WO1994028032A1 - Polymerisation process - Google Patents
Polymerisation process Download PDFInfo
- Publication number
- WO1994028032A1 WO1994028032A1 PCT/GB1994/001074 GB9401074W WO9428032A1 WO 1994028032 A1 WO1994028032 A1 WO 1994028032A1 GB 9401074 W GB9401074 W GB 9401074W WO 9428032 A1 WO9428032 A1 WO 9428032A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- liquid
- gas
- bed
- fluidised bed
- reactor
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B05—SPRAYING OR ATOMISING IN GENERAL; APPLYING FLUENT MATERIALS TO SURFACES, IN GENERAL
- B05B—SPRAYING APPARATUS; ATOMISING APPARATUS; NOZZLES
- B05B7/00—Spraying apparatus for discharge of liquids or other fluent materials from two or more sources, e.g. of liquid and air, of powder and gas
- B05B7/02—Spray pistols; Apparatus for discharge
- B05B7/04—Spray pistols; Apparatus for discharge with arrangements for mixing liquids or other fluent materials before discharge
- B05B7/0416—Spray pistols; Apparatus for discharge with arrangements for mixing liquids or other fluent materials before discharge with arrangements for mixing one gas and one liquid
- B05B7/0433—Spray pistols; Apparatus for discharge with arrangements for mixing liquids or other fluent materials before discharge with arrangements for mixing one gas and one liquid with one inner conduit of gas surrounded by an external conduit of liquid upstream the mixing chamber
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B05—SPRAYING OR ATOMISING IN GENERAL; APPLYING FLUENT MATERIALS TO SURFACES, IN GENERAL
- B05B—SPRAYING APPARATUS; ATOMISING APPARATUS; NOZZLES
- B05B7/00—Spraying apparatus for discharge of liquids or other fluent materials from two or more sources, e.g. of liquid and air, of powder and gas
- B05B7/02—Spray pistols; Apparatus for discharge
- B05B7/08—Spray pistols; Apparatus for discharge with separate outlet orifices, e.g. to form parallel jets, i.e. the axis of the jets being parallel, to form intersecting jets, i.e. the axis of the jets converging but not necessarily intersecting at a point
-
- 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
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00044—Temperature measurement
- B01J2208/00061—Temperature measurement of the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00088—Flow rate measurement
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
- B01J2208/00336—Controlling the temperature by direct heat exchange adding a temperature modifying medium to the reactants
- B01J2208/00353—Non-cryogenic fluids
- B01J2208/00362—Liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00539—Pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00119—Heat exchange inside a feeding nozzle or nozzle reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00121—Controlling the temperature by direct heating or cooling
- B01J2219/00128—Controlling the temperature by direct heating or cooling by evaporation of reactants
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
- Y10S526/901—Monomer polymerized in vapor state in presence of transition metal containing catalyst
Definitions
- the present invention relates to a continuous process for the gas-phase polymerisation of olefins in a fluidised bed reactor, and in particular to a process having improved levels of productivity.
- Processes for the homopolymerisation and copolymerisation of olefins in the gas phase are well known in the art. Such processes can be conducted for example by introducing the gaseous monomer into a stirred and/or fluidised bed comprising preformed polyolefin and a catalyst for the polymerisation.
- the polymerisation is conducted in a fluidised bed reactor wherein a bed of polymer particles are maintained in a fluidised state by means of an ascending gas stream comprising the gaseous reaction monomer.
- the start-up of such a polymerisation generally employs a bed of preformed polymer particles similar to the polymer which it is desired to manufacture.
- fresh polymer is generated by the catalytic polymerisation of the monomer, and polymer product is withdrawn to maintain the bed at more or less constant volume.
- An industrially favoured process employs a fluidisation grid to distribute the fluidising gas to the bed, and to act as a support for the bed when the supply of gas is cut off.
- the polymer produced is generally withdrawn from the reactor via a discharge conduit arranged in the lower portion of the reactor, near the fluidisation grid.
- the fluidised bed comprises a bed of growing polymer particles, polymer product particles and catalyst particles.
- This reaction mixture is maintained in a fluidised condition by the continuous upward flow from the base of the reactor of a fluidising gas which comprises recycle gas from the top of the reactor together with make-up feed.
- the fluidising gas enters the bottom of the reactor and is passed, preferably through a fluidisation grid, to the fluidised bed.
- the polymerisation of olefins is an exothermic reaction and it is therefore necessary to provide means to cool the bed to remove the heat of polymerisation. In the absence of such cooling the bed would increase in temperature until, for example, the catalyst became inactive or the bed commenced to fuse.
- the preferred method for removing the heat of polymerisation is by supplying to the polymerisation reactor a gas, preferably the fluidising gas, which is at a temperature lower than the desired polymerisation temperature, passing the gas through the fluidised bed to conduct away the heat of polymerisation, removing the gas from the reactor and cooling it by passage through an external heat exchanger, and recycling it to the bed.
- the temperature of the recycle gas can be adjusted in the heat- exchanger to maintain the fluidised bed at the desired polymerisation temperature.
- the recycle gas generally comprises the monomeric olefin, optionally together with, for example, diluent gas or a gaseous chain transfer agent such as hydrogen.
- the recycle gas serves to supply the monomer to the bed, to fluidise the bed, and to maintain the bed at the desired temperature.
- Monomers consumed by the polymerisation reaction are normally replaced by adding make up gas to the recycle gas stream.
- the production rate i.e. the space time yield in terms of weight of polymer produced per unit volume of reactor space per unit time
- the rate of heat removal can be increased for example, by increasing the velocity of the recycle gas and/or reducing the temperature of the recycle gas.
- the velocity of the recycle gas which can be used in commercial practice. Beyond this limit the bed can become unstable or even lift out of the reactor in the gas stream, leading to blockage of the recycle line and damage to the recycle gas compressor or blower.
- GB 1415442 relates to the gas phase polymerisation of vinyl chloride in a stirred or fluidised bed reactor, the polymerisation being carried out in the presence of at least one gaseous diluent having a boiling point below that of vinyl chloride.
- Example 1 of this reference describes the control of the temperature of polymerisation by the intermittent addition of liquid vinyl chloride to fluidised polyvinyl chloride material. The liquid vinyl chloride evaporated immediately in the bed resulting in the removal of the heat of polymerisation.
- US 3625932 describes a process for polymerisation of vinyl chloride wherein beds of polyvinyl chloride particles within a multiple stage fluidised bed reactor are kept fluidised by the introduction of gaseous vinyl chloride monomer at the bottom of the reactor. Cooling of each of the beds to remove heat of polymerisation generated therein is provided by spraying liquid vinyl chloride monomer into the ascending gas stream beneath the trays on which the beds are fluidised.
- FR 2215802 relates to a spray nozzle of the non-return valve type, suitable for spraying liquids into fluidised beds, for example in the gas fluidised bed polymerisation of ethylenically unsaturated monomers.
- the liquid which is used for cooling the bed, can be the monomer to be polymerised, or if ethylene is to be polymerised, it can be a liquid saturated hydrocarbon.
- the spray nozzle is described by reference to the fluidised bed polymerisation of vinyl chloride.
- GB 1398965 discloses the fluidised bed polymerisation of ethylenically unsaturated monomers, especially vinyl chloride, wherein thermal control of the polymerisation is effected by injecting liquid monomer into the bed using one or more spray nozzles situated at a height between 0 and 752 of that of the fluidised material in the reactor.
- US 4390669 relates to homo- or copoly erisation of olefins by a multi-step gas phase process which can be carried out in stirred bed reactors, fluidised bed reactors, stirred fluidised bed reactors or tubular reactors.
- polymer obtained from a first polymerisation zone is suspended in an intermediate zone in an easily volatile liquid hydrocarbon, and the suspension so obtained is fed to a second polymerisation zone where the liquid hydrocarbon evaporates.
- gas from the second polymerisation zone is conveyed through a cooler (heat exchanger) wherein some of the liquid hydrocarbon condenses (with comonomer if this is employed) .
- the volatile liquid condensate is partly sent in the liquid state to the polymerisation vessel where it is vaporised for utilisation in removing the heat of polymerisation by its latent heat of evaporation.
- This reference does not state specifically how the liquid is introduced into the polymerisation.
- EP 89691 relates to a process for increasing the space time yield in continuous gas fluidised bed processes for the polymerisation of fluid monomers, the process comprising cooling part or all of the unreacted fluids to form a two phase mixture of gas and entrained liquid below the dew point and reintroducing said two phase mixture into the reactor. This technique is referred to as operation in the "condensing mode".
- EP89691 states that a primary limitation on the extent to which the recycle gas stream can be cooled below the dew point is in the requirement that gas-to- liquid be maintained at a level sufficient to keep the liquid phase of the two phase fluid mixture in an entrained or suspended condition until the liquid is vaporised, and further states that the quantity of liquid in the gas phase should not exceed about 20 weight percent, and preferably should not exceed about 10 weight percent, provided always that the velocity of the two phase recycle stream is high enough to keep the liquid phase in suspension in the gas and to support the fluidised bed within the reactor.
- EP 89691 further discloses that it is possible to form a two-phase fluid stream within the reactor at the point of injection by separately injecting gas and liquid under conditions which will produce a two phase stream, but that there is little advantage seen in operating in this fashion due to the added and unnecessary burden and cost of separating the gas and liquid phases after cooling.
- EP173261 relates in particular to improvements in the distribution of fluid introduced into fluidised bed reactors and refers in particular to operation in the condensing mode as described in EP89691 (supra). More particularly, EP173261 states that operation using an inlet to the base of the reactor (beneath the distribution plate or grid) of the standpipe/conical cap type (as depicted in the drawings of EP 89691) is not satisfactory for a condensing mode of operation due to liquid flooding or frothing in the bottom head, a phenomenon experienced with commercial reactors at relatively low levels of liquid in the recycle stream.
- a continuous gas fluidised bed process for the polymerisation of olefin monomer selected from (a) ethylene, (b) propylene (c) mixtures of ethylene and propylene and (d) mixtures of a, b or c with one or more other alpha-olefins in a fluidised bed reactor by continuously recycling a gaseous stream comprising at least some of the ethylene and/or propylene through a fluidised bed in said reactor in the presence of a polymerisation catalyst under reactive conditions, at least part of the said gaseous stream withdrawn from said reactor being cooled to a temperature at which liquid condenses out, separating at least part of the condensed liquid from the gaseous stream and introducing at least part of the separated liquid directly into the fluidised bed at or above the point at which the gaseous stream passing through the fluidised bed has substantially reached the temperature of the gaseous stream being withdrawn from the reactor.
- the gaseous recycle stream withdrawn from the reactor (hereafter referred to as the "unreacted fluids") comprises unreacted gaseous monomers, and optionally, inert hydrocarbons, reaction activators or moderators as well as entrained catalyst and polymer particles.
- the recycled gaseous stream fed to the reactor additionally comprises sufficient make-up monomers to replace those monomers polymerised in the reactor.
- the process according to the present invention is suitable for the manufacture of polyolefins in the gas phase by the polymerisation of one or more olefins at least one of which is ethylene or propylene.
- Preferred alpha-olefins for use in the process of the present invention are those having from 3 to 8 carbon atoms.
- small quantities of alpha olefins having more than 8 carbon atoms, for example 9 to 18 carbon atoms can be employed if desired.
- the preferred alpha-olefins are but-1-ene, pent-1-ene, hex- 1-ene, 4-methylpent-l-ene, oct-1-ene and butadiene.
- Examples of higher olefins that can be copolymerised with the primary ethylene or propylene monomer, or as partial replacement for the C -Cg monomer are dec-1-ene and ethylidene norbornene.
- the ethylene or propylene is present as the major component of the copolymer, and preferably is present in an amount at least 70% of the total monomers.
- LLDPE linear low density polyethylene
- HDPE high density polyethylene
- the liquid which condenses out of the recycle gaseous stream can be a condensable monomer, e.g. butene, hexene, octene used as a comonomer for the production of LLDPE or may be an inert condensable liquid, e.g. butane, pentane, hexane. It is important that the liquid should vaporise within the bed under the polymerisation conditions being employed so that the desired cooling effect is obtained and to avoid substantial accumulation of liquid within the bed. Suitably at least 95, preferably at least 98 weight percent and most preferably substantially all of the liquid fed to the bed evaporates therein.
- the process is particularly suitable for polymerising olefins at a pressure of between 0.5 and 6 MPa and at a temperature of between 30°C and 130°C.
- a pressure of between 0.5 and 6 MPa the temperature is suitably in the range 80-90°C and for HDPE the temperature is typically 85-105°C depending on the activity of the catalyst used.
- the polymerisation reaction may be carried out in the presence of a catalyst system of the Ziegler-Natta type, consisting of a solid catalyst essentially comprising a compound of a transition metal and of a cocatalyst comprising an organic compound of a metal (i.e. an organometallic compound, for example an alkylaluminiu compound) .
- a catalyst system of the Ziegler-Natta type consisting of a solid catalyst essentially comprising a compound of a transition metal and of a cocatalyst comprising an organic compound of a metal (i.e. an organometallic compound, for example an alkylaluminiu compound) .
- a metal i.e. an organometallic compound, for example an alkylaluminiu compound
- a high-activity catalyst consisting essentially of a chromium oxide activated by a heat treatment and associated with a granular support based on a refractory oxide.
- the process is also suitable for use with metallocene catalysts and Ziegler catalysts supported on silica.
- the catalyst may suitably be employed in the form of a prepolymer powder prepared beforehand during a prepolymerization stage with the aid of a catalyst as described above.
- the prepolymerization may be carried out by any suitable process, for example, polymerisation in a liquid hydrocarbon diluent or in the gas phase using a batch process, a semi-continuous process or a continuous process.
- the preferred process according to the present invention is one wherein substantially the whole of the recycle gaseous stream is cooled and separated and wherein substantially the whole of the separated liquid is introduced into the fluidised bed.
- the recycle gaseous stream is divided into a first stream and a second stream.
- the first stream is passed directly to the reactor in a conventional way by injection below the fluidisation grid and the second stream is cooled and the stream separated into a gas and a liquid stream.
- the gas stream may be returned to the first stream and reintroduced into the reactor below the bed, for example, below the fluidisation grid if such a grid is employed.
- the separated liquid is introduced into the fluidised bed according to the present invention.
- the recycle gaseous stream is suitably cooled by means of a heat exchanger or exchangers to a temperature such that liquid is condensed in the gas stream.
- a heat exchanger or exchangers are well known in the art.
- the gaseous stream leaving the top of the reactor can entrain a quantity of catalyst and polymer particles and these may be removed if desired from the recycle gaseous stream by means of a cyclone. A small proportion of these particles or fines may remain entrained in the recycle gaseous stream and, after cooling and separating the liquid from the gas, the fines can, if desired, be reintroduced into the fluidised bed together with the separated liquid stream.
- the recycle gas stream may also comprise inert hydrocarbons used for the injection of catalyst, reaction activators or moderators into the reactor.
- Make-up monomers for example ethylene to replace monomers consumed by the polymerisation reaction may be added to the recycle gas stream at any suitable location.
- Condensable monomers for example, butene, hexene, 4- methylpent-1-ene and octene, which can, for example, be used as comonomers for the production of LLDPE, or inert condensable liquids, for example, pentane, isopentane, butane and hexane, may be introduced as liquids.
- Inert condensable liquids, for example, pentane may for example be injected into the recycle gaseous stream between the heat exchanger and the separator.
- the comonomer for example, butene can, if desired, be injected into the recycle gaseous stream before passage to the heat exchanger.
- Suitable means for separating the liquid are for example cyclone separators, large vessels which reduce the velocity of the gas stream to effect separation (knock-out drums), demister type gas- liquid separators and liquid scrubbers, for example, venturi scrubbers.
- Such separators are well known in the art.
- the use of a demister type of gas-liquid separator is particularly advantageous in the process of the present invention.
- a further advantage of using a demister type of separator is that the pressure drop within the separator can be lower than in other types of separators thereby enhancing the efficiency of the overall process.
- a particularly suitable demister separator for use in the process of the present invention is a commercially available vertical gas separator known as a "Peerless" (Type DPV P8X) .
- This type of separator uses the coalescence of liquid droplets on a vane arrangement to separate the liquid from the gas.
- a large -liquid reservoir is provided in the bottom of the separator for collection of the liquid. The liquid reservoir enables the liquid to be stored thereby providing control over the discharge of the liquid from the separator.
- This type of separator is very efficient and gives substantially 100 X separation of condensed liquid from the gas stream.
- a filter mesh may be arranged in the liquid reservoir of the separator to collect any remaining fines present in the separated liquid.
- the separated liquid is suitably introduced into the fluidised bed at or above the point at which the recycle gaseous stream being fed to the reactor has substantially reached the temperature of the recycle gaseous stream being withdrawn from the reactor.
- the introduction of the separated liquid may be at a plurality of points within this region of the fluidised bed and these may be at different heights within this region.
- the point or points of introduction of the liquid are arranged such that the local concentration of liquid does not adversely affect the fluidisation of the bed or the quality of the product, and to enable the liquid to disperse rapidly from each point and vaporise in the bed to remove the heat of polymerisation from the exothermic reaction.
- the amount of liquid introduced for cooling purposes may much more closely approach the maximum loading that can be tolerated without disturbing the fluidisation characteristics of the bed and hence offers the opportunity to achieve enhanced levels of reactor productivity.
- the liquid can, if desired, be introduced into the fluidised bed at different heights within the bed. Such a technique can facilitate improved control over comonomer incorporation. Controlled metering of liquid into the fluidised bed provides useful additional control over the temperature profile of the bed and, in the case that the liquid contains comonomer, provides useful control over the comonomer incorporation into the copolymer.
- the liquid is preferably introduced into the lower part of the region of the fluidised bed at which the recycle gaseous stream has substantially reached the temperature of the gaseous stream being withdrawn from the reactor.
- Commercial processes for the gas fluidised bed polymerisation of olefins are generally operated under substantially isothermal, steady state conditions. However, although at least a major portion of the fluidised bed is maintained at the desired substantially isothermal polymerisation temperature, there normally exists a temperature gradient in the region of the bed immediately above the point of introduction of the cooled recycle gaseous stream into the bed. The lower temperature limit of this region wherein the temperature gradient exists is the temperature of the incoming cool recycle gas stream, and the upper limit is the substantially isothermal bed temperature.
- this temperature gradient normally exists in a layer of about 15 to 30 cm (6 to 12 inches) above the grid.
- the liquid is introduced into the bed above the region where this temperature gradient exists, i.e. in the part of the bed which has substantially reached the temperature of the gaseous stream leaving the reactor.
- the point or points of introduction of the liquid into the fluidised bed may for example be approximately 50-70 cm above the fluidisation grid.
- the process according to the present invention may be carried out, for example, by first determining the temperature profile within the fluidised bed during polymerisation using, for example, thermocouples located in or on the walls of the reactor.
- the point or points of introduction of the liquid is/are then arranged to ensure that the liquid enters into the region of the bed at which the recycle gaseous stream has substantially reached the temperature of the gaseous stream being withdrawn from the reactor.
- Figure 1 represents the temperature profile within a typical fluidised bed reactor suitable for use in the gas-phase polymerisation of olefins.
- the temperature profile (Figure 1A) is shown in a fluidised bed used to prepare HDPE at a rate of 23.7 tonnes/hr.
- the temperatures were measured using thermocouples located on the walls of the reactor corresponding to different positions (1-5) within the fluidised bed.
- the locations of 1-5 in the fluidised bed reactor are shown in Figure IB.
- the level of the fluidisation grid (A) and the top of the fluidised bed (B) are indicated on the temperature profile and the diagram.
- the temperature gradient referred to above can be seen as the region between position 1 and position 3.
- the region in which the recycle gaseous stream has substantially reached the temperature of the unreacted fluids leaving the reactor is shown as the region between position 3 and position 5. It is into this region that the separated liquid is introduced into the fluidised bed in accordance with the process according to the present invention.
- the liquid is preferably introduced into the fluidised bed in the lower part of this region i.e. just above position 3 on the temperature profile in Figure 1A.
- a further advantage of the process of the present invention is that by introducing the liquid separately into the fluidised bed, accurate metering means can be employed to regulate the delivery of the liquid to the bed.
- This technique facilitates improved control of the cooling, and provides improved control over the delivery to the bed of any liquid comonomer fed in this manner.
- the process of the present invention can be operated in a manner that does not rely, for example, on any need to maintain liquid entrained in the recycle gas stream. Consequently the quantity of liquid fed to the bed can be varied over much broader limits than hitherto.
- the improved control over the rate of addition to the bed of comonomer or inert hydrocarbons may, for example, be used to control the density of the polymer formed and the space time yield at which such polymer is formed.
- Fluidisation grids suitable for use in the process of the present invention can be of conventional design, for example, a flat or dished plate perforated by a plurality of holes distributed more or less uniformly across its surface. The holes may for example be of diameter of about 5 mm.
- the process of the present invention is operated with a gas velocity in the fluidised bed which must be greater than or equal to that required for fluidisation of the bed.
- the minimum gas velocity is generally approximately 6 cm/sec but the process of the present invention is preferably carried out using a gas velocity in the range 40 to 100, most preferably 50 to 70 cm/sec.
- the catalyst or prepolymer can, if desired, be introduced into the fluidised bed directly with the separated liquid stream. This technique can lead to improved dispersion of the catalyst or prepolymer in the bed.
- liquid or liquid-soluble additives for example, activators, cocatalysts and the like, can be introduced into the bed together with the condensed liquid by the process according to the present invention.
- make-up ethylene for example, to replace the ethylene consumed during the polymerisation, may be advantageously introduced into the separated gas stream prior to its reintroduction into the bed (for example below the fluidisation grid if such is employed) .
- the make-up ethylene may be added to the separated gas stream rather than into the recycle gaseous stream before separation, the quantity of liquid which may be recovered from the separator may be increased and the productivity improved.
- the separated liquid stream may be subjected to additional cooling (e.g. using refrigeration techniques) before being introduced into the fluidised bed.
- additional cooling e.g. using refrigeration techniques
- Cooling of the separated liquid stream may be achieved by use of suitable cooling means e.g. a simple heat exchanger or refrigerator located between the separator and the reactor.
- suitable cooling means e.g. a simple heat exchanger or refrigerator located between the separator and the reactor.
- a further advantage of this particular aspect of the present invention is that, by cooling the liquid before introduction into the fluidised bed, any tendency for catalyst or prepolymer which may be contained in the liquid stream to cause polymerisation before introduction into the bed will be reduced.
- the liquid may be introduced into the fluidised-bed by suitably arranged injection means.
- a single injection means may be used or a plurality of injection means may be arranged within the fluidised bed.
