrate solution (98 wt.% At) 42.52; secondary steam (0.3ab bar at 170 ° C) 16.84.
    The output from condenser 19 of condensate at 65 C is 16.84 t / h.
    The waste heat from the secondary steam from the conduit 15 can also be used to preheat air, which is supplied upon receipt of the product in granular form.
    Example 2. Entering into the reactor 1, t / h: nitric acid (60 wt.% At 40 C) 54,69; anhydrous ammonia (at 20 s) 8.87.
    The output of the reactor 1: a solution of ammonium nitrate (65.6 wt.% With and 6.1 abs.bar) 63,56 t / h
    Enter into the evaporator 9: ammonium nitrate solution (74.8 wt.% At 70 C and 0.2 abs. Bar) 41.80 t / h.
    The output from the separator solution of ammonium nitrate (99.7 wt,%, 175 C, 0.07 abs.bar).
    The output from condenser 19 of condensate at 60 C is 21.76 t / h.
    The proposed method allows to more deeply use the heat of the neutralization reaction without using steam from the side and to obtain solutions.
    ammonium nitrate concentration of 98.0- 99.7 wt.%. The known method allows to obtain a solution of ammonia nitrate.
    concentration of not more than 80-83%.
    权利要求:
    Claims (2)
    [1]
    1. A method of producing ammonium nitrate, which includes neutralizing nitric acid with ammonia under heating and pressure above the saturated vapor pressure, evaporating the resulting ammonium nitrate solution using
    neutralization heat, characterized in that, in order to increase the concentration of ammonium nitrate solution, neutralization is carried out at 180-185 ° C, in the resulting solution
    ammonium nitrate before evaporation, the pressure is reduced to evaporation pressure and evaporation is carried out using the heat of the solution circulating from the neutralization stage, and
    the amount of circulating solution is selected from the conditions of maintaining the predetermined temperature and pressure conditions of the neutralization stage.
    [2]
    2. The method of pop, 1, is different, and so that the neutralization is carried out at a pressure of 5-6 abs. Bar.
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    同族专利:
    公开号 | 公开日
    DE3113783A1|1982-10-14|
    FR2503126A1|1982-10-08|
    GB2096124B|1984-06-20|
    GB2096124A|1982-10-13|
    FR2503126B1|1984-04-27|
    BE892740A|1982-08-02|
    DE3113783C2|1987-01-02|
    NL8201440A|1982-11-01|
    DD202858A5|1983-10-05|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2580919C2|2011-05-16|2016-04-10|Дзе Юниверсити Оф Сидней|Complex method for obtaining ammonium nitrate|BE379205A|1930-06-02|
    BE435028A|1938-06-27|
    BE507178A|1950-11-27|
    FR1168683A|1957-02-26|1958-12-12|Improvements in the manufacture of granulated ammonium nitrate|
    BE620837A|1962-02-08|
    DE1179543B|1962-10-04|1964-10-15|Uhde Gmbh Friedrich|Process for the production of ammonium nitrate by neutralizing aqueous nitric acid with gaseous ammonia|
    US3690820A|1969-06-13|1972-09-12|Chemical Construction Corp|Production of ammonium nitrate|LU84636A1|1983-02-08|1984-11-08|Pouilliart Roger Victor|PROCESS AND APPARATUS FOR THE PRODUCTION OF AMMONIUM NITRATE|
    ES2004070A6|1987-01-21|1988-12-01|Union Explosivos Rio Tinto|Process and installation for the production of ammonium nitrate.|
    US8152988B2|2007-08-31|2012-04-10|Energy & Enviromental Research Center Foundation|Electrochemical process for the preparation of nitrogen fertilizers|
    US9005422B2|2007-08-31|2015-04-14|Energy & Environmental Research Center Foundation|Electrochemical process for the preparation of nitrogen fertilizers|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19813113783|DE3113783C2|1981-04-04|1981-04-04|Process and device for the production of ammonium nitrate|
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