• 专利附录
  • 专利说明
  • 权利要求
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  • 优先权
    • 专利摘要:
    The invention relates to the production of urea used as a fertilizer in agriculture. The process is conducted from NHj and COj at a ratio of (4.5–5): 1, at an operating pressure of 145–200 atm and a temperature of 184–190 ° C in the presence of a carbonate solution at molar ratio and CO 0, 5 in the same reactor. The resulting urea-containing solution with an excess of NH is treated under adiabatic conditions of 3.8-10.6% fresh COj (of its total amount) for 3-8 with return from the fiery NHj to the synthesis zone. The solution is then sent to the carbonate decomposition zone for contacting with the remaining portion of fresh CO. It is advisable to treat the urea-containing solution from the synthesis zone with a portion of the stream of fresh COj in a Venturi type mixer, in which the 002 stream is passed in a stream with a urea solution. These conditions reduce the high-pressure steam consumption from 474 to 150–190 kg. 1 hp f-ly, 4 ill. I O)
    公开号:SU1417794A3
    申请号:SU853898059
    申请日:1985-05-17
    公开日:1988-08-15
    发明作者:Царди Умберто
    申请人:Аммониа Казале С.А. (Фирма)；
    IPC主号:
    专利说明:

    vj

    with
    four
     CH
    The invention relates to the synthesis of ociina, in particular to the method of urea preparation, which is used in the production of nitrogen fertilizers, j
    The aim of the invention is to reduce the flow of high pressure steam.
    Figures 1 to 4 show embodiments of the method.
    The urea solution obtained in the tO reactor R with a high degree of conversion and containing ammonia, the amount of which exceeds the stoichiometric, is treated in the adiabatic stage S, where the main g: part of the excess ammonia is removed by close contact of the urea solution with a small amount fresh carbon dioxide supplied to stage S via line 1 (see figure 1). 20 Pipeline 2 supplies the urea solution from the reactor R of a conventional design to stage S, and direct recycling of the separated excess ammonia from stage S is carried out via line 25 to the reactor. Then, a urea solution with a minimum amount of excess ammonia from stage S is fed via conduit 4 to the ST section of the distillation of light fractions of known construction, where the carbamate is removed with maximum efficiency in a film-type exchanger in countercurrent with fresh carbon dioxide used as a stripping agent and enter 35 through pipeline 5.
    The vapors (mainly NHg and CO as a result of carbamate decomposition) from the steam section ST are fed through conduit 6 to the condenser for carbonate CC, from which extruded heat is removed by conduit .7 to form the steam used in the conventional processing steps. urea solution .45
    The carbamate solution condenser SS also receives the carbamate solution through line 8 and the inert gases that are removed from the reactor R through line 9. These inert CQ gases, after removing the remaining NHj and CO in the carbamate condenser SS, are removed from the system. Ammonia from line 10 is partially fed through line 11 to the reactor after pre- heating in heater P to establish heat equilibrium in the reactor and partly to condenser for carbamate CC (line 12). Pipeline 13 is supplied with fresh carbon dioxide, the main part of which is sent to the steam section ST via line 5, and the smaller part is fed to stage S via line 1.
    The urea solution after treatment in the steam section (ST) with the optimum residual carbamate content is passed through conduit 14 at the normal processing stage to obtain the desired final urea product.
    The carbamate solution from the carbamate condenser CC is recycled to the reactor by gravity and pipeline 15.
    A short contact (a few seconds) of the urine solution with excess ammonia and fresh carbon dioxide injected at stage S of the adiabatic ammonia separation is critical.
    Referring to Fig. 1, a layer of a corresponding mass transfer promoter L is located in a separate tank E, the upper part of which T acts as a separator for collecting ammonia. D - liquid distributor.
    Referring to Fig. 2, the ammonia removal stage S is carried out in the lower part of the reactor R, where the layer L of the corresponding mass transfer promoter is located in the empty space ES of the bottom of the reactor, according to fig.The removal stage a; miaka is also carried out in the lower part of the reactor R, but in the ES space of reduced diameter where the layer L of the corresponding mass transfer promoter is located.
    Figure 4 shows a preferred embodiment of the method. In stage S of the adiabatic ammonia separation, close contact between the urea solution with excess ammonia (stream 2) and the injected fresh carbon dioxide (stream 1) is achieved in a very short period of time with very high mass transfer in a VM Venturi mixer. Then, in the ES separator, ammonia vapors are separated from the urea solution .. ...,
    The examples below describe isobar systems in which the distillation sections have a lower
    pressure than at the ammonia separation stage.
    Example 1. Operating conditions of the reactor R: molar ratio, molar ratio 0.4, temperature 188 ° C, pressure 180 bar, degree of conversion (00-2 to urea) 74%.