- a preferred arrangement is to provide a plurality of injection means substantially equally spaced in the fluidised bed in the region of the introduction of the liquid.
- the number of injection means used is that number which is required to provide sufficient penetration and dispersion of liquid at each injection means to achieve good dispersion of liquid across the bed.
- a preferred number of injection means is four.
- Each of the injection means may, if desired, be supplied with the separated liquid by means of a common conduit suitably arranged within the reactor. This can be provided, for example, by means of a conduit passing up through the centre of the reactor.
- the injection means are preferably arranged such that they protrude substantially vertically into the fluidised bed, but may be arranged such that they protrude from the walls of the reactor in a substantially horizontal direction.
- the rate at which the liquid can be introduced into the bed depends primarily on the degree of cooling desired in the bed, and this in turn depends on the desired rate of production from the bed.
- the rates of production obtainable from commercial fluidised bed polymerisation processes for the polymerisation of olefins depend, inter alia on the activity of the catalysts employed, and on the kinetics of such catalysts. Thus for example, when catalysts having very high activity are employed, and high production rates are desired, the rate of liquid addition will be high.
- Typical rates of liquid introduction may be, for example, in the range 0.3 to 4.9 cubic metres of liquid per cubic metre of bed material per hour, or even higher.
- the rate of liquid addition may be, for example, in the range 0.5 to 1.5 cubic metres of liquid per cubic metre of bed material per hour.
- the weight ratio of liquid:total gas which may be introduced into the bed can be for example in the range 1:100 to 2:1, preferably in the range 5:100 to 85:100, most preferably in the range 6:100 to 25:100.
- total gas is meant the gas which is returned to the reactor to fluidise the bed together with any gas used to assist in the operation of the injection means, e.g. atomising gas.
- any catalyst which is present in the liquid may benefit from the localised cooling effect of the liquid penetration surrounding each injection means which may avoid hot spots and consequent agglomeration.
- the preferred injection means is a nozzle or a plurality of nozzles which include gas-induced atomising nozzles in which a gas is used to assist in the injection of the liquid, or liquid-only spray- type nozzles.
- a continuous gas fluidised bed process for the polymerisation of olefin monomer selected from (a) ethylene, (b) propylene (c) mixtures of ethylene and propylene and (d) mixtures of a, b or c with one or more other alpha-olefins in a fluidised bed reactor by continuously recycling a gaseous stream comprising at least some of the ethylene and/or propylene through a fluidised bed in said reactor in the presence of a polymerisation catalyst under reactive conditions, at least part of the said gaseous stream withdrawn from said reactor being cooled to a temperature at which liquid condenses out, separating at least part of the condensed liquid from the gaseous stream and introducing the liquid directly into the fluidised bed by one or more liquid-only nozzles or gas- induced atomising nozzles.
- the fluidised bed is preferably supported above a fluidisation grid.
- the injection means are suitably nozzles which protrude into the bed through the reactor wall
- a further aspect of the present invention provides a process for the polymerisation of olefin monomer, the olefin monomer preferably being selected from (a) ethylene, (b) propylene (c) mixtures of ethylene and propylene and (d) mixtures of a, b or c with one or more other alpha-olefin olefins, in a fluidised bed reactor by continuously recycling a gaseous stream comprising the monomer, preferably comprising at least the ethylene and/or propylene, through a fluidised bed in said reactor in the presence of a polymerisation catalyst under reactive conditions t - at least part of the said gaseous stream withdrawn from said reactor being cooled to a temperature at which liquid condenses out, separating at least part of the condensed liquid from the gaseous stream and introducing at least part of the separated liquid directly into the fluidised bed at or above the point at which the gaseous stream passing through the fluidised bed has substantially reached the temperature of the gaseous stream being
- the momentum flux of each of the liquid or liquid/gas jets is at least 250xl0 3 and most preferably at least 300xl0 3 Kg s" 1 m ⁇ 2 x m s" 1 .
- a horizontal momentum flux in the range 300X10 3 to 500xl0 3 Kg s "1 m "2 x m s ⁇ l.
- the horizontal component of the velocity of the jet is calculated from Cosine Q° x actual jet velocity, wherein Q° is the angle the jet makes with the horizontal.
- the direction of motion of the one or more liquid or liquid/gas jets into the bed is preferably substantially horizontal.
- one or more of the jet outlets deliver the liquid or liquid/gas jets in a direction other than horizontal preferably these are directed at an angle not greater than 45°, most preferably not more than 20° to the horizontal.
- the one or more nozzles are suitably each equipped with one or more jet outlets.
- the number of nozzles, and the number and distribution of the jet outlets are important factors in obtaining good distribution of liquid within the bed. If a plurality of nozzles are employed, they are preferably vertically disposed and spaced horizontally and substantially equidistant from one another. In this case, they are also preferably spaced equidistant from one another and from the vertical wall of the fluidised bed.
- the number of nozzles per 10 square metres of the horizontal crossectional area of the bed is preferably in the range 1 to 4, most preferably in the range 2 to 3. Where the calculated number is not an integer, it is preferably rounded up to an integer.
- the number of jet outlets in each nozzle is preferably in the range 1 to 40 most preferably in the range 3 to 16.
- the jet outlets are preferably arranged circumferentially and equidistant from one another around the nozzle.
- the jets of liquid may consist solely of liquid or may comprise a liquid/gas mixture.
- gas may be merely carried in the liquid, or may be employed to atomise the liquid, or to provide motive force to propel the liquid.
- a suitable gas-induced atomising nozzle for use in the process according to the present invention comprises
- the atomising gas may suitably be an inert gas for example nitrogen but is preferably make-up ethylene.
- Each nozzle may be provided with a plurality of outlets of suitable configuration.
- the outlets may for example comprise circular holes, slots, ellipsoids or other suitable configurations.
- Each nozzle may comprise a plurality of outlets of varying configuration.
- the size of the outlets is preferably such that there is little pressure drop through the outlets.
- outlets are preferably symmetrically arranged around the circumference of each nozzle but may also be arranged asymmetrically therein.
- the atomising gas supply to each nozzle is maintained at a pressure sufficient to break the liquid into small droplets and to prevent particle ingress from the fluidised bed or particle blockage of the outlets of the nozzle.
- the relative size of the mixing chamber is arranged to ensure optimum atomisation.
- the volume of the mixing (atomising) chamber relative to the volume of liquid passing through the chamber expressed as: Volume of mixing chamber (in cubic cm)/ Liquid flowrate (cubic cm per second), is preferably in the range 5xl0" 3 to 5x10"1 seconds.
- the velocity of the liquid is preferably maintained at a velocity sufficient to ensure that any particles, for example fines, do not separate out of the liquid stream.
- the weight ratio of atomising gas to liquid supplied to each nozzle is typically in the range 5:95 to 25:75.
- Figure 2 represents a nozzle suitable for use in the process according to the present invention.
- the nozzle comprises a housing 7 comprising an upper region 8 and a lower region 9.
- the upper region is provided with a number of outlets 10 arranged on its circumference and a mixing chamber 11 arranged therein.
- the lower region is provided with a centrally located conduit 12 opening into the mixing chamber and an outer conduit 13 located around the inner conduit.
- the conduit 13 communicates with the mixing chamber by suitably arranged openings 14.
- Pressurised liquid is supplied to the nozzle by conduit 13 and atomising gas is supplied to conduit 12.
- the lower region of the nozzle 9 is connected by conventional means to a supply of pressurised liquid and atomising gas. After mixing with the gas in the chamber 11 the liquid is discharged from the nozzle via the outlets 10 as an atomised spray.
- a preferred gas-induced atomiser nozzle is one wherein the outlets comprise a series of substantially horizontal slots arranged around the circumference of the nozzle.
- the nozzle may also comprise a vertically orientated hole or holes located to ensure that any particles adhering to the top of the nozzle may be removed by the pressurised gas-liquid mixture.
- the slots may typically be of a size equivalent to a hole of diameter of about 6.5 mm and may for example be of dimension 0.75 mm x 3.5 mm.
- the injection means may alternatively comprise liquid-only spray-type nozzle or nozzles.
- a suitable liquid-only spray nozzle for use in the process according to the present invention comprises at least one inlet for pressurised liquid and at least one outlet for said pressurised liquid, sufficient liquid pressure being maintained within the nozzle to ensure that the liquid emerging from the outlet has the desired momentum flux.
- the pressure drop in each nozzle can be regulated if desired, for example, by the use of restrictive devices such as valves.
- the outlets may comprise similar configurations as defined above for the gas-induced atomiser nozzles.
- the preferred configuration for the outlets in the liquid spray nozzle is circular holes.
- the holes are preferably of diameter in the range 0.5 to 5 mm., most preferably in the range 0.5 to 2.5 mm.
- the droplet size of the liquid is influenced by a number of factors in particular in the gas-induced atomiser nozzles by the ratio of the liquid to atomising gas supplied to the nozzle and the size and configuration of the atomising chamber.
- a desirable liquid droplet size for a gas-induced atomiser nozzle is from about 50 micron to about 1000 microns.
- the liquid droplet size is influenced primarily by the pressure drop in the nozzle and the size and configuration of the outlets.
- a desired liquid droplet size for the liquid spray nozzle is from about 2000 microns to about 4000 microns.
- Such droplets can be generated, for example, by disruption of a liquid jet by the motion of the solid particles forming the bed.
- the pressure drop in either type of nozzle must be sufficient to prevent the ingress of particles from the fluidised bed.
- the pressure drop is suitably in the range 2 to 7, preferably 3 to 5 bar and, in the liquid spray nozzles in the range 2 to 7, preferably 4 to 5 bar.
- suitable means are arranged to provide for an emergency gas purge to prevent blockage of the nozzle by the ingress of particles from the fluidised bed.
- a suitable purging gas is nitrogen. It is important that the outlets of the gas-induced atomising nozzles or the liquid-only nozzles are of sufficient size to allow for the passage of any fines which may be present in the separated liquid stream.
- outlets may be arranged at different levels within each nozzle.
- the outlets may be arranged in a series of rows.
- the number of outlets on each nozzle is preferably between 4 and 40, for example between 20 and 40, most preferably from 4 to 16.
- the diameter of such a nozzle is preferably in the range 4 to 30 cm, e.g. 10 to 30 cm, and is most preferably of approximately 7 to 12 cm.
- gas phase fluidised bed polymerisation may be started in a conventional manner for example by charging the bed with particulate polymer particles and then initiating the gas flow through the bed.
- the liquid may be introduced into the bed, for example using the injection means described above.
- the atomising gas supply to the gas-induced nozzles or the purging gas flow to the liquid spray nozzles must be maintained at a velocity sufficient to prevent the ingress of particles into the outlets of the nozzles.
- Figures 3-5 show diagrammatically processes according to the present invention.
- Figure 3 illustrates a gas-phase fluidised bed reactor consisting essentially of a reactor body 15 which is generally an upright cylinder having a fluidisation grid 16 located in its base.
- the reactor body comprises a fluidised bed 17 and a velocity reduction zone 18 which is generally of increased cross-section compared to the fluidised bed.
- the gaseous reaction mixture leaving the top of the fluidised bed reactor constitutes recycle gaseous stream and is passed via line
- Removed fines may suitably be returned to the fluidised bed.
- the recycle gaseous stream leaving the cyclone passes to a first heat exchanger 21 and a compressor 22.
- a second heat exchanger 23 is present to remove the heat of compression after the recycle gaseous stream has passed through the compressor 22.
- the heat exchanger or exchangers can be arranged either upstream or downstream of the compressor 22. After cooling and compression to a temperature such that a condensate is formed, the resultant gas-liquid mixture is passed to the separator 24 where the liquid is removed.
- the gas leaving the separator is recycled via line 25 to the bottom of the reactor 15.
- the gas is passed via the fluidisation grid 16 to the bed thereby ensuring that the bed is maintained in a fluidised condition.
- the separated liquid from the separator 24 is passed via line 25 to the reactor 15. If necessary a pump 26 may be suitably located in line 25' . Catalyst or prepolymer are fed to the reactor via line 27 into the separated liquid stream.
- Product polymer particles may be suitably removed from the reactor via line 28.
- the arrangement shown in Figure 3 is particularly suitable for use when retrofitting existing gas phase polymerisation reactors using fluidised bed processes.
- Figure 4 illustrates an alternative arrangement for performing the process of the present invention.
- the compressor 22 is located in line 25 after separation of the recycle gaseous stream by the separator 24. This has the advantage that the compressor has a reduced quantity of gas to compress and can therefore be of reduced size achieving a better process optimisation and cost.
- Figure 5 illustrates a further arrangement for performing the process of the present invention whereby the compressor 22 is again arranged in line 25 after the separator 24 but before the second heat exchanger 23 which is located in the separated gas stream rather than located before the separator. Again this arrangement gives a better process optimisation.
- the process according to the present invention will now be further illustrated with reference to the following Examples.
- Examples 1 to 8 represent copolymerisations of ethylene with a variety of alpha-olefins using a conventional Ziegler catalyst and Examples 9 to 11 represent homopolymerisation of ethylene using a conventional silica supported chromium oxide catalyst.
- the space time yield and the reactor inlet temperature were computed using a heat balance computer program with an accuracy of ⁇ 152.
- the dew point temperature and the rate of flow of the recycled liquid were computed for the polymerisation system using a conventional software program with an accuracy of about ⁇ 10%.
- Examples 1, 3, 4 and 10 most closely represent typical process conditions for performing the process according to the present invention.
- the results are given in Table 1 and Table 2 and clearly show improved space time yields obtainable using the process of the present invention.
- the "2 Liquid in Recycled Stream" in Tables 1 and 2 represents, as a percentage, the total weight of liquid recycled through the injection means divided by the total weight of gas (recycle gas plus any atomising gas) . .
- test rig was used to test the introduction of liquid into a fluidised bed by use of injection means as described above.
- the arrangement of the test rig is shown in Figure 6.
- the test rig comprises an aluminium fluidisation vessel 50 having a velocity reduction zone 56 containing a bed 51 of polyethylene powder (high density or linear low density polyethylene) , previously prepared by gas fluidised bed polymerisation of ethylene in an industrial scale gas fluidised bed plant.
- the bed 51 was fluidised by passing a continuous stream of dry nitrogen gas through line 52 and preheater 53 into the base chamber 54 of vessel 50, and thence into the bed through grid 55.
- the nitrogen gas was supplied from a commercial liquid nitrogen supply tank, and the quantity of nitrogen supplied to fluidise the and the gas pressure in the system were controlled by means of valves 57 and 69, the volume flow rate being determined using a conventional turbine meter (not shown) .
- the preheater unit had a nominal heating capacity of 72kW which was controllable to heat the nitrogen gas to the desired temperature.
- Volatile liquid hydrocarbon 58 (1-hexene or n-pentane) was introduced into the fluidised bed 51 from a cooler/de ister tank 59 by means of a pump 60 and line 61. The volatile liquid hydrocarbon entered the bed through nozzle/jet outlet arrangement 62 which penetrated into the bed.
- nozzle/jet outlet arrangements were tested, some being of the liquid-only type, and others being of the gas atomising type.
- atomising gas was introduced through line 63 (for an example of this type of nozzle, see Figure 2 of the accompanying drawings) .
- Volatile liquid hydrocarbon entering the fluidised bed through the nozzle/jet outlet arrangement 62 evaporated in the bed thus causing cooling by absorbing latent heat of evaporation.
- the nitrogen fluidising gas and the accompanying volatilised liquid hydrocarbon emerged from the top of the bed into the velocity reduction zone 56 wherein the bulk of any polyethylene powder entrained in the gas stream fell back into the bed.
- the gas then passed into line 64, filter unit 65 and through non-return valve 66 into the cooler/demister tank 59.
- the cooler/demister tank 59 contained two heat exchangers 67, 68.
- Heat exchanger 67 was cooled by passage therethrough of cold water, and 68 was cooled by circulating a refrigerated ethylene glycol/water antifreeze solution. Passage of the gas over the heat exchangers 67, 68 cooled the gas and caused the liquid hydrocarbon (hexene or pentane) to condense out.
- the condensed hydrocarbon collected in the base of tank 59, from whence it was recycled back to the bed.
- the nitrogen gas thus substantially freed from hydrocarbon was then passed through back-pressure regulating valve 69 to the atmosphere.
- the fluidisation and vaporisation of the liquid hydrocarbon in the bed was monitored using commercially available X-ray imaging apparatus comprising an X-ray source 70, an image intensifier 71 and a CCD (charge coupled device) video camera 72 the output of which was continuously recorded on a video tape recorder (not shown).
- the X-ray source, image intensifier and video camera were mounted on a moveable gantry 73 to enable the field of view of the bed to be changed at will.
- the process of the present invention provides substantial improvements in productivity of gas fluidised bed polymerisation processes over existing processes.
- the process of the present invention can be employed in new plant or can be employed in existing plant to obtain substantial increases in productivity and better control of liquid addition to the bed.
- substantial reductions in capital costs can be achieved by using smaller reaction vessels, compressors and other ancillary equipment than would have been necessary to achieve comparable productivities from conventional plant.
- modification of such plant in accordance with the present invention provides substantial increases in productivity and improved control of the process.
