• 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:
    1. Process for the preparation of an isocyanic acid/ammonia gas mixture having a low cyanuric acid content by heating molten urea, which is blown into a fluidized bed consisting of an inert material, to temperatures of 300 to 480 degrees C in the course of less than 1 second, characterized in that the molten urea is sprayed, into the fluidized bed, 35 to 200 mm above the inlet point of the fluidizing gas, at an outlet velocity of 3 to 15 m/second, parallel to the direction of flow of the fluidizing gas and at a minimum distance of 300 mm from wall surfaces and/or surfaces serving for heat exchange.
    公开号:SU1344242A3
    申请号:SU843741552
    申请日:1984-05-04
    公开日:1987-10-07
    发明作者:Вайс Петер；Сикора Рудольф；Загедер Эрвин
    申请人:Хеми Линц, Аг (Фирма)；
    IPC主号:
    专利说明:

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    This invention relates to the preparation of 1 azov mixture of isocyanic acid and ammonia by heating molten urea in a fluidized bed of inert material.
    The purpose of the invention is to simplify the process and reduce the feed rate of the reagents while maintaining the high quality of the product.
    FIG. 1 shows a fluidized bed reactor for the implementation of the proposed method using a nozzle for one substance. FIG. 2 the same, the cross section along the plane passing above the bottom.
    The pseudo-fluidized cylindrical reactor 1: the enamel layer is provided with a gas-permeable bottom 2, on which is a fluidized bed of inert granular material 3, Hole A for introducing fluidized E1; its gas 5 is made in bottom 2 near the nozzle. 6, located in the center of the bottom, have a larger cross section than the holes in the areas farther from the nozzle. In any case, the minimum distance of 300 mm from the heated wall must be observed.


    Nok 7 of the reactor. For supplying the melt to the nozzle serves pipeline 8.
    If there are several entry points for liquid urea, which is typical primarily for large reactors, which in this case have heat exchangers inside the reaction chamber, then it is recommended to install the nozzles 6 on the bottom 2 in a certain order. So, for example, three nozzles can be arranged so that they form the vertices of an equilateral triangle (Fig. 2). If four nozzles are provided, then depending on the size of the reactor, it is possible both the location of the fourth nozzle in the center of an equilateral triangle and the placement of nozzles in the form of a square. In a similar way, the arrangement of five or more nozzles can be carried out, and, of course, it is also necessary to observe the minimum distance to the heated walls 7 of the reactor or to the heat exchangers present in it.
    In principle, any nozzle design is suitable that provides melt flow at a selectable rate. It may be, for example,
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    Neno in the form of a solid flat or round nozzle.
    Molten urea is introduced by means of a nozzle mounted on the bottom plate of a fluidized bed reactor in which openings are made for introducing a fluidizing gas.
    At the same time, observance of the minimum distance to the surface of the walls or heat exchanging surfaces is one of the prerequisites for the successful implementation of the proposed method. 5 If urea is blown in only one place of the reactor into the fluidized bed, it is most advisable to disperse the insertion point in the center of the bottom surface of the reactor. If there are several injection points, they should be evenly distributed over the bottom surfaces of the reactor, taking into account the required minimum distance to heated surfaces. The maximum distance between the point of entry of molten urea and the heated surface of the reactor corresponds to the radius of the reactor.
    Although a conventional double nozzle (if one exists) can still be used to deposit urea, it is not necessary to pass an injected gas higher than that of the gas that serves as a carrier gas of the fluidized bed, to prevent unwanted formation of cyanuric acid. speed through the outer annular gap of the nozzle. In the proposed method, it is possible to pass a gas nozzle through the annular gap at the same rate as the fluidizing gas, which then performs the same function as the fluidizing gas. Due to this, there is no need for separate devices for generating a higher pressure for the injected gas, which greatly simplifies the process.
    It is preferable to generally refuse the introduction of urea through a double nozzle and the use of a blown gas and introduce the molten urea into the fluidized bed through a simple single nozzle.
    It turned out to be expedient to introduce into the reactor directly around the urea exit site a greater amount of fluidizing gas than in the rest of the bottom plate of pe0
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    actor, which is achieved by increasing the hole area per unit area in comparison with the rest of the bottom of the reactor. This can be achieved either through large cross-sections of fluidizing gas inlet holes around the nozzle, or through a larger number of fluidizing gas injection holes per unit area. Holes for gas injection near the nozzle can also be designed in such a way that fluidizing gas flows in the direction of the nozzle in larger quantities than in the direction opposite the nozzle.