    Composition of flows, kg (%) / Flow 13 of fresh CO 48.833 / 100 ° C Flow 1 of fresh C02 per tadium S of ammonia separation 4.375 / 100 ° C
    (9.5)
    Stream 5 of fresh CO in the apparatus with the distillation of light dressings; - ST
    Stream 10 fresh NHj
    Stream 2 urea solution from the reactor:
    NH,. 72.250 (40.19) COj16.125 (8.97)
    Urea 62,500 (34,77) HjO28,875 (16,07)
    Temperature 188 ° C. Flow 4 of urea solution from stage S in section for individual light fractions ST; .
    41.458 / 100 ° С 35, 417/25 С
    29,750 (21,17) 20,000 (14,24), 62,500 (44,48) 28,250 (20,11)
    Temperature 191 ° C oh roar re
    42.500 (97.42) 0.500 (1.14) 0.625 (1.44) Temperature 190 ° С



    16,000 (12.98) 17.250 (14.00) 62.500 (51.71) 27.500 (22.31) Temperature 175 ° C
    13,750 (23,43)
    44.208 (75.30)
    0.750 (1.27) Temperature
    Stream 8. Carbamate solution from lower sections:. NHj COj
    16,000 (38,10)
    17,250 (41,07)
    8,750 (20,83)
    Steam consumption 190 kg at a pressure of 22 bar for 1000 kg of urea. ; In the lower sections to remove and
    The 5 I recycle of residual CO contained in the urea solution that leaves the CO 2 desorber (section for distilling off the light fractions), up to the final vacuum concentration of the urea solution, to obtain the finished product, steam can be used under pressure of 6-7 bar. in the condenser for carbamate CC. When applying the method of direct recovery5 of heat (a system with multiple
    effect) additional steam will not form within the battery of the installation. The contact time of fresh carbon dioxide with a solution of
    0 | 3a 4 s.
    PRI mme R 2. Operating conditions for the reactor are E molar ratio IjHj / COi 4.5, molar ratio H O / CO2, 0.4, temperature 188 ° С, pressure 5 bar, 180 conversion rate (with / 1 to urea) 74%.
    Composition of flows, kg (%): Flow 13 of fresh carbon dioxide 45.833 / 100 ° С 0 Flow 1 of fresh carbon dioxide per stage S of ammonia separation1.744 / 100 С
    (3.8)
    5 Flow (5) of fresh carbon dioxide into section ST44.084 / 100 С Flow 10 of fresh NHj 35.417 / 25 С Flow (2) of solution 0 of urea from reactor K
    72.250 (40.19) 16.125 (8.97)
    Urea62,500 (34.77)
    H-zO28,875 (16,07)
    5Temperature 188 ° С
    Flow 4 of urea solution from stage S to section ST
    NHj-CO 2
    Nhg.
    CO,
    Urea HiO
    Stream 3. Direct my ammonia recycle to reactor R:
    NHj: COj
    but
    Flow 14 of urea solution from section ST:
    ЫНз
    COj
    Urea
    H-iO
    Flow 6 of CNS + CO.jH3 vapor ST section:
    NHj
    CQj HO Oh
    53.519 (32.96) 17.669 (10.88) 62.500 (38.49) 28.687 (17.67) Temperature 191 ° С
    18.731 (97.97) 0.200 (1.05) 0.188 (0.98) Temperature 190 С
    16,000 (12.98) 17.250 (14.00) 62.500 (50.71) 27.500 (22.31): Temperature 175 s
    37,519 (45,09)
    Stream 8 rast of a carbamate thief from niAh sections:
    NH ,,
    44.508 (53.49) 1.187 (1.42).
     Temperature
    CO AND 20
    16,000 (38.10) 17,250 (41.07) 8,750 (20.83)
    Contact time flow. CO with synthesis solution 5c.
    Example In comparison with example 2, the operating conditions are modified so that the desorption section ST operates under adiabatic conditions. In this case, the desorption section ST may be a device other than a tubular heat exchanger (for example, a column with plates), but to reduce the residence time the film-type tubular device is optimal.
    The operating conditions of the reactor R are: molar ratio NHj / CO 5, molar ratio 0.5, temperature 190 ° C, pressure 200 bar, the speed of covery (CO to urea) 76.