- Example 12 and Comparative Example 13 illustrate the use of the same nozzle arrangement, but in the Comparative Example, the addition of liquid to the "cold" zone of a gas fluidised bed polymerisation is simulated by running the bed at 45°C in comparison with the 98°C employed in Example 12. Under these circumstances lumps of polymer wet with liquid hydrocarbon formed around the nozzle. Examples 12, 14 and comparative Example 13 employed gas induced atomising nozzles, and Example 15 a liquid only nozzle. Examples 12, 14 and 15 all produced good penetration and dispersion of the liquid hydrocarbon, the liquid penetration being stopped only by the vessel wall. In Compatative Example 12, liquid penetration was inhibited by the formation of agglomerated lumps of polymer/liquid hydrocarbon 27 TABLE 1
Abstract
Description
Claims
Priority Applications (19)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL94311280A PL177865B1 (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
CA002161432A CA2161432C (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
JP7500343A JPH08510497A (en) | 1993-05-20 | 1994-05-19 | Polymerization method |
EP94915621A EP0699213B1 (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
AU67260/94A AU694924C (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
UA95104678A UA40615C2 (en) | 1993-05-20 | 1994-05-19 | method for continuous gas phase polymerization in fluidized bed (variants) and method for polymerization of olefin monomer in reactor with fluidized bed |
RO95-01861A RO116551B1 (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
SK1433-95A SK281033B6 (en) | 1993-05-20 | 1994-05-19 | Continuous process for the polymerisation of olefins, device for implementing this process |
US08/256,052 US5541270A (en) | 1993-05-20 | 1994-05-19 | Polymerization process |
RU95122233A RU2144042C1 (en) | 1993-05-20 | 1994-05-19 | Polymerization method |
BR9406535A BR9406535A (en) | 1993-05-20 | 1994-05-19 | Continuous gaseous fluidized process for the polymerization of olefinic monomer and process for the polymerization of olefinic monomers |
KR1019950705119A KR100300468B1 (en) | 1993-05-20 | 1994-05-19 | Polymerization Method |
DE69408450T DE69408450T2 (en) | 1993-05-20 | 1994-05-19 | POLYMERIZATION PROCESS |
BG100102A BG62854B1 (en) | 1993-05-20 | 1995-10-27 | Polymerisation process |
FI955561A FI112230B (en) | 1993-05-20 | 1995-11-17 | The polymerization process |
NO954648A NO309327B1 (en) | 1993-05-20 | 1995-11-17 | Continuous process for gas phase polymerization of olefins in a fluid bed reactor |
US08/602,013 US5733510A (en) | 1993-05-20 | 1996-02-15 | Fluidized bed polymerization reactor |
GR980400143T GR3025973T3 (en) | 1993-05-20 | 1998-01-21 | Polymerisation process |
HK98109687A HK1008963A1 (en) | 1993-05-20 | 1998-08-04 | Polymerisation process |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB939310390A GB9310390D0 (en) | 1993-05-20 | 1993-05-20 | Polymerization process |
GB9310390.1 | 1993-05-20 | ||
GB939310388A GB9310388D0 (en) | 1993-05-20 | 1993-05-20 | Polymerization process |
GB939310387A GB9310387D0 (en) | 1993-05-20 | 1993-05-20 | Polymerization process |
GB9310387.7 | 1993-05-20 | ||
GB9310388.5 | 1993-05-20 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1994028032A1 true WO1994028032A1 (en) | 1994-12-08 |
Family
ID=27266692
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB1994/001074 WO1994028032A1 (en) | 1993-05-20 | 1994-05-19 | Polymerisation process |
Country Status (31)
Country | Link |
---|---|
US (4) | US5541270A (en) |
EP (3) | EP0926163A3 (en) |
JP (1) | JPH08510497A (en) |
KR (1) | KR100300468B1 (en) |
CN (1) | CN1077111C (en) |
AT (2) | ATE186056T1 (en) |
BG (1) | BG62854B1 (en) |
BR (1) | BR9406535A (en) |
CA (1) | CA2161432C (en) |
CZ (1) | CZ289037B6 (en) |
DE (2) | DE69408450T2 (en) |
DZ (1) | DZ1782A1 (en) |
EG (1) | EG20361A (en) |
ES (1) | ES2113104T3 (en) |
FI (1) | FI112230B (en) |
GR (1) | GR3025973T3 (en) |
HK (1) | HK1008963A1 (en) |
HU (1) | HU214842B (en) |
IN (1) | IN190621B (en) |
MY (1) | MY121539A (en) |
NO (1) | NO309327B1 (en) |
NZ (1) | NZ266173A (en) |
PL (1) | PL177865B1 (en) |
RO (1) | RO116551B1 (en) |
RU (1) | RU2144042C1 (en) |
SG (1) | SG49037A1 (en) |
SK (1) | SK281033B6 (en) |
TW (1) | TW347397B (en) |
UA (1) | UA40615C2 (en) |
WO (1) | WO1994028032A1 (en) |
ZA (1) | ZA943399B (en) |
Cited By (92)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1996020780A1 (en) * | 1995-01-06 | 1996-07-11 | Bp Chemicals Limited | Twin fluid nozzle |
WO1997018888A1 (en) * | 1995-11-23 | 1997-05-29 | Bp Chemicals Limited | Atomiser nozzle |
FR2741549A1 (en) * | 1995-11-29 | 1997-05-30 | Bp Chemicals Snc | METHOD FOR INTRODUCING A CATALYST INTO A GASEOUS OLEFIN POLYMERIZATION REACTOR |
EP0780404A2 (en) | 1995-12-18 | 1997-06-25 | Union Carbide Chemicals & Plastics Technology Corporation | Improvement in fluidized bed reaction systems using unsupported catalyts |
WO1997025355A1 (en) * | 1996-01-05 | 1997-07-17 | Bp Chemicals Limited | Polymerisation process |
EP0803519A1 (en) | 1996-04-26 | 1997-10-29 | Bp Chemicals S.N.C. | Polymerisation process |
US5698642A (en) * | 1995-07-20 | 1997-12-16 | Montel Technology Company Bv | Process and apparatus for the gas-phase polymerization of α-olefins |
EP0814100A1 (en) * | 1996-06-21 | 1997-12-29 | Bp Chemicals S.N.C. | Polymerisation process |
EP0824118A1 (en) * | 1996-08-13 | 1998-02-18 | BP Chemicals Limited | Polymerisation process |
EP0824114A1 (en) * | 1996-08-13 | 1998-02-18 | Bp Chemicals S.N.C. | Polymerisation process |
EP0824115A1 (en) * | 1996-08-13 | 1998-02-18 | Bp Chemicals S.N.C. | Polymerisation process |
EP0825204A1 (en) * | 1996-08-13 | 1998-02-25 | BP Chemicals Limited | Polymerisation process |
WO1998016562A1 (en) * | 1996-10-17 | 1998-04-23 | Eastman Chemical Company | Method for improved cooling of fluid bed polymer reactor |
WO1998020054A1 (en) * | 1996-11-07 | 1998-05-14 | Buna Sow Leuna Olefinverbund Gmbh | Process for producing polyethylene of very high molecular weight and method for activating the catalyst support |
EP0853091A1 (en) | 1997-01-13 | 1998-07-15 | Bp Chemicals S.N.C. | Polymerisation process |
EP0855411A1 (en) * | 1997-01-24 | 1998-07-29 | BP Chemicals Limited | Gas Phase polymerization process |
WO1998037101A1 (en) * | 1997-02-19 | 1998-08-27 | Union Carbide Chemicals & Plastics Technology Corporation | Improved control of solution catalyst droplet size with an effervescent spray nozzle |
WO1998037102A1 (en) * | 1997-02-19 | 1998-08-27 | Union Carbide Chemicals & Plastics Technology Corporation | Improved control of solution catalyst droplet size with a perpendicular spray nozzle |
WO1998054231A1 (en) * | 1997-05-30 | 1998-12-03 | Union Carbide Chemicals & Plastics Technology Corporation | Improved method of fluidized bed temperature control |
WO1999000430A1 (en) * | 1997-06-27 | 1999-01-07 | Bp Chemicals Limited | Polymerisation process |
WO1999006451A1 (en) * | 1997-07-31 | 1999-02-11 | Union Carbide Chemicals & Plastics Technology Corporation | Control of gas phase polymerization reactions |
WO2000032651A1 (en) * | 1998-11-30 | 2000-06-08 | Bp Chemicals Limited | Polymerisation control process |
FR2792852A1 (en) | 1999-04-30 | 2000-11-03 | Bp Chemicals Snc | Spring nozzle for injecting condensed liquid into polymerisation reactor comprises inlet pipe and sleeve with orifices sliding inside and at pipe end returned by spring |
FR2792853A1 (en) | 1999-04-30 | 2000-11-03 | Bp Chemicals Snc | SPRING NOZZLE WITH 360 DEGREE SLOT, FOR INJECTING LIQUID INTO A FLUIDIZED BED REACTOR |
NL1012082C2 (en) * | 1999-05-18 | 2000-11-21 | Dsm Nv | Fluidised bed reactor. |
US6225422B1 (en) * | 1996-08-13 | 2001-05-01 | Bp Chemicals Limited | Gas fluidized bed polymerization process for olefins |
FR2806327A1 (en) | 2000-03-17 | 2001-09-21 | Bp Chemicals Snc | VARIABLE LIQUID LEVEL NOZZLE |
WO2001087990A1 (en) * | 2000-05-15 | 2001-11-22 | Dsm N.V. | Fluidised bed reactor with asymmetric gas inlet |
US6413900B1 (en) | 1995-08-10 | 2002-07-02 | Exxonmobil Chemical Patents Inc. | Metallocene stabilized alumoxane |
US6451938B1 (en) | 1997-02-25 | 2002-09-17 | Exxon Mobil Chemical Patents Inc. | Polymerization catalyst system comprising heterocyclic fused cyclopentadienide ligands |
US6451726B1 (en) | 1998-08-03 | 2002-09-17 | Basell Poliolefine Italia S.P.A. | Pre-polymerized catalyst components for the polymerization of olefins |
US6469110B1 (en) | 1997-06-24 | 2002-10-22 | Borealis Technology Oy | Process for preparing polypropylene alloys |
US6468938B1 (en) | 1998-03-23 | 2002-10-22 | Basell Technology Company Bv | Prepolymerized catalyst components for the polymerization of olefins |
US6472482B1 (en) | 2000-04-04 | 2002-10-29 | Basell Polyolefine Gmbh | Gas-phase polymerization with direct cooling |
US6479599B1 (en) | 1997-04-04 | 2002-11-12 | Bp Chemicals Limited | Catalyst system for high yield synthesis of polyolefins |
WO2003011920A1 (en) * | 2001-07-31 | 2003-02-13 | Bp Chemicals Limited | Degassing process |
WO2003033550A1 (en) * | 2001-10-17 | 2003-04-24 | Bp Chemicals Limited | Process control for the (co)-polymerisation of olefins |
US6627573B2 (en) | 2000-07-20 | 2003-09-30 | The Dow Chemical Company | Expanded anionic compounds comprising hydroxyl or quiescent reactive functionality and catalyst activators therefrom |
US6716786B1 (en) | 1998-02-20 | 2004-04-06 | The Dow Chemical Company | Supported catalyst comprising expanded anions |
US6943133B2 (en) | 2000-10-20 | 2005-09-13 | Univation Technologies, Llc | Diene functionalized catalyst supports and supported catalyst compositions |
WO2006020624A1 (en) | 2004-08-09 | 2006-02-23 | Dow Global Technologies Inc. | Supported bis(hydroxyarylaryloxy) catalysts for manufacture of polymers |
WO2007025640A1 (en) * | 2005-09-02 | 2007-03-08 | Borealis Technology Oy | Process for polymerizing olefins in the presence of an olefin polymerization catalyst |
US7223711B2 (en) | 2000-05-12 | 2007-05-29 | Basell Polyolefine Gmbh | Pre-polymerized catalyst components for the polymerization of olefins |
US7531606B2 (en) | 2004-05-26 | 2009-05-12 | Chevron Phillips Chemical Company Lp | Method for operating a gas phase polymerization reactor |
WO2009077185A1 (en) * | 2007-12-18 | 2009-06-25 | Basell Polyolefine Gmbh | Gas-phase process for the polymerization of alpha-olefins |
EP2221328A2 (en) | 2004-03-17 | 2010-08-25 | Dow Global Technologies Inc. | Catalyst composition comprising shuttling agent for ethylene multi-block copolymer formation |
US7829495B2 (en) | 1996-07-16 | 2010-11-09 | Exxonmobil Chemical Patents Inc. | Olefin polymerization process with alkyl-substituted metallocenes |
EP2277928A1 (en) | 1998-11-02 | 2011-01-26 | Dow Global Technologies Inc. | Shear thinning ethylene/alpha-olefin interpolymers and their preparation |
US7947787B2 (en) | 2005-09-15 | 2011-05-24 | Dow Global Technologies Llc | Control of polymer architecture and molecular weight distribution via multi-centered shuttling agent |
EP2327727A1 (en) | 2004-03-17 | 2011-06-01 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for ethylene copolymer formation |
US7981992B2 (en) | 2005-03-17 | 2011-07-19 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for regio-irregular multi-block copolymer formation |
EP2357203A2 (en) | 2004-03-17 | 2011-08-17 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for higher olefin multi-block copolymer formation |
EP2357206A2 (en) | 2005-03-17 | 2011-08-17 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for tactic/atactic multi-block copolymer formation |
WO2011136492A2 (en) | 2010-04-30 | 2011-11-03 | 대림산업 주식회사 | Gas-phase polymerization of alpha-olefins |
WO2012072417A1 (en) | 2010-11-29 | 2012-06-07 | Ineos Commercial Services Uk Limited | Polymerisation control process |
US8202953B2 (en) | 2006-05-17 | 2012-06-19 | Dow Global Technologies Llc | High efficiency solution polymerization process |
US8361578B2 (en) | 2007-12-20 | 2013-01-29 | Borealis Technology Oy | Process for coating a pipe with high throughput using multimodal ethylene copolymer, and coated pipes obtained thereof |
US8501881B2 (en) | 2009-11-13 | 2013-08-06 | Borealis Ag | Process for olefin polymerization |
WO2013135564A1 (en) * | 2012-03-16 | 2013-09-19 | Ineos Europe Ag | Process |
WO2013156491A1 (en) | 2012-04-19 | 2013-10-24 | Ineos Europe Ag | Catalyst for the polymerisation of olefins, process for its production and use |
US8765885B2 (en) | 2010-11-29 | 2014-07-01 | Ineos Sales (Uk) Limited | Apparatus and process for the polymerisation of olefins |
US8822602B2 (en) | 2010-11-12 | 2014-09-02 | Borealis Ag | Heterophasic propylene copolymers with stiffness/impact/flowability balance |
US8981021B2 (en) | 2007-03-30 | 2015-03-17 | Univation Technologies, Llc | Systems and methods for fabricating polyolefins |
EP2848635A1 (en) | 2013-09-16 | 2015-03-18 | Ineos Europe AG | Polymerization process |
WO2015097012A1 (en) * | 2013-12-23 | 2015-07-02 | Ineos Europe Ag | Scavenger injection |
WO2015097013A1 (en) | 2013-12-23 | 2015-07-02 | Ineos Europe Ag | Process |
US9175105B2 (en) * | 2005-05-10 | 2015-11-03 | Ineos Sales (Uk) Limited | Copolymers |
US9410009B2 (en) | 2005-03-17 | 2016-08-09 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for tactic/ atactic multi-block copolymer formation |
US20160289348A1 (en) * | 2010-12-20 | 2016-10-06 | Ineos Sales (Uk) Limited | Process and apparatus for the polymerisation of olefins |
WO2016182920A1 (en) | 2015-05-08 | 2016-11-17 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US9540467B2 (en) | 2013-08-14 | 2017-01-10 | Ineos Europe Ag | Polymerization process |
US9663590B2 (en) | 2013-09-10 | 2017-05-30 | Ineos Europe Ag | Process for the (co-)polymerisation of olefins |
WO2018048472A1 (en) * | 2016-09-09 | 2018-03-15 | Exxonmobil Chemical Patents Inc. | Pilot plant scale semi-condensing operation |
WO2018063764A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018063765A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018063767A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018118155A1 (en) | 2016-12-20 | 2018-06-28 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018170056A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170138A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170208A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170248A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170227A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
EP3467077A1 (en) * | 2006-10-03 | 2019-04-10 | Univation Technologies, LLC | System for olefin polymerization |
US10584196B2 (en) | 2015-06-23 | 2020-03-10 | Borealis Ag | Process for producing LLDPE resins |
US10899942B2 (en) | 2016-09-28 | 2021-01-26 | Borealis Ag | Process for producing a coated pipe |
US10982025B2 (en) | 2016-11-25 | 2021-04-20 | Borealis Ag | Process for producing polyolefin film composition and films prepared thereof |
US11041036B2 (en) | 2016-09-27 | 2021-06-22 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US11142591B2 (en) | 2016-12-20 | 2021-10-12 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US11192970B2 (en) | 2016-09-27 | 2021-12-07 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2022010622A1 (en) | 2020-07-07 | 2022-01-13 | Exxonmobil Chemical Patents Inc. | Processes for making 3-d objects from blends of polyethylene and polar polymers |
US11254809B2 (en) | 2017-06-21 | 2022-02-22 | Borealis Ag | Polymer composition and a process for production of the polymer composition |
US11274170B2 (en) | 2016-09-27 | 2022-03-15 | Exxonmobil Chemical Patents Inc. | Polymerization process |
Families Citing this family (590)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6538080B1 (en) * | 1990-07-03 | 2003-03-25 | Bp Chemicals Limited | Gas phase polymerization of olefins |
US6015779A (en) | 1996-03-19 | 2000-01-18 | Energy & Environmental International, L.C. | Methods for forming amorphous ultra-high molecular weight polyalphaolefin drag reducing agents |
JPH10152509A (en) * | 1996-05-14 | 1998-06-09 | Mitsui Chem Inc | Vapor-phase polymerization and vapor-phase polymerization apparatus and blower therefor |
US6069212A (en) * | 1996-08-20 | 2000-05-30 | Bp Amoco Corporation | Transfer of polymer particles between vapor phase polymerization reactors containing quench-cooled subfluidized particulate beds of polymerized monomer |
GB9622715D0 (en) * | 1996-10-31 | 1997-01-08 | Bp Chem Int Ltd | Nozzle |
US6630545B2 (en) | 1997-09-15 | 2003-10-07 | The Dow Chemical Company | Polymerization process |
US6150297A (en) | 1997-09-15 | 2000-11-21 | The Dow Chemical Company | Cyclopentaphenanthrenyl metal complexes and polymerization process |
US6076810A (en) * | 1997-10-21 | 2000-06-20 | Exxon Research And Engineering Co. | Throat and cone gas injector and gas distribution grid for slurry reactor |
US6677265B1 (en) | 1997-12-08 | 2004-01-13 | Albemarle Corporation | Process of producing self-supported catalysts |
DE19801859A1 (en) | 1998-01-20 | 1999-07-22 | Bayer Ag | Prevention of instability in gas phase polymerization of rubber |
JPH11209414A (en) * | 1998-01-29 | 1999-08-03 | Idemitsu Petrochem Co Ltd | Polymerization process of olefin |
US6271321B1 (en) | 1998-02-18 | 2001-08-07 | Eastman Chemical Company | Process for producing polyethylene |
US6191239B1 (en) | 1998-02-18 | 2001-02-20 | Eastman Chemical Company | Process for producing polyethylene |
US6228957B1 (en) | 1998-02-18 | 2001-05-08 | Eastman Chemical Company | Process for producing polyethlene |
US6534613B2 (en) | 1998-02-18 | 2003-03-18 | Eastman Chemical Company | Process for producing polyethylene |
GB9809207D0 (en) | 1998-04-29 | 1998-07-01 | Bp Chem Int Ltd | Novel catalysts for olefin polymerisation |
US6245868B1 (en) | 1998-05-29 | 2001-06-12 | Univation Technologies | Catalyst delivery method, a catalyst feeder and their use in a polymerization process |
DE69935815T2 (en) | 1998-07-01 | 2007-12-27 | Exxonmobil Chemical Patents Inc., Baytown | Elastic mixture with crystal polymers and crystallizable polymers of propene |
US6291613B1 (en) | 1998-10-27 | 2001-09-18 | Eastman Chemical Company | Process for the polymerization of olefins |
ATE528327T1 (en) | 1998-10-27 | 2011-10-15 | Westlake Longview Corp | METHOD FOR POLYMERIZING OLEFINS. |
US6189236B1 (en) * | 1998-11-05 | 2001-02-20 | Union Carbide Chemicals & Plastics Technology Corporation | Process for drying a reactor system employing a fixed bed adsorbent |
US6143843A (en) * | 1999-01-22 | 2000-11-07 | Union Carbide Chemicals & Plastics Technology Corporation | Simulated condensing mode |
US6218484B1 (en) * | 1999-01-29 | 2001-04-17 | Union Carbide Chemicals & Plastics Technology Corporation | Fluidized bed reactor and polymerization process |
US6300432B1 (en) | 1999-03-30 | 2001-10-09 | Eastman Chemical Company | Process for producing polyolefins |
US6313236B1 (en) | 1999-03-30 | 2001-11-06 | Eastman Chemical Company | Process for producing polyolefins |
US6288181B1 (en) | 1999-03-30 | 2001-09-11 | Eastman Chemical Company | Process for producing polyolefins |
BR9917247B1 (en) | 1999-03-30 | 2010-11-30 | process for polymerizing an olefin and / or an olefin and at least one or more other olefin (s), process for reducing the electrostatic charge generated in the polymerization of an olefin and / or an olefin and at least one or more other olefin (s), film, and, article. | |
US6306981B1 (en) * | 1999-04-02 | 2001-10-23 | Union Carbide Chemicals & Plastics Technology Corporation | Gas phase polymerization process |
US6150478A (en) | 1999-06-04 | 2000-11-21 | Union Carbide Chemicals & Plastics Technology Corporation | Ultrasonic catalyst feed for fluid bed olefin polymerization |
US6417299B1 (en) | 1999-06-07 | 2002-07-09 | Eastman Chemical Company | Process for producing ethylene/olefin interpolymers |
US6417298B1 (en) | 1999-06-07 | 2002-07-09 | Eastman Chemical Company | Process for producing ethylene/olefin interpolymers |
