OLEFIN POLYMERIZATION PROCESS

Abstract

The present invention relates to an olefin polymerization process comprising polymerization of at least one olefin monomer in one or more polymerization reactors. In addition, the present invention relates to a system for vapor phase polymerization of at least one polymerizable monomer.

Claims

1. An olefin polymerization process comprising polymerization of at least one olefin monomer in one or more polymerization reactors wherein the polymerization process is carried out in an apparatus comprising: a) one or more reactor vessels to which olefin monomer and catalyst components can be added and which contain an agitated bed of forming polymer particles; b) a means for removing a stream comprising polymer particles from the reactor; c) a means for removing a gas-liquid stream comprising unreacted olefin monomers from the reactor; d) a means for withdrawing a liquid recycle stream from the gas-liquid stream; e) a means for recycle a gas-liquid stream of c) to the reactor; wherein the process further comprises the steps of i) withdrawing a gaseous stream from the stream comprising polymer particles; ii) contacting a liquid recycle stream from d) with said gaseous stream from i) thereby forming a mixture; iii) withdrawing a liquid stream from the mixture of ii); iv) recycling a vapor stream from the mixture of ii) to the polymerization reactor.

2. An olefin polymerization process according to claim 1, wherein the gaseous stream originating from i) is compressed before contacting the gaseous stream with a liquid recycle stream from d).

3. An olefin polymerization process according to claim 1, wherein the vapor stream from the mixture of ii) is compressed before recycling the vapor stream to the polymerization reactor.

4. An olefin polymerization process according to claim 1, wherein step d) is carried out after cooling of the combined stream.

5. An olefin polymerization process according to claim 1, wherein the pressure prevailing in step ii) is lower than the pressure prevailing in the polymerization reactor.

6. An olefin polymerization process according to claim 1, wherein the process is a homopolymer production process.

7. An olefin polymerization process according to claim 1, wherein the process is an ethylene copolymer production process.

8. A system suitable for a vapor phase polymerization of at least one polymerizable monomer according to claim 1, comprising one or more reactor vessels to which olefin monomer and catalyst components can be added and which contain an agitated bed of forming polymer particles, a means for feeding monomer feed to said one or more reactor vessels, a means for removing a stream comprising polymer particles from the reactor, a means for removing a gas-liquid stream comprising unreacted olefin monomers from the reactor, a means for withdrawing a liquid recycle stream from the gas-liquid stream and a means for recycle a gas-liquid stream to the reactor, said system further comprising a means for withdrawing a gaseous stream from the stream comprising polymer particles, a means for contacting a liquid recycle stream with a gaseous stream thereby forming a mixture, a means for withdrawing a liquid stream from the mixture, and a means for recycling a vapor stream from the mixture to the polymerization reactor.

9. A system according to claim 8, wherein said means for contacting a liquid recycle stream with a gaseous stream comprise a single stage flash vessel.

10. A system according to claim 8, wherein said means for contacting a liquid recycle stream with a gaseous stream comprise a multi stage vapor-liquid contacting column.

11. A system according to claim 1, wherein said means for contacting a liquid recycle stream with a gaseous stream comprise a reboiler and/or condensor.

Description

[0035] The present invention will now be discussed with reference to the drawings. The drawings are only for illustrative purposes. The for skilled man known equipment such as pumps, valves, measuring and control system have been omitted.

[0036] FIG. 1 shows a process flow diagram of an olefin polymerization process according to the prior art.

[0037] FIG. 2 shows a process flow diagram of an olefin polymerization process according to the present invention.

[0038] In both FIGS. 1 and 2 the same reference numbers have been used, whenever necessary.

