Ineos Manufacturing Belgium Nv

Solvay (societe Anonyme)

Solvay Polyolefins Europe-belgium (societe Anonyme)

Ineos Europe Ag

Benoit Koch

Daniel Marissal

Brent R Walworth

Marc Parisel

Fabienne Wijzen

Andre Rulmont

Helmut Derleth

Christophe Moineau

Abel Grosjean

Choon Kooi Chai

Andre Frederich

Luc Marie Ghislain Dheur

Stefan Spitzmesser

Paul Fiasse

Luc Dheur

Luc Girardot

Charles Detrez

Paul Johnson

Fabien Bini

Stefan Klaus Spitzmesser

Polyethylene composition having a density of 950-960 kg/m, a SHIof 4-12, a melt index MIbetween 0.2 and 2 g/10 min, and a relationship between spiral flow 'SF' (measured in mm at 250&#xb0; C./1000 bar/100 mm/s) and ESCR 'E' (measured in hours) of E&#x3e;200&#x2212;SF. The composition contains 48-62 wt % of an ethylene polymer (A) and 38-52 wt % of an ethylene copolymer (B). Copolymer (B) has a higher weight average molecular weight than polymer (A), and both of fractions (A) and (B) have a reverse comonomer distribution such that comonomer content increases with increasing molecular weight in the individual fraction.

Polymer composition for caps and closures

Silica supported catalyst composition useful in olefin polymerization, having a SiOcontent not more than 70 weight %, a transition metal (M) content between 2.5 and 9.1 weight %, a magnesium content between 0.5 and 3.3 weight %, an aluminium content between 0.3 and 5 weight % and a chlorine content between 5 and 30 weight %. The silica support has, prior to addition of catalytically active ingredients, a residual surface hydroxyl content between 0.6 and 2 mmole/g of silica, and the molar ratio of transition metal (M) to magnesium is between 0.3 and 2.5.

Catalyst for the polymerisation of olefins, process for its production and use

Process for polymerizing ethylene in a reactor system containing one or more reactors in series, having a characteristic such that the average polymerization productivity [kgPE/kgcata] per unit ethylene per hour a1 during operation at any first residence time r1 is less than 1.7 (a2r2&#x2212;a1r1)/(r2&#x2212;r1), where a2 is the average polymerization productivity [kgPE/kgcata] per unit ethylene per hour during operation at any second residence time r2 where r2&#x3e;r1, a2 and r2 being measured either in the same reactor in the case of a single reactor polymerization, or in a reactor subsequent to the reactor in which a1 and r1 are measured in the case where the polymerization takes place in more than one reactor. The specific yield of the reactor system is greater than 0.3 tonnes/m. Operating the system under the above conditions results in improved productivity/unit ethylene.

Slurry phase polymerisation process

Copolymers of ethylene and &#x3b1;-olefins having (a) a density (D) in the range 0.900-0.940 g/cm, (b) a melt index MI(2.16 kg, 190&#xb0; C.) in the range of 0.01-50 g/10 min, (c) a melt index MI(2.16 kg, 190&#xb0; C.) and Dow Rheology Index (DRI) satisfying the equation [DRI/MI]&#x3e;2.65, and (d) a Dart Drop Impact (DDI) in g of a blown film having a thickness of 25 &#x3bc;m produced from the copolymer satisfying the equation DDI&#x2267;1900&#xd7;{1&#x2212;Exp [&#x2212;750(D&#x2212;0.908)]}&#xd7;{Exp [(0.919&#x2212;D)/0.0045]}. The copolymers may be prepared using metallocene catalysis and are preferably prepared in multistage processes carried out in loop reactors in the slurry phase. The copolymers exhibit long chain branching as defined by Dow Rheology Index (DRI) and exhibit unexpected improvements in mechanical properties, in particular dart drop impact, when extruded into blown films.

Polymers

Process for producing a multimodal polyethylene in at least two loop reactors connected in series. In the process 20-80 wt % of a high molecular weight (HMW) polymer is made in suspension in a first reactor and 20-80 wt % of a low molecular weight (LMW) polymer is made in suspension in a second reactor, one polymer being made in the presence of the other in either order. The ratio of the average activity in the LMW reactor to the average activity in the HMW reactor is from 0.25 and 1.5, where average activity in each reactor is defined as the rate of polyethylene produced in the reactor (kgPE/hr)/[ethylene concentration in the reactor (mol %)&#xd7;residence time in the reactor (hours)&#xd7;feed rate of catalyst into the reactor (g/hr)], residence time being defined as the mass of the polymer in the reactor (kg)/the output rate of polymer from the reactor (kg/hr), and the volumes of the two reactors differ by less than 10%.

Process for producing a multimodal polyethylene in at least two reactors connected in series, in which 20-80 wt % of a first polymer is made in suspension in a first reactor and 80-20 wt % of a second polymer is made in suspension in a second reactor in the presence of the first polymer, and a stream or slurry containing the resulting polymer is withdrawn from the second reactor and transferred to a flash tank operating at a pressure and temperature such that at least 50 mol % of the liquid component of the slurry, or the non-polymer component of the stream entering the flash tank, is withdrawn from the flash tank as a vapour, wherein the concentration in the stream or slurry entering the flash tank of components having a molecular weight below 50 g/mol, C(mol %), satisfies the equation C&#x3c;7+0.07(40&#x2212;T)+4.4(P&#x2212;0.8)&#x2212;7(C/C) where Tand Pare respectively the temperature (in &#xb0; C.) and pressure (MPa g) at the location where the vapour withdrawn from the flash tank is condensed, and Cand Care the molar concentrations in the flash tank of hydrogen and ethylene respectively.