US6187879B1 (en) | 1999-08-31 | 2001-02-13 | Eastman Chemical Company | Process for producing polyolefins |
US6191238B1 (en) | 1999-08-31 | 2001-02-20 | Eastman Chemical Company | Process for producing polyolefins |
BR9917469B1 (en) | 1999-08-31 | 2008-11-18 | process for polymerizing an olefin and / or an olefin and at least one or more other olefins, film, and article. | |
US6391985B1 (en) | 1999-10-21 | 2002-05-21 | Union Carbide Chemicals & Plastics Technology Corporation | High condensing mode polyolefin production under turbulent conditions in a fluidized bed |
DE19960415C1 (en) * | 1999-12-15 | 2001-08-16 | Anton More | Method and device for producing silanes |
US6281306B1 (en) | 1999-12-16 | 2001-08-28 | Univation Technologies, Llc | Method of polymerization |
BRPI0107604B1 (en) | 2000-01-12 | 2015-03-31 | Westlake Longview Corp | Solid procatalyst, catalyst system, and process for polymerizing at least one or more olefins |
US6465383B2 (en) | 2000-01-12 | 2002-10-15 | Eastman Chemical Company | Procatalysts, catalyst systems, and use in olefin polymerization |
US6696380B2 (en) | 2000-01-12 | 2004-02-24 | Darryl Stephen Williams | Procatalysts, catalyst systems, and use in olefin polymerization |
FI108001B (en) * | 2000-01-28 | 2001-11-15 | Borealis Polymers Oy | Fluid supply |
US6455644B1 (en) | 2000-02-28 | 2002-09-24 | Union Carbide Chemicals & Plastics Technology Corporation | Polyolefin production using condensing mode in fluidized beds, with liquid phase enrichment and bed injection |
US6815512B2 (en) * | 2000-02-28 | 2004-11-09 | Union Carbide Chemicals & Plastics Technology Corporation | Polyolefin production using condensing mode in fluidized beds, with liquid phase enrichment and bed injection |
US6359083B1 (en) * | 2000-05-02 | 2002-03-19 | Eastman Chemical Company | Olefin polymerization process |
GB0014584D0 (en) * | 2000-06-14 | 2000-08-09 | Bp Chem Int Ltd | Apparatus and process |
US6660812B2 (en) * | 2000-07-13 | 2003-12-09 | Exxonmobil Chemical Patents Inc. | Production of olefin derivatives |
US6548610B2 (en) * | 2000-10-06 | 2003-04-15 | Univation Technologies, Llc | Method and apparatus for reducing static charges during polymerization of olefin polymers |
US6905654B2 (en) | 2000-10-06 | 2005-06-14 | Univation Technologies, Llc | Method and apparatus for reducing static charges during polymerization of olefin polymers |
US6815011B2 (en) | 2000-11-27 | 2004-11-09 | Energy & Environmental International, L.C. | Alpha olefin monomer partitioning agents for drag reducing agents and methods of forming drag reducing agents using alpha olefin monomer partitioning agents |
US6489408B2 (en) * | 2000-11-30 | 2002-12-03 | Univation Technologies, Llc | Polymerization process |
CA2434795C (en) | 2001-01-16 | 2010-01-26 | Energy & Environmental International, L.C. | Methods for forming amorphous ultra-high molecular weight polyolefins for use as drag reducing agents |
DE60238049D1 (en) | 2001-04-12 | 2010-12-02 | Exxonmobil Chem Patents Inc | Process for the polymerization of propylene and ethylene in solution |
US7012046B2 (en) * | 2001-06-08 | 2006-03-14 | Eaton Gerald B | Drag reducing agent slurries having alfol alcohols and processes for forming drag reducing agent slurries having alfol alcohols |
EP1927617A1 (en) | 2001-07-19 | 2008-06-04 | Univation Technologies, LLC | Polyethylene films with improved physical properties. |
US6759492B2 (en) | 2001-07-24 | 2004-07-06 | Eastman Chemical Company | Process for the polymerization of ethylene and interpolymers thereof |
US6646073B2 (en) | 2001-07-24 | 2003-11-11 | Eastman Chemical Company | Process for the polymerization of ethylene and interpolymers thereof |
US6660817B2 (en) | 2001-07-24 | 2003-12-09 | Eastman Chemical Company | Process for the polymerization of ethylene and interpolymers thereof |
US6635726B2 (en) | 2001-07-24 | 2003-10-21 | Eastman Chemical Company | Process for the polymerization of ethylene and interpolymers thereof |
DE10139477A1 (en) * | 2001-08-10 | 2003-02-20 | Basell Polyolefine Gmbh | Optimization of heat removal in a gas phase fluidized bed process for polyethylene production using ethane to increase the heat capacity of the fluidized bed gas |
EP1444276A1 (en) | 2001-11-06 | 2004-08-11 | Dow Global Technologies, Inc. | Isotactic propylene copolymers, their preparation and use |
US6927256B2 (en) | 2001-11-06 | 2005-08-09 | Dow Global Technologies Inc. | Crystallization of polypropylene using a semi-crystalline, branched or coupled nucleating agent |
US6703338B2 (en) | 2002-06-28 | 2004-03-09 | Univation Technologies, Llc | Polymerization catalyst activators, method of preparing, and their use in polymerization processes |
US20050232995A1 (en) * | 2002-07-29 | 2005-10-20 | Yam Nyomi V | Methods and dosage forms for controlled delivery of paliperidone and risperidone |
US20050208132A1 (en) * | 2002-07-29 | 2005-09-22 | Gayatri Sathyan | Methods and dosage forms for reducing side effects of benzisozazole derivatives |
US7179426B2 (en) * | 2002-09-12 | 2007-02-20 | Chevron Phillips Chemical Company, Lp | Large catalyst activator |
ATE432248T1 (en) * | 2002-09-25 | 2009-06-15 | Shell Int Research | METHOD FOR PRODUCING A LINEAR OLEFIN OLIGOMER USING A HEAT EXCHANGER |
CN1684930A (en) * | 2002-09-25 | 2005-10-19 | 国际壳牌研究有限公司 | Process for making a linear alpha-olefin oligomer using a heat exchanger |
US7943700B2 (en) * | 2002-10-01 | 2011-05-17 | Exxonmobil Chemical Patents Inc. | Enhanced ESCR of HDPE resins |
US7414098B2 (en) | 2002-10-09 | 2008-08-19 | Basell Polioefine Italia S.P.A. | Gas-phase catalytic polymerization of olefins |
AU2003302033A1 (en) | 2002-10-15 | 2004-06-15 | Exxonmobil Chemical Patents Inc. | Multiple catalyst system for olefin polymerization and polymers produced therefrom |
US7223822B2 (en) | 2002-10-15 | 2007-05-29 | Exxonmobil Chemical Patents Inc. | Multiple catalyst and reactor system for olefin polymerization and polymers produced therefrom |
WO2004037404A1 (en) * | 2002-10-24 | 2004-05-06 | Exxonmobil Chemical Patents Inc. | Inlet distribution device for upflow polymerization reactors |
US6630548B1 (en) | 2002-11-01 | 2003-10-07 | Equistar Chemicals, Lp | Static reduction |
US7459500B2 (en) * | 2002-11-05 | 2008-12-02 | Dow Global Technologies Inc. | Thermoplastic elastomer compositions |
US7579407B2 (en) * | 2002-11-05 | 2009-08-25 | Dow Global Technologies Inc. | Thermoplastic elastomer compositions |
US20100291334A1 (en) * | 2002-12-27 | 2010-11-18 | Univation Technologies, Llc | Broad Molecular Weight Polyethylene Having Improved Properties |
US6989344B2 (en) * | 2002-12-27 | 2006-01-24 | Univation Technologies, Llc | Supported chromium oxide catalyst for the production of broad molecular weight polyethylene |
US6841498B2 (en) * | 2003-02-12 | 2005-01-11 | Formosa Plastic Corporation, U.S.A. | Catalyst system for ethylene (co)polymerization |
US7365039B2 (en) | 2003-03-21 | 2008-04-29 | Dow Global Technologies Inc. | Morphology controlled olefin polymerization process |
WO2004092228A1 (en) | 2003-04-17 | 2004-10-28 | Basell Poliolefine Italia S.R.L. | Gas-phase olefin polymerization process |
US6759489B1 (en) | 2003-05-20 | 2004-07-06 | Eastern Petrochemical Co. | Fluidized bed methods for making polymers |
AU2004247640B2 (en) * | 2003-05-30 | 2009-12-24 | Univation Technologies, Llc | Gas phase polymerization and method of controlling same |
EP1687346B1 (en) | 2003-11-14 | 2012-06-06 | ExxonMobil Chemical Patents Inc. | Propylene-based elastomers and uses thereof |
US6870010B1 (en) | 2003-12-01 | 2005-03-22 | Univation Technologies, Llc | Low haze high strength polyethylene compositions |
US7410926B2 (en) * | 2003-12-30 | 2008-08-12 | Univation Technologies, Llc | Polymerization process using a supported, treated catalyst system |
US20050182210A1 (en) | 2004-02-17 | 2005-08-18 | Natarajan Muruganandam | De-foaming spray dried catalyst slurries |
WO2005092503A1 (en) * | 2004-03-16 | 2005-10-06 | Union Carbide Chemicals & Plastics Technology Corporation | Aluminum phosphate-supported group 6 metal amide catalysts for oligomerization of ethylene |
GB0411742D0 (en) | 2004-05-26 | 2004-06-30 | Exxonmobil Chem Patents Inc | Transition metal compounds for olefin polymerization and oligomerization |
US7193017B2 (en) * | 2004-08-13 | 2007-03-20 | Univation Technologies, Llc | High strength biomodal polyethylene compositions |
ATE517944T1 (en) * | 2004-10-13 | 2011-08-15 | Exxonmobil Chem Patents Inc | ELASTOMERIC REACTOR BLEND COMPOSITIONS |
US7399874B2 (en) | 2004-10-29 | 2008-07-15 | Exxonmobil Chemical Patents Inc. | Catalyst compound containing divalent tridentate ligand |
US7253239B2 (en) * | 2004-10-29 | 2007-08-07 | Westlake Longview Corporation | Method for preventing or inhibiting fouling in a gas-phase polyolefin polymerization process |
US7829623B2 (en) | 2004-11-05 | 2010-11-09 | Exxonmobil Chemical Patents Inc. | Thermoplastic vulcanizates having improved fabricability |
US7745526B2 (en) | 2004-11-05 | 2010-06-29 | Exxonmobil Chemical Patents Inc. | Transparent polyolefin compositions |
US7598327B2 (en) * | 2004-11-10 | 2009-10-06 | Chevron Phillips Chemical Company Lp | Method for polymerizing olefins in a gas phase reactor using a seedbed during start-up |
US7473750B2 (en) | 2004-12-07 | 2009-01-06 | Fina Technology, Inc. | Random copolymers and formulations useful for thermoforming and blow molding applications |
ATE404628T1 (en) | 2004-12-16 | 2008-08-15 | Exxonmobil Chem Patents Inc | POLYMER COMPOSITIONS INCLUDING THEIR USES AND PRODUCTION METHODS |
US7803876B2 (en) | 2005-01-31 | 2010-09-28 | Exxonmobil Chemical Patent Inc. | Processes for producing polymer blends and polymer blend pellets |
US7312279B2 (en) * | 2005-02-07 | 2007-12-25 | Univation Technologies, Llc | Polyethylene blend compositions |
US7081285B1 (en) | 2005-04-29 | 2006-07-25 | Fina Technology, Inc. | Polyethylene useful for blown films and blow molding |
US20060247394A1 (en) * | 2005-04-29 | 2006-11-02 | Fina Technology, Inc. | Process for increasing ethylene incorporation into random copolymers |
US7645834B2 (en) * | 2005-04-29 | 2010-01-12 | Fina Technologies, Inc. | Catalyst system for production of polyolefins |
US7220806B2 (en) | 2005-04-29 | 2007-05-22 | Fina Technology, Inc. | Process for increasing ethylene incorporation into random copolymers |
US6995235B1 (en) | 2005-05-02 | 2006-02-07 | Univation Technologies, Llc | Methods of producing polyolefins and films therefrom |
EP1731536A1 (en) | 2005-06-09 | 2006-12-13 | Innovene Manufacturing France SAS | Supported polymerisation catalysts |
US20070004876A1 (en) * | 2005-06-22 | 2007-01-04 | Fina Technology, Inc. | Cocatalysts for olefin polymerizations |
US20070003720A1 (en) * | 2005-06-22 | 2007-01-04 | Fina Technology, Inc. | Cocatalysts useful for preparing polyethylene pipe |
US7282546B2 (en) | 2005-06-22 | 2007-10-16 | Fina Technology, Inc. | Cocatalysts for reduction of production problems in metallocene-catalyzed polymerizations |
US20070004875A1 (en) * | 2005-06-22 | 2007-01-04 | Fina Technology, Inc. | Cocatalysts useful for improving polyethylene film properties |
US7634937B2 (en) | 2005-07-01 | 2009-12-22 | Symyx Solutions, Inc. | Systems and methods for monitoring solids using mechanical resonator |
TW200722441A (en) | 2005-09-15 | 2007-06-16 | Dow Global Technologies Inc | Catalytic olefin block copolymers via polymerizable shuttling agent |
US7737206B2 (en) | 2005-11-18 | 2010-06-15 | Exxonmobil Chemical Patents Inc. | Polyolefin composition with high filler loading capacity |
WO2007070041A1 (en) | 2005-12-14 | 2007-06-21 | Exxonmobil Chemical Patents Inc. | Halogen substituted metallocene compounds for olefin polymerization |
DE102006004429A1 (en) * | 2006-01-31 | 2007-08-02 | Advanced Micro Devices, Inc., Sunnyvale | Forming metallization layers for high-density integrated circuit component interconnection, also deposits dielectric material of low permitivity |
US7982085B2 (en) * | 2006-02-03 | 2011-07-19 | Exxonmobil Chemical Patents Inc. | In-line process for generating comonomer |
US8003839B2 (en) * | 2006-02-03 | 2011-08-23 | Exxonmobil Chemical Patents Inc. | Process for generating linear apha olefin comonomers |
WO2007092136A2 (en) * | 2006-02-03 | 2007-08-16 | Exxonmobil Chemical Patents, Inc. | Process for generating alpha olefin comonomers |
US7687672B2 (en) * | 2006-02-03 | 2010-03-30 | Exxonmobil Chemical Patents Inc. | In-line process for generating comonomer |
US7858833B2 (en) * | 2006-02-03 | 2010-12-28 | Exxonmobil Chemical Patents Inc. | Process for generating linear alpha olefin comonomers |
US7714083B2 (en) * | 2006-03-08 | 2010-05-11 | Exxonmobil Chemical Patents Inc. | Recycle of hydrocarbon gases from the product tanks to a reactor through the use of ejectors |
US7683002B2 (en) | 2006-04-04 | 2010-03-23 | Fina Technology, Inc. | Transition metal catalyst and formation thereof |
US20070299222A1 (en) | 2006-04-04 | 2007-12-27 | Fina Technology, Inc. | Transition metal catalysts and formation thereof |
US20070235896A1 (en) * | 2006-04-06 | 2007-10-11 | Fina Technology, Inc. | High shrink high modulus biaxially oriented films |
US20070249793A1 (en) * | 2006-04-19 | 2007-10-25 | Vanderbilt Jeffrey J | Simplified process to prepare polyolefins from saturated hydrocarbons |
US7696289B2 (en) * | 2006-05-12 | 2010-04-13 | Exxonmobil Chemical Patents Inc. | Low molecular weight induced condensing agents |
GB0610667D0 (en) | 2006-05-30 | 2006-07-05 | Nova Chem Int Sa | Supported polymerization catalysts |
US7449529B2 (en) * | 2006-07-11 | 2008-11-11 | Fina Technology, Inc. | Bimodal blow molding resin and products made therefrom |
US7893181B2 (en) * | 2006-07-11 | 2011-02-22 | Fina Technology, Inc. | Bimodal film resin and products made therefrom |
US20080051538A1 (en) * | 2006-07-11 | 2008-02-28 | Fina Technology, Inc. | Bimodal pipe resin and products made therefrom |
US7514510B2 (en) | 2006-07-25 | 2009-04-07 | Fina Technology, Inc. | Fluorenyl catalyst compositions and olefin polymerization process |
US7470759B2 (en) * | 2006-07-31 | 2008-12-30 | Fina Technology, Inc. | Isotactic-atactic polypropylene and methods of making same |
US8198373B2 (en) * | 2006-10-02 | 2012-06-12 | Exxonmobil Chemical Patents Inc. | Plastic toughened plastics |
US7538167B2 (en) * | 2006-10-23 | 2009-05-26 | Fina Technology, Inc. | Syndiotactic polypropylene and methods of preparing same |
US20080114130A1 (en) * | 2006-11-10 | 2008-05-15 | John Ashbaugh | Resin composition for production of high tenacity slit film, monofilaments and fibers |
WO2008079733A1 (en) | 2006-12-15 | 2008-07-03 | Fina Technology, Inc. | Polypropylene blown film |
WO2008082954A1 (en) * | 2006-12-29 | 2008-07-10 | Fina Technology, Inc. | Succinate-containing polymerization catalyst system using n-butylmethyldimethoxysilane for preparation of polypropylene film grade resins |
KR101057854B1 (en) * | 2007-01-22 | 2011-08-19 | 주식회사 엘지화학 | Particle Size Control Method of Polyolefin |
CN103159872B (en) | 2007-03-06 | 2015-08-19 | 尤尼威蒂恩技术有限责任公司 | The method of applying solution catalysts to reactor surfaces |
US7754834B2 (en) * | 2007-04-12 | 2010-07-13 | Univation Technologies, Llc | Bulk density promoting agents in a gas-phase polymerization process to achieve a bulk particle density |
RU2454430C2 (en) | 2007-10-11 | 2012-06-27 | Юнивейшн Текнолоджиз, Ллк | Continuity additives and use thereof in polymerisation processes |
TW200932762A (en) | 2007-10-22 | 2009-08-01 | Univation Tech Llc | Polyethylene compositions having improved properties |
EP2112175A1 (en) | 2008-04-16 | 2009-10-28 | ExxonMobil Chemical Patents Inc. | Activator for metallocenes comprising one or more halogen substituted heterocyclic heteroatom containing ligand coordinated to an alumoxane |
US8129485B2 (en) | 2007-11-27 | 2012-03-06 | Univation Technologies, Llc | Integrated hydrocarbons feed stripper and method of using the same |
PL2072587T3 (en) | 2007-12-20 | 2020-11-02 | Borealis Technology Oy | Coated pipes having improved mechanical properties at elevated temperatures and a method of production thereof |
PL2072586T3 (en) | 2007-12-20 | 2021-05-31 | Borealis Technology Oy | Coated pipes having improved mechanical properties and a method of production thereof |
EP2072589A1 (en) | 2007-12-20 | 2009-06-24 | Borealis Technology Oy | Process for coating a pipe with high throughput using multimodal ethylene copolymer, and coated pipes obtained thereof |
EP2112173A1 (en) | 2008-04-16 | 2009-10-28 | ExxonMobil Chemical Patents Inc. | Catalyst compounds and use thereof |
ES2666896T3 (en) | 2007-12-24 | 2018-05-08 | Borealis Technology Oy | Reactor system and process for the catalytic polymerization of olefins and the use of such a reactor system in the catalytic polymerization of olefins |
EP2082797A1 (en) | 2007-12-24 | 2009-07-29 | Borealis Technology OY | Reactor system for the catalytic polymerization of olefins comprising shielding means and a process and use thereof |
EP2090356A1 (en) | 2007-12-24 | 2009-08-19 | Borealis Technology OY | Reactor systems and process for the catalytic polymerization of olefins, and the use of such reactor system in catalytic polymeration of olefins |
EP2222725B1 (en) * | 2007-12-27 | 2019-06-19 | Univation Technologies, LLC | Systems and methods for removing entrained particulates from gas streams |
US8476365B2 (en) * | 2008-01-24 | 2013-07-02 | Dow Global Technologies, Llc | Method for gas phase polymerization |
US8859084B2 (en) * | 2008-01-29 | 2014-10-14 | Fina Technology, Inc. | Modifiers for oriented polypropylene |
US8003741B2 (en) | 2008-02-07 | 2011-08-23 | Fina Technology, Inc. | Ziegler-Natta catalyst |
US20090202770A1 (en) * | 2008-02-08 | 2009-08-13 | Fengkui Li | Polypropylene/polyisobutylene blends and films prepared from same |
WO2010074994A1 (en) | 2008-12-22 | 2010-07-01 | Univation Technologies, Llc | Systems and methods for fabricating polymers |
MX2010009313A (en) * | 2008-02-26 | 2010-11-09 | Liquamelt Corp | Energy-activated room temperature-pumpable polymer compositions and devices for activating and dispensing the same. |
EP2103632A1 (en) | 2008-03-20 | 2009-09-23 | Ineos Europe Limited | Polymerisation process |
BRPI0910770A2 (en) * | 2008-04-22 | 2015-09-29 | Univation Tech Llc | reactor system and processes for their use |
WO2009144144A1 (en) | 2008-05-27 | 2009-12-03 | Basell Poliolefine Italia S.R.L. | Process for the gas-phase polymerization of olefins |
EP2130859A1 (en) | 2008-06-02 | 2009-12-09 | Borealis AG | Polymer compositions having improved homogeneity and odour, a method for making them and pipes made thereof |
EP2130862A1 (en) | 2008-06-02 | 2009-12-09 | Borealis AG | Polymer compositions and pressure-resistant pipes made thereof |
EP2130863A1 (en) | 2008-06-02 | 2009-12-09 | Borealis AG | High density polymer compositions, a method for their preparation and pressure-resistant pipes made therefrom |
EP2133367A1 (en) | 2008-06-09 | 2009-12-16 | INEOS Manufacturing Belgium NV | Novel Copolymers |
US8545971B2 (en) * | 2008-06-30 | 2013-10-01 | Fina Technology, Inc. | Polymeric compositions comprising polylactic acid and methods of making and using same |
US8268913B2 (en) * | 2008-06-30 | 2012-09-18 | Fina Technology, Inc. | Polymeric blends and methods of using same |
US8759446B2 (en) * | 2008-06-30 | 2014-06-24 | Fina Technology, Inc. | Compatibilized polypropylene and polylactic acid blends and methods of making and using same |
US8580902B2 (en) | 2008-08-01 | 2013-11-12 | Exxonmobil Chemical Patents Inc. | Catalyst system, process for olefin polymerization, and polymer compositions produced therefrom |
CN103951769A (en) | 2008-08-01 | 2014-07-30 | 埃克森美孚化学专利公司 | Catalyst system and process for olefin polymerization |
US8378040B2 (en) | 2008-09-24 | 2013-02-19 | Univation Technologies, Llc | Methods for cleaning the distributor plate in a fluidized bed reactor system |
