WO2018038796A1 - Procédés de polymérisation d'oléfine - Google Patents

Procédés de polymérisation d'oléfine Download PDF

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Publication number
WO2018038796A1
WO2018038796A1 PCT/US2017/038791 US2017038791W WO2018038796A1 WO 2018038796 A1 WO2018038796 A1 WO 2018038796A1 US 2017038791 W US2017038791 W US 2017038791W WO 2018038796 A1 WO2018038796 A1 WO 2018038796A1
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Prior art keywords
effluent
hydrogen
molecular weight
titanocene
polymerization
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Application number
PCT/US2017/038791
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English (en)
Inventor
Christopher G. Bauch
Blu E. ENGLEHORN
Kevin W. Lawson
Todd S. Edwards
Keith W. Trapp
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Exxonmobil Chemical Patents Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by Exxonmobil Chemical Patents Inc. filed Critical Exxonmobil Chemical Patents Inc.
Priority to SG11201900345XA priority Critical patent/SG11201900345XA/en
Priority to EP17736830.5A priority patent/EP3504250A1/fr
Priority to CN201780051158.3A priority patent/CN109641986A/zh
Priority to US16/315,830 priority patent/US10934372B2/en
Publication of WO2018038796A1 publication Critical patent/WO2018038796A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F6/00—Post-polymerisation treatments
    • C08F6/006—Removal of residual monomers by chemical reaction, e.g. scavenging
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2410/00—Features related to the catalyst preparation, the catalyst use or to the deactivation of the catalyst
    • C08F2410/01—Additive used together with the catalyst, excluding compounds containing Al or B

