The invention relates to a method for producing a hydrocarbon resin, in which method a monomer mixture which contains an aromatic component containing indene and/or C.sub.1-4 alkylindene and a cyclic diolefin component containing a cyclic diolefin compound is polymerized by heating to a polymerization temperature of at least 180? C. to obtain a product stream containing hydrocarbon resin, wherein oligomers which contain units originating from the cyclic diolefin compound and/or units originating from the aromatic component are separated from the product stream and returned to the monomer mixture, and wherein the hydrocarbon resin is heated in an annealing step to a temperature of 150? C. to 300? C. for a period of 15 minutes to 240 hours. The invention also relates to a hydrocarbon resin that is obtainable by the method, to a hydrogenated hydrocarbon resin, and to the use of the hydrocarbon resin and the hydrogenated hydrocarbon resin.

The invention relates to a method for producing a hydrocarbon resin, in which method a monomer mixture which contains an aromatic component containing indene and/or C.sub.1-4 alkylindene and a cyclic diolefin component containing a cyclic diolefin compound is polymerized by heating to a polymerization temperature of at least 180? C. to obtain a product stream containing hydrocarbon resin, wherein oligomers which contain units originating from the cyclic diolefin compound and/or units originating from the aromatic component are separated from the product stream and returned to the monomer mixture, and wherein the hydrocarbon resin is heated in an annealing step to a temperature of 150? C. to 300? C. for a period of 15 minutes to 240 hours. The invention also relates to a hydrocarbon resin that is obtainable by the method, to a hydrogenated hydrocarbon resin, and to the use of the hydrocarbon resin and the hydrogenated hydrocarbon resin.

A continuous process for making polyolefines are disclosed. The process involves a membrane-assisted separation of non-reacted olefins downstream a polymerisation reactor and enables economical production of polyolefines from non-polymer grade olefin monomers. Uses of membranes adapted to such processes are also disclosed. And, further disclosed are membranes, membrane modules, and separation units adapted to such process as well as polymerisation plants comprising such membrane separation units.

A continuous process for making polyolefines are disclosed. The process involves a membrane-assisted separation of non-reacted olefins downstream a polymerisation reactor and enables economical production of polyolefines from non-polymer grade olefin monomers. Uses of membranes adapted to such processes are also disclosed. And, further disclosed are membranes, membrane modules, and separation units adapted to such process as well as polymerisation plants comprising such membrane separation units.

Ethylene-based polymer, LDPE, is made in a high pressure polymerization process to comprising at least the step of polymerizing a reaction mixture comprising ethylene, using a reactor configuration comprising (A) at least two reaction zones, a first reaction zone (reaction zone 1) and an i reaction zone (reaction zone i where i>2), (B) at least two ethylene feed streams, each feed stream comprising a percentage of the total make-up ethylene fed to the polymerization process, in which a first ethylene feed stream is sent to reaction zone 1 and a second ethylene feed stream is sent to reaction zone i, and (C) a control system to control the percentage of the total make-up ethylene in the ethylene feed stream sent to reaction zone 1 and the percentage of the total make-up ethylene in the ethylene feed stream sent to reaction zone i.

An eductor, a process and apparatus for gas phase polymerization of olefins in a polymerization reactor are disclosed. The process and apparatus employ an eductor which has an inlet which makes a bend of less than about 90 toward the outlet after entering the mixing chamber of the eductor.

A process for recovering valuables from vent gas in polyolefin production is disclosed. The process includes a compression cooling separation step, a heavy hydrocarbon separation step, a light hydrocarbon separation step, a N.sub.2 purification step, and a turbo expansion step in sequence. The N.sub.2 purification step comprises a membrane separation procedure. The light hydrocarbon separation step comprises at least one gas-liquid separation procedure. A first gas, which is obtained by the gas-liquid separation procedure and is heated through heat exchange with multiple streams in the light hydrocarbon separation step, enters the heavy hydrocarbon separation step and is further heated; the heated first gas then enters the N.sub.2 purification step; a first generated gas, which is obtained by the membrane separation procedure of the N.sub.2 purification step, enters the heavy hydrocarbon separation step and the light hydrocarbon separation step in sequence, and is cooled through heat exchange with multiple streams in the heavy hydrocarbon separation step and the light hydrocarbon separation step; and then the cooled first generated gas enters the turbo expansion step. The energy consumption of a compressor can be greatly reduced. An external cooling medium with a temperature lower than an ambient temperature is not needed. The purity and recovery of N.sub.2 and hydrocarbons can be improved, which can facilitate reduction of energy consumption of a whole system, an investment, and a material consumption.

A process for recovering valuables from vent gas in polyolefin production is disclosed. The process includes a compression cooling separation step, a heavy hydrocarbon separation step, a light hydrocarbon separation step, a N.sub.2 purification step, and a turbo expansion step in sequence. The N.sub.2 purification step comprises a membrane separation procedure. The light hydrocarbon separation step comprises at least one gas-liquid separation procedure. A first gas, which is obtained by the gas-liquid separation procedure and is heated through heat exchange with multiple streams in the light hydrocarbon separation step, enters the heavy hydrocarbon separation step and is further heated; the heated first gas then enters the N.sub.2 purification step; a first generated gas, which is obtained by the membrane separation procedure of the N.sub.2 purification step, enters the heavy hydrocarbon separation step and the light hydrocarbon separation step in sequence, and is cooled through heat exchange with multiple streams in the heavy hydrocarbon separation step and the light hydrocarbon separation step; and then the cooled first generated gas enters the turbo expansion step. The energy consumption of a compressor can be greatly reduced. An external cooling medium with a temperature lower than an ambient temperature is not needed. The purity and recovery of N.sub.2 and hydrocarbons can be improved, which can facilitate reduction of energy consumption of a whole system, an investment, and a material consumption.

A process for separation of a hydrocarbon-containing feed stream can include cooling the hydrocarbon-containing feed stream using an absorption refrigeration cycle to form a cooled feed stream. The cooled feed stream can be subjected to distillation conditions to remove a bottom stream including co-monomer; and an overhead stream including hydrocarbon diluents, olefin monomer, and components selected from H.sub.2, N.sub.2, O.sub.2, CO, CO.sub.2, and formaldehyde. The overhead stream can be subjected to distillation conditions adapted to remove a bottom stream including substantially olefin-free hydrocarbon diluents; a side stream including hydrocarbon diluent; and an overhead vapor stream including olefin monomer, diluents, and components selected from H.sub.2, N.sub.2, O.sub.2, CO, CO.sub.2, and formaldehyde. The overhead vapor stream can be cooled using an absorption refrigeration cycle to form a cooled overhead vapor stream. Olefin monomers can be separated from diluents in the cooled overhead vapor stream.

A high pressure polymerization, as described herein, to form an ethylene-based polymer, comprising the following steps: polymerizing a reaction mixture comprising ethylene, using a reactor system comprising at least three ethylene-based feed streams and a reactor configuration that comprises at least four reaction zones, and at least one of the following a) through c), is met: (a) up to 100 wt % of the ethylene stream to the first zone comes from a high pressure recycle, and/or up to 100 wt % of the last ethylene stream to a zone comes from the output from a Primary compressor system; and/or (b) up to 100 wt % of the ethylene stream to first zone comes from the output from a Primary compressor system, and/or up to 100 wt % of the last ethylene stream to a zone comes from a high pressure recycle; and/or (c) the ethylene stream to the first zone, and/or the last ethylene stream to a zone, each comprises a controlled composition; and wherein each ethylene stream to a zone receives an output from two or more cylinders of the last compressor stage of a Hyper compressor system.