CA2736415A1 (en) | 2008-09-25 | 2010-04-01 | Basell Polyolefine Gmbh | Impact resistant lldpe composition and films made thereof |
JP2012503687A (en) | 2008-09-25 | 2012-02-09 | バーゼル・ポリオレフィン・ゲーエムベーハー | Impact resistant LLDPE composition and film produced therefrom |
US9334342B2 (en) | 2008-10-01 | 2016-05-10 | Fina Technology, Inc. | Polypropylene for reduced plate out in polymer article production processes |
EP2177548A1 (en) | 2008-10-14 | 2010-04-21 | Ineos Europe Limited | Copolymers and films thereof |
BRPI0920267A2 (en) * | 2008-10-15 | 2016-02-10 | Univation Tech Llc | circulating fluidized bed reactor |
EP2182526A1 (en) | 2008-10-31 | 2010-05-05 | Borealis AG | Cable and polymer composition comprising an multimodal ethylene copolymer |
EP2182524A1 (en) | 2008-10-31 | 2010-05-05 | Borealis AG | Cable and Polymer composition comprising a multimodal ethylene copolymer |
EP2182525A1 (en) | 2008-10-31 | 2010-05-05 | Borealis AG | Cable and polymer composition comprising a multimodal ethylene copolymer |
US20100119855A1 (en) * | 2008-11-10 | 2010-05-13 | Trazollah Ouhadi | Thermoplastic Elastomer with Excellent Adhesion to EPDM Thermoset Rubber and Low Coefficient of Friction |
ATE551369T1 (en) | 2008-11-17 | 2012-04-15 | Borealis Ag | MULTI-STEP PROCESS FOR PRODUCING POLYETHYLENE WITH REDUCED GEL FORMATION |
EP2361268B1 (en) | 2008-12-22 | 2012-11-07 | Univation Technologies, LLC | Systems and methods for fabricating polymers |
WO2010080871A1 (en) | 2009-01-08 | 2010-07-15 | Univation Technologies, Llc | Additive for gas phase polymerization processes |
WO2010080870A2 (en) | 2009-01-08 | 2010-07-15 | Univation Technologies,Llc | Additive for polyolefin polymerization processes |
EP2223943B1 (en) | 2009-02-25 | 2011-10-19 | Borealis AG | Multimodal polymer of propylene, composition containing the same and a process for manufacturing the same |
EP2223944A1 (en) | 2009-02-26 | 2010-09-01 | Borealis AG | Process for producing semicrystalline propylene polymers |
US20100247887A1 (en) | 2009-03-26 | 2010-09-30 | Fina Technology, Inc. | Polyolefin films for in-mold labels |
US8653198B2 (en) | 2009-03-26 | 2014-02-18 | Fina Technology, Inc. | Method for the preparation of a heterophasic copolymer and uses thereof |
US9090000B2 (en) | 2009-03-26 | 2015-07-28 | Fina Technology, Inc. | Injection stretch blow molded articles and random copolymers for use therein |
CN101927141B (en) * | 2009-06-19 | 2012-07-04 | 中国石油化工股份有限公司 | Method for transferring polymer particles among gas-phase polymerization reactors |
RU2011152483A (en) | 2009-07-23 | 2013-06-27 | Юнивейшн Текнолоджиз, Ллк | REACTION SYSTEM FOR POLYMERIZATION |
US8957167B2 (en) | 2009-07-28 | 2015-02-17 | Univation Technologies, Llc | Polymerization process using a supported constrained geometry catalyst |
ES2858349T3 (en) | 2009-07-29 | 2021-09-30 | Dow Global Technologies Llc | Multi-headed chain transport agents and their use for the preparation of block copolymers |
US9174384B2 (en) * | 2009-09-01 | 2015-11-03 | Fina Technology, Inc. | Multilayer polypropylene films and methods of making and using same |
WO2011058089A1 (en) | 2009-11-13 | 2011-05-19 | Borealis Ag | Process for producing a polymerization catalyst |
EP2322568B1 (en) | 2009-11-13 | 2013-05-15 | Borealis AG | Process for producing an olefin polymerization catalyst |
US8603933B2 (en) | 2009-11-13 | 2013-12-10 | Borealis Ag | Process for recovering a transition metal compound |
US8425924B2 (en) | 2009-11-24 | 2013-04-23 | Exxonmobil Chemical Patents Inc. | Propylene compositions containing a pyrethroid and products made therefrom |
US8722820B2 (en) | 2009-12-07 | 2014-05-13 | Univation Technologies, Llc | Methods for reducing static charge of a catalyst and methods for using the catalyst to produce polyolefins |
WO2011075258A1 (en) | 2009-12-18 | 2011-06-23 | Univation Technologies, Llc | Methods for making polyolefin products having different shear thinning properties and haze |
WO2011078923A1 (en) | 2009-12-23 | 2011-06-30 | Univation Technologies, Llc | Methods for producing catalyst systems |
US8592535B2 (en) | 2010-01-11 | 2013-11-26 | Fina Technology, Inc. | Ziegler-natta catalyst systems and polymers formed therefrom |
EP2348056A1 (en) | 2010-01-26 | 2011-07-27 | Ineos Europe Limited | Process for the gas phase polymerisation of olefins |
CN102803308B (en) | 2010-02-18 | 2015-04-01 | 尤尼威蒂恩技术有限公司 | Methods for operating a polymerization reactor |
US8835582B2 (en) | 2010-02-22 | 2014-09-16 | Univation Technologies, Llc | Catalyst systems and methods for using same to produce polyolefin products |
RU2573325C2 (en) | 2010-02-22 | 2016-01-20 | Инеос Коммершиал Сервисиз Юк Лимитед | Improved method of polyolefin production |
US8058461B2 (en) | 2010-03-01 | 2011-11-15 | Exxonmobil Chemical Patents Inc. | Mono-indenyl transition metal compounds and polymerization therewith |
MY157091A (en) | 2010-04-13 | 2016-04-29 | Univation Tech Llc | Polymer blends and films made therefrom |
US10351640B2 (en) | 2010-04-22 | 2019-07-16 | Fina Technology, Inc. | Formation of Ziegler-Natta catalyst using non-blended components |
EP2397221B1 (en) | 2010-06-17 | 2017-04-12 | Borealis AG | Control system for a gas phase reactor, a gas phase reactor for catalytic production of polyolefines, a method for catalytic productions of polyolefines and a use of the control system |
US8278403B2 (en) | 2010-07-08 | 2012-10-02 | Fina Technology, Inc. | Multi-component catalyst systems and polymerization processes for forming broad composition distribution polymers |
WO2012009215A1 (en) | 2010-07-16 | 2012-01-19 | Univation Technologies, Llc | Systems and methods for measuring static charge on particulates |
WO2012009216A1 (en) | 2010-07-16 | 2012-01-19 | Univation Technologies, Llc | Systems and methods for measuring particle accumulation on reactor surfaces |
GB201012273D0 (en) | 2010-07-22 | 2010-09-08 | Ineos Mfg Belguim Nv | Polymer compositon |
WO2012015898A1 (en) | 2010-07-28 | 2012-02-02 | Univation Technologies, Llc | Systems and methods for measuring velocity of a particle/fluid mixture |
US20120046429A1 (en) | 2010-08-23 | 2012-02-23 | Fina Technology, Inc. | Sequential Formation of Ziegler-Natta Catalyst Using Non-blended Components |
US8557906B2 (en) | 2010-09-03 | 2013-10-15 | Exxonmobil Chemical Patents Inc. | Flame resistant polyolefin compositions and methods for making the same |
KR101821026B1 (en) | 2010-10-21 | 2018-01-22 | 유니베이션 테크놀로지즈, 엘엘씨 | Polyethylene and process for production thereof |
EP2452957A1 (en) | 2010-11-12 | 2012-05-16 | Borealis AG | Improved process for producing heterophasic propylene copolymers |
EP2452960B1 (en) | 2010-11-12 | 2015-01-07 | Borealis AG | Process for preparing propylene polymers with an ultra high melt flow rate |
EP2452959B1 (en) | 2010-11-12 | 2015-01-21 | Borealis AG | Process for producing propylene random copolymers and their use |
WO2012068703A1 (en) | 2010-11-24 | 2012-05-31 | Exxonmobil Asia Pacific Research & Development Co., Ltd. | High filler loaded polymer composition |
SG190429A1 (en) | 2010-11-30 | 2013-06-28 | Univation Tech Llc | Catalyst composition having improved flow characteristics and methods of making and using the same |
CN103228682B (en) | 2010-11-30 | 2015-07-22 | 尤尼威蒂恩技术有限责任公司 | Processes for the polymerization of olefins with extracted metal carboxylate salts |
EP2465876A1 (en) | 2010-12-15 | 2012-06-20 | INEOS Manufacturing Belgium NV | Activating supports |
MX337727B (en) | 2010-12-17 | 2016-03-16 | Univation Tech Llc | Systems and methods for recovering hydrocarbons from a polyolefin purge gas product. |
RU2577324C2 (en) | 2010-12-22 | 2016-03-20 | Юнивейшн Текнолоджиз, Ллк | Additive for methods of polyolefin polymerisation |
US9012359B2 (en) | 2011-01-20 | 2015-04-21 | Ineos Sales (Uk) Limited | Activating supports |
US10711077B2 (en) | 2011-02-07 | 2020-07-14 | Fina Technology, Inc. | Ziegler-natta catalyst composition with controlled morphology |
US8586192B2 (en) | 2011-02-15 | 2013-11-19 | Fina Technology, Inc. | Compatibilized polymeric compositions comprising polyolefin-polylactic acid copolymers and methods of making the same |
US9382347B2 (en) | 2011-02-16 | 2016-07-05 | Fina Technology Inc | Ziegler-Natta catalysts doped with non-group IV metal chlorides |
EP2495038B1 (en) | 2011-03-02 | 2020-09-02 | Borealis AG | A process for the production polymers |
HUE051319T2 (en) | 2011-03-02 | 2021-03-01 | Borealis Ag | High throughput reactor assembly for polymerization of olefins |
CA2734167C (en) | 2011-03-15 | 2018-03-27 | Nova Chemicals Corporation | Polyethylene film |
CA2739969C (en) | 2011-05-11 | 2018-08-21 | Nova Chemicals Corporation | Improving reactor operability in a gas phase polymerization process |
CN103534279B (en) | 2011-05-13 | 2016-08-17 | 尤尼威蒂恩技术有限责任公司 | The carbon monoxide-olefin polymeric being spray-dried and the polymerization using it |
CA2740755C (en) | 2011-05-25 | 2019-01-15 | Nova Chemicals Corporation | Chromium catalysts for olefin polymerization |
US9321859B2 (en) | 2011-06-09 | 2016-04-26 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
CA2742454C (en) | 2011-06-09 | 2018-06-12 | Nova Chemicals Corporation | Methods for controlling ethylene copolymer properties |
US9243092B2 (en) | 2011-06-09 | 2016-01-26 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
US9315591B2 (en) | 2011-06-09 | 2016-04-19 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
US9221935B2 (en) | 2011-06-09 | 2015-12-29 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
CA2742461C (en) | 2011-06-09 | 2018-06-12 | Nova Chemicals Corporation | Modified phosphinimine catalysts for olefin polymerization |
US9127106B2 (en) | 2011-06-09 | 2015-09-08 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
US9127094B2 (en) | 2011-06-09 | 2015-09-08 | Nova Chemicals (International) S.A. | Modified phosphinimine catalysts for olefin polymerization |
EP2535372B1 (en) | 2011-06-15 | 2016-09-14 | Borealis AG | In-situ reactor blend of a Ziegler-Natta catalysed, nucleated polypropylene and a metallocene catalysed polypropylene |
WO2013028283A1 (en) | 2011-08-19 | 2013-02-28 | Univation Technologies, Llc | Catalyst systems and methods for using same to produce polyolefin products |
CA2749835C (en) | 2011-08-23 | 2018-08-21 | Nova Chemicals Corporation | Feeding highly active phosphinimine catalysts to a gas phase reactor |
EP2570455A1 (en) | 2011-09-16 | 2013-03-20 | Borealis AG | Polyethylene composition with broad molecular weight distribution and improved homogeneity |
ES2729280T3 (en) | 2011-11-08 | 2019-10-31 | Univation Tech Llc | Methods to produce polyolefins with catalytic systems |
KR102022132B1 (en) | 2011-11-08 | 2019-09-17 | 유니베이션 테크놀로지즈, 엘엘씨 | Methods of preparing a catalyst system |
RU2014124115A (en) | 2011-11-15 | 2015-12-27 | В.Р.Грейс Энд Ко.-Конн. | METHOD OF POLYMERIZATION OF PROPYLENE |
EP2594333B1 (en) | 2011-11-21 | 2014-07-30 | Borealis AG | Method for recovering polymer and apparatus therefor |
SG11201402631YA (en) | 2011-11-30 | 2014-08-28 | Univation Tech Llc | Methods and systems for catalyst delivery |
EP2785786B1 (en) | 2011-12-01 | 2018-05-30 | Ineos Europe AG | Polymer blends |
EP2599828A1 (en) | 2011-12-01 | 2013-06-05 | Borealis AG | Multimodal polyethylene composition for the production of pipes with improved slow crack growth resistance |
CA2760264C (en) | 2011-12-05 | 2018-08-21 | Nova Chemicals Corporation | Passivated supports for use with olefin polymerization catalysts |
EP2791189B1 (en) | 2011-12-14 | 2018-05-02 | Ineos Europe AG | Novel polymers |
US8580893B2 (en) | 2011-12-22 | 2013-11-12 | Fina Technology, Inc. | Methods for improving multimodal polyethylene and films produced therefrom |
EP2617741B1 (en) | 2012-01-18 | 2016-01-13 | Borealis AG | Process for polymerizing olefin polymers in the presence of a catalyst system and a method of controlling the process |
WO2013110727A2 (en) | 2012-01-26 | 2013-08-01 | Ineos Europe Ag | Copolymers for wire and cable applications |
ES2752139T3 (en) | 2012-03-05 | 2020-04-03 | Univation Tech Llc | Methods for preparing catalyst compositions and polymeric products produced therefrom |
CA2798855C (en) | 2012-06-21 | 2021-01-26 | Nova Chemicals Corporation | Ethylene copolymers having reverse comonomer incorporation |
US9115233B2 (en) | 2012-06-21 | 2015-08-25 | Nova Chemicals (International) S.A. | Ethylene copolymer compositions, film and polymerization processes |
WO2014023637A1 (en) | 2012-08-06 | 2014-02-13 | Ineos Europe Ag | Polymerisation process |
US9382359B2 (en) | 2012-08-29 | 2016-07-05 | Borealis Ag | Reactor assembly and method for polymerization of olefins |
WO2014065989A1 (en) | 2012-10-26 | 2014-05-01 | Exxonmobil Chemical Patents Inc. | Polymer blends and articles made therefrom |
US10221263B2 (en) | 2012-11-01 | 2019-03-05 | Univation Technologies, Llc | Mixed compatible Ziegler-Natta / chromium catalysts for improved polymer products |
US9587993B2 (en) * | 2012-11-06 | 2017-03-07 | Rec Silicon Inc | Probe assembly for a fluid bed reactor |
EP2730611B1 (en) | 2012-11-09 | 2017-01-04 | Abu Dhabi Polymers Company Limited (Borouge) | Drip irrigation pipe comprising a polymer composition comprising a multimodal polyethylene base resin |
ES2604934T3 (en) | 2012-11-09 | 2017-03-10 | Abu Dhabi Polymers Company Limited (Borouge) | Polymeric composition comprising a mixture of a multimodal polyethylene and an additional ethylene polymer suitable for the manufacture of a drip irrigation tube |
WO2014074981A1 (en) | 2012-11-12 | 2014-05-15 | Univation Technologies, Llc | Recycle gas cooler systems for gas-phase polymerization processes |
CN104853917A (en) | 2012-11-21 | 2015-08-19 | 埃克森美孚化学专利公司 | Films comprising ethlyene-based polymers and methods of making same |
CA2797620C (en) | 2012-12-03 | 2019-08-27 | Nova Chemicals Corporation | Controlling resin properties in a gas phase polymerization process |
EP2740761B1 (en) | 2012-12-05 | 2016-10-19 | Borealis AG | Polyethylene composition with improved balance of slow crack growth resistance, impact performance and pipe pressure resistance for pipe applications |
CN104837630B (en) | 2012-12-05 | 2017-02-22 | 埃克森美孚化学专利公司 | Ethylene-based polymers and articles made therefrom |
EP2743278A1 (en) * | 2012-12-11 | 2014-06-18 | Basell Polyolefine GmbH | Process for degassing and buffering polyolefin particles obtained by olefin polymerization |
EP2934889A2 (en) | 2012-12-18 | 2015-10-28 | ExxonMobil Chemical Patents Inc. | Polyethylene films and method of making same |
EP2745926A1 (en) | 2012-12-21 | 2014-06-25 | Borealis AG | Gas phase polymerization and reactor assembly comprising a fluidized bed reactor and an external moving bed reactor |
EP2745927A1 (en) | 2012-12-21 | 2014-06-25 | Borealis AG | Fluidized bed reactor with internal moving bed reaction unit |
CA2800056A1 (en) | 2012-12-24 | 2014-06-24 | Nova Chemicals Corporation | Polyethylene blend compositions |
EP2749580B1 (en) | 2012-12-28 | 2016-09-14 | Borealis AG | Process for producing copolymers of propylene |
BR112015015373B1 (en) | 2012-12-28 | 2020-12-15 | Univation Technologies, Llc | METHOD FOR INTEGRATING ALUMINOXAN PRODUCTION IN THE PRODUCTION OF A CATALYST |
US10280283B2 (en) | 2012-12-28 | 2019-05-07 | Univation Technologies, Llc | Supported catalyst with improved flowability |
CN105121015A (en) | 2013-01-14 | 2015-12-02 | 尤尼威蒂恩技术有限责任公司 | Methods for preparing catalyst systems with increased productivity |
US20150353651A1 (en) | 2013-01-30 | 2015-12-10 | Univation Technologies, Llc | Processes for making catalyst compositions having improved flow |
EP2953985B1 (en) | 2013-02-07 | 2023-06-07 | Univation Technologies, LLC | Preparation of polyolefin |
JP6466395B2 (en) * | 2013-03-14 | 2019-02-06 | ダブリュー・アール・グレイス・アンド・カンパニー−コネチカット | Propylene / butene interpolymer production system and method |
JP2016512275A (en) | 2013-03-15 | 2016-04-25 | ユニベーション・テクノロジーズ・エルエルシー | Ligand for catalyst |
CN105143281B (en) | 2013-03-15 | 2018-06-01 | 尤尼威蒂恩技术有限责任公司 | For three tooth nitrogen class ligands of olefin polymerization catalysis |
PL2796501T3 (en) | 2013-04-22 | 2017-01-31 | Abu Dhabi Polymers Company Limited (Borouge) | Multimodal polypropylene composition for pipe applications |
EP2796499B1 (en) | 2013-04-22 | 2018-05-30 | Abu Dhabi Polymers Company Limited (Borouge) | Polypropylene composition with improved impact resistance for pipe applications |
ES2632593T3 (en) | 2013-04-22 | 2017-09-14 | Borealis Ag | Two-stage process of producing polypropylene compositions |
EP2796498B1 (en) | 2013-04-22 | 2018-09-12 | Abu Dhabi Polymers Company Limited (Borouge) | Multimodal polypropylene composition for pipe applications |
EP2796473B1 (en) | 2013-04-22 | 2017-05-31 | Borealis AG | Multistage process for producing low-temperature resistant polypropylene compositions |
PL2796500T3 (en) | 2013-04-22 | 2018-12-31 | Abu Dhabi Polymers Company Limited (Borouge) | Propylene random copolymer composition for pipe applications |
EP2796474B1 (en) | 2013-04-22 | 2018-01-10 | Borealis AG | Multistage process for producing polypropylene compositions |
CN105209505B (en) | 2013-05-14 | 2017-04-19 | 埃克森美孚化学专利公司 | Ethylene-based polymers and articles made therefrom |
US9604893B2 (en) | 2013-06-05 | 2017-03-28 | Univation Technologies, Llc | Protecting phenol groups |
US20160102429A1 (en) | 2013-07-02 | 2016-04-14 | Exxonmobil Chemical Patents Inc. | Carpet Backing Compositions and Carpet Backing Comprising the Same |
KR102205747B1 (en) * | 2013-09-12 | 2021-01-20 | 더블유.알. 그레이스 앤드 캄파니-콘. | Gas-phase polymerization process with wet zone |
EP2853562A1 (en) | 2013-09-27 | 2015-04-01 | Borealis AG | Two-stage process for producing polypropylene compositions |
EP2860203B1 (en) | 2013-10-10 | 2016-12-14 | Borealis AG | Multistage process for producing polyethylene compositions |
EP2860204B1 (en) | 2013-10-10 | 2018-08-01 | Borealis AG | Polyethylene composition for pipe applications |
EP2860201A1 (en) | 2013-10-10 | 2015-04-15 | Borealis AG | High temperature resistant polyethylene and process for the production thereof |
EP2860202B1 (en) | 2013-10-10 | 2018-05-30 | Borealis AG | High temperature resistant polyethylene and process for the production thereof |
EP2860200B1 (en) | 2013-10-10 | 2017-08-02 | Borealis AG | Polyethylene composition for pipe and pipe coating applications |
CA2933157C (en) | 2013-12-09 | 2021-11-16 | Univation Technologies, Llc | Feeding polymerization additives to polymerization processes |
EP2883885A1 (en) | 2013-12-13 | 2015-06-17 | Borealis AG | Multistage process for producing polyethylene compositions |
EP2883887A1 (en) | 2013-12-13 | 2015-06-17 | Borealis AG | Multistage process for producing polyethylene compositions |
US9206293B2 (en) | 2014-01-31 | 2015-12-08 | Fina Technology, Inc. | Polyethyene and articles produced therefrom |
ES2944883T3 (en) | 2014-02-11 | 2023-06-26 | Univation Tech Llc | Production of polyolefin products |
CA2943378C (en) | 2014-04-02 | 2023-09-12 | Univation Technologies, Llc | Continuity compositions and methods of making and using the same |
FR3020578B1 (en) * | 2014-05-05 | 2021-05-14 | Total Raffinage Chimie | INJECTION DEVICE, ESPECIALLY FOR INJECTING A LOAD OF HYDROCARBONS IN A REFINING UNIT. |
CN106458883A (en) | 2014-06-11 | 2017-02-22 | 弗纳技术股份有限公司 | Chlorine-resistant polyethylene compound and articles made therefrom |
US9624321B2 (en) | 2014-06-13 | 2017-04-18 | Fina Technology, Inc. | Formation of a Ziegler-Natta catalyst |
US9650448B2 (en) | 2014-06-13 | 2017-05-16 | Fina Technology, Inc. | Formation of a Ziegler-Natta catalyst |
CN106459284A (en) | 2014-06-16 | 2017-02-22 | 尤尼威蒂恩技术有限责任公司 | Polyethylene resins |
MX2016016258A (en) | 2014-06-16 | 2017-05-01 | Univation Tech Llc | Methods of modifying the melt flow ratio and/or swell of polyethylene resins. |
