• 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:
    A process is described for increasing the space time yield of polymer production in a fluidized bed reactor employing an exothermic polymerization reaction by cooling the recycle stream to below its dew point and returning the resultant two-phase fluid stream to the reactor to maintain the fluidized bed at a desired temperature above the dew point of the recycle stream.
    公开号:SU1473713A3
    申请号:SU833599267
    申请日:1983-03-22
    公开日:1989-04-15
    发明作者:Митчел Дженкинс Ш Джон；Лоренс Джоунс Рассел；Майкл Джоунс Томас；Берет Самил
    申请人:Юнион Карбид Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to the technology of polyolefin production and can be used in the chemical industry.
    The purpose of the invention is to increase the yield of the target product.
    Example 1 A fluidized bed gas phase reaction system operates with a partially condensed reflux to obtain a hexene-1 (propylene) copolymer with ethylene.
    The composition of the reverse flow,%: nitrogen 34.7; ethylene 38.1; ethane 8.9; propylene 5.1 hexene-1 4.8; hydrogen 7.3; methane 0.1.
    Reverse flow dew point temperature 57.8 ° С at heat exchanger pressure. The inlet gas temperature in the reactor is 48 ° C. The amount of liquid in the circulating gas is 4.6 wt.%. Catalyst - complex compound of tetrahydrofuran, magnesium chloride and titanium chloride, reduced
    4b 1
    with j
    oh

    cm
    314
    diethylaluminium chloride (the ratio of diethylaluminium chloride to tetrahydrofuran 0.4 and tri-n-hexylaluminium to tetrahydrofuran is 0.4; it is impregnated with triethylaluminum silica. The temperature of the reactor is 88 ° C. The pressure of the reactor is 18.9, the peripheral velocity gas in a fluidized bed 71 cm / s, a layer height of 11.3 m, a layer diameter of 2.4 m. Copolymer yield per unit of time per unit volume of 0.08 g / cm / h, copolymer density 0.918 g / cm,
    MI Research Institute.
    activator - triethylamine
    PRI me R 2 - (control). The process is carried out analogously to example 1, but the cooling of the reverse flow and the rate of introduction of the catalyst are changed.
    The composition of the reverse flow,%: nitrogen 36.5; ethylene 38.2; ethane 11.2; propylene 5.0; hexene-1 4.1; hydrogen 4.8; methane is not detected.
    The dew-point temperature of the return flow is 53.2 ° C (at the heat exchanger pressure), the gas inlet temperature to the reactor is 60.6 ° C, there is no liquid in the circulating gas, the temperature of the reactor is 87.1 ° C, the pressure of the reactor is 18.9 MPa, and the peripheral velocity gas in the fluidized bed 71 cm / s. The height of the layer is 11.3 m, the diameter of the layer is 2.4 m, the copolymer yield per unit of time per unit volume is 0.032, the density of the copolymer is 0.918 g / cm3, and the activator is triethyl aluminum.
    Example 3. Instead of propylene and 1-hexene, butene-1 is used as the monomer of the alpha-olefin type.
    The composition of the reverse flow,%: hydrogen 6,3; ethylene 57.8; butene-1 26.7; inert 9.2.
    The return dew point temperature is 49.7 ° С at the pressure of the heat exchanger, the gas inlet temperature to the reactor is 47.2 ° C, the fluid is circulating
    the gas contains 1.2 wt.%, the catalyst is a complex compound of tetrahydrofuran, magnesium chloride and titanium chloride, reduced by tri-n-hexylamine (the molar ratio of three-n-hexylamine to tetrahydrofuran is 0.7), which was impregnated with dioxide triethylamine treated silicon.
    , - Q
    five
    0
    five
    0
    five
    0
    45
    50
    55
    The temperature of the reactor is 87.5 ° C, the pressure of the reactor is 18.5 atm, the peripheral gas velocity in the fluidized bed is 71 cm / s, the height of the layer is 11.3 m, the layer diameter is 2.4 m. Copolymer yield per pass 0.1, density 0.918 g / cm, activator - triethyl aluminum.
    PRI me R 4 (control). The process is carried out as in Example 3, but without the presence of liquid in the recirculating gas stream.
