CONTINUOUS GAS FLUIDIZED BED POLYMERIZATION PROCESS

Abstract

The invention relates to a process for the preparation of a polyolefin in a reaction system from one or more -olefin monomers of which at least one is ethylene or propylene, 5 wherein the reaction system comprises a reactor, a product purge bin, a granular feed bin, wherein the granular feed bin is located downstream of the product purge bin, a recovery unit and an extrusion unit directly coupled to the granular fed bin, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an 10 inlet for a recycle stream located under the distribution plate, wherein the process comprises a) feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate, b) feeding the one or more -olefin monomers to the reactor, 15 c) circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream, d) withdrawing a stream comprising the polyolefin and fluids from the reactor and 20 passing said stream into the product purge bin, e) purging the product purge bin with a purge stream comprising a first inert gas, preferably nitrogen and steam such that a stream comprising a purged polyolefin and a stream comprising fluids, wherein the stream comprising the fluids is substantially free of steam, is obtained, 25 f) introducing at least part of the stream comprising the fluids back into the reactor via the recovery unit, g) introducing the stream comprising the purged polyolefin into the granular feed bin and h) contacting a deactivating stream comprising steam with the purged polyolefin in the 30 granular feed bin to obtain a polyolefin that is substantially free of active polymerization catalyst.

Claims

1. A process for the preparation of a polyolefin in a reaction system from one or more -olefin monomers of which at least one is ethylene or propylene, wherein the reaction system comprises a reactor, a product purge bin, a granular feed bin, wherein the granular feed bin is located downstream of the product purge bin, a recovery unit and an extrusion unit directly coupled to the granular fed bin, wherein the reactor comprises a fluidized bed, an expanded section located at or near the top of the reactor, a distribution plate located at the lower part of the reactor and an inlet for a recycle stream located under the distribution plate, wherein the process comprises a) feeding a polymerization catalyst to the fluidized bed in the area above the distribution plate, b) feeding the one or more -olefin monomers to the reactor, c) circulating fluids from the top of the reactor to the bottom of the reactor, wherein the circulating fluids are cooled using a heat exchanger, resulting in a cooled recycle stream comprising liquid, and wherein the cooled recycle stream is introduced into the reactor using the inlet for the recycle stream, d) withdrawing a stream comprising the polyolefin and fluids from the reactor and passing said stream into the product purge bin, e) purging the product purge bin with a purge stream comprising a first inert gas, and steam such that a stream comprising a purged polyolefin and a stream comprising fluids, wherein the stream comprising the fluids is substantially free of steam, is obtained, f) introducing at least part of the stream comprising the fluids back into the reactor via the recovery unit, g) introducing the stream comprising the purged polyolefin into the granular feed bin and h) contacting a deactivating stream comprising steam with the purged polyolefin in the granular feed bin to obtain a polyolefin that is substantially free of active polymerization catalyst.

2. The process according to claim 1, wherein a second inert gas, is added to the deactivating stream in step h) such that condensation of the steam is avoided.

3. The process according to claim 1, further comprising the step of feeding the polyolefin that is substantially free of active polymerization catalyst to the extrusion unit.

4. The process according to claim 1, wherein the polyolefin is selected from the group of polypropylene and polyethylene.

5. The process according to claim 1, wherein the polyolefin that is substantially free of active polymerization catalyst obtained by step h) has a B-index which is at least 10% lower than a reference polyolefin obtained by a process identical to the process of the present invention except in the absence of step h).

6. The process according to claim 1, wherein nitrogen is added to the stream comprising the purged polyolefin, after which the stream comprising the purged polyolefin and nitrogen is introduced into the granular feed bin.

7. A reaction system for the preparation of a polyolefin from one or more -olefin monomers of which at least one is ethylene or propylene, wherein the reaction system comprises a reactor (8), a product purge bin (100), a granular feed bin (200), wherein the granular feed bin (200) is located downstream of the product purge bin (100), a recovery unit (7) and an extrusion unit (300) directly coupled to the granular fed bin (200), wherein the reactor (8) comprises a fluidized bed, an expanded section (4) located at or near the top of the reactor (8), a distribution plate (6) located at the lower part of the reactor and an inlet for a recycle stream (10) located under the distribution plate (6), wherein the system is arranged such that a) a polymerization catalyst (20) is fed to the fluidized bed in the area above the distribution plate (6), b) the one or more -olefin monomers is fed to the reactor (8), c) fluids are circulated from the top of the reactor to the bottom of the reactor (8), wherein the circulating fluids are cooled using a heat exchanger (5), resulting in a cooled recycle stream (10) comprising liquid, and wherein the cooled recycle stream (10) is introduced into the reactor (8) using the inlet for the recycle stream (10), d) a stream (30) comprising the polyolefin and fluids is withdrawn from the reactor and said stream is passed into the product purge bin, e) the product purge bin (100) is purged with a purge stream (101) comprising a first inert gas and steam such that a stream (110) comprising a purged polyolefin and a stream (102) comprising fluids, wherein the stream (102) comprising the fluids is substantially free of steam, is obtained, f) at least part of the stream (102) comprising the fluids is introduced back into the reactor (8) via the recovery unit (7), g) the stream (110) comprising the purged polyolefin is introduced into the granular feed bin (200) and h) contacting a deactivating stream (210) comprising steam with the purged polyolefin in the granular feed bin (200) to obtain a polyolefin (210) that is substantially free of active polymerization catalyst.

8. The process according to claim 1, wherein the first inert gas is nitrogen.

9. The process according to claim 2, wherein the second inert gas is nitrogen.

10. The process according to claim 9, further comprising adding nitrogen above the condensation temperature of steam.

11. The process according to claim 4, wherein the polyolefin is high density polyethylene or linear low density polyethylene.

12. The reactor system of claim 7, wherein the first inert gas is nitrogen.

Description

EXAMPLE

[0108] Ethylene and 1-butene were polymerized using a Ziegler-Natta catalyst in the presence of hydrogen to produce LLDPE (MFI 5 g/10 min (IS01133:2011, 190 C./2.16 kg) and 0.935 g/cm.sup.3 density (IS01872-2) in a system shown in FIG. 1.

[0109] When nitrogen was used to fluff the LLDPE powder present in the granular feed bin (GFB), the Hunter B-value (B-index) was measured in the range from 2.2-2.9. Within 3 hours after stopping the nitrogen and feeding steam to the GFB, the B-index dropped to a value of 1.2.

[0110] The B-index of the pellets produced during the polymerization was monitored for 11 hours. The B-Index of the pellets produced was checked every 1 hour. The B-Index was measured to be in the range of 2.2 to 2.9.

[0111] After the steam addition to the GFB was stopped and nitrogen was re-connected to fluff the product in the GFB, the B-index increased to 1.9.

[0112] The example was repeated and a similar drop in B-index was observed when flushing the GFB with steam.