Definitions

  • This invention relates to olefin polymerization processes and, in particular, to olefin polymerization processes where hydrogen is used to regulate the molecular weight of the resultant polymer.
  • one mechanism for controlling the polymer molecular weight is to add a chain terminating agent to the process.
  • a chain terminating agent is usually hydrogen (3 ⁇ 4).
  • the hydrogen level in the effluent from the first reactor will have to be reduced if the second reactor is to produce high molecular weight polymer.
  • the same problem is encountered in other polymerization reactor systems when, for example, it is desired to transition toward the manufacture of a very high molecular weight product and the prior product required a high hydrogen content that must be reduced quickly to avoid production of excess off-specification polymer product.
  • purging of the hydrogen in recycle and effluent streams must be accomplished by venting a stream high in hydrogen content to a flare, fuel line, or other appropriate waste control device.
  • the purged stream may consist of as little as 2 mol%, up to as high as 15 mol% or even 20 mol% hydrogen, while the remainder of the stream is primarily monomer which could otherwise be recycled back to the process.
  • the purge stream rate is typically several hundred pounds per hour, and in many cases up to 500 lb/hr or even 750 lb/hr.
  • the purge rate of the stream may be as high as 1000-1500 lb/hr. Removing hydrogen through typical methods, such as venting, can lead to costly loss of monomer and/or can extend transition times thereby generating significant amounts of off-spec polymer product.
  • FIG. 1 is a graph showing the effect of titanocene concentration on polymer melt flow rate (MFR) in the polymerization process of Example 1.
  • FIG. 2 is a graph showing the effect of titanocene concentration on polymerization catalyst activity in the polymerization process of Example 1.
  • the process described herein includes the addition of a hydrogenation catalyst to certain polymerization effluent streams containing unreacted olefin monomer and hydrogen so as to permit rapid reduction in the hydrogen level of the effluent stream before part or all of the effluent stream is supplied to a polymerization reactor where low hydrogen levels are required, for example to produce a high molecular weight polymer.
  • a hydrogenation catalyst to certain polymerization effluent streams containing unreacted olefin monomer and hydrogen so as to permit rapid reduction in the hydrogen level of the effluent stream before part or all of the effluent stream is supplied to a polymerization reactor where low hydrogen levels are required, for example to produce a high molecular weight polymer.
  • a "reactor” is any type of vessel or containment device in any configuration of one or more reactors, and/or one or more reaction zones, wherein a similar polymer is produced; however, two or more reactors that are fluidly connected with one another may each produce a different polymer.
  • the term “hydrogenation catalyst” means any chemical composition that is active to promote the reaction of an olefinic monomer with hydrogen in such a way to either transform it to another substance (e.g., combine with an alkene to form an alkane), or bind it and reduce or eliminate its further reactivity.
  • the hydrogenation catalyst is selected such that it is substantially inactive for the promotion of polymerization of olefinic monomers.
  • Metals, supported or not, such as palladium and/or platinum can be suitable hydrogenation catalysts.
  • Some hydrogenation catalysts require an "activator" such as an aluminum alkyl compound or blend of such compounds.
  • the hydrogenation catalyst comprises a titanocene catalyst precursor (or referred to herein as a "titanocene”) as used in combination with an aluminum alkyl compound.
  • the titanocene catalyst precursor is selected from C2 and C 3 - symmetric titanocene cations comprising any two ligands selected from cyclopentadienyl ligands and ligands isolobal to cyclopentadienyl (“Cp”), and anions selected from halogen, alkyl, and alkoxy groups.
  • the titanocene catalyst precursor is C2 symmetric, such as a bis -cyclopentadienyl titanium dihalide or dialkyl, or bis-indenyl titanium dihalide or dialkyl.
  • Suitable aluminum alkyls include those having the general formula AIR3, where R is a CI to C12 alkyl, more preferably a CI to C8 alkyl, and most preferably a CI to C5 alkyl, preferably triethylaluminum.
  • the molar ratio of aluminum alkyl to titanocene can vary widely, but generally is at least 1 to 1, such as from 1 to 5.
  • the titanocene is reduced from Ti (IV) to Ti (III) by complexing with the aluminum alkyl compound deactivating the titanocene for polymerization, but activating it for hydrogenation.
  • a representative reaction is:
  • titanocene and aluminum alkyl can be combined simultaneously or separately in time and space.
  • titanocene may be introduced as a complex in solution with an aluminum alkyl and a solvent, for example n-hexane, to a polymerization effluent stream.
  • the feed rate of titanocene complex solution is controlled in order to achieve the required degree removal of hydrogen in the stream prior to the recovery and/or recycle of the monomer back to a polymerization reactor feed.
  • titanocene may be introduced to the effluent stream or upstream as an intermittent 'shot' of un- complexed titanocene in solid form or slurry via an appropriate feed system. This solid/slurry stream is then swept into the targeted location where it can be complexed with an alkyl already in the effluent and/or additional alkyl may be added.
  • the present process comprises (or consists essentially of, or consists of) adding a hydrogenation catalyst to a polymerization effluent stream from a first polymerization reactor which is operated to produce an olefin polymer having a first molecular weight and which is fluidly connected to, and arranged in series with, a second polymerization reactor which is operated to produce an olefin polymer having a second molecular weight higher than the first molecular weight.
  • the effluent stream from the first polymerization reactor contains hydrogen, whereas a lower or zero hydrogen level is required to produce the higher molecular weight polymer in the second polymerization reactor.
  • a feed comprising at least one olefin monomer and hydrogen is contacted with a polymerization catalyst in the first polymerization reactor under conditions effective to polymerize at least part of the at least one monomer and produce a first effluent containing the olefin polymer having a first molecular weight, unreacted monomer and residual hydrogen.
  • a polymerization catalyst in the first polymerization reactor under conditions effective to polymerize at least part of the at least one monomer and produce a first effluent containing the olefin polymer having a first molecular weight, unreacted monomer and residual hydrogen.
  • all of the first effluent is then contacted with the hydrogenation catalyst under conditions effective to hydrogenate at least part of the unreacted monomer and produce a second effluent comprising a lower level of hydrogen than the first effluent.
  • At least part of the second effluent and at least one olefin monomer is then contacted with a polymerization catalyst in the second polymerization reactor to produce a third effluent containing the olefin polymer having a second molecular weight higher than the first molecular weight.
  • the third effluent comprises a polymer product comprising the olefin polymer having a first molecular weight and the olefin polymer having a second molecular weight.
  • the polymer product can then be recovered from the third effluent.
  • the hydrogenation catalyst need be added or combined with such effluent.
