Abstract: A process for polymerizing olefin monomer(s) in a gas-solids olefin polymerization reactor comprising a top zone; a middle zone, which comprises a top end in direct contact with said top zone and which is located below said top zone, the middle zone having a generally cylindrical shape; and a bottom zone, which is in direct contact with a bottom end of the middle zone and which is located below the middle zone; comprising the following steps: introducing a fluidization gas stream into the bottom zone; polymerizing olefin monomer(s) in the presence of a polymerization catalyst in a dense phase formed by particles of a polymer of the olefin monomer(s) suspended in an upwards flowing stream of the fluidization gas in the middle zone; introducing a jet gas stream through one or more jet gas feeding ports in a jet gas feeding area of the middle zone at the dense phase in the middle zone of the gas-solids olefin polymerization reactor; wherein the kinetic energy (EJG) input in the reactor by the jet stream is betwe

Abstract: The present invention relates to a process and apparatus for withdrawing polymer agglomerates from a fluidised bed polymerisation reactor, the polymerisation reactor comprising a bottom zone having a generally conical shape and no fluidisation grid. The agglomerates are withdrawn by using an agglomerate trap below the bottom zone. A value of a process variable indicative of the content of agglomerates in the agglomerate trap is measured and the opening time of the valves transferring polymer to and from the agglomerate trap is adjusted based on the measured value.

Abstract: The present invention relates to a process and apparatus for withdrawing polymer agglomerates from a fluidised bed polymerisation reactor, the polymerisation reactor comprising a bottom zone having a generally conical shape and no fluidisation grid. The agglomerates are withdrawn by using an agglomerate trap below the bottom zone. A value of a process variable indicative of the content of agglomerates in the agglomerate trap is measured and the opening time of the valves transferring polymer to and from the agglomerate trap is adjusted based on the measured value.

Abstract: The present invention deals with an olefin polymerisation process. At least one olefin is polymerised in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone above and connected to said bottom zone; and a generally conical upwards tapering top zone above and connected to said middle zone. Fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor, and withdrawn from the top zone of the reactor. The gas is then compressed, cooled and returned into the bottom zone of the reactor. A fluidised bed is thus formed within the reactor where the growing polymer particles are suspended in the upwards rising gas stream wherein the superficial velocity of the fluidisation gas is less than the transport velocity of the particles. There is no fluidisation grid in the reactor.

Abstract: The present invention deals with an olefin polymerisation process. At least one olefin is polymerised in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone above and connected to said bottom zone; and a generally conical upwards tapering top zone above and connected to said middle zone. Fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor, and withdrawn from the top zone of the reactor. The gas is then compressed, cooled and returned into the bottom zone of the reactor. A fluidised bed is thus formed within the reactor where the growing polymer particles are suspended in the upwards rising gas stream wherein the superficial velocity of the fluidisation gas is less than the transport velocity of the particles. There is no fluidisation grid in the reactor.

Abstract: The present invention relates to a process for treating polyolefin granules in a treatment vessel comprising the steps of: —Providing a bed of granules in liquid in said treatment vessel —Withdrawing a first stream of liquid from said treatment vessel, wherein said first stream of liquid contains hydrocarboneous compounds —introducing a first stream of vapor into said treatment vessel —Withdrawing a second stream of vapor from said treatment vessel wherein said second stream of vapor contains volatile hydrocarboneous compounds —Recovering the granules from said treatment vessel wherein said first stream of vapor has a temperature from Tb to Tb+10° C., wherein Tb is the boiling point of the liquid at the applied pressure, and said first stream of vapor produces an upwards rising vapor stream in said treatment vessel, the superficial vapor velocity of which is no more than 0.2 m/s, and a plant suitable for conducting said process.

Abstract: Polypropylene composition comprising propylene homopolymer (H-PP) and a propylene copolymer (C-PP), said copolmyer comprises (a) a propylene copolymer fraction (A) having a comonomer content of equal or above 1.0 wt.-%, the comomers are C5 to C12 ?-olefins, and (b) a propylene copolymer action (B) having a comonomer content of 4.0 to 20.0 wt-%, the comomers are C5 to C12 ?-olefins, wherein further (i) the comonomer content in propylene copolymer fraction (A) is lower compared to the comonomer content in the propylene copolymer fraction (B), (ii) the propylene copolymer (C-PP) has a comonomer content of at least 2.0 wt.-%, the comomers are C5 to C12 ?-olefins, (iii) the weight ratio [(A)/(B)] of the propylene copolymer fraction (A) to the propylene copolymer fraction (B) is in the range of 20/80 to 80/20, and (iv) the weight ratio [(C-PP)/(H-PP)] of the propylene copolymer (C-PP) to the propylene homopolymer (H-PP) is in the range of 95/5 to 75/25.