    The composition of the reverse flow,%: hydrogen 4.5; ethylene 59.3; butene-1 26.7, inert 9.5. Reverse flow dew point temperature 44 ° С at heat exchanger pressure, inlet temperature
    gas into the reactor 56 C, the catalyst is a complex of tetrahydrofuran, magnesium chloride and titanium chloride, reduced only by tri-n-hexyl-aluminum (the molar ratio of tri-n-hexylamine to tetrahydrofuran is 0.7), which was impregnated with silicon dioxide, treated triethylaluminium. The temperature of the reactor is 83.7 ° C, the pressure of the reactor is 18.5 ati, the peripheral gas velocity in the fluidized bed is 65.3 cm / s, the height of the layer is 11.4 m, the layer diameter is 2.4 m. Copolymer yield per pass is 0.06 g / cm / h, the density of the copolymer is 0.918 g / cm, the activator is triethyl aluminum4.
    Examples 5-10. The process conditions are shown in the table. Various backflows are used to enhance the cooling of the fluidized bed during the polymerization of hexene-1 (C), butene-1 (C4) ethylene (C2), ethylene-propylene (Ce), ethylene-butene-1, pentene-1 (), ethylene, and isopentane as an inert liquid in the polymerization of butene-1-ethylene and ethylene.
    As can be seen from the examples, the proposed method can significantly increase the yield of copolymers (from 0.06 to 0.17 g / cm / h).
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of producing polyolefins by continuous gas-phase polymerization of ethylene or its copolymerization with Ce-Sb-olefins-1 at 50-110 ° C and 8.5-18.9 ppm in the presence of a supported titanium catalyst in the form of the MgCl-HTiCl complex compound.
    51
    with tetrahydrofuran, reduced by tri-n-hexyl aluminum or its mixture with diethyl aluminum chloride and deposited on SiCL treated with triethyl aluminum, while the process is carried out in a fluidized bed of polymer particles supported by a gas stream containing nitrogen, monomers, hydrogen and inert additives
    737136
    alkanes with recirculation of this stream (through the reaction zone with the addition of fresh monomers to it, characterized in that, in order to increase the yield of polymers, the recirculated gas flow is cooled before forming into the reaction zone, containing 1, 2-11.5 wt.% Liquid.
    Compiled by V. Filimonov L. Pcholinska Editor Tehred L. Oliynyk Corrector N. Korol
    Order 1730/5 &
    Circulation 411
    VNIIL of the State Committee for Inventions and Discoveries at the State Committee for Science and Technology of the USSR 4/5, Moscow, Zh-35, Raushsk nab. 113035
    Subscription
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    同族专利:
    公开号 | 公开日
    JPS58201802A|1983-11-24|
    DE3380840D1|1989-12-21|
    ZA83991B|1983-11-30|
    FI830924A0|1983-03-18|
    FI76353B|1988-06-30|
    NO163821B|1990-04-17|
    EP0089691A2|1983-09-28|
    CS257764B2|1988-06-15|
    EP0241947A3|1987-11-25|
    IE59795B1|1994-04-06|
    JPH08333410A|1996-12-17|
    IL67943D0|1983-06-15|
    HU197680B|1989-05-29|
    ES520822A0|1984-11-01|
    NO830746L|1983-09-26|
    DZ520A1|2004-09-13|
    PL241143A1|1984-03-26|
    NZ203222A|1986-01-24|
    PL148356B1|1989-10-31|
    CA1214000A|1986-11-12|
    DE3382632D1|1992-12-03|
    TR21919A|1985-11-04|
    KR840004127A|1984-10-06|
    EP0089691B1|1989-11-15|
    FI830924L|1983-09-25|
    FI76353C|1988-10-10|
    EP0089691A3|1984-09-05|
    HU203490B|1991-08-28|
    NO163821C|1990-07-25|
    ES8500963A1|1984-11-01|
    DE3382632T2|1993-06-03|
    GR77430B|1984-09-14|
    IE830627L|1983-09-24|
    AR243546A1|1993-08-31|
    IL67943A|1986-09-30|
    AU7948791A|1991-09-26|
    CS199583A2|1987-09-17|
    AT47968T|1989-12-15|
    AU8214087A|1988-03-31|
    AU1268883A|1983-09-29|
    IN158241B|1986-10-04|
    JP2762072B2|1998-06-04|
    PH19889A|1986-08-13|
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    JPH0694485B2|1994-11-24|
    MX161951A|1991-03-08|
    JPH08333409A|1996-12-17|
    AT81798T|1992-11-15|
    EG16311A|1991-08-30|
    EP0241947B1|1992-10-28|
    JP2762071B2|1998-06-04|
    KR880000394B1|1988-03-21|
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    US36154782A| true| 1982-03-24|1982-03-24|
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