  • the aluminum alkyl may have been in the first polymerization reactor as a scavenger, or as a co-catalyst for the polymerization catalyst, or unreacted aluminum alkyl added for removing hydrogen from a previous step.
  • the olefinic component of the feed to the first polymerization reactor may consist of a single olefin monomer, such as ethylene or propylene, such that the polymer produced is a homopolymer or may comprise a plurality of different olefin monomers, such as ethylene and/or propylene and one or more a-olefins, such as 1-butene, 1-hexene and/or 1-octene, such that the polymer produced is a copolymer.
  • the at least one olefin monomer supplied to the second polymerization reactor may consist of a single olefin monomer, such as ethylene or propylene, or may comprise a plurality of different olefin monomers, such as ethylene and/or propylene and one or more a-olefins, such as 1-butene, 1-hexene and/or 1- octene.
  • the olefinic component of the feed to the first polymerization reactor may be the different from the at least one olefin monomer supplied to the second polymerization reactor, but more preferably the olefinic components are the same so that a polymer product having a bimodal molecular weight distribution can be produced by the first and second polymerization reactors.
  • the olefinic components comprise at least 50, or 60, or 70, or 80 wt% propylene by weight of the monomers present in the stream and/or reactor, and the polymer produced is a polypropylene homopolymer or copolymer comprising within the range from 0.1, or 4 wt% to 6, or 12, or 18, or 20, or 26, or 30 wt% ⁇ -olefins units derived from ethylene, 1-butene, 1-hexene and/or 1-octene.
  • Polypropylene copolymers can include so called "impact copolymers" which are a heterogeneous blend of polypropylene homopolymer and ethylene-propylene copolymers comprising up to 40, or 50 wt% ethylene content.
  • impact copolymers are a heterogeneous blend of polypropylene homopolymer and ethylene-propylene copolymers comprising up to 40, or 50 wt% ethylene content.
  • the amount of hydrogen in the feed to the first polymerization reactor may be within a range from 100 or 200 or 400 mppm to 1,000 or 5,000 or 10,000 or 25,000 or 50,000 mppm (mole parts per million, or ppm on a molar basis) relative to the total amount of monomer in the feed.
  • the amount of hydrogen desired in the second effluent will depend on the nature and molecular weight of the olefin polymer to be produced in the second reactor.
  • the amount of hydrogen in the second effluent may vary from 0 or 10 or 20 or 50 or 100 mppm to 200 or 300 or 400 or 500 or 1,000 or 4,000 or 8,000 or 10,000 mppm or even higher relative to the total monomer in the second reactor.
  • the second effluent may contain at least 50 wt % less, such at least 90 wt% less, even 99 wt% less hydrogen than the first effluent stream.
  • the hydrogenation catalyst can be added at any convenient location in the polymerization reactor system, such as to a connecting line between the first and second polymerization reactors.
  • the hydrogenation catalyst is added to the first effluent before the latter enters the second polymerization reactor.
  • the amount of hydrogenation catalyst added will depend on the hydrogen reduction required, the residence time and the activity of the hydrogenation catalyst. For example, in the case of a catalyst comprising titanocene and aluminum alkyl, the hydrogenation activity of the catalyst is on the order of 2000 mole H 2 /mole Ti/minute.
  • the process of the first embodiment is suitable for use in any type of polymerization reactor system that requires the removal of hydrogen between two series- connected polymerization reactors.
  • the process can be conducted with a system having three or more polymerization reactors, provided the system includes at least two reactors which are in fluid connection and where the hydrogen level in a first upstream reactor is more than the hydrogen level required in a second down stream reactor.
  • the process can be employed with all types of polymerization reactors, but is particularly intended for use in reactors operating in the slurry phase, such as loop reactors or stirred tank reactors.
  • a non-limiting example of the present process comprises at least two slurry reactors fluidly connected and arranged in series, meaning that fluids and gases are allowed to flow from one reactor to another to carry polymer, monomer, catalyst and/or other gases such as hydrogen in such a manner that polymerization can occur in, for example, the first reactor then can continue in, for example, the second reactor.
  • the present process comprises (or consists essentially of, or consists of) adding a hydrogenation catalyst to a combined recycle stream from first and second polymerization reactors which are fluidly connected to and arranged in series, where the first reactor is being operated to produce a portion of the final polymer product with very high molecular weight and the second reactor is producing very low molecular weight polymer with very high residual hydrogen content.
  • the combined recycle stream would be too high in hydrogen to be fed to the first reactor without significant venting and loss of monomer.
  • a feed comprising at least one olefin monomer is contacted with a polymerization catalyst in the first polymerization reactor under conditions effective to polymerize at least part of the at least one monomer and produce a first effluent containing an olefin polymer having a first molecular weight and unreacted monomer.
  • At least part of, and in most embodiments, all of the first effluent is then combined with at least one olefin monomer and hydrogen and contacted with a polymerization catalyst in the second polymerization reactor to produce a second effluent containing an olefin polymer having a second molecular weight lower than the first molecular weight, unreacted monomer and hydrogen.
  • At least part of the second effluent is then contacted with a hydrogenation catalyst under conditions effective to hydrogenate at least part of the unreacted monomer and produce a third effluent which comprises a lower level of hydrogen than the second effluent and which, at least in part, is subsequently recycled to the first polymerization reactor.
  • at least part of the polymer product is recovered from the second effluent or the third effluent prior to the recycling of the third effluent to the first polymerization reactor.
  • the olefinic component of the feed to the first polymerization reactor in the second embodiment may consist of a single olefin monomer, such as ethylene or propylene, such that the polymer produced is a homopolymer or may comprise a plurality of different olefin monomers, such as ethylene and/or propylene and one or more a-olefins, such as 1-butene, 1-hexene and/or 1-octene, such that the polymer produced is a copolymer.
  • the at least one olefin monomer supplied to the second polymerization reactor may consist of a single olefin monomer, such as ethylene or propylene, or may comprise a plurality of different olefin monomers, such as ethylene and/or propylene and one or more a-olefins, such as 1-butene, 1-hexene and/or 1-octene.
  • the olefinic component of the feed to the first polymerization reactor may be the different from the at least one olefin monomer supplied to the second polymerization reactor, but more preferably the olefinic components are the same so that a polymer product having a bimodal molecular weight distribution can be produced by the first and second polymerization reactors.
  • the amount of hydrogen, if any, present in the feed to the first polymerization reactor in the second embodiment will depend on the nature and molecular weight of the olefin polymer to be produced in the first reactor.