WO2016028277A1 (en) | 2014-08-19 | 2016-02-25 | Univation Technologies, Llc | Fluorinated catalyst supports and catalyst systems |
EP3183057A1 (en) | 2014-08-19 | 2017-06-28 | Univation Technologies, LLC | Fluorinated catalyst supports and catalyst systems |
EP3183059A1 (en) | 2014-08-19 | 2017-06-28 | Univation Technologies, LLC | Fluorinated catalyst supports and catalyst systems |
EP2995631A1 (en) | 2014-09-12 | 2016-03-16 | Borealis AG | Process for producing graft copolymers on polyolefin backbone |
US10196508B2 (en) | 2014-10-24 | 2019-02-05 | Exxonmobil Chemical Patents Inc. | Thermoplastic vulcanizate compositions |
CA2870027C (en) | 2014-11-07 | 2022-04-26 | Matthew Zaki Botros | Blow molding composition and process |
CA2871463A1 (en) | 2014-11-19 | 2016-05-19 | Nova Chemicals Corporation | Passivated supports: catalyst, process and product |
ES2930262T3 (en) | 2014-11-26 | 2022-12-09 | Borealis Ag | film layer |
KR101907331B1 (en) | 2014-11-26 | 2018-10-11 | 보레알리스 아게 | Polyethylene composition for a film layer |
WO2016091803A1 (en) | 2014-12-08 | 2016-06-16 | Borealis Ag | Process for producing pellets of copolymers of propylene |
RU2701923C2 (en) * | 2014-12-09 | 2019-10-02 | Чайна Петролеум Энд Кемикал Корпорейшн | Device for polymerisation of olefins and method of polymerisation of olefins |
CN107001945B (en) | 2014-12-12 | 2020-12-18 | 埃克森美孚研究工程公司 | Aromatic hydrogenation catalyst and use thereof |
WO2016094843A2 (en) | 2014-12-12 | 2016-06-16 | Exxonmobil Chemical Patents Inc. | Olefin polymerization catalyst system comprising mesoporous organosilica support |
WO2016094870A1 (en) | 2014-12-12 | 2016-06-16 | Exxonmobil Chemical Patents Inc. | Olefin polymerization catalyst system comprising mesoporous organosilica support |
US10155826B2 (en) | 2014-12-12 | 2018-12-18 | Exxonmobil Research And Engineering Company | Olefin polymerization catalyst system comprising mesoporous organosilica support |
CA2874344C (en) | 2014-12-15 | 2021-08-31 | Nova Chemicals Corporation | Spheroidal catalyst for olefin polymerization |
EP3237459B1 (en) | 2014-12-22 | 2019-01-30 | SABIC Global Technologies B.V. | Process for transitioning between incompatible catalysts |
KR20170109548A (en) | 2014-12-22 | 2017-09-29 | 사빅 글로벌 테크놀러지스 비.브이. | Method for converting between non-fusable catalysts |
SG11201705607QA (en) | 2015-01-21 | 2017-08-30 | Univation Tech Llc | Methods for controlling polymer chain scission |
SG11201705576YA (en) | 2015-01-21 | 2017-08-30 | Univation Tech Llc | Methods for gel reduction in polyolefins |
WO2016124676A1 (en) | 2015-02-05 | 2016-08-11 | Borealis Ag | Process for producing polyethylene |
EP3053936A1 (en) | 2015-02-06 | 2016-08-10 | Borealis AG | Process for producing copolymers of ethylene with alpha-olefins |
EP3053976A1 (en) | 2015-02-09 | 2016-08-10 | Borealis AG | Adhesive composition |
CA2974878C (en) | 2015-02-20 | 2019-08-20 | Borealis Ag | Process for producing heterophasic copolymers of propylene |
EP3268399B1 (en) | 2015-03-10 | 2021-01-20 | Univation Technologies, LLC | Spray dried catalyst compositions, methods for preparation and use in olefin polymerization processes |
US10494454B2 (en) | 2015-03-24 | 2019-12-03 | Sabic Global Technologies B.V. | Process for transitioning between incompatible catalysts |
EP3274380B1 (en) | 2015-04-20 | 2020-08-19 | ExxonMobil Chemical Patents Inc. | Catalyst composition comprising fluorided support and processes for use thereof |
US10533063B2 (en) | 2015-04-20 | 2020-01-14 | Exxonmobil Chemical Patents Inc. | Supported catalyst systems and processes for use thereof |
US10618989B2 (en) | 2015-04-20 | 2020-04-14 | Exxonmobil Chemical Patents Inc. | Polyethylene composition |
US10195589B2 (en) | 2015-04-20 | 2019-02-05 | Univation Technologies, Llc | Bridged bi-aromatic ligands and olefin polymerization catalysts prepared therefrom |
CN107531601A (en) | 2015-04-20 | 2018-01-02 | 尤尼威蒂恩技术有限责任公司 | Bridging biaryl perfume base ligand and transistion metal compound prepared therefrom |
CN107531839B (en) | 2015-04-24 | 2021-05-25 | 尤尼威蒂恩技术有限责任公司 | Method for operating a polymerization reactor |
EP3288984B1 (en) | 2015-04-27 | 2023-08-09 | Univation Technologies, LLC | Supported catalyst compositions having improved flow properties and preparation thereof |
CA2890606C (en) | 2015-05-07 | 2022-07-19 | Nova Chemicals Corporation | Process for polymerization using dense and spherical ziegler-natta type catalyst |
CN104815779B (en) * | 2015-05-14 | 2017-10-27 | 神华集团有限责任公司 | Gas-phase polymerization system and its spray nozzle device |
CA2891693C (en) | 2015-05-21 | 2022-01-11 | Nova Chemicals Corporation | Controlling the placement of comonomer in an ethylene copolymer |
CA2892552C (en) | 2015-05-26 | 2022-02-15 | Victoria Ker | Process for polymerization in a fluidized bed reactor |
CA2892882C (en) | 2015-05-27 | 2022-03-22 | Nova Chemicals Corporation | Ethylene/1-butene copolymers with enhanced resin processability |
WO2016195824A1 (en) | 2015-05-29 | 2016-12-08 | Exxonmobil Chemical Patents Inc. | Polymerization process using bridged metallocene compounds supported on organoaluminum treated layered silicate supports |
EP3303675A4 (en) | 2015-06-05 | 2019-01-09 | ExxonMobil Chemical Patents Inc. | Spunbond fabrics comprising propylene-based elastomer compositions and methods thereof |
WO2017005867A1 (en) | 2015-07-09 | 2017-01-12 | Ineos Europe Ag | Copolymers and films thereof |
CA2900772C (en) | 2015-08-20 | 2022-07-12 | Nova Chemicals Corporation | Method for altering melt flow ratio of ethylene polymers |
US10577435B2 (en) | 2015-08-26 | 2020-03-03 | Sabic Global Technologies B.V. | Ethylene gas phase polymerisation process |
EP3135694A1 (en) * | 2015-08-27 | 2017-03-01 | SABIC Global Technologies B.V. | Process for continuous polymerization of olefin monomers in a reactor |
KR101749542B1 (en) * | 2015-09-03 | 2017-06-21 | 한택규 | Process for selective oligomerization of Ethylene |
EP3350236B1 (en) | 2015-09-17 | 2023-10-04 | ExxonMobil Chemical Patents Inc. | Polyethylene polymers and articles made therefrom |
EP3353217A4 (en) | 2015-09-24 | 2018-11-07 | ExxonMobil Chemical Patents Inc. | Polymerization process using pyridyldiamido compounds supported on organoaluminum treated layered silicate supports |
EP3356374A1 (en) | 2015-09-30 | 2018-08-08 | Dow Global Technologies LLC | Multi- or dual-headed compositions useful for chain shuttling and process to prepare the same |
US10822433B2 (en) | 2015-12-22 | 2020-11-03 | Sabic Global Technologies B.V. | Process for transitioning between incompatible catalysts |
WO2017139031A1 (en) | 2016-02-10 | 2017-08-17 | Exxonmobil Chemical Patents Inc. | Polyethylene shrink films and processes for making the same |
ES2818733T3 (en) | 2016-03-29 | 2021-04-13 | Univation Tech Llc | Metal complexes |
US10790404B2 (en) | 2016-03-30 | 2020-09-29 | Exxonmobil Chemical Patents Inc. | Thermoplastic vulcanizate compositions for photovoltaic cell applications |
KR102344637B1 (en) | 2016-03-31 | 2021-12-30 | 다우 글로벌 테크놀로지스 엘엘씨 | Olefin Polymerization Catalyst |
EP3436487B1 (en) | 2016-03-31 | 2020-01-22 | Dow Global Technologies LLC | Olefin polymerization catalyst systems and methods of use thereof |
SG11201808185XA (en) | 2016-03-31 | 2018-10-30 | Dow Global Technologies Llc | Olefin polymerization catalyst systems and methods of use thereof |
US11299607B2 (en) | 2016-04-22 | 2022-04-12 | Exxon Mobil Chemical Patents Inc. | Polyethylene sheets |
EP3238938A1 (en) | 2016-04-29 | 2017-11-01 | Borealis AG | Machine direction oriented films comprising multimodal copolymer of ethylene and at least two alpha-olefin comonomers |
US10844529B2 (en) | 2016-05-02 | 2020-11-24 | Exxonmobil Chemicals Patents Inc. | Spunbond fabrics comprising propylene-based elastomer compositions and methods for making the same |
US9803037B1 (en) | 2016-05-03 | 2017-10-31 | Exxonmobil Chemical Patents Inc. | Tetrahydro-as-indacenyl catalyst composition, catalyst system, and processes for use thereof |
EP3452521B1 (en) | 2016-05-03 | 2023-07-12 | ExxonMobil Chemical Patents Inc. | Tetrahydroindacenyl catalyst composition, catalyst system, and processes for use thereof |
EP3464390A1 (en) | 2016-05-27 | 2019-04-10 | ExxonMobil Chemical Patents Inc. | Metallocene catalyst compositions and polymerization process therewith |
CN109415544B (en) | 2016-05-31 | 2022-07-05 | 博里利斯股份公司 | Polymer composition and method for producing the same |
PL3252085T3 (en) | 2016-05-31 | 2023-02-13 | Borealis Ag | Jacket with improved properties |
EP3257879A1 (en) | 2016-06-17 | 2017-12-20 | Borealis AG | Bi- or multimodal polyethylene with low unsaturation level |
US20190144583A1 (en) | 2016-06-17 | 2019-05-16 | Borealis Ag | Bi- or multimodal polyethylene terpolymer with enhanced rheological properties |
EP3472238B1 (en) | 2016-06-17 | 2020-04-15 | Borealis AG | Bi- or multimodal polyethylene with enhanced rheological properties |
EP3257895A1 (en) | 2016-06-17 | 2017-12-20 | Borealis AG | Bi- or multimodal polyethylene terpolymer with enhanced rheological properties |
ES2799148T3 (en) | 2016-06-17 | 2020-12-15 | Borealis Ag | Bi- or multimodal polyethylene with low level of unsaturation |
US20190256695A1 (en) | 2016-06-22 | 2019-08-22 | Borealis Ag | Polymer composition and a process for production of the polymer composition |
KR102301007B1 (en) | 2016-06-23 | 2021-09-10 | 보레알리스 아게 | Process for catalyst deactivation |
WO2018017180A1 (en) | 2016-07-21 | 2018-01-25 | Exxonmobil Chemical Patents Inc. | Rotomolded compositions, articles, and processes for making the same |
CA3038149C (en) | 2016-09-27 | 2023-08-22 | Univation Technologies, Llc | Method for long chain branching control in polyethylene production |
US11066495B2 (en) | 2016-09-30 | 2021-07-20 | Dow Global Technology Llc | Phosphaguanidine group IV metal olefin polymerization catalysts |
KR102459739B1 (en) | 2016-09-30 | 2022-10-28 | 다우 글로벌 테크놀로지스 엘엘씨 | Double-linked phosphoguanidine Group 4 metal complex and olefin polymerization catalyst produced therefrom |
CN109952324B (en) | 2016-09-30 | 2023-06-09 | 陶氏环球技术有限责任公司 | Blocked multi-or double-headed compositions suitable for chain shuttling and methods of making the same |
KR102444560B1 (en) | 2016-09-30 | 2022-09-20 | 다우 글로벌 테크놀로지스 엘엘씨 | Multi- or dual-head components useful for chain shuttling and the process of preparing them |
WO2018063813A1 (en) | 2016-09-30 | 2018-04-05 | Dow Global Technologies Llc | Thioguanidine group iv transition metal catalysts and polymerization systems |
WO2018064339A1 (en) | 2016-09-30 | 2018-04-05 | Dow Global Technologies Llc | Bis-phosphaguanidine and poly-phosphaguanidine ligands with group iv metal catalysts produced therefrom |
BR112019005911B1 (en) | 2016-09-30 | 2022-10-11 | Dow Global Technologies Llc | COMPOSITION AND POLYMERIZATION METHOD |
JP7123040B2 (en) | 2016-09-30 | 2022-08-22 | ダウ グローバル テクノロジーズ エルエルシー | Method for preparing multi-headed or double-headed compositions useful for chain shuttling |
US10730038B2 (en) | 2016-10-05 | 2020-08-04 | Exxonmobil Chemical Patents, Inc. | Metallocene catalysts, catalyst systems, and methods for using the same |
WO2018067289A1 (en) | 2016-10-05 | 2018-04-12 | Exxonmobil Chemical Patents Inc. | Sterically hindered metallocenes, synthesis and use |
WO2018071250A1 (en) | 2016-10-14 | 2018-04-19 | Exxonmobil Chemical Patents Inc. | Oriented films comprising ethylene-based and methods of making same |
CN110062777A (en) | 2016-10-19 | 2019-07-26 | 埃克森美孚化学专利公司 | Hybrid catalyst system and its application method |
WO2018075243A1 (en) | 2016-10-19 | 2018-04-26 | Exxonmobil Chemical Patents Inc. | Supported catalyst systems and methods of using same |
JP6967073B2 (en) | 2016-10-28 | 2021-11-17 | フイナ・テクノロジー・インコーポレーテツドFina Technology, Incorporated | Use of crystallinity-reducing agents in polypropylene for application to BOPP |
EP3538571B1 (en) | 2016-11-08 | 2022-06-01 | Univation Technologies, LLC | Bimodal polyethylene |
KR102454616B1 (en) | 2016-11-08 | 2022-10-18 | 유니베이션 테크놀로지즈, 엘엘씨 | polyethylene composition |
CA3043011A1 (en) | 2016-11-08 | 2018-05-17 | Univation Technologies, Llc | Polyethylene composition |
CN109891221B (en) | 2016-11-17 | 2023-01-24 | 尤尼威蒂恩技术有限责任公司 | Method for measuring solids content in slurry catalyst composition |
JP6934518B2 (en) | 2016-11-18 | 2021-09-15 | エクソンモービル ケミカル パテンツ インコーポレイテッド | Polymerization method using a chromium-containing catalyst |
RU2736712C1 (en) | 2016-11-25 | 2020-11-19 | Бореалис Аг | Novel composition and method |
CA3044897A1 (en) | 2016-11-28 | 2018-05-31 | Univation Technologies, Llc | Producing a polyethylene polymer |
WO2018102091A1 (en) | 2016-12-02 | 2018-06-07 | Exxonmobil Chemical Patents Inc. | Polyethylene films |
WO2018102080A1 (en) | 2016-12-02 | 2018-06-07 | Exxonmobil Chemical Patens Inc. | Olefin polymerization catalyst systems and methods for making the same |
US10023666B2 (en) * | 2016-12-13 | 2018-07-17 | Chevron Phillips Chemical Company Lp | Process for transitioning between low percentage chrome and high percentage chrome catalysts |
US10563055B2 (en) | 2016-12-20 | 2020-02-18 | Exxonmobil Chemical Patents Inc. | Carpet compositions and methods of making the same |
WO2018118258A1 (en) | 2016-12-20 | 2018-06-28 | Exxonmobil Chemical Patents Inc. | Methods for controlling start up conditions in polymerization processes |
CN110267994A (en) | 2016-12-22 | 2019-09-20 | 埃克森美孚化学专利公司 | The olefin Polymerization catalyst compositions of spray drying and the polymerization for using it |
WO2018130539A1 (en) | 2017-01-11 | 2018-07-19 | Sabic Global Technologies B.V. | Chromium oxide catalyst for ethylene polymerization |
EP3568421B1 (en) | 2017-01-11 | 2023-12-27 | SABIC Global Technologies B.V. | Chromium oxide catalyst for ethylene polymerization |
HUE054322T2 (en) | 2017-01-20 | 2021-08-30 | Basell Poliolefine Italia Srl | Method for feeding a fluid to a gas phase polymerization reactor |
US11230614B2 (en) | 2017-02-03 | 2022-01-25 | Exxonmobil Chemical Patent Inc. | Methods for making polyethylene polymers |
CN110431158A (en) | 2017-02-07 | 2019-11-08 | 埃克森美孚化学专利公司 | The method for reducing the catalyst activity loss of Ziegler-Natta catalyst |
MX2019009220A (en) | 2017-02-13 | 2019-09-10 | Univation Tech Llc | Bimodal polyethylene resins. |
WO2018151790A1 (en) | 2017-02-20 | 2018-08-23 | Exxonmobil Chemical Patents Inc. | Hafnocene catalyst compounds and process for use thereof |
WO2018151903A1 (en) | 2017-02-20 | 2018-08-23 | Exxonmobil Chemical Patents Inc. | Supported catalyst systems and processes for use thereof |
WO2018151904A1 (en) | 2017-02-20 | 2018-08-23 | Exxonmobil Chemical Patents Inc. | Group 4 catalyst compounds and process for use thereof |
KR20190112293A (en) | 2017-02-20 | 2019-10-04 | 엑손모빌 케미칼 패턴츠 인코포레이티드 | Group 4 catalyst compound and method of using the same |
CN110637049B (en) | 2017-04-06 | 2022-04-05 | 埃克森美孚化学专利公司 | Cast film and method for producing same |
WO2018191000A1 (en) | 2017-04-10 | 2018-10-18 | Exxonmobil Chemicl Patents Inc. | Methods for making polyolefin polymer compositions |
ES2939177T3 (en) | 2017-05-10 | 2023-04-19 | Univation Tech Llc | Catalyst systems and processes for using them |
CA2969627C (en) | 2017-05-30 | 2024-01-16 | Nova Chemicals Corporation | Ethylene copolymer having enhanced film properties |
WO2018226311A1 (en) | 2017-06-08 | 2018-12-13 | Exxonmobil Chemical Patents Inc. | Polyethylene blends and extrudates and methods of making the same |
ES2786756T3 (en) | 2017-06-20 | 2020-10-13 | Borealis Ag | A method, an arrangement and use of an arrangement for the polymerization of olefins |
CN109135067A (en) | 2017-06-27 | 2019-01-04 | 阿布扎比聚合物有限责任公司(博禄) | For manufacturing the polypropene composition of high-voltage tube |
WO2019022801A1 (en) | 2017-07-24 | 2019-01-31 | Exxonmobil Chemical Patents Inc. | Polyethylene films and methods od making the same |
EP3661984B1 (en) | 2017-08-04 | 2022-01-19 | ExxonMobil Chemical Patents Inc. | Films made from polyethylene compositions and processes for making the same |
WO2019027586A1 (en) | 2017-08-04 | 2019-02-07 | Exxonmobil Chemical Patents Inc. | Mixed catalysts with 2, 6-bis(imino)pyridy| iron complexes and bridged hafnocenes |
WO2019027587A1 (en) | 2017-08-04 | 2019-02-07 | Exxonmobil Chemical Patents Inc. | Polyethylene compositions and films prepared therefrom |
EP3697822A1 (en) | 2017-08-04 | 2020-08-26 | ExxonMobil Chemical Patents Inc. | Mixed catalysts with unbridged hafnocenes with -ch2-sime3 moieties |
SG11202001172PA (en) | 2017-08-28 | 2020-03-30 | Univation Tech Llc | Bimodal polyethylene |
CA3074827A1 (en) | 2017-09-11 | 2019-03-14 | Univation Technologies, Llc | Carbon black-containing bimodal polyethylene composition |
JP6986163B2 (en) | 2017-10-23 | 2021-12-22 | エクソンモービル ケミカル パテンツ インコーポレイテッド | Catalyst system and polymerization method using it |
CN111315567B (en) | 2017-10-24 | 2022-02-25 | 博里利斯股份公司 | Multilayer polymeric film |
CA3079202A1 (en) | 2017-10-27 | 2019-05-02 | Univation Technologies, Llc | Selectively transitioning polymerization processes |
CA3079148A1 (en) | 2017-10-27 | 2019-05-02 | Univation Technologies, Llc | Polyethylene copolymer resins and films |
WO2019094131A1 (en) | 2017-11-13 | 2019-05-16 | Exxonmobil Chemical Patents Inc. | Polyethylene compositions and articles made therefrom |
EP3710499A1 (en) | 2017-11-13 | 2020-09-23 | ExxonMobil Chemical Patents Inc. | Polyethylene compositions and articles made therefrom |
US11111325B2 (en) | 2017-11-15 | 2021-09-07 | Exxonmobil Chemical Patents Inc. | Polymerization processes |
CN111448226B (en) | 2017-11-15 | 2023-08-25 | 埃克森美孚化学专利公司 | Polymerization process |
EP3710501A2 (en) | 2017-11-15 | 2020-09-23 | ExxonMobil Chemical Patents Inc. | Polymerization processes |
CN111356869B (en) | 2017-11-17 | 2022-02-22 | 埃克森美孚化学专利公司 | PE-RT pipeline and manufacturing method thereof |
US10934376B2 (en) | 2017-11-28 | 2021-03-02 | Exxonmobil Chemical Patents Inc. | Polyethylene compositions and films made therefrom |
CN111511781B (en) | 2017-11-28 | 2023-07-11 | 埃克森美孚化学专利公司 | Catalyst system and polymerization process using the same |
WO2019108327A1 (en) | 2017-12-01 | 2019-06-06 | Exxonmobil Chemical Patents Inc. | Films comprising polyethylene composition |
WO2019108977A1 (en) | 2017-12-01 | 2019-06-06 | Exxonmobil Chemical Patents Inc. | Catalyst systems and polymerization processes for using the same |
WO2019112927A1 (en) | 2017-12-05 | 2019-06-13 | Univation Technologies, Llc | Activated spray-dried ziegler-natta catalyst system |
KR102636033B1 (en) | 2017-12-05 | 2024-02-14 | 유니베이션 테크놀로지즈, 엘엘씨 | Modified spray-dried Ziegler-Natta (pre)catalyst system |
US11591417B2 (en) | 2017-12-13 | 2023-02-28 | Exxonmobil Chemical Patents Inc. | Deactivation methods for active components from gas phase polyolefin polymerization processes |
JP7313350B2 (en) | 2017-12-18 | 2023-07-24 | ダウ グローバル テクノロジーズ エルエルシー | Zirconocene-titanocene catalyst system |
JP2021506993A (en) | 2017-12-18 | 2021-02-22 | ダウ グローバル テクノロジーズ エルエルシー | Hafnosen-Titanocene catalytic system |
WO2019162760A1 (en) | 2018-02-05 | 2019-08-29 | Exxonmobil Chemical Patents Inc. A Corporation Of State Of Delaware | Enhanced processability of lldpe by addition of ultra-high molecular weight high density polyethylene |
US11440979B2 (en) | 2018-02-19 | 2022-09-13 | Exxonmobil Chemical Patents Inc. | Catalysts, catalyst systems, and methods for using the same |
WO2019166652A1 (en) | 2018-03-02 | 2019-09-06 | Borealis Ag | Process |
WO2019173030A1 (en) | 2018-03-08 | 2019-09-12 | Exxonmobil Chemical Patents Inc. | Methods of preparing and monitoring a seed bed for polymerization reactor startup |
CN111741988A (en) | 2018-03-19 | 2020-10-02 | 尤尼威蒂恩技术有限责任公司 | Ethylene/1-hexene copolymer |
WO2019182968A1 (en) | 2018-03-19 | 2019-09-26 | Exxonmobil Chemical Patents Inc. | Processes for producing high propylene content pedm using tetrahydroindacenyl catalyst systems |