[0039] According to the flowsheet shown in FIG. 1 the olefin polymerization process 100 comprises a reactor 6 with an inlet 1 (liquid) and an inlet 4 (vapor). In reactor 6 the reactants form the polymer particles and a mixed stream 10 of polymer particles and vapor is withdrawn from reactor 6. Mixed stream 10 is sent to a product discharge vessel 11 wherein a separation takes place between a stream 12 of polymer particles and a gas stream 13. Stream 13 is sent to a multi-stage compressor 14, including a first compressor 16 and a second compressor 15. The stream 25 coming from first compressor 16 is sent to the inlet of second compressor 15. The resulting compressed stream 17 is contacted with stream 18, i.e. the vapor outlet of reactor 6. The combined stream 19 is sent to a condenser 7 resulting is a cooled stream 8. Part of stream 8 is a purge 3 (liquid) of the recycle loop. The remainder part 9 is recycled to reactor 6. Multi-stage compressor 14 as shown herein comprises two separate compressors but it should be noted that such a multi-stage compressor may comprise more compressors.

[0040] As shown in FIG. 1 purge 3 is sent to other process units, i.e. there is no direct recycle or return of that purge 3 to the reactor 6.

[0041] According to the flowsheet shown in FIG. 2 the olefin polymerization process 200 comprises a reactor 6 with an inlet 1, a vapor-liquid outlet 18 and a vapor-particles outlet 10. Outlet 10 is a mixed stream of polymer particles and vapor withdrawn from reactor 6. That mixed stream of polymer particles and vapor withdrawn from reactor 6 is sent to a product discharge vessel 11 wherein a separation takes place between a stream 12 of polymer particles and a gas stream 13. Gas stream 13 is sent to a compressor 16 and the compressed vapor stream 25 is sent to a vapor-liquid contactor 26. A liquid purge 3 of the vapor-liquid 18 coming from reactor 6 is sent to the inlet of vapor-liquid contactor 26. In vapor-liquid contactor 26 an intimate contact between vapor stream 25 and liquid purge 3 takes place resulting in liquid effluent 28, i.e. another liquid purge. Gas recycle 27 from vapor-liquid contactor 26 is sent to compressor 15 and the compressed vapor stream 17 is recycled back to the recycle loop. Compressor 15 and 16 may form a multi-stage compressor 14.The combination of vapor stream 17 and vapor-liquid outlet 18 from reactor 6 is sent to unit 7 resulting in a stream 19 and a stream 4. According to another embodiment (not shown here) vapor stream 17 can bypass unit 7 and is thus directly combined with vapor stream 4. After withdrawing a liquid purge 3 from stream 19 the remainder stream 9 is combined with stream 2 and the resulting stream 1 is used as the inlet for reactor 6. It is noted that some reference numbers, such as 20-24, have not be used in the present description.

[0042] As shown in FIG. 2 purge 3 is recycled to the reactor 6 via intermediate process steps. These intermediate process steps comprise the step of contacting the gas from the product discharge vessel with that purge in a vapor-liquid contactor. After that contact a liquid stream is withdrawn from that vapor-liquid contactor and a gas recycle from that vapor-liquid contactor is carried out. Before returning that recycle gas stream back to the polymerization reactor the recycle gas stream is compressed to the inlet pressure of the polymerization reactor. FIG. 2 is thus different from FIG. 1.

[0043] In order to demonstrate the benefits of the present olefin polymerization process (as shown in FIG. 2) over the olefin polymerization process according to the prior art (as shown in FIG. 1) a polypropylene polymerization plant model has been fitted in Mobatec Modeller to describe the plant operation and polymerization kinetics. The plant model provides the concentrations of species in the various stream using empirical or scientific thermodynamic relations. An Aspen Plus (AspenTech) model of the Vapor-Liquid Contactor 26 (see FIG. 2) was constructed for a single stage vapor-liquid contactor. The Aspen plus model was then used to investigate various cases of possible flows, conditions and composition data of the streams 3 (Purge of Recycle Loop (Liquid)) and 13 (Gas from Product Discharge Vessel (Vapor)) from a database. Based on the Aspen Plus model flow, conditions and composition data of streams 17 (Outlet of Multi-Stage Compressor (high pressure gas recycle)) and 28 (Effluent from Vapor-Liquid Contactor) are obtained.

[0044] The results of the simulation will be discussed now.

