Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: A process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor which is controlled by a pressure control valve at the outlet of the polymerization reactor, the process comprising continuously monitoring the pressure within the polymerization reactor, feeding a pressure signal to a controller for controlling the control valve and having the controller altering the opening of the pressure control valve to control the pressure within the polymerization reactor, wherein the controller starts an emergency shutdown program when the pressure control valve closes more than a preset threshold value and the pressure within the polymerization reactor decreases below a preset pressure threshold.

Abstract: A process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor which is controlled by a pressure control valve at the outlet of the polymerization reactor, the process comprising continuously monitoring the pressure within the polymerization reactor, feeding a pressure signal to a controller for controlling the control valve and having the controller altering the opening of the pressure control valve to control the pressure within the polymerization reactor, wherein the controller starts an emergency shutdown program when the pressure control valve closes more than a preset threshold value and the pressure within the polymerization reactor decreases below a preset pressure threshold.

Abstract: A process for separating polymeric and gaseous components of a polymer-monomer mixture at a pressure of from 0.12 MPa to 0.6 MPa and a temperature of from 120° C. to 300° C. in a separation vessel is provided. The separation vessel has a vertically arranged cylindrical shape with a ratio of length to diameter L/D of from 0.6 to 10 and an inlet pipe capable of introducing the polymer-monomer mixture into the separation vessel which the inlet pipe extends vertically from the top of the separation vessel into the separation vessel. Further a process for preparing ethylene homopolymers or copolymers from ethylenically unsaturated monomers in the presence of free-radical polymerization initiators at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa comprising such a process for separating a polymer-monomer mixture is provided.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: The present disclosure provides a low density polyethylene (LDPE) having (A) a density from 0.910 to 0.924 g/cm3, determined according to ISO 1183 at 23° C.; (B) an elongational hardening of at least 4.2, at 150° C. at an elongational rate of 1 s?1; (C) a ratio Mw/Mn of at least 18, where (i) Mw is the weight average molar mass, measured by a MALLS detector coupled to a GPC, and (ii) Mn is the number average molar mass, measured by GPC (Gel Permeation Chromatography); and (D) a Mw of at least 230,000 g/mol. The present disclosure also provides an article of manufacture made from or containing (A) a substrate and (B) a coating layer made from or containing the disclosed LDPE. The present disclosure further provides a polymerization process occurring (A) in the presence of oxygen as the only radical initiating agent and (B) in the absence of solvents.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: Process for copolymerizing ethylene and esters of vinyl alcohol in the presence of free-radical polymerization initiators at pressures in the range of from 110 MPa to 500 MPa and temperatures in the range of from 100° C. to 350° C. in a continuously operated polymerization apparatus comprising a polymerization reactor and one or more compressors, which compress the monomer mixture fed to the polymerization reactor to the polymerization pressure, wherein the monomer mixture is compressed by a sequence of compression stages in which the compressed gas mixture is cooled after each compression stage and the fraction of the monomer mixture, which is liquid after this cooling, is separated off and returned to the polymerization apparatus in liquid form, and wherein at least a part of the liquid fractions obtained after compressing the monomer mixture in the respective compression stage to a pressure of from 0.2 MPa to 10 MPa is purified before being returned to the polymerization process.

Abstract: The present technology relates to a process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out in a continuously operated tubular reactor at temperatures from 100° C. to 350° C. and pressures from 180 MPa to 340 MPa, with a specific reactor surface area Asp of 2 m2/(t/h) to 5.5 m2/(t/h), and the tubular reactor has a specific ratio RDsp of 0.0050 MPa?1 to 0.0069 MPa?1 and an inner surface which has a surface roughness Ra of 2 ?m or less.

Abstract: Process for the preparation of ethylene homopolymers or copolymers in the presence of free-radical polymerization initiators at from 100° C. to 350° C. and pressures in the range of from 160 MPa to 350 MPa in a tubular reactor with at least two spatially separated initiator injection points, wherein injecting initiator rises the temperature of the reaction mixture in the reaction zone following the injection point, and the first initiator injection point of the tubular reactor is not provided with initiator or is provided with so little initiator that the temperature of the reaction mixture does not rise more than 20° C.

Abstract: In a method of removing volatile oxidizable compounds from particles present in a container, a gas stream is continuously introduced into the container, the gas stream takes up the oxidizable compound from the particles in the container and a gas stream laden with the oxidizable compound is discharged from the container. In the method of the present invention, oxygen is added to the gas stream which has been discharged and the oxidizable compound present in the discharged gas stream is subsequently at least partly catalytically oxidized by means of the oxygen and this oxidized gas stream forms at least part of the gas stream introduced, so that the gas stream is circulated. This makes safe and inexpensive removal of the oxidizable compounds from the particles possible.

Abstract: Process for the preparation of ethylene homopolymers or copolymers in a high pressure reactor with at least two spatially separated initiator injection points by polymerizing ethylene and optionally further monomers in the presence of at least two different mixtures of free-radical polymerization initiators at from 100° C. to 350° C. and pressures in the range of from 160 MPa to 350 MPa, wherein the process comprises the following steps: a) providing at least two different initiators as solution in a suitable solvent or in liquid state, b) mixing the initiators and optionally additional solvent in at least two static mixers and c) feeding each of the mixtures to a different initiator injection point of the high pressure reactor, and apparatus for feeding initiator mixtures to a high pressure reactor with at least two spatially separated initiator injection points.

Abstract: Process for the preparation of ethylene homopolymers or copolymers in a high pressure reactor with at least two spatially separated initiator injection points by polymerizing ethylene and optionally further monomers in the presence of at least two different mixtures of free-radical polymerization initiators at from 100° C. to 350° C. and pressures in the range of from 160 MPa to 350 MPa, wherein the process comprises the following steps: a) providing at least two different initiators as solution in a suitable solvent or in liquid state, b) mixing the initiators and optionally additional solvent in at least two static mixers and c) feeding each of the mixtures to a different initiator injection point of the high pressure reactor, and apparatus for feeding initiator mixtures to a high pressure reactor with at least two spatially separated initiator injection points.

Abstract: Process for the preparation of ethylene homopolymers or copolymers in the presence of free-radical polymerization initiators at from 100° C. to 350° C. and pressures in the range of from 160 MPa to 350 MPa in a tubular reactor with at least two spatially separated initiator injection points, wherein injecting initiator rises the temperature of the reaction mixture in the reaction zone following the injection point, and the first initiator injection point of the tubular reactor is not provided with initiator or is provided with so little initiator that the temperature of the reaction mixture does not rise more than 20° C.

Abstract: In a method of removing volatile oxidizable compounds from particles present in a container, a gas stream is continuously introduced into the container, the gas stream takes up the oxidizable compound from the particles in the container and a gas stream laden with the oxidizable compound is discharged from the container. In the method of the present invention, oxygen is added to the gas stream which has been discharged and the oxidizable compound present in the discharged gas stream is subsequently at least partly catalytically oxidized by means of the oxygen and this oxidized gas stream forms at least part of the gas stream introduced, so that the gas stream is circulated. This makes safe and inexpensive removal of the oxidizable compounds from the particles possible.