    Composition of flows, kg f%): Flow 13 of fresh CO. 45.833 / 100 ° С Flow 1 of fresh COi to stage S of ammonia separation 4.875 / 100 ° C (10, Flow 5 of fresh CO
    0
    five
    in section ST Stream 10 fresh NHg
    Stream 2 urea solution from the reactor:
    NH3
    WITH
    Urea
    Hj, 0
    Flow 4 of urea solution from stage S to section ST:
    NHj
    WITH,
    Urea
    Stream 3. Direct my ammonia recycle to reactor R:
    NHj
    WITH,
    five
    five
    0
    Flow 14 of urea solution 0 from section ST:
    Shz with
    40.958 / 1004 35.417 / 25 ° С
    81.062 (42.86). 14.500 (7.67) 62.500 (33.05) 31.063 (16.42) Temperature 190 ° С
    29,750 (21.03)
    18,875 (13,35)
    62,500 (44.19)
    . 30,313 (21,43)
    Temperature
    51,312 (97.62)
    0.500 (0.95) 0.750 (1.43) Temperature 19G
    Urea
    Stream 6
    NHj-pairs, CO of
    0 ST desorption section
    NH,
    20.625 (15.24) 22,500 (16.63)
    62,500 (46,19 29.688 (21.94) Temperature 1 65 ° C.
    COj H, rO
    five
    9.125 (19.39) 37.333 (79.29)
    0.625 () Steam consumption for the ST desorption section is zero. In the sections located in the lower part of the reactor (not shown), steam can be used to remove and recycle large residues of CO contained in the urea solution coming out of the CO-desorber, which forms in the condenser for carbamate, to the final concentration of urea solution in vacuum to obtain the finished product. When using the technology of direct heat recovery (multiple action system) reduced amount of steam
    under pressure 8 bar, i.e. 150 kg per 1000 kg of urea, transferred from the battery installation. The contact time of COz with the 8c synthesis solution.
    EXAMPLE 4 Based on carbon dioxide desorption method (Stamicarbon method), which is modified according to the invention with modernization of the installation to implement the Stamicarbon method in order to reduce energy consumption.
    The operating conditions of the reactor R are: molar ratio NH / COjSjZ, molar ratio H O / CO-j 0.4, temperature, pressure 145 bar, cte, - conversion stump (COA to urea) 62%.
    Composition of streams, kg (%): Flow 13 of fresh CO 45.833 / 100 ° C Flow 1 of fresh CO 2 S122 stage of separation of ammonia 2.112 / 100 ° C
    (4.6)
    Feed 5 fresh C02
    to section ST43,721/1004
    Stream 10 fresh
    and mora:


    ra
    35.417 / 25 ° С
    56,000 (31.55) 28.125 (15.84) 62.500 (35.21) 30.875 (17.40) Temperature 185 ° С
    44.250 (25.44) 30.037 (17.95) 62.500 (37.34) 30.575 (18.27) Temperature 185 С



    11.750 (95.92) (1.63) 0.300 (2.75)
    Temperature 185 ° С
    section art
    9.133 (8.22) 10.846 (9.77) 62.500 (56.28) 28.575 (25.73)
    Temperature
    Ars of a sec
    35,117 (35,10) 62,919 (62,90)
    2,000 (2,00) Temperature 185 С
    five
    0
    five
    0 Flow 8 of carbamate solution from lower sections: NH,
     3 SO hours
    9.133 (30.64) 10.846 (36.39) 9.825 (32.97)
    The steam consumption at a pressure of 22 bar in the system (desorption section using COj) is reduced to 100 kg per 1000 kg of urea with moderate capital investment in the installation for the stage S of ammonia separation. The contact time of CO j with the synthesis solution is 7 s. PRI me R 5. Change known methods without desorption with full or
    5 partial recycling (methods of montedison, mitsui, toazu and others) to reduce energy consumption. When stage S is used to separate ammonia and direct ammonia recycle to process the urea solution from the reactor before the first decomposition stage, a small amount of ammonia and, therefore, water is recycled to the section located in the lower part of the reactor,
    5 thereby improving the conversion rate from the reactor with reduced water evaporation. For these reasons (high conversion, reduced amount of recycled carbamate
    0 and evaporated water) a reduction in steam consumption under a pressure of 8–15 bar from batteries up to 300 kg per 1000 kg of urea can be achieved. Contact time. With 3c synthesis solution,
    Example 6: Modernization of installations using the Snamprogetti method for NHj desorption in order to reduce energy consumption and reduce maintenance costs
    Q and operation.
    When stage S is used to separate and recycle ammonia, carried out downstream of the desorption section, to remove excess gas.
    5 ammonia in the treated urea solution stream (high ammonia content in the urea solution from the reactor contributes to the separation of the carbamate by self-desorption of NHj in the desorption
    9
    sections), a small amount of ammonia must be recycled to the downstream sections. This eliminates the use of a distillation column for the separation and recycling of pure ammonia with high costs and high energy consumption. The time of contact with the solution of synthesis 8c.

    The proposed method allows to reduce the consumption of high-pressure steam to 150-190 kg.