Abstract: Polypropylene composition comprising a propylene homopolymer having a melt flow rate MFR2 (230° C.) in the range of 1.0 to 20.0 g/10 min and a propylene copolymer, said copolmyer comprises •a polypropylene fraction having a comonomer content of not more than 1.0 wt.-%, the comomers are C5 to C12 ?-olefins, and •a propylene copolymer fraction having a comonomer content 4.0 to 20.0 wt.-%, the comomers are C5 to C12 ?-olefins, wherein further •the propylene copolymer has a comonomer content of at least 2.5 wt.-%, the comomers are C5 to C12 ?-olefins, •the melt flow rate MFR2 (230° C.) of the propylene homopolymer is higher than the melt flow rate MFR2 (230° C.) of the polypropylene fraction, •the weight ratio of the polypropylene fraction to the propylene copolymer fraction is in the range of 30/70 to 70/30, and •the weight ratio of the propylene copolymer to the propylene homopolymer is in the range of 95/5 to 75/25.

Abstract: The present invention relates to a process for treating polyolefin granules in a treatment vessel comprising the steps of: —Providing a bed of granules in liquid in said treatment vessel —Withdrawing a first stream of liquid from said treatment vessel, wherein said first stream of liquid contains hydrocarboneous compounds —introducing a first stream of vapour into said treatment vessel —Withdrawing a second stream of vapour from said treatment vessel wherein said second stream of vapour contains volatile hydrocarboneous compounds —Recovering the granules from said treatment vessel wherein said first stream of vapour has a temperature from Tb to Tb+10° C., wherein Tb is the boiling point of the liquid at the applied pressure, and said first stream of vapour produces an upwards rising vapour stream in said treatment vessel, the superficial vapour velocity of which is no more than 0.2 m/s, and a plant suitable for conducting said process.

Abstract: Polypropylene composition comprising propylene homopolymer (H-PP) and a propylene copolymer (C-PP), said copolmyer comprises (a) a propylene copolymer fraction (A) having a comonomer content of equal or above 1.0 wt.-%, the comomers are C5 to C12 ?-olefins, and (b) a propylene copolymer action (B) having a comonomer content of 4.0 to 20.0 wt-%, the comomers are C5 to C12 ?-olefins, wherein further (i) the comonomer content in propylene copolymer fraction (A) is lower compared to the comonomer content in the propylene copolymer fraction (B), (ii) the propylene copolymer (C-PP) has a comonomer content of at least 2.0 wt.-%, the comomers are C5 to C12 ?-olefins, (iii) the weight ratio [(A)/(B)] of the propylene copolymer fraction (A) to the propylene copolymer fraction (B) is in the range of 20/80 to 80/20, and (iv) the weight ratio [(C-PP)/(H-PP)] of the propylene copolymer (C-PP) to the propylene homopolymer (H-PP) is in the range of 95/5 to 75/25.

Abstract: Polypropylene composition comprising a propylene homopolymer having a melt flow rate MFR2 (230° C.) in the range of 1.0 to 20.0 g/10 min and a propylene copolymer, said copolmyer comprisesa polypropylene fraction having a comonomer content of not more than 1.0 wt.-%, the comomers are C5 to C12 ?-olefins, anda propylene copolymer fraction having a comonomer content 4.0 to 20.0 wt.-%, the comomers are C5 to C12 ?-olefins, wherein furtherthe propylene copolymer has a comonomer content of at least 2.5 wt.-%, the comomers are C5 to C12 ?-olefins, the melt flow rate MFR2 (230° C.) of the propylene homopolymer is higher than the melt flow rate MFR2 (230° C.) of the polypropylene fraction, the weight ratio of the polypropylene fraction to the propylene copolymer fraction is in the range of 30/70 to 70/30, andthe weight ratio of the propylene copolymer to the propylene homopolymer is in the range of 95/5 to 75/25.