    Example 1. In an externally heated fluidized bed reactor with a diameter of 1200 mm and a height of 2000 mm, which is filled with sand with a grain diameter of 0.1 - 1 mm, the fluidized bed is maintained by blowing in .50 cfm. NHj meters per hour through the holes in the circular bottom. The reactor is heated from the outside. Ammonia is introduced into it as a fluidizing gas at a temperature that ensures the temperature of the sand at a temperature of 360 ° C. Through a single nozzle installed in the center of the circular bottom with an internal diameter of 1 mm and a distance of 600 mm. the end of which is located at a distance of 45 mm from the bottom surface, 25 kg enters the fluidized bed. urea per hour, which corresponds to a feed rate of 7.25 wines for less than 1 s, is quantitatively converted into a mixture of isocyanic acid and ammonia, which is continuously removed from the reactor. The gas withdrawn from the reactor contains 1.96% by volume of isocyanic acid. No crust formation due to the formation of cyanuric acid is observed.
    PRI me R 2 A heated fluidized bed reactor of the same size as indicated in example 1 is equipped with an injection nozzle installed in the center of a circular bottom. The inner and outer tubes of this nozzle end at the same height. The inner tube of the nozzle, 600 mm from the wall surfaces and the end of which is at a distance of 45 mm from 5
    44242
    the bottom surface has a conditional passage of 1 mm. The fluidized bed is filled with sand with a grain diameter of 0.1-1 mm, which is maintained in a fluidized state by the employee as a fluidizing agent. ammonia gas introduced through the bottom of the reactor at a speed of 70 m / s. Through the annular .JQ gap nozzle ammonia enters at the same speed as the injected gas. The temperature of the sand is equal.
    Through the nozzle into the fluidized bed enters 25 kg of molten urine - 5 hours, which corresponds to a feed rate of 7.25 m / s.
    Urea is quantitatively converted to less than 1 s in a mixture of isocyanic acid and ammonia. The withdrawn 2Q gas from the reactor contains 1.96% by volume of isocyanic acid. No deposits are found due to the formation of cyanuric acid.
    Example In a pseudo-25 fluidized bed reactor as in example 1, through a nozzle 600 mm from the wall surfaces and the upper end of which is at a distance of 200 mm from the bottom surface, 10.3 kg of liquid was introduced into the fluidized bed. urea per hour, which corresponds to a feed rate of 3 m / s. Urea for less than 1 s is quantitatively converted into a mixture of isocyanic acid, with ammonia, which is continuously removed from the upper part of the reactor. pa. The gas withdrawn from the reactor contains 0.82% vol. isocyanic acid. No crust formation due to precipitation of cyanuric acid is observed.
    Example 4: A fluidized bed reactor is introduced into a fluidized bed through a nozzle that is 5,600 mm from the wall surfaces and whose upper end is 150 mm above the bottom surface, 13.1 kg of molten urea per hour. that corresponds to a feed speed of 3.5 m / s. Urea is quantitatively converted in less than 1 s to a mixture consisting of isocyanic acid and ammonia, which is continuously removed from the reactor through its top 5. The gas withdrawn from the reactor contains 1.05% by volume of isocyanic acid. There is no crust formation due to cyanuric acid deposition.
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     . 13442426
    5. Into the reactor with pseudo-crust formations due to
    no precipitation of cyanuric acid is observed.
    PRI me R 8. In a fluidized bed reactor, analogously to the example.
    Example
    liquefied layer in a fluidized bed is introduced analogously to example 1 through a nozzle with an internal diameter of 0.78 mm, 600 mm from the surface
    The upper walls of which are at a distance of 80 mm from the bottom surface, 25 kg of molten urea per hour, which corresponds to a feed rate of 12 m / s. The urea in less than 1 s is quantitatively converted into a mixture of isocyanic acid and ammonia, which is continuously output t from the top of the reactor. The gas withdrawn from the reactor contains 1.96% by volume of isocyanic acid. There is no crust formation due to the formation of cyanuric acid.