[0045] In the results below the temperature range for stream 3 is in a range of 20-50 C. That range is primarily correlated to the temperature of the cooling water temperature. The temperature range for stream 13 is in a range of 55-110 C. Please note that as long as stream 3 is colder than stream 13, there will be some heat benefit, i.e. stream 28 is warmer (see FIG. 2). Consequently, the cooling load of the condensor of the entire system/plant is thus reduced. The temperature for both stream 13 and stream 3 in the experiments shown in Table 1 (prior art) and Table 2 (according to the invention) will be in the same range. The same applies for the temperature range for stream 13 and stream 3 in the experiments shown in Table 4 (prior art) and Table 5 (according to the invention) and in the experiments shown in Table 7 prior art) and Table 8 (according to the invention). The inventors assume that the temperature of these streams may slightly change for the embodiments according to the invention. Such a small difference in temperature may be caused by the exact routing of stream 17, i.e. stream 17 may be sent to the inlet of unit 7 or may be combined with the vapor stream coming from that unit 7, i.e. bypassing unit 7.

TABLE-US-00001 TABLE 1 Stream 13 (Vapor) Stream 3 (Liquid = Plant bleed) Propylene: 85% Propylene: 90% Propane: 15% Propane: 10% (=30 kg/h) Flow: 1000 kg/h Flow: 300 kg/h T = Warm T = Cold

TABLE-US-00002 TABLE 2 Table 2 Stream 13 (Vapor) Stream 3 (Liquid) Propylene: 85% Propylene: 90% Propane: 15% Propane: 10% Flow: 1000 kg/h Flow: 500 kg/h

TABLE-US-00003 TABLE 3 Stream 17 (Vapor) Stream 28 (Liquid = Plant bleed) Propylene: 86.8% Propylene: 85.6% Propane: 13.2% Propane: 14.4% (=30 kg/h) Flow: 1292 kg/h Flow: 208 kg/h T = Colder as Stream 13 T = Warmer as Stream 3

[0046] Table 1, 2 and 3 refer to a process for a homopolymer production. The data shown in Table 1 refer to a process according to the prior art (FIG. 1). The calculations are normalized to stream 13=1000 kg/h and assumed 10% propane in stream 3. The same normalization applies for the data shown in Table 2 and Table 3. Both Table 2 and Table 3 refer to process flow diagram according to FIG. 2.

[0047] From the simulation results one can see that the additional process unit in the process according to the present invention, namely the Vapor-Liquid Contactor as a single stage flash vessel, provides 1% saving for monomer feed (polymer grade, 99.5%) that recycles back via the monomer plant. This lower recycle stream could mean a possibility to increase the cracker feed by 1%.

TABLE-US-00004 TABLE 4 Stream 13 (Vapor) Stream 3 (Liquid = Plant bleed) Ethylene: 5% Ethylene: 10% Propylene: 60% Propylene: 70% Propane: 35% Propane: 20% (=43 kg/h) Flow: 1000 kg/h Flow: 215 kg/h T = Warm T = Cold

TABLE-US-00005 TABLE 5 Stream 13 (Vapor) Stream 3 (Liquid) Ethylene: 5% Ethylene: 10% Propylene: 60% Propylene: 70% Propane: 35% Propane: 20% Flow: 1000 kg/h Flow: 160 kg/h

TABLE-US-00006 TABLE 6 Stream 17 (Vapor) Stream 28 (Liquid = Plant bleed) Ethylene: 6% Ethylene: 2.5% Propylene: 61.4% Propylene: 61.2% Propane: 32.6% Propane: 36.3% (=43 kg/h) Flow: 1040 kg/h Flow: 120 kg/h T = Colder as Stream 13 T = Warmer as Stream 3

[0048] Table 4, 5 and 6 refer to a process for ethylene copolymer production. The data shown in Table 4 refer to a process flow diagram according to the prior art (FIG. 1). The calculations are normalized to stream 13=1000 kg/h and assumed 10% ethylene and 20% propane in stream 3. The same normalization applies for the data shown in Table 5 and Table 6. Both Table 5 and Table 6 refer to a process flow diagram according to FIG. 2.