Polymerisation process in which polyethylene is produced in slurry in a polymerisation reactor in the presence of a Ziegler Natta catalyst and an activator, and a stream or slurry containing the polymer is withdrawn from the reactor and transferred to a flash tank operating at a pressure and temperature such that at least 50 mol % of the liquid or non-polymer component of the stream entering the flash tank or slurry is withdrawn from the flash tank as a vapour and at least 98 mol % of the vapour withdrawn from the flash tank is capable of being condensed at a temperature of between 15 and 50&#xb0; C., without compression. A by-product suppressor, which reduces the amount of by-product formed per unit of polyethylene produced by at least 10%, compared with an identical polymerisation process where the by-product suppressor is not present, is used in the reactor. The molar ratio of the by-product suppressor added to the reactor to titanium added to the reactor is between 0.2 and 1.

Process for producing a multimodal polyethylene in at least two reactors connected in series, in which 20-80 wt % of a high molecular weight (HMW) polymer is made in suspension in a first reactor and 20-80 wt % of a low molecular weight (LMW) polymer is made in suspension in a second reactor in the presence of the HMW polymer, wherein the solids concentration in the second LMW reactor, defined as the mass of polymer divided by the total mass of slurry, is at least 35 wt %, most preferably between 45 wt % and 60 wt %, and/or the ratio of solids concentration in the first reactor to that in the second reactor is maintained at less than 1.0, preferably between 0.6 and 0.8, and further wherein the volume of the second reactor is at least 10%, preferably at least 30% and more preferably at least 50% greater than the volume of the first reactor.

Process for producing a multimodal polyethylene in at least two reactors connected in series, in which 20-80 wt % of a high molecular weight (HMW) polymer is made in suspension in a first reactor and 20-80 wt % of a low molecular weight (LMW) polymer is made in suspension in a second reactor. The ratio of the average activity in the LMW reactor to the average activity in the HMW reactor is from 0.25 and 1.5, where average activity in each reactor is defined as the rate of polyethylene produced in the reactor (kgPE/hr)/[ethylene concentration in the reactor (mol %)&#xd7;residence time in the reactor (hours)&#xd7;feed rate of catalyst into the reactor (g/hr)], residence time being defined as the mass of the polymer in the reactor (kg)/the output rate of polymer from the reactor (kg/hr). The volume of the second reactor is at least 10% greater than the volume of the first reactor, and the ratio of length to diameter of the first reactor, L/D(1), is greater than that of the second reactor, L/D(2).

The olefin polymerization catalyst comprises a supported transition metal, magnesium and halogen; the support comprises aluminum phosphate and at least one oxide of silica or alumina. The catalyst is formed by impregnating the support with a liquid complex formed by reacting a magnesium compound and a transition metal compound, which can contain either oxygen or halogen, and then precipitating the complex on the support with an organoaluminum compound which may be halogenated. The catalyst is used with an organometallic cocatalyst.

Catalyst intended for the polymerization of olefins, process for its manufacture and use

An ethylene polymer having a density greater than 959 kg/m3 and a resistance to slow cracking greater than 23 hours. A composition containing this polymer, hollow bodies obtained using at least one such ethylene polymer, and a process for the manufacture of said polymer.

Hollow bodies made of ethylene polymer and method of making same

Process for the manufacture of a support containing silica and at least one constituent chosen from alumina and aluminum phosphate, according to which an alcohol, water, a silicon alkoxide and an acid are mixed under conditions such that gelling or precipitation of silica is prevented, an acidic solution of an aluminum compound and/or a solution of a source of phosphate ions are added thereto, a gelling agent is added thereto, a gel is recovered which is washed with water and then by means of an organic liquid, the gel is then dried by atomization until a powder is obtained, and the powder is calcined. Polymerization of olefins in the presence of a catalyst containing chromium on a support as described above.

Process for the preparation of a support for catalysts, catalyst for the

Process for the manufacture of a support for olefin polymerization catalysts comprising silica, aluminium phosphate and optionally alumina, according to which a source of silica, chosen from alkaline aqueous silica sols and alkaline aqueous solutions of inorganic silicate, is added, in a first step, to an aqueous solution of a source of phosphate ions which has a pH of less than 5, the pH of the medium being maintained below 5 throughout the first step, an aluminium compound is added, in a second step, to the medium obtained from the first step and a precipitate is formed, in a third step, by adding a precipitation agent to the medium obtained from the second step, the pH of the precipitation medium being maintained above or equal to 5.

Process for the manufacture of a support for olefin polymerization

A catalyst system for olefin polymerization, including a catalytic solid based on chromium deposited on a support containing silica, alumina and aluminium phosphate and a cocatalyst chosen from organoaluminium compounds. One of the essential characteristics of the invention is the combination of an organoaluminium compound as cocatalyst with a catalytic solid based on chromium deposited on a support containing silica, alumina and aluminium phosphate.

Growing community of inventors

Hannut, Belgium

Benoit Koch