  • the amount of hydrogen in the feed to the first polymerization reactor may vary from 0 or 10 or 20 or 50 or 100 mppm to 200 or 300 or 400 or 500 or 1,000 or 4,000 or 8,000 or 10,000 mppm or even higher relative to the total monomer in the first reactor.
  • the amount of hydrogen added to the first effluent will depend on the nature and molecular weight of the olefin polymer to be produced in the second reactor and may, for example, vary from 100 or 200 or 400 mppm to 1,000 or 5,000 or 10,000 or 25,000 or 50,000 mppm relative to the total amount of monomer added to the second reactor.
  • hydrogen reduction of the second effluent of at least 50 wt%, such at least 90 wt%, or even 99 wt% may be required. This is achieved by addition of the hydrogenation catalyst, either alone or in combination with venting of the second effluent.
  • the process of the second embodiment can be employed with all types of polymerization reactors including stirred gas phase reactors and fluidized bed reactors, singly or in series, but is particularly intended for use in reactors operating in the slurry phase, such as loop reactors or stirred tank reactors.
  • the present process comprises (or consists essentially of, or consists of) adding a hydrogenation catalyst to an effluent stream from a polymerization reactor, where the effluent stream contains unreacted olefin monomer and hydrogen and it is required to reduce the level of hydrogen in the effluent steam before the unreacted monomer is recycled to the same polymerization reactor.
  • a hydrogenation catalyst to an effluent stream from a polymerization reactor, where the effluent stream contains unreacted olefin monomer and hydrogen and it is required to reduce the level of hydrogen in the effluent steam before the unreacted monomer is recycled to the same polymerization reactor.
  • a first feed comprising at least one olefin monomer and hydrogen is contacted with a polymerization catalyst in a polymerization reactor under conditions effective to polymerize at least part of the at least one monomer and produce a first effluent containing an olefin polymer having a first molecular weight, unreacted monomer and residual hydrogen.
  • At least part of the first effluent is then contacted with a hydrogenation catalyst under conditions effective to hydrogenate at least part of the unreacted monomer and produce a second effluent comprising a lower level of hydrogen than the first effluent.
  • At least part of the second effluent can then be recycled to the polymerization reactor together with additional monomer. Operation of the polymerization reactor can then be switched to the production of olefin polymer having a second molecular weight higher than the first molecular weight. In most embodiments, low molecular weight olefin polymer is recovered from the first effluent or the second effluent prior to the recycling of the second effluent to the polymerization reactor.
  • the olefinic component of the feed to the polymerization reactor employed in the third embodiment may consist of a single olefin monomer, such as ethylene or propylene, or may comprise a plurality of different olefin monomers, such as ethylene and/or propylene and one or more a-olefins, such as 1-butene, 1- hexene and/or 1-octene.
  • the process of the third embodiment can be employed with all types of polymerization reactors, it is particularly intended for use in reactors operating in the slurry phase, such as loop reactors or stirred tank reactors.
  • control of the propylene or ethylene hydrogenation reaction using hydrogenation catalysts in a polymerization reactor incorporates any one or more of three aspects: (1) full dispersion of the material into the reaction medium; (2) residence time to provide for completion of the reaction; and (3) flow control of a very small, yet specific quantity of hydrogenation catalyst to achieve the necessary molar ratio of hydrogenation catalyst to hydrogen in the system.
  • the catalyst in one aspect of this invention is introduced to the reactor or feed stream as a liquid solution in which hydrogenation catalyst is activated with an aluminum alkyl (in the case of titanocene) and then diluted in a hydrocarbon solvent, for example n-hexane.
  • a high velocity stream of paraffin, olefin, or oil alone can be used to carry the solid hydrogenation catalyst as a slurry to the reaction injection point and remaining aluminum alkyl from the reaction process then acts as the activating agent for the titanocene, starting the hydrogenation reaction upon injection.
  • this is a preferred method due to reduced handling and raw material costs associated with the activator (if needed) and any solvents required in an alternate system as discussed previously.
  • Any type of polymerization catalyst can be used to effect the formation of polyolefin in the process of the invention.
  • Useful catalysts include metallocenes and other single site catalyst and their associated activators, and Ziegler-Natta catalysts and their associated activator.
  • the aluminum alkyls described herein in relation to the hydrogenation catalyst may also be used as the activator for the polymerization catalyst.
  • the aluminum alkyl that is used in the polymerization of a-olefins to form polyolefins may also be the aluminum alkyl that activates the titanocene hydrogenation catalyst, thus, in those cases additional aluminum alkyl may not need to be added with the titanocene.
  • a step of venting an effluent stream, such as by a low pressure venting system, to remove hydrogen is absent.
  • the general polymerization procedure is as follows: Into a nitrogen-purged 2 liter autoclave was added 1 mL 1.0 M triethylaluminum in hexane and 1 mL of 0.1 M external donor solution in hexane. Hydrogen (83 mmol, or other amount as specified) was then fed into the reactor. A mineral oil slurry (or other medium) containing 7.5 mg of Ziegler-Natta catalyst, 1 mL 1.0 M triethylaluminum in hexane and 1 mL of 0.1 M external donor solution in hexane was flushed into the reactor with 1250 mL liquid propylene. The reactor was heated to 70°C and stirred for 60 minutes. After venting the propylene, the polymer was dried in vacuo at room temperature.
  • the first set of tests used a mineral oil slurry of solid Cp2TiCh which was added to the reactor either in the pre-contact bomb (with catalyst, TEAL, and secondary electron donor) or in the reactor prior to catalyst introduction.
  • the addition of the solid titanocene demonstrated the in-situ preparation of the hydrogenation catalyst by reacting it with the TEAL present in the polymerization reactor.
  • the second method of addition involved prior preparation of the hydrogenation catalyst by mixing Cp2TiCh and TEAL (1:4 molar ratio) in hexane to make a 0.004 M solution.
  • Standard propylene polymerizations were performed using a Mg/Ti-based Ziegler- Natta catalyst with varying amounts of titanocene. The results are shown in FIG. 1 and 2.
  • Tianocene in rxr refers to solid titanocene added to reactor after the addition of TEAL and donor
  • Tianocene in precontact refers to solid titanocene added to Ziegler-Natta catalyst, TEAL, donor slurry
  • Tianocene/TEAL in rxr refers to a solution of titanocene in a solvent with TEAL (1:4) added and donor.
  • melt flow rate of linear polyolefins correlates well with its molecular weight (weight average and number average). Thus, as the MFR of a polymer increases, its molecular weight generally decreases.
  • the polymer MFR (ASTM D1238, 2.16 kg, and 230°C) dropped from the standard value ("standard value” represents the production of propylene homopolymer which uses the same Ziegler-Natta catalyst and the electron donor cyclohexylmethyl dimethoxysilane and 83 mmol 3 ⁇ 4) of 6 g/10 min to less than 0.1 g/10 min after the addition of 0.002 mmol of titanocene in the precontact bomb.