    Example In a fluidized bed reactor as in example 1, through a nozzle with an internal diameter of 0.70 mm, which is 600 mm from the wall surfaces and the upper end of which is at a distance of 35 mm from the bottom surface, 25 kg of molten urea are introduced into the fluidized bed. per hour, which corresponds to a feed rate of 15 m / s. Urea for less than 1 s is quantitatively converted into a mixture of isocyanic acid. ammonia lots that are continuously withdrawn from the top of the reactor. The gas withdrawn from the reactor contains 1.96% by volume of isocyanic acid. No crusting due to precipitation of cyanuric acid is observed,
    The method is 7.-In a fluidized bed reactor having a diameter of 600 mMe as in Example 1 with 110 norm-cubic meters. meters NH per hour, a fluidized bed 1500 mm high is maintained. Through a nozzle with an internal diameter of 0.70 mm, which is 300 mm from the surfaces of the wall and whose upper end is located at a distance of 150 Mt i from the bottom surface, the fluidized layer is introduced into the fluidized bed t 6 kg of molten urea per hour, which corresponds to a feed rate of 3.5 m / s. Urea is quantitatively converted in less than 1 second to a mixture of isocyanic acid and ammonia, which is continuously removed from the top of the reactor. The gas withdrawn from the reactor contains 1.60% by volume of isocyanic acid.
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    1 through a nozzle with an inner diameter of 1 mm, the upper end of which is 200 mm from the bottom surface, 10.3 kg of molten urea per hour is injected into a fluidized bed heated to 320 ° C, which corresponds to a feed rate of 3 m / s. Urea, after less than 1 s, is quantitatively converted into a mixture of isocyanic acid with ammonia, which is continuously removed from the upper part of the reactor. The gas withdrawn from the reactor contains vol.% Of isocyanic acid. No crust formation due to wasps; 1 wait of cyanuric acid is not observed.
    EXAMPLE 9 A fluidized bed reactor is similarly applied to 5 RU 1 through a nozzle with an inner diameter of 1 mm, which is 600 mm from the wall surfaces and the upper end of which is 200 mm from the surface. bottoms, heated, to pseudo. The liquefied layer injected 10.3 kg of molten urea per hour, which corresponds to a feed rate of 3 m / s. The urea for less than 1 s is quantitatively converted into a mixture of isocyanic acid and ammonia, which is continuously removed from the top of the reactor. The gas withdrawn from the reactor contains 0.82% by volume of isocyanic acid. No crust formation due to precipitation of cyanuric acid is observed.
    Example 10 (comparative). In a fluidized bed of the reactor, similarly to example 1, 10.3 kg of molten urea per Q hour was introduced through a nozzle with an internal diameter of 1 mm, the upper end of which was located 10 mm from the bottom surface, filing 3 m / s. During the reaction, the formation of a crust due to imbalance or cyanuric acid was detected, and therefore the reaction was suspended.
    Example 11 (comparative). In a fluidized bed of the reactor as in example 1, through a nozzle with an inner diameter of 1 mm, the upper end of which is at a distance of
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    300 MM from the bottom surface; a, 10.3 kg of molten urea per hour is injected, which corresponds to a feed rate of 3 m / s. The reaction is incomplete, since not all of the urea decomposes. Urea was found along with isocyanic acid in the gas obtained as a result of the decomposition reaction.
    Example 12 (comparative). In a fluidized bed of the reactor, as in Example 1, 8 kg of molten urea per hour was introduced through a nozzle with an inner diameter of 1 mm, the upper end of which was at a distance of 35 mm from the bottom surface, which corresponds to a feed rate of 2.3 m / s. During the reaction, cyanuric acid is precipitated, which necessitates termination of the reaction due to the formation of a crust.
    Example 13 (comparative). In a fluidized bed of the reactor, as in Example 1, a 27 kg of molten urea per hour was introduced through a nozzle with an internal diameter of 0.7 mm, the upper end of which is 200 MJI from the bottom surface, which corresponds to the feed rate 15.9 m / s. The decomposition of urea is incomplete; urea is found along with isocyanic acid in the gas obtained as a result of the decomposition reaction.
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    The results of the embodiments of the proposed method are tabulated and reveal the dependence of the impurity content in the final product.
    on process conditions.
     (
    The proposed method is simplified in comparison with the known method, and allows reducing the feed rate of the reactants while maintaining a high product yield.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of obtaining a gas mixture of isocyanic acid and ammonia, including thermal decomposition of dissolved urea in a fluidized bed of inert material at 320-480 ° C for a time not longer than 1 second with a parallel supply of fluidizing gas — ammonia — and molten urea from the bottom a cylindrical reactor, characterized in that, in order to simplify the process., and to reduce the feed rate of the reactants while maintaining the high quality of the product, molten urea is introduced into the fluidized bed at 35–200 mm at the pseudo slurry and gas are not spaced 300 mm from the surface of the reactor walls during its feed rate of 3-15 m / s.
