초록 ▼

The invention relates to A process for the polymerization of ethylene to produce a polyethylene resin in at least two slurry loop reactors connected to each other in series, the resin having a bimodal molecular weight distribution, a molecular weight distribution MWD of at least 7.0, an HLMI of from

The invention relates to A process for the polymerization of ethylene to produce a polyethylene resin in at least two slurry loop reactors connected to each other in series, the resin having a bimodal molecular weight distribution, a molecular weight distribution MWD of at least 7.0, an HLMI of from 1 to 100 g/10 min, and a density of from 0.935 to 0.960 g/cm3, wherein in one reactor 30 to 47 wt % based on the total weight of the polyethylene resin of a high molecular weight (HMW) polyethylene fraction is produced having an HL275 of from 0.05 to 1.8 g/10 min (the equivalent of HLMI of from 0.01 to 1.56 g/10 min), a density of from 0.925 to 0.942 g/cm3 and an MWD of at least 5.0, and in the other reactor a low molecular weight (LMW) polyethylene fraction is produced having an HLMI of from 10 to 1500 g/10 min and a density of from 0.960 to 0.975 g/cm3, in the presence of a Ziegler-Natta catalyst system.

대표청구항 ▼

1. A process for the polymerisation of ethylene to produce a polyethylene resin in at least two slurry loop reactors connected to each other in series, the resin having a bimodal molecular weight distribution, a molecular weight distribution MWD of at least 7.0, an HLMI of from 1 to 100 g/10min, and

1. A process for the polymerisation of ethylene to produce a polyethylene resin in at least two slurry loop reactors connected to each other in series, the resin having a bimodal molecular weight distribution, a molecular weight distribution MWD of at least 7.0, an HLMI of from 1 to 100 g/10min, and a density of from 0.935 to 0.960 g/cm3, wherein in one reactor 30 to 47 wt % based on the total weight of the polyethylene resin of a high molecular weight (HMW) polyethylene fraction is produced having an HL275 of from 0.05 to 1.8 g/10 min (HLMI=HL275÷3.2), a density of from 0.925 to 0.942 g/cm3 and an MWD of at least 5.0,and in the other reactor a low molecular weight (LMW) polyethylene fraction is produced having an HLMI of from 10 to 1500 g/10 min and a density of from 0.960 to 0.975 g/cm3,in the presence of a Ziegler-Natta catalyst system,wherein density is measured according to ASTM 1505 at a temperature of 23° C., wherein the HLMI is measured according to ASTM D 1238 at a temperature of 190° C. and under a load of 21.6 kg, and wherein the HL275 is measured according to the measurement of HLMI in ASTM D 1238 at a temperature of 190° C. and under a load of 21.6 kg, except that a die of 2.75 mm broad is used. 2. The process according to claim 1 wherein the Ziegler-Natta catalyst has a particle size distribution d50 of from 4 to 12 μm, preferably 5 to 11 μm, most preferably 5 to 10 μm. 3. The process according to claim 1 wherein the Ziegler-Natta catalyst system comprises a Ziegler-Natta catalyst component D and a preactivating agent, wherein the Ziegler Natta catalyst component D is obtainable by a) generating a reaction product A by contacting a magnesium dialkoxide compound with a halogenating agent;b) contacting reaction product A with a first halogenating/titanating agent to form reaction product B;c) contacting reaction product B with a second halogenating/titanating agent to form reaction product C; andd) contacting reaction product C with a third halogenating/titanating agent to form catalyst component D. 4. The process according to claim 1 wherein the HMW fraction is produced in the first reactor and the LMW fraction is produced in the second reactor. 5. The process according to claim 1 wherein the polyethylene resin has a percentage swell at a shear rate of 71.3s−1 is at least 50%, wherein percentage swell was measured on a capillary rheometer according to ISO11443:2005 at a temperature of 210° C. the capillar having an effective die length of 10 mm, a diameter of 2 mm and an aperture of 180° , with the proviso that the extruded samples were 10 cm long instead of 5 cm long. 6. The process according to claim 1 for preparing polyethylene resin for tight-head drums wherein the resin has a Charpy impact resistance according to ISO 179-1 at −30° C. of at least 55 kJ/m2, and wherein the resin preferably has an HLMI of 1 to 4 g/10 min. 7. The process according to claim 1 wherein the preactivating agent is an organoaluminium compound. 8. The process according to claim 7 wherein the organoaluminium compound is triethyl aluminium (TEAL).