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  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Polymerisation Methods In General (AREA)
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Abstract

La présente invention décrit un procédé de réduction du niveau d'hydrogène dans certains effluents de polymérisation et écoulements de recyclage contenant des monomères de propylène n'ayant pas réagi et de l'hydrogène par mise en contact des écoulements avec un catalyseur d'hydrogénation afin de convertir au moins une partie du propylène en l'alcane correspondant. Le procédé convient particulièrement aux effluents provenant d'un réacteur de polymérisation en suspension qui a été utilisé pour produire un homopolymère ou un copolymère de polypropylène ayant un premier poids moléculaire et au moins une partie de l'effluent devant être fournie à un réacteur de polymérisation en suspension pour produire un homopolymère ou un copolymère de polypropylène ayant un second poids moléculaire supérieur.
PCT/US2017/038791 2016-08-23 2017-06-22 Procédés de polymérisation d'oléfine WO2018038796A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
SG11201900345XA SG11201900345XA (en) 2016-08-23 2017-06-22 Olefin polymerization processes
EP17736830.5A EP3504250A1 (fr) 2016-08-23 2017-06-22 Procédés de polymérisation d'oléfine
CN201780051158.3A CN109641986A (zh) 2016-08-23 2017-06-22 烯烃聚合方法
US16/315,830 US10934372B2 (en) 2016-08-23 2017-06-22 Olefin polymerization processes