EP3768774A1 (en) | 2018-03-21 | 2021-01-27 | Borealis AG | Bi- or multimodal polyethylene composition |
US11518825B2 (en) | 2018-03-23 | 2022-12-06 | Univation Technologies, Llc | Catalyst formulations |
WO2019190897A1 (en) | 2018-03-26 | 2019-10-03 | Dow Global Technologies Llc | Spray-dried zirconocene catalyst system |
BR112020018814B1 (en) | 2018-03-28 | 2023-12-12 | Univation Technologies, Llc | BIMODAL POLYETHYLENE COMPOSITION, METHOD FOR PRODUCING A BIMODAL POLYETHYLENE COMPOSITION, MANUFACTURED ARTICLE AND BOTTLE CAP OR CLOSURE |
CN112351987B (en) | 2018-04-26 | 2024-02-02 | 埃克森美孚化学专利公司 | Non-coordinating anionic activators containing cations having large alkyl groups |
US11441023B2 (en) | 2018-04-27 | 2022-09-13 | Exxonmobil Chemical Patents Inc. | Polyethylene films and methods of making the same |
CN112055719B (en) | 2018-05-02 | 2022-11-25 | 埃克森美孚化学专利公司 | Method for scaling-up from pilot plant to larger production facilities |
WO2019217173A1 (en) | 2018-05-02 | 2019-11-14 | Exxonmobil Chemical Patents Inc. | Methods for scale-up from a pilot plant to a larger production facility |
CN112154174B (en) | 2018-05-22 | 2024-02-06 | 埃克森美孚化学专利公司 | Method of forming a film and related computing device |
CN112513109B (en) | 2018-05-24 | 2024-02-02 | 尤尼威蒂恩技术有限责任公司 | Unimodal polyethylene copolymers and films thereof |
EP3807327A1 (en) | 2018-06-12 | 2021-04-21 | Dow Global Technologies Llc | Activator-nucleator formulations |
WO2019241044A1 (en) | 2018-06-13 | 2019-12-19 | Univation Technologies, Llc | Spray-dried ziegler-natta (pro)catalyst systems |
US11945889B2 (en) | 2018-06-13 | 2024-04-02 | Univation Technologies Llc | Bimodal polyethylene copolymer and film thereof |
EP3810666A1 (en) | 2018-06-19 | 2021-04-28 | ExxonMobil Chemical Patents Inc. | Polyethylene compositions and films prepared therefrom |
EP3823999A1 (en) | 2018-07-19 | 2021-05-26 | Borealis AG | Process for the preparation of an uhmwpe homopolymer |
US11649305B2 (en) | 2018-07-31 | 2023-05-16 | Univation Technologies, Llc | Unimodal polyethylene copolymer and film thereof |
EP3830145A1 (en) | 2018-07-31 | 2021-06-09 | Univation Technologies, LLC | Unimodal polyethylene copolymer and film thereof |
BR112021001038B1 (en) | 2018-07-31 | 2024-01-30 | Dow Global Technologies Llc | POLYETHYLENE FORMULATION, E, ARTICLE |
WO2020046664A1 (en) | 2018-08-29 | 2020-03-05 | Univation Technologies, Llc | Method of changing melt rheology property of bimodal polyethylene polymer |
CA3109500A1 (en) | 2018-08-29 | 2020-03-05 | Univation Technologies, Llc | Bimodal polyethylene copolymer and film thereof |
WO2020046406A1 (en) | 2018-08-30 | 2020-03-05 | Exxonmobil Chemical Patents Inc. | Polymerization processes and polymers made therefrom |
US20200087495A1 (en) | 2018-09-14 | 2020-03-19 | Fina Technology, Inc. | Polyethylene and controlled rheology polypropylene polymer blends and methods of use |
WO2020068413A1 (en) | 2018-09-28 | 2020-04-02 | Univation Technologies, Llc | Bimodal polyethylene copolymer composition and pipe made thereof |
WO2020088987A1 (en) | 2018-10-31 | 2020-05-07 | Borealis Ag | Polyethylene composition for high pressure resistant pipes with improved homogeneity |
EP3647645A1 (en) | 2018-10-31 | 2020-05-06 | Borealis AG | Polyethylene composition for high pressure resistant pipes |
US20210395404A1 (en) | 2018-11-01 | 2021-12-23 | Exxonmobil Chemical Patents Inc. | In-line trimming of dry catalyst feed |
EP3873947A1 (en) | 2018-11-01 | 2021-09-08 | ExxonMobil Chemical Patents Inc. | On-line adjustment of mixed catalyst ratio by trim and olefin polymerization with the same |
US20220056168A1 (en) | 2018-11-01 | 2022-02-24 | Exxonmobil Chemical Patents Inc. | Slurry Trim Feeder Modifications |
WO2020092606A1 (en) | 2018-11-01 | 2020-05-07 | Exxonmobil Chemical Patents Inc. | On-line adjustment of mixed catalyst ratio and olefin polymerization |
WO2020092588A1 (en) | 2018-11-01 | 2020-05-07 | Exxonmobil Chemical Patents Inc. | Mixed catalyst systems with properties tunable by condensing agent |
EP3873950A1 (en) | 2018-11-01 | 2021-09-08 | ExxonMobil Chemical Patents Inc. | On-line adjustment of catalysts by trim and olefin polymerization |
SG11202103828RA (en) | 2018-11-06 | 2021-05-28 | Dow Global Technologies Llc | Alkane-soluble non-metallocene precatalysts |
US20210403615A1 (en) | 2018-11-06 | 2021-12-30 | Dow Global Technologies Llc | Method of olefin polymerization using alkane-soluble non-metallocene precatalyst |
SG11202103831TA (en) | 2018-11-06 | 2021-05-28 | Dow Global Technologies Llc | Alkane-soluble non-metallocene precatalysts |
CN113242883B (en) | 2018-11-07 | 2023-09-22 | 北欧化工公司 | Polyolefin compositions with improved impact and whitening resistance |
US20220010114A1 (en) | 2018-11-15 | 2022-01-13 | Abu Dhabi Polymers Co. Ltd (Borouge) L.L.C. | Polymer composition for blow molding applications |
SG11202102809UA (en) | 2018-11-28 | 2021-04-29 | Abu Dhabi Polymers Co Ltd Borouge | Polyethylene composition for film applications |
US20220119564A1 (en) | 2018-11-29 | 2022-04-21 | Borealis Ag | Process to produce a polymer and polymer |
CN113227244A (en) | 2018-12-27 | 2021-08-06 | 埃克森美孚化学专利公司 | Propylene-based spunbond fabrics with faster crystallization time |
EP3902851A1 (en) | 2018-12-28 | 2021-11-03 | Borealis AG | A process for producing polyolefin film composition and films prepared thereof |
WO2020136164A1 (en) | 2018-12-28 | 2020-07-02 | Borealis Ag | A process for producing polyolefin film composition and films prepared thereof |
CN113330041B (en) | 2019-01-25 | 2024-01-12 | Sabic环球技术有限责任公司 | Chromium oxide catalyst for ethylene polymerization |
JP2022522649A (en) | 2019-02-20 | 2022-04-20 | フイナ・テクノロジー・インコーポレーテツド | Polymer composition with low warpage |
CN113677713A (en) | 2019-03-21 | 2021-11-19 | 埃克森美孚化学专利公司 | Process for improving gas phase polymerization |
EP3941950A1 (en) | 2019-03-21 | 2022-01-26 | ExxonMobil Chemical Patents Inc. | Methods for improving production in gas phase polymerization |
EP3715385B1 (en) | 2019-03-26 | 2024-01-31 | SABIC Global Technologies B.V. | Chromium oxide catalyst for ethylene polymerization |
CN113710731A (en) | 2019-04-17 | 2021-11-26 | 埃克森美孚化学专利公司 | Method for improving UV weatherability of thermoplastic vulcanizate |
US20220169762A1 (en) | 2019-04-30 | 2022-06-02 | Dow Global Technologies Llc | Bimodal poly(ethylene-co-1-alkene) copolymer |
CA3137111A1 (en) | 2019-04-30 | 2020-11-05 | Dow Global Technologies Llc | Bimodal poly(ethylene-co-1-alkene) copolymer |
WO2020223142A1 (en) | 2019-04-30 | 2020-11-05 | Dow Global Technologies Llc | Metal-ligand complexes |
SG11202113216TA (en) | 2019-06-10 | 2021-12-30 | Univation Tech Llc | Polyethylene blend |
BR112021025518A2 (en) | 2019-06-24 | 2022-02-01 | Borealis Ag | Process for producing a propylene copolymer and polymerization unit to produce a propylene copolymer |
US20220267649A1 (en) | 2019-07-17 | 2022-08-25 | Exxonmobil Chemical Patents Inc. | Pressure Sensitive Adhesives Comprising Propylene-Ethylene(-Diene) Copolymers |
AU2020316600B2 (en) | 2019-07-22 | 2023-11-30 | Abu Dhabi Polymers Co. Ltd (Borouge) L.L.C. | Single site catalysed multimodal polyethylene composition |
AR119631A1 (en) | 2019-08-26 | 2021-12-29 | Dow Global Technologies Llc | COMPOSITION BASED ON BIMODAL POLYETHYLENE |
US20220332864A1 (en) | 2019-09-05 | 2022-10-20 | Exxonmobil Chemical Patents Inc. | Processes for producing polyolefins and impact copolymers with broad molecular weight distribution and high stiffness |
EP4034577A1 (en) | 2019-09-26 | 2022-08-03 | Univation Technologies, LLC | Bimodal polyethylene homopolymer composition |
EP3835327A1 (en) | 2019-12-09 | 2021-06-16 | Borealis AG | System for producing polyolefin and process for recovering polymerization product from gas phase reactor |
WO2021150377A1 (en) | 2020-01-24 | 2021-07-29 | Exxonmobil Chemical Patents Inc. | Methods for producing bimodal polyolefins and impact copolymers |
WO2021154204A1 (en) | 2020-01-27 | 2021-08-05 | Formosa Plastics Corporation, U.S.A. | Process for preparing catalysts and catalyst compositions |
WO2021154442A1 (en) | 2020-01-31 | 2021-08-05 | Exxonmobil Research And Engineering Company | Polyethylene films having high tear strength |
CN115135681A (en) | 2020-02-17 | 2022-09-30 | 埃克森美孚化学专利公司 | Propylene-based polymer composition with high molecular weight tail |
WO2021173362A1 (en) | 2020-02-24 | 2021-09-02 | Exxonmobil Chemical Patents Inc. | Lewis base catalysts and methods thereof |
US20230159679A1 (en) | 2020-03-18 | 2023-05-25 | Exxonmobil Chemical Patents Inc. | Extrusion Blow Molded Articles and Processes for Making Same |
WO2021188361A1 (en) | 2020-03-20 | 2021-09-23 | Exxonmobil Chemical Patents Inc. | Linear alpha-olefin copolymers and impact copolymers thereof |
WO2021191018A1 (en) | 2020-03-24 | 2021-09-30 | Borealis Ag | Polyethylene composition for a film layer |
KR20220144406A (en) | 2020-03-24 | 2022-10-26 | 보레알리스 아게 | Polyethylene composition for film layer |
CN115397873A (en) | 2020-04-01 | 2022-11-25 | 陶氏环球技术有限责任公司 | Bimodal linear low density polyethylene copolymers |
CA3168710A1 (en) | 2020-04-07 | 2021-10-14 | Nova Chemicals Corporation | High density polyethylene for rigid articles |
CN111482146B (en) * | 2020-04-17 | 2022-02-22 | 中国石油化工股份有限公司 | Three-phase separator, three-phase reactor and three-phase reaction method |
US20230182366A1 (en) | 2020-05-19 | 2023-06-15 | Exxonmobil Chemical Patents Inc. | Extrusion Blow Molded Containers And Processes For Making Same |
KR20230018410A (en) | 2020-05-29 | 2023-02-07 | 다우 글로벌 테크놀로지스 엘엘씨 | Damped Hybrid Catalyst |
EP4157899A1 (en) | 2020-05-29 | 2023-04-05 | Dow Global Technologies LLC | Catalyst systems and processes for producing polyethylene using the same |
BR112022024087A2 (en) | 2020-05-29 | 2022-12-20 | Dow Global Technologies Llc | PROCESS FOR PRODUCING POLYETHYLENE, AND METHOD FOR PREPARING THE CATALYST SYSTEM |
US20230151126A1 (en) | 2020-05-29 | 2023-05-18 | Dow Global Technologies Llc | Attenuated post-metallocene catalysts |
BR112022023898A2 (en) | 2020-05-29 | 2022-12-27 | Dow Global Technologies Llc | METHODS FOR PRODUCING A PRODUCTIVITY ENHANCED NON-METALSCENE CATALYST, FEEDING A PRODUCTIVITY ENHANCED NON-METALLOCENIC CATALYST INTO A Slug Phase, Solution Phase, or Gaseous Phase Polymerization Reactor, and for producing a Polyolefin Polymer, Non-Metallocene Catalyst ENHANCED PRODUCTIVITY, MULTIMODAL CATALYST SYSTEM, POLYOLFIN POLYMER AND MANUFACTURED ARTICLE |
WO2021243214A1 (en) | 2020-05-29 | 2021-12-02 | Dow Global Technologies Llc | Catalyst systems and processes for producing polyethylene using the same |
CA3180272A1 (en) | 2020-05-29 | 2021-12-02 | Bo Liu | Single reactor bimodal polyethylene with improved modulus for extrusion blow molding drum applications |
CN115515991A (en) | 2020-05-29 | 2022-12-23 | 陶氏环球技术有限责任公司 | Attenuated post metallocene catalyst |
US20230144520A1 (en) | 2020-05-29 | 2023-05-11 | Dow Global Technologies Llc | Attenuated post-metallocene catalysts |
BR112022023957A2 (en) | 2020-05-29 | 2023-11-14 | Dow Global Technologies Llc | METHODS FOR CHEMICALLY CONVERTING A UNIMODAL BINDING-METAL PRECATALYST INTO A BIMODAL BINDING-METAL CATALYST AND MANUFACTURING A POLY(ETHYLENE-CO-ALPHA-OLEPHINE) COPOLYMER, POLY(ETHYLENE-CO-ALPHA-OLEPHINE COPOLYMER ), MANUFACTURED ARTICLE, AND, MULTIMODAL CATALYST SYSTEM |
CN116234838A (en) | 2020-07-23 | 2023-06-06 | 博里利斯股份公司 | Multimodal ethylene copolymers |
JP2023538501A (en) | 2020-08-05 | 2023-09-08 | ダウ グローバル テクノロジーズ エルエルシー | Thermoplastic compositions containing recycled polymers and articles made therefrom |
MX2023001205A (en) | 2020-08-05 | 2023-04-14 | Dow Global Technologies Llc | Thermoplastic compositions comprising bimodal polyethylene and articles manufactured therefrom. |
EP4192888A1 (en) | 2020-08-10 | 2023-06-14 | ExxonMobil Chemical Patents Inc. | Methods for delivery of non-aromatic solutions to polymerization reactors |
US20230272195A1 (en) | 2020-08-25 | 2023-08-31 | Exxonmobil Chemical Patents Inc. | High Density Polyethylene Compositions With Exceptional Physical Properties |
KR20220039181A (en) | 2020-09-22 | 2022-03-29 | 주식회사 엘지화학 | Apparatus for preparing oligomer |
EP4217407A1 (en) | 2020-09-22 | 2023-08-02 | Dow Global Technologies LLC | Bimodal polyethylene copolymer and film thereof |
CN116194496A (en) | 2020-09-30 | 2023-05-30 | 尤尼威蒂恩技术有限责任公司 | Bimodal polyethylene copolymers for PE-80 pipe applications |
US20230322972A1 (en) | 2020-10-08 | 2023-10-12 | Exxonmobil Chemical Patents Inc. | Supported Catalyst Systems and Processes for Use Thereof |
KR20230088387A (en) | 2020-10-15 | 2023-06-19 | 다우 글로벌 테크놀로지스 엘엘씨 | Olefin polymerization catalyst with 6-amino-N-aryl azaindole ligand |
CN116490525A (en) | 2020-11-19 | 2023-07-25 | 埃克森美孚化学专利公司 | Polyolefin discharge process and apparatus |
EP4247825A1 (en) | 2020-11-23 | 2023-09-27 | ExxonMobil Chemical Patents Inc. | Metallocene polypropylene prepared using aromatic solvent-free supports |
WO2022108971A1 (en) | 2020-11-23 | 2022-05-27 | Exxonmobil Chemical Patents Inc. | Toluene free supported methylalumoxane precursor |
US20240018278A1 (en) | 2020-11-23 | 2024-01-18 | ExxonMobil Technology and Engineering Company-Chem | Improved Process to Prepare Catalyst from In-Situ Formed Alumoxane |
EP4263706A1 (en) | 2020-12-21 | 2023-10-25 | INEOS Europe AG | Polypropylene blend |
EP4019583B1 (en) | 2020-12-28 | 2024-04-10 | ABU DHABI POLYMERS CO. LTD (BOROUGE) - Sole Proprietorship L.L.C. | Polyethylene composition for film applications with improved toughness and stiffness |
EP4029914A1 (en) | 2021-01-14 | 2022-07-20 | Borealis AG | Heterophasic polyolefin composition |
CN112843968A (en) * | 2021-01-30 | 2021-05-28 | 郑州睿强实验设备有限公司 | Solid-state flue gas treatment device for chemical experiment |
US20240059801A1 (en) | 2021-02-11 | 2024-02-22 | Exxonmobil Chemical Patents Inc. | Processes for polymerizing one or more olefins |
JP2024507772A (en) | 2021-02-15 | 2024-02-21 | ダウ グローバル テクノロジーズ エルエルシー | Method for producing poly(ethylene-co-1-alkene) copolymer with reversed comonomer distribution |
EP4301792A2 (en) | 2021-03-05 | 2024-01-10 | ExxonMobil Chemical Patents Inc. | Processes for making and using slurry catalyst mixtures |
WO2022214420A1 (en) | 2021-04-06 | 2022-10-13 | Sabic Global Technologies B.V. | Chromium based catalyst for ethylene polymerization |
US20220340723A1 (en) | 2021-04-26 | 2022-10-27 | Fina Technology, Inc. | Thin Single-Site Catalyzed Polymer Sheets |
CN117412994A (en) | 2021-06-10 | 2024-01-16 | 陶氏环球技术有限责任公司 | Catalyst composition with modified activity and preparation method thereof |
WO2022258804A1 (en) | 2021-06-11 | 2022-12-15 | Borealis Ag | A process for producing a multimodal ethylene polymer and films prepared therefrom |
CA3231623A1 (en) | 2021-09-20 | 2023-03-23 | Dow Global Technologies Llc | Process of making catalytically-active prepolymer composition and compositions made thereby |
WO2023042155A1 (en) | 2021-09-20 | 2023-03-23 | Nova Chemicals (International) S.A. | Olefin polymerization catalyst system and polymerization process |
WO2023064917A1 (en) | 2021-10-15 | 2023-04-20 | Univation Technologies, Llc | Hdpe lpbm resin using advanced chrome catalyst by polyethylene gas phase technology |
WO2023064921A1 (en) | 2021-10-15 | 2023-04-20 | Univation Technologies, Llc | Hdpe intermediate bulk container resin using advanced chrome catalyst by polyethylene gas phase technology |
WO2023069407A1 (en) | 2021-10-21 | 2023-04-27 | Univation Technologies, Llc | Bimodal poly(ethylene-co-1-alkene) copolymer and blow-molded intermediate bulk containers made therefrom |
WO2023081577A1 (en) | 2021-11-02 | 2023-05-11 | Exxonmobil Chemical Patents Inc. | Polyethylene compositions, articles thereof, and methods thereof |
WO2023096864A1 (en) | 2021-11-23 | 2023-06-01 | Dow Global Technologies Llc | Supported catalyst systems containing a carbon bridged, anthracenyl substituted bis-biphenyl-phenoxy organometallic compound for making polyethylene and poly ethylene copolymer resins in a gas phase polymerization reactor |
WO2023096865A1 (en) | 2021-11-23 | 2023-06-01 | Dow Global Technologies Llc | Supported catalyst systems containing a silocon bridged, anthracenyl substituted bis-biphenyl-phenoxy organometallic compound for making polyethylene and polyethylene copolymer resins in a gas phase polymerization reactor |
WO2023096868A1 (en) | 2021-11-23 | 2023-06-01 | Dow Global Technologies Llc | Supported catalyst systems containing a germanium bridged, anthracenyl substituted bis-biphenyl-phenoxy organometallic compound for making polyethylene and polyethylene copolymer resins in a gas phase polymerization reactor |
WO2023154769A1 (en) | 2022-02-11 | 2023-08-17 | Dow Global Technologies Llc | Bimodal medium density polyethylene compositions suitable for use as microirrigation drip tapes |
CA3221979A1 (en) | 2022-03-22 | 2023-10-05 | Nova Chemicals Corporation | Organometallic complex, olefin polymerization catalyst system and polymerization process |
EP4257640A1 (en) | 2022-04-04 | 2023-10-11 | Borealis AG | Pipe comprising a polypropylene composition |
WO2023239560A1 (en) | 2022-06-09 | 2023-12-14 | Formosa Plastics Corporaton, U.S.A. | Clay composite support-activators and catalyst compositions |
WO2023244901A1 (en) | 2022-06-15 | 2023-12-21 | Exxonmobil Chemical Patents Inc. | Ethylene-based polymers, articles made therefrom, and processes for making same |
WO2023250240A1 (en) | 2022-06-24 | 2023-12-28 | Exxonmobil Chemical Patents Inc. | Low cost processes of in-situ mao supportation and the derived finished polyolefin catalysts |
WO2024025741A1 (en) | 2022-07-27 | 2024-02-01 | Exxonmobil Chemical Patents Inc. | Polypropylene compositions with enhanced strain hardening and methods of producing same |
EP4317216A1 (en) | 2022-08-03 | 2024-02-07 | Abu Dhabi Polymers Co. Ltd (Borouge) LLC | Low density ethylene terpolymer composition |
EP4344869A1 (en) | 2022-09-30 | 2024-04-03 | Borealis AG | Multimodal ethylene copolymer composition and films comprising the same |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0088638A2 (en) * | 1982-03-10 | 1983-09-14 | Montedison S.p.A. | Distributor for a fluidized bed reactor |
EP0089691A2 (en) * | 1982-03-24 | 1983-09-28 | Union Carbide Corporation | Continuous process for the production of polymer in a fluidized bed reactor |
US4640963A (en) * | 1985-02-15 | 1987-02-03 | Standard Oil Company (Indiana) | Method and apparatus for recycle of entrained solids in off-gas from a gas-phase polyolefin reactor |
EP0260154A2 (en) * | 1986-09-12 | 1988-03-16 | Toa Nenryo Kogyo Kabushiki Kaisha | Gas dispersion plate for gas phase polymerization device |
EP0301872A1 (en) * | 1987-07-31 | 1989-02-01 | BP Chemicals Limited | Process for gas phase polymerisation of olefins in a fluidised bed reactor |
EP0173261B1 (en) * | 1984-08-24 | 1991-09-25 | Union Carbide Corporation | Improvements in fluidized bed polymerization reactors |
Family Cites Families (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR1487845A (en) * | 1965-07-27 | 1967-07-07 | Sir Soc Italiana Resine Spa | Process for the polymerization of gaseous vinyl monomers and in particular of alpha-olefins |
GB1110566A (en) * | 1965-07-27 | 1968-04-18 | Sir Soc Italiana Resine Spa | Method of polymerizing gaseous vinyl-type monomers |
DE1720292B2 (en) * | 1967-08-10 | 1975-05-22 | Basf Ag, 6700 Ludwigshafen | Process for the production of propylene polymers |
US3625932A (en) * | 1967-12-26 | 1971-12-07 | Phillips Petroleum Co | Vapor phase polymerization of vinyl chloride in a multiple stage fluidized bed reactor |
US4003712A (en) * | 1970-07-29 | 1977-01-18 | Union Carbide Corporation | Fluidized bed reactor |
US4012573A (en) * | 1970-10-09 | 1977-03-15 | Basf Aktiengesellschaft | Method of removing heat from polymerization reactions of monomers in the gas phase |
FR2177480B1 (en) * | 1972-03-07 | 1974-08-30 | Solvay | |