[0049] From the simulation results one can see that the additional process unit in the process according to the present invention, namely the Vapor-Liquid Contactor as a single stage flash vessel, provides 1% saving for a 99.5% monomer feed that recycles back via the monomer plant. This lower recycle stream could mean a possibility to increase the cracker feed by 1%.

TABLE-US-00007 TABLE 7 Stream 13 (Vapor) Stream 3 (Liquid = Plant bleed) Ethylene: 5% Ethylene: 10% Propylene: 60% Propylene: 70% Propane: 35% Propane: 20% (=43 kg/h) Flow: 1000 kg/h Flow: 215 kg/h T = Warm T = Cold

TABLE-US-00008 TABLE 8 Stream 13 (Vapor) Stream 3 (Liquid) Ethylene: 5% Ethylene: 10% Propylene: 60% Propylene: 70% Propane: 35% Propane: 20% Flow: 1000 kg/h Flow: 190 kg/h

TABLE-US-00009 TABLE 9 Stream 17 (Vapor) Stream 28 (Liquid = Plant bleed) Ethylene: 6.2% Ethylene: 2.2% Propylene: 61.6% Propylene: 61.4% Propane: 32.2% Propane: 36.4% (=43 kg/h) Flow: 1070 kg/h Flow: 120 kg/h T = Colder as Stream 13 T = Warmer as Stream 3

[0050] Table 7, 8 and 9 refer to a process for ethylene copolymer production. The data shown in Table 7 refer to a process flow diagram according to the prior art (FIG. 1). The calculations are normalized to stream 13=1000 kg/h and assumed 10% ethylene and 20% propane in stream 3. The same normalization applies for the data shown in Table 8 and Table 9. Both Table 8 and Table 9 refer to a process flow diagram according to FIG. 2.

[0051] From the simulation results one can see that the additional process unit in the process according to the present invention, namely the Vapor-Liquid Contactor as a single stage flash vessel at 20% lower pressure compared to stream 19 (see FIG. 2), provides 1% saving for monomer feed that recycles back via the monomer plant. This lower recycle stream could mean a possibility to increase the cracker feed by 1%.

FIG. 1

[0052] 1. Reactor Feed [0053] 2. Monomer Feed (Liquid) [0054] 3. Purge of Recycle Loop (Liquid) [0055] 4. Reactor Feed (Vapor) [0056] 5. Combined Reactor Feed [0057] 6. Reactor [0058] 7. Condenser [0059] 8. Outlet of Condensor [0060] 9. Recycle Loop (Liquid) [0061] 10. Reactor Product (Polymer and Vapor) [0062] 11. Product Discharge Vessel/Baghouse [0063] 12. Powder Product (Polymer) [0064] 13. Gas from Product Discharge Vessel (Vapor) [0065] 14. Multi-Stage Compressor [0066] 15. Second Compressor [0067] 16. First Compressor [0068] 17. Outlet of Multi-Stage Compressor (high pressure gas recycle) [0069] 18. Reactor Outlet (Vapor) [0070] 19. Combined Reactor Outlet and Outlet of Multi-Stage Compressor [0071] 100. Olefin Polymerization Process

FIG. 2

[0072] 1. Reactor Feed [0073] 2. Monomer Feed [0074] 3. Purge of Recycle Loop (Liquid) [0075] 4. Reactor Feed (Vapor) [0076] 6. Reactor [0077] 7. Condenser [0078] 10. Reactor Product (Polymer and Vapor) [0079] 11. Product Discharge Vessel/Baghouse [0080] 12. Powder Product (Polymer) [0081] 13. Gas from Product Discharge Vessel (Vapor) [0082] 14. Multi-Stage Compressor [0083] 15. Second Compressor [0084] 16. First Compressor [0085] 17. Outlet of Multi-Stage Compressor (high pressure gas recycle) [0086] 18. Reactor Outlet (Vapor) [0087] 19. Combined Reactor Outlet and Outlet of Multi-Stage Compressor [0088] 25. Low pressure gas from First Compressor [0089] 26. Vapor-Liquid Contactor [0090] 27. Gas recycle from Vapor-Liquid Contactor [0091] 28. Effluent from Vapor-Liquid Contactor [0092] 200. Olefin Polymerization Process