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US201662378361P 2016-08-23 2016-08-23
US62/378,361 2016-08-23
EP16192004.6 2016-10-03
EP16192004 2016-10-03

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Cited By (1)

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Publication number Priority date Publication date Assignee Title
US20210198387A1 (en) * 2018-06-21 2021-07-01 Basell Polyolefine Gmbh Suspension process for preparing ethylene copolymers in a reactor cascade

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US4851488A (en) 1987-04-23 1989-07-25 Shell Oil Company Process for altering hydrogenated polymer compositions from high melt flow to low melt flow
US4980421A (en) 1988-04-28 1990-12-25 Japan Synthetic Rubber Co., Ltd. Novel catalyst for hydrogenation of polymer and process for hydrogenating polymer with the catalyst
JPH08151408A (ja) 1994-11-30 1996-06-11 Tonen Corp α− オレフィンの重合方法
EP0905151A1 (fr) 1997-09-27 1999-03-31 Fina Research S.A. Production de polyéthylène ayant une large distribution de poids moléculaire
EP1041090A1 (fr) 1999-03-29 2000-10-04 Fina Research S.A. Production de polyéthylène ayant une large distribution de poids moléculaire
US20100036070A1 (en) 2008-08-08 2010-02-11 Sumitomo Chemical Company, Limited Process for producing olefin polymer (1)
WO2013154907A2 (fr) 2012-04-13 2013-10-17 Chevron Phillips Chemical Company Lp Séparations de composants lors d'une polymérisation
US20130289277A1 (en) 2012-04-26 2013-10-31 Dainippon Sumitomo Pharma Co., Ltd. Medicament for treating mental and behavioural disorders
US9045569B2 (en) 2011-01-14 2015-06-02 W. R. Grace & Co.-Conn. Process of making modified metallocene catalyst, catalyst produced and use thereof

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Publication number Priority date Publication date Assignee Title
US4851488A (en) 1987-04-23 1989-07-25 Shell Oil Company Process for altering hydrogenated polymer compositions from high melt flow to low melt flow
US4980421A (en) 1988-04-28 1990-12-25 Japan Synthetic Rubber Co., Ltd. Novel catalyst for hydrogenation of polymer and process for hydrogenating polymer with the catalyst
JPH08151408A (ja) 1994-11-30 1996-06-11 Tonen Corp α− オレフィンの重合方法
EP0905151A1 (fr) 1997-09-27 1999-03-31 Fina Research S.A. Production de polyéthylène ayant une large distribution de poids moléculaire
EP1041090A1 (fr) 1999-03-29 2000-10-04 Fina Research S.A. Production de polyéthylène ayant une large distribution de poids moléculaire
US20100036070A1 (en) 2008-08-08 2010-02-11 Sumitomo Chemical Company, Limited Process for producing olefin polymer (1)
US7897705B2 (en) 2008-08-08 2011-03-01 Sumitomo Chemical Company, Limited Process for producing olefin polymer
US9045569B2 (en) 2011-01-14 2015-06-02 W. R. Grace & Co.-Conn. Process of making modified metallocene catalyst, catalyst produced and use thereof
WO2013154907A2 (fr) 2012-04-13 2013-10-17 Chevron Phillips Chemical Company Lp Séparations de composants lors d'une polymérisation
US20130289277A1 (en) 2012-04-26 2013-10-31 Dainippon Sumitomo Pharma Co., Ltd. Medicament for treating mental and behavioural disorders

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20210198387A1 (en) * 2018-06-21 2021-07-01 Basell Polyolefine Gmbh Suspension process for preparing ethylene copolymers in a reactor cascade
US11834531B2 (en) * 2018-06-21 2023-12-05 Basell Polyolefine Gmbh Suspension process for preparing ethylene copolymers in a reactor cascade

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