    7
    FIG. /
    a & .2
    Compiled by E.Naumova
    Editor N. Lazarenko Tehred I.Popovich Proofreader A.T. sko- “
    Order 4839/58 Circulation 455 Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
     ™. "". ".-" .. ".". ".".-.-.- -. ". - -. “-. ,
    Production and printing company, Uzhgorod, st. Project, 4
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    同族专利:
    公开号 | 公开日
    PL143671B1|1988-03-31|
    DE3316494A1|1984-11-08|
    JPS6230129B2|1987-06-30|
    JPS59217620A|1984-12-07|
    PL247532A1|1985-02-13|
    EP0124704A3|1987-06-03|
    EP0124704A2|1984-11-14|
    DE3481507D1|1990-04-12|
    DE3316494C2|1991-04-18|
    EP0124704B1|1990-03-07|
    AT50752T|1990-03-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE4233533A1|1992-08-13|1994-04-14|Chemie Linz Deutschland|Process for the preparation of isocyanic acid by decomposing N, N-disubstituted ureas|
    RU2600356C2|2011-07-01|2016-10-20|Альцхем Аг|Method of producing ammonia from its precursor for reducing nitrogen oxides in exhaust gases|AT256117B|1963-04-04|1967-08-10|Chemie Linz Ag|Process for the catalytic production of melamine from gaseous cyanic acid|
    AT258881B|1964-01-14|1967-12-11|Chemie Linz Ag|Process for the production of a low-cyanuric acid-ammonia gas mixture from urea|
    AT257621B|1964-08-19|1967-10-10|American Cyanamid Co|Process for the production of melamine from urea|
    DE1275150B|1966-06-28|1968-08-14|Standard Elektrik Lorenz Ag|Procedure for route search, busy identification and signaling in multi-level switching networks|
    DE1717162C3|1968-03-05|1973-10-18|Lentia Gmbh, Chem. U. Pharm. Erzeugnisse - Industriebedarf, 8000 Muenchen|Process for the preparation of a cyanic acid-ammonia mixture from molten urea|
    JPS542640A|1977-06-08|1979-01-10|Hitachi Ltd|Allocating circuit for microprogram address|
    US4404755A|1981-08-25|1983-09-20|Foster Wheeler Energy Corporation|Fluidized bed heat exchanger utilizing induced diffusion and circulation|AT115555T|1989-07-28|1994-12-15|Chemie Linz Gmbh|METHOD FOR THE PRODUCTION OF UNSYMMETRICALLY SUBSTITUTED UREAS.|
    US5223635A|1989-07-28|1993-06-29|Chemie Linz Gesellschaft M.B.H.|Preparation of organic compounds using as a reactant an adduct of isocyanic acid and a tertiary amine or an ether|
    AT115556T|1989-07-28|1994-12-15|Chemie Linz Gmbh|METHOD FOR PRODUCING UNSYMMETRICALLY SUBSTITUTED UREAS, CARBAMATES, THIOCARBAMATES AND SUBSTITUTED ISOCYANATES.|
    US5248755A|1989-07-28|1993-09-28|Chemie Linz Gesellschaft M.B.H.|Process for the preparation of asymmetrically substituted ureas, carbamates or thiocarbamates|
    EP0416236B1|1989-07-28|1995-11-08|Chemie Linz GmbH|Process for the isolation isocyanic acid from a gaseous mixture of isocyanic acid and ammonia|
    DE3928595A1|1989-08-29|1991-03-07|Chemie Linz Deutschland|Asymmetrically substd. urea prodn. - by passing prim. or sec. amine into hot gaseous mixt. of isocyanic acid and ammonia and cooling reaction mixt. to condense prod.|
    DE3928566A1|1989-08-29|1991-03-07|Chemie Linz Deutschland|Unsymmetrically-substd. urea prepn. - by reaction of prim. or sec. amine with substd. ammonium isocyanate in inert diluent|
    EP0582022A1|1992-08-03|1994-02-09|Paul Scherrer Institut|Process for production of gaseous ammonia from urea|
    AT403475B|1994-07-22|1998-02-25|Chemie Linz Gmbh|METHOD FOR PRODUCING CYANURIC ACID|
    DE4431811A1|1994-09-07|1996-03-14|Chemie Linz Deutschland|High purity cyanuric acid prodn.|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3316494A|DE3316494C2|1983-05-05|1983-05-05|
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