    权利要求:
    Claims (2)
    [1]
    Claim 15
    and urea, with the removal of free ammonia and decomposition of the carbamate by stripping off fresh carbon dioxide in a countercurrent, differing from the fact that, in order to reduce high-pressure steam consumption, the urine-containing solution is treated under adiabatic conditions 3.8-10 , 6% fresh carbon dioxide of its total amount for 38 seconds with the return of distilled ammonia to the synthesis zone, and the resulting solution is sent to the carbamate decomposition zone for contacting with the remaining part of fresh carbon dioxide.
    [2]
    2. Method POP.1, differ1. The method of producing urea from ammonia and carbon dioxide at a ratio of 4.5-5: 1, a working pressure of 145-200 at and a temperature of 184-190 C20, and with the fact that processing the stream in the presence of a carbamate solution at the urea-containing solution from the zone molar ratio: CO-2 synthesis part of the stream of fresh dioxide-0.4 - 0.5 in one reactor with carbon half-si is carried out in a mixer with a urea-containing solution, such as Venturi, in which the stream of fresh containing excess ammonium carbon dioxide is skipped, residual carbamate
    eleven
    i-;
    JOi
    Fig. {
    ten
    and urea, with the removal of free ammonia and decomposition of the carbamate by stripping off fresh carbon dioxide in a countercurrent, differing from the fact that, in order to reduce high-pressure steam consumption, the urine-containing solution is treated under adiabatic conditions 3.8-10 , 6% fresh carbon dioxide of its total amount for 38 seconds with the return of distilled ammonia to the synthesis zone, and the resulting solution is sent to the carbamate decomposition zone for contacting with the remaining part of fresh carbon dioxide.
    y and with the fact that the processing of the urea-containing-solution stream from the synthesis zone with a part of the stream of fresh carbon dioxide is carried out in a Venturi-type mixer, in which a stream of fresh carbon dioxide is passed into pr 2. Method POP.1, I also differ in that the processing of a stream of a évin-containing solution from the baking zone is performed with a part of a stream of fresh dioxide carbon in a Venturi mixer, in which a stream of fresh carbon monoxide is passed in a urea solution.
    / Tj /
    L / sr
    /
    / "
    ““ 3O
    FIG. 2
    2 71
    /
    /five
    X
    3
    x
    V
    FIE
    类似技术:
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    同族专利:
    公开号 | 公开日
    CA1329625C|1994-05-17|
    IN164714B|1989-05-13|
    EP0180704B1|1988-10-12|
    US4613696A|1986-09-23|
    DE3565532D1|1988-11-17|
    AT37868T|1988-10-15|
    EP0180704A1|1986-05-14|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2491274C2|2008-05-20|2013-08-27|Уреа Касале С.А.|Method of modernising urea production apparatus|BG35038A3|1977-05-05|1984-01-16|Montedison Spa,It|Method and installation for synthesis of urea|
    US4235816A|1979-03-08|1980-11-25|Snamprogetti S.P.A.|Integrated ammonia-urea process|
    JPS5811432B2|1979-10-08|1983-03-02|Mitsui Toatsu Kagaku Kk|
    JPS6234033B2|1980-03-13|1987-07-24|Mitsui Toatsu Kagaku Kk|
    US4311856A|1980-12-31|1982-01-19|Toyo Engineering Corp.|Process for synthesizing urea|
    IT1212524B|1982-06-08|1989-11-30|Montedison Spa|PROCESS PERFECTED FOR THE TRANSFER, FROM THE LIQUID PHASE TO THE GASEOUS PHASE, OF THE EXCESS AMMONIA CONTAINED IN AQUEOUS SOLUTIONS OF UREA.|NL8602769A|1986-11-03|1988-06-01|Stamicarbon|METHOD FOR CONCENTRATING A UREA SOLUTION AND APPARATUS FOR CARRYING OUT THE METHOD|
    US4869887A|1987-10-30|1989-09-26|Dijk Christiaan P Van|Integrated ammonia-urea process|
    US4988491A|1989-04-11|1991-01-29|Christiaan Van Dijk|Flexible integration of the production of ammonia and urea|
    US6150555A|1992-05-08|2000-11-21|Urea Casale, S.A.|Process for urea production|
    DE69326881D1|1993-01-07|1999-12-02|Urea Casale Sa|Improved process for producing urea using a carbon dioxide removal step|
    NL1007713C2|1997-12-05|1999-06-08|Dsm Nv|Process for the preparation of urea.|
    ES2560857T3|2005-04-19|2016-02-23|Casale Sa|Urea and related plant production process|
    US7687041B2|2008-02-27|2010-03-30|Kellogg Brown & Root Llc|Apparatus and methods for urea production|
    EP2199279A1|2008-12-17|2010-06-23|Urea Casale S.A.|Improvement to the high-pressure loop in a process for synthesis of urea|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CH247784|1984-05-19|
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