The present invention relates to a process and apparatus for producing alpha-olefin polymers in the presence of a polymerization catalyst in a continuously operated multistage polymerisation sequence, the process comprising the steps of (a) polymerizing an alpha-olefin monomer and optionally one or more alpha-olefin co-monomers in a slurry reactor in the presence of a hydrocarbon diluent or liquid monomer in a slurry phase to obtain an alpha-olefin polymer, the slurry phase having a first concentration of solids, (b) continuously withdrawing from the slurry reactor a polymer slurry containing polymer and a fluid phase, (c) concentrating at least a part of the polymer slurry by removing a part of the fluid phase to provide a 1.sup.st product stream comprising a concentrated slurry having a second solids concentration, which is higher than the first solids concentration, and a 2.sup.nd product stream mainly comprising the fluid phase, (d) polymerizing said 1.sup.st product stream in the presence of alpha-olefin monomers and optionally one or more alpha-olefin co-monomers in a first gas phase reactor (GPR1) arranged downstream of said slurry reactor to obtain a 1.sup.st alpha-olefin product stream, (e) polymerizing a 3.sup.rd product stream, withdrawn from said slurry reactor, in the presence of alpha-olefin monomers and optionally one or more alpha-olefin co-monomers in a second gas phase reactor (GPR2) to obtain a 2.sup.nd alpha-olefin product stream.

The present disclosure relates to a process for producing 1,1,2-trichloroethane. According to the present disclosure, a process for producing 1,1,2-trichloroethane with a simplified equipment and a high reaction yield is provided.

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

The present invention discloses methods for removing volatile components from an ethylene polymer effluent stream from a polymerization reactor, and related polyethylene recovery and volatile removal systems. In these methods and systems, the polymer solids temperature is increased significantly prior to introduction of the polymer solids into a purge column for the final stripping of volatile components from the polymer solids.

A process of polymerizing olefins comprising combining propylene with a polymerization catalyst, hydrogen, and at least one external electron donor, such as at least one amino-silane donor, to form polypropylene in a first polymerization medium under solution or slurry conditions at or below the bubble point; removing hydrogen from the first polymerization medium and providing a first olefin/polyolefin separation step to form a second polymerization medium; transferring the second polymerization medium to a gas phase reactor and further combining with ethylene; obtaining a propylene-based impact copolymer. The propylene-based impact copolymer desirably has a melt flow rate of at least 60 g/10 min and is useful in automotive components.

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity.

The invention relates to a process and system for the continuous polymerization of one or more -olefin monomers comprising the steps of: a) introducing catalyst and/or polymer from at least one loop reactor to at least one second reactor b) withdrawing fluids from the at least one second reactor c) cooling fluids comprising the withdrawn fluids with a cooling unit d) introducing the cooled fluids to a separator to separate at least part of the liquid from these fluids to form a liquid phase and a gas/liquid phase e) introducing the gas/liquid phase below to the reactor below a distribution plate f) introducing the liquid phase to a settling tank to separate liquid from fines that settle down in the settling tank g) introducing liquid from the settling tank upstream of the cooling unit, h) introducing the slurry comprising solid polymer particles from the settling tank to the at least one loop reactor.

The present invention discloses methods for removing volatile components from an ethylene polymer effluent stream from a polymerization reactor, and related polyethylene recovery and volatile removal systems. In these methods and systems, the polymer solids temperature is increased significantly prior to introduction of the polymer solids into a purge column for the final stripping of volatile components from the polymer solids.

The present disclosure describes a process for the production of alkylaromatics that may be performed using a loop reactor comprising the steps of: introducing an alkylatable aromatic compound; introducing an olefin; introducing a catalyst; adjusting the alkylatable aromatic compound to a pre-reaction temperature that is below a desired reaction temperature; optionally, adjusting the olefin to a second pre-reaction temperature that is below the desired reaction temperature; optionally, adjusting the catalyst to a third pre-reaction temperature that is below the desired reaction temperature; initially contacting the catalyst and olefin under conditions to control the temperature of the reaction of the catalyst and olefin; mixing and/or circulating the alkylatable aromatic compound, the olefin and the catalyst; and maintaining the alkylatable aromatic compound and olefin at the desired reaction temperature.