BE786462R (en) * | 1972-07-19 | 1973-01-19 | Solvay | CHLORIDE POLYMERIZATION PROCESS |
FR2215802A5 (en) * | 1972-12-28 | 1974-08-23 | Solvay | Fluidised bed polymn using cooling liq. injection - with non return valve on nozzles to prevent back flow of powder clogging feed pipes |
JPS56166207A (en) * | 1980-05-27 | 1981-12-21 | Mitsui Petrochem Ind Ltd | Gas-phase polymerization of olefin |
US4287327A (en) * | 1980-09-29 | 1981-09-01 | Standard Oil Company (Indiana) | Process for controlling polymer particle size in vapor phase polymerization |
DE3200725A1 (en) * | 1982-01-13 | 1983-07-21 | Robert Bosch Gmbh, 7000 Stuttgart | BRAKE SYSTEM |
US4543399A (en) * | 1982-03-24 | 1985-09-24 | Union Carbide Corporation | Fluidized bed reaction systems |
US4588790A (en) * | 1982-03-24 | 1986-05-13 | Union Carbide Corporation | Method for fluidized bed polymerization |
US4877587A (en) * | 1984-08-24 | 1989-10-31 | Union Carbide Chemicals And Plastics Company Inc. | Fluidized bed polymerization reactors |
US4933149A (en) * | 1984-08-24 | 1990-06-12 | Union Carbide Chemicals And Plastics Company Inc. | Fluidized bed polymerization reactors |
FR2617411B1 (en) * | 1987-06-30 | 1989-11-17 | Bp Chimie Sa | DEVICE AND METHOD FOR SUPPLYING GAS TO A FLUIDIZED BED APPARATUS |
FR2634212B1 (en) * | 1988-07-15 | 1991-04-19 | Bp Chimie Sa | APPARATUS AND METHOD FOR POLYMERIZATION OF GASEOUS OLEFINS IN A FLUIDIZED BED REACTOR |
FR2642429B1 (en) * | 1989-01-31 | 1991-04-19 | Bp Chimie Sa | PROCESS AND APPARATUS FOR POLYMERIZATION OF GASEOUS OLEFINS IN A FLUIDIZED BED REACTOR |
US5352749A (en) * | 1992-03-19 | 1994-10-04 | Exxon Chemical Patents, Inc. | Process for polymerizing monomers in fluidized beds |
US5436304A (en) * | 1992-03-19 | 1995-07-25 | Exxon Chemical Patents Inc. | Process for polymerizing monomers in fluidized beds |
US5317036A (en) * | 1992-10-16 | 1994-05-31 | Union Carbide Chemicals & Plastics Technology Corporation | Gas phase polymerization reactions utilizing soluble unsupported catalysts |
US5462999A (en) * | 1993-04-26 | 1995-10-31 | Exxon Chemical Patents Inc. | Process for polymerizing monomers in fluidized beds |
WO1994025495A1 (en) * | 1993-05-20 | 1994-11-10 | Exxon Chemical Patents Inc. | Process for polymerizing monomers in fluidized beds |
-
1994
- 1994-05-17 ZA ZA943399A patent/ZA943399B/en unknown
- 1994-05-18 DZ DZ940051A patent/DZ1782A1/en active
- 1994-05-18 IN IN606DE1994 patent/IN190621B/en unknown
- 1994-05-19 BR BR9406535A patent/BR9406535A/en not_active IP Right Cessation
- 1994-05-19 AT AT97201508T patent/ATE186056T1/en active
- 1994-05-19 US US08/256,052 patent/US5541270A/en not_active Expired - Lifetime
- 1994-05-19 SK SK1433-95A patent/SK281033B6/en unknown
- 1994-05-19 WO PCT/GB1994/001074 patent/WO1994028032A1/en active IP Right Grant
- 1994-05-19 PL PL94311280A patent/PL177865B1/en not_active IP Right Cessation
- 1994-05-19 DE DE69408450T patent/DE69408450T2/en not_active Expired - Lifetime
- 1994-05-19 SG SG1996005460A patent/SG49037A1/en unknown
- 1994-05-19 EP EP99101676A patent/EP0926163A3/en not_active Withdrawn
- 1994-05-19 HU HU9503302A patent/HU214842B/en not_active IP Right Cessation
- 1994-05-19 ES ES94915621T patent/ES2113104T3/en not_active Expired - Lifetime
- 1994-05-19 RU RU95122233A patent/RU2144042C1/en not_active IP Right Cessation
- 1994-05-19 AT AT94915621T patent/ATE163017T1/en active
- 1994-05-19 EG EG29094A patent/EG20361A/en active
- 1994-05-19 DE DE69421418T patent/DE69421418T2/en not_active Expired - Lifetime
- 1994-05-19 CN CN94192172A patent/CN1077111C/en not_active Expired - Lifetime
- 1994-05-19 RO RO95-01861A patent/RO116551B1/en unknown
- 1994-05-19 NZ NZ266173A patent/NZ266173A/en unknown
- 1994-05-19 EP EP94915621A patent/EP0699213B1/en not_active Expired - Lifetime
- 1994-05-19 CA CA002161432A patent/CA2161432C/en not_active Expired - Lifetime
- 1994-05-19 JP JP7500343A patent/JPH08510497A/en active Pending
- 1994-05-19 UA UA95104678A patent/UA40615C2/en unknown
- 1994-05-19 CZ CZ19952940A patent/CZ289037B6/en not_active IP Right Cessation
- 1994-05-19 KR KR1019950705119A patent/KR100300468B1/en not_active IP Right Cessation
- 1994-05-19 EP EP97201508A patent/EP0802202B1/en not_active Expired - Lifetime
- 1994-05-20 MY MYPI94001304A patent/MY121539A/en unknown
- 1994-05-20 TW TW083104574A patent/TW347397B/en not_active IP Right Cessation
-
1995
- 1995-10-27 BG BG100102A patent/BG62854B1/en unknown
- 1995-11-17 FI FI955561A patent/FI112230B/en not_active IP Right Cessation
- 1995-11-17 NO NO954648A patent/NO309327B1/en not_active IP Right Cessation
-
1996
- 1996-02-15 US US08/602,013 patent/US5733510A/en not_active Expired - Lifetime
- 1996-02-15 US US08/602,014 patent/US5668228A/en not_active Expired - Lifetime
- 1996-07-09 US US08/678,457 patent/US5804677A/en not_active Expired - Lifetime
-
1998
- 1998-01-21 GR GR980400143T patent/GR3025973T3/en unknown
- 1998-08-04 HK HK98109687A patent/HK1008963A1/en not_active IP Right Cessation
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0088638A2 (en) * | 1982-03-10 | 1983-09-14 | Montedison S.p.A. | Distributor for a fluidized bed reactor |
EP0089691A2 (en) * | 1982-03-24 | 1983-09-28 | Union Carbide Corporation | Continuous process for the production of polymer in a fluidized bed reactor |
EP0173261B1 (en) * | 1984-08-24 | 1991-09-25 | Union Carbide Corporation | Improvements in fluidized bed polymerization reactors |
US4640963A (en) * | 1985-02-15 | 1987-02-03 | Standard Oil Company (Indiana) | Method and apparatus for recycle of entrained solids in off-gas from a gas-phase polyolefin reactor |
EP0260154A2 (en) * | 1986-09-12 | 1988-03-16 | Toa Nenryo Kogyo Kabushiki Kaisha | Gas dispersion plate for gas phase polymerization device |
EP0301872A1 (en) * | 1987-07-31 | 1989-02-01 | BP Chemicals Limited | Process for gas phase polymerisation of olefins in a fluidised bed reactor |
Cited By (150)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100419325B1 (en) * | 1995-01-06 | 2004-05-31 | 비피 케미칼즈 리미티드 | A pair of fluid nozzles |
AU699258B2 (en) * | 1995-01-06 | 1998-11-26 | Bp Chemicals Limited | Twin fluid nozzle |
WO1996020780A1 (en) * | 1995-01-06 | 1996-07-11 | Bp Chemicals Limited | Twin fluid nozzle |
US5698642A (en) * | 1995-07-20 | 1997-12-16 | Montel Technology Company Bv | Process and apparatus for the gas-phase polymerization of α-olefins |
US6413900B1 (en) | 1995-08-10 | 2002-07-02 | Exxonmobil Chemical Patents Inc. | Metallocene stabilized alumoxane |
KR100458668B1 (en) * | 1995-11-23 | 2005-01-15 | 비피 케미칼즈 리미티드 | Nozzle |
US6096839A (en) * | 1995-11-23 | 2000-08-01 | Bp Chemicals Limited | Atomizer nozzle |
AU706078B2 (en) * | 1995-11-23 | 1999-06-10 | Bp Chemicals Limited | Atomiser nozzle |
WO1997018888A1 (en) * | 1995-11-23 | 1997-05-29 | Bp Chemicals Limited | Atomiser nozzle |
CN1094784C (en) * | 1995-11-23 | 2002-11-27 | 英国石油化学品有限公司 | Atomiser nozzle |
EP0776691A1 (en) | 1995-11-29 | 1997-06-04 | BP Chemicals Limited | Process for introducing a solid catalyst into a gas-phase olefin polymerization reactor |
US5922818A (en) * | 1995-11-29 | 1999-07-13 | Bp Chemicals Limited | Process for a gas phase olefin polymerization |
FR2741549A1 (en) * | 1995-11-29 | 1997-05-30 | Bp Chemicals Snc | METHOD FOR INTRODUCING A CATALYST INTO A GASEOUS OLEFIN POLYMERIZATION REACTOR |
EP0780404A2 (en) | 1995-12-18 | 1997-06-25 | Union Carbide Chemicals & Plastics Technology Corporation | Improvement in fluidized bed reaction systems using unsupported catalyts |
AU703936B2 (en) * | 1996-01-05 | 1999-04-01 | Bp Chemicals Limited | Polymerisation process |
WO1997025355A1 (en) * | 1996-01-05 | 1997-07-17 | Bp Chemicals Limited | Polymerisation process |
EP0803519A1 (en) | 1996-04-26 | 1997-10-29 | Bp Chemicals S.N.C. | Polymerisation process |
EP0814100A1 (en) * | 1996-06-21 | 1997-12-29 | Bp Chemicals S.N.C. | Polymerisation process |
US7829495B2 (en) | 1996-07-16 | 2010-11-09 | Exxonmobil Chemical Patents Inc. | Olefin polymerization process with alkyl-substituted metallocenes |
US6225422B1 (en) * | 1996-08-13 | 2001-05-01 | Bp Chemicals Limited | Gas fluidized bed polymerization process for olefins |
EP0825204A1 (en) * | 1996-08-13 | 1998-02-25 | BP Chemicals Limited | Polymerisation process |
EP0824115A1 (en) * | 1996-08-13 | 1998-02-18 | Bp Chemicals S.N.C. | Polymerisation process |
EP0824114A1 (en) * | 1996-08-13 | 1998-02-18 | Bp Chemicals S.N.C. | Polymerisation process |
US5898053A (en) * | 1996-08-13 | 1999-04-27 | Bp Chemicals Limited | Polymerisation process |
EP0824118A1 (en) * | 1996-08-13 | 1998-02-18 | BP Chemicals Limited | Polymerisation process |
US6111036A (en) * | 1996-10-17 | 2000-08-29 | Eastman Chemical Company | Method for improving cooling of fluid bed polymer reactor |
WO1998016562A1 (en) * | 1996-10-17 | 1998-04-23 | Eastman Chemical Company | Method for improved cooling of fluid bed polymer reactor |
WO1998020054A1 (en) * | 1996-11-07 | 1998-05-14 | Buna Sow Leuna Olefinverbund Gmbh | Process for producing polyethylene of very high molecular weight and method for activating the catalyst support |
WO1998030605A1 (en) * | 1997-01-13 | 1998-07-16 | Bp Chemicals Limited | Polymerisation process |
US6437062B1 (en) | 1997-01-13 | 2002-08-20 | Bp Chemicals Limited | Gas phase olefin polymerization process |
AU747055B2 (en) * | 1997-01-13 | 2002-05-09 | Bp Chemicals Limited | Polymerisation process |
KR100580902B1 (en) * | 1997-01-13 | 2006-05-17 | 비피 케미칼즈 리미티드 | Polymerisation process |
EP0853091A1 (en) | 1997-01-13 | 1998-07-15 | Bp Chemicals S.N.C. | Polymerisation process |
EP0855411A1 (en) * | 1997-01-24 | 1998-07-29 | BP Chemicals Limited | Gas Phase polymerization process |
FR2758823A1 (en) * | 1997-01-24 | 1998-07-31 | Bp Chemicals Snc | GAS PHASE POLYMERIZATION PROCESS |
CN1117100C (en) * | 1997-01-24 | 2003-08-06 | 英国石油化学品有限公司 | Gas phase polymerization process |
US6284848B1 (en) | 1997-01-24 | 2001-09-04 | Bp Chemicals Limited | Gas phase polymerization process |
US6362290B2 (en) | 1997-01-24 | 2002-03-26 | Bp Chemicals Limited | Gas phase polymerization process |
US5962606A (en) * | 1997-02-19 | 1999-10-05 | Union Carbide Chemicals & Plastics Technology Corporation | Control of solution catalyst droplet size with an effervescent spray nozzle |
WO1998037101A1 (en) * | 1997-02-19 | 1998-08-27 | Union Carbide Chemicals & Plastics Technology Corporation | Improved control of solution catalyst droplet size with an effervescent spray nozzle |
WO1998037102A1 (en) * | 1997-02-19 | 1998-08-27 | Union Carbide Chemicals & Plastics Technology Corporation | Improved control of solution catalyst droplet size with a perpendicular spray nozzle |
AU721547B2 (en) * | 1997-02-19 | 2000-07-06 | Univation Technologies Llc | Improved control of solution catalyst droplet size with an effervescent spray nozzle |
US6075101A (en) * | 1997-02-19 | 2000-06-13 | Union Carbide Chemicals & Plastics Technology Corporation | Control of solution catalyst droplet size with a perpendicular spray nozzle |
AU738931B2 (en) * | 1997-02-19 | 2001-09-27 | Univation Technologies Llc | Improved control of solution catalyst droplet size with a perpendicular spray nozzle |
US6451938B1 (en) | 1997-02-25 | 2002-09-17 | Exxon Mobil Chemical Patents Inc. | Polymerization catalyst system comprising heterocyclic fused cyclopentadienide ligands |
US6479599B1 (en) | 1997-04-04 | 2002-11-12 | Bp Chemicals Limited | Catalyst system for high yield synthesis of polyolefins |
WO1998054231A1 (en) * | 1997-05-30 | 1998-12-03 | Union Carbide Chemicals & Plastics Technology Corporation | Improved method of fluidized bed temperature control |
US6469110B1 (en) | 1997-06-24 | 2002-10-22 | Borealis Technology Oy | Process for preparing polypropylene alloys |
AU750242B2 (en) * | 1997-06-27 | 2002-07-11 | Bp Chemicals Limited | Polymerisation process |
WO1999000430A1 (en) * | 1997-06-27 | 1999-01-07 | Bp Chemicals Limited | Polymerisation process |
WO1999006451A1 (en) * | 1997-07-31 | 1999-02-11 | Union Carbide Chemicals & Plastics Technology Corporation | Control of gas phase polymerization reactions |
US6716786B1 (en) | 1998-02-20 | 2004-04-06 | The Dow Chemical Company | Supported catalyst comprising expanded anions |
US6468938B1 (en) | 1998-03-23 | 2002-10-22 | Basell Technology Company Bv | Prepolymerized catalyst components for the polymerization of olefins |
US6451726B1 (en) | 1998-08-03 | 2002-09-17 | Basell Poliolefine Italia S.P.A. | Pre-polymerized catalyst components for the polymerization of olefins |
US6797794B2 (en) | 1998-08-03 | 2004-09-28 | Basell Poliolefine Italia S.P.A. | Olefins produced from pre-polymerized catalyst component catalysts |
EP2277928A1 (en) | 1998-11-02 | 2011-01-26 | Dow Global Technologies Inc. | Shear thinning ethylene/alpha-olefin interpolymers and their preparation |
US6586539B2 (en) | 1998-11-30 | 2003-07-01 | Bp Chemicals Limited | Polymerization control process |
EP1484344A3 (en) * | 1998-11-30 | 2005-08-17 | Innovene Europe Limited | Polymerisation control process |
EP1484344A2 (en) * | 1998-11-30 | 2004-12-08 | BP Chemicals Limited | Polymerisation control process |
WO2000032651A1 (en) * | 1998-11-30 | 2000-06-08 | Bp Chemicals Limited | Polymerisation control process |
US6509425B2 (en) | 1999-04-30 | 2003-01-21 | Bp Chemicals Limited | Process for introducing a liquid in a fluidized bed |
WO2000066273A1 (en) | 1999-04-30 | 2000-11-09 | Bp Chemicals Limited | Process for introducing a liquid in a fluidised bed |
KR100707761B1 (en) * | 1999-04-30 | 2007-04-17 | 비피 케미칼즈 리미티드 | Process for introducing a liquid in a fluidised bed |
FR2792853A1 (en) | 1999-04-30 | 2000-11-03 | Bp Chemicals Snc | SPRING NOZZLE WITH 360 DEGREE SLOT, FOR INJECTING LIQUID INTO A FLUIDIZED BED REACTOR |
FR2792852A1 (en) | 1999-04-30 | 2000-11-03 | Bp Chemicals Snc | Spring nozzle for injecting condensed liquid into polymerisation reactor comprises inlet pipe and sleeve with orifices sliding inside and at pipe end returned by spring |
NL1012082C2 (en) * | 1999-05-18 | 2000-11-21 | Dsm Nv | Fluidised bed reactor. |
WO2000069552A1 (en) * | 1999-05-18 | 2000-11-23 | Dsm N.V. | Fluidised bed polymerisation |
FR2806327A1 (en) | 2000-03-17 | 2001-09-21 | Bp Chemicals Snc | VARIABLE LIQUID LEVEL NOZZLE |
US6472482B1 (en) | 2000-04-04 | 2002-10-29 | Basell Polyolefine Gmbh | Gas-phase polymerization with direct cooling |
US7223711B2 (en) | 2000-05-12 | 2007-05-29 | Basell Polyolefine Gmbh | Pre-polymerized catalyst components for the polymerization of olefins |
WO2001087990A1 (en) * | 2000-05-15 | 2001-11-22 | Dsm N.V. | Fluidised bed reactor with asymmetric gas inlet |
US7094901B2 (en) | 2000-07-20 | 2006-08-22 | Dow Global Michigan Technologies Inc. | Expanded anionic compounds comprising hydroxyl or quiescent reactive functionality and catalyst activators therefrom |
US6627573B2 (en) | 2000-07-20 | 2003-09-30 | The Dow Chemical Company | Expanded anionic compounds comprising hydroxyl or quiescent reactive functionality and catalyst activators therefrom |
US6943133B2 (en) | 2000-10-20 | 2005-09-13 | Univation Technologies, Llc | Diene functionalized catalyst supports and supported catalyst compositions |
US7582710B2 (en) | 2001-07-31 | 2009-09-01 | Ineos Europe Limited | Degassing process |
WO2003011920A1 (en) * | 2001-07-31 | 2003-02-13 | Bp Chemicals Limited | Degassing process |
US8114945B2 (en) | 2001-10-17 | 2012-02-14 | Ineos Europe Limited | Process control for the (co)-polymerisation of olefins |
WO2003033550A1 (en) * | 2001-10-17 | 2003-04-24 | Bp Chemicals Limited | Process control for the (co)-polymerisation of olefins |
EP2327727A1 (en) | 2004-03-17 | 2011-06-01 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for ethylene copolymer formation |
EP2357203A2 (en) | 2004-03-17 | 2011-08-17 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for higher olefin multi-block copolymer formation |
EP2221328A2 (en) | 2004-03-17 | 2010-08-25 | Dow Global Technologies Inc. | Catalyst composition comprising shuttling agent for ethylene multi-block copolymer formation |
EP2221329A1 (en) | 2004-03-17 | 2010-08-25 | Dow Global Technologies Inc. | Catalyst composition comprising shuttling agent for ethylene multi-block copolymer formation |
EP2792690A1 (en) | 2004-03-17 | 2014-10-22 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for ethylene multi-block copolymer formation |
US7531606B2 (en) | 2004-05-26 | 2009-05-12 | Chevron Phillips Chemical Company Lp | Method for operating a gas phase polymerization reactor |
WO2006020624A1 (en) | 2004-08-09 | 2006-02-23 | Dow Global Technologies Inc. | Supported bis(hydroxyarylaryloxy) catalysts for manufacture of polymers |
US9410009B2 (en) | 2005-03-17 | 2016-08-09 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for tactic/ atactic multi-block copolymer formation |
US8981028B2 (en) | 2005-03-17 | 2015-03-17 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for tactic/ atactic multi-block copolymer formation |
US7981992B2 (en) | 2005-03-17 | 2011-07-19 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for regio-irregular multi-block copolymer formation |
EP2357206A2 (en) | 2005-03-17 | 2011-08-17 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for tactic/atactic multi-block copolymer formation |
EP3424966A1 (en) | 2005-03-17 | 2019-01-09 | Dow Global Technologies Llc | Catalyst composition comprising shuttling agent for tactic/ atactic multi-block copolymer formation |
EP2894176A1 (en) | 2005-03-17 | 2015-07-15 | Dow Global Technologies LLC | Catalyst composition comprising shuttling agent for regio-irregular multi-block copolymer formation |
US9228030B2 (en) | 2005-05-10 | 2016-01-05 | Ineos Sales (Uk) Limited | Copolymers |
US9175105B2 (en) * | 2005-05-10 | 2015-11-03 | Ineos Sales (Uk) Limited | Copolymers |
EA012959B1 (en) * | 2005-09-02 | 2010-02-26 | Бореалис Текнолоджи Ой | Process for polymerizing olefins in the presence of an olefin polymerization catalyst |
WO2007025640A1 (en) * | 2005-09-02 | 2007-03-08 | Borealis Technology Oy | Process for polymerizing olefins in the presence of an olefin polymerization catalyst |
US7851567B2 (en) | 2005-09-02 | 2010-12-14 | Borealis Technology Oy | Process for polymerizing olefins in the presence of an olefin polymerization catalyst |
US7947787B2 (en) | 2005-09-15 | 2011-05-24 | Dow Global Technologies Llc | Control of polymer architecture and molecular weight distribution via multi-centered shuttling agent |
US8202953B2 (en) | 2006-05-17 | 2012-06-19 | Dow Global Technologies Llc | High efficiency solution polymerization process |
EP3467077A1 (en) * | 2006-10-03 | 2019-04-10 | Univation Technologies, LLC | System for olefin polymerization |
US8981021B2 (en) | 2007-03-30 | 2015-03-17 | Univation Technologies, Llc | Systems and methods for fabricating polyolefins |
US8084557B2 (en) | 2007-12-18 | 2011-12-27 | Basell Polyolefine Gmbh | Gas-phase process for the polymerization of alpha-olefins |
WO2009077185A1 (en) * | 2007-12-18 | 2009-06-25 | Basell Polyolefine Gmbh | Gas-phase process for the polymerization of alpha-olefins |
US8361578B2 (en) | 2007-12-20 | 2013-01-29 | Borealis Technology Oy | Process for coating a pipe with high throughput using multimodal ethylene copolymer, and coated pipes obtained thereof |
US8501881B2 (en) | 2009-11-13 | 2013-08-06 | Borealis Ag | Process for olefin polymerization |
WO2011136492A2 (en) | 2010-04-30 | 2011-11-03 | 대림산업 주식회사 | Gas-phase polymerization of alpha-olefins |
US8058368B1 (en) | 2010-04-30 | 2011-11-15 | Daelim Industrial Co., Ltd. | Gas-phase polymerization of alpha-olefin |
US8822602B2 (en) | 2010-11-12 | 2014-09-02 | Borealis Ag | Heterophasic propylene copolymers with stiffness/impact/flowability balance |
RU2608124C2 (en) * | 2010-11-29 | 2017-01-13 | Инеос Коммершиал Сервисиз Юк Лимитед | Method of controlling polymerisation |
US8765885B2 (en) | 2010-11-29 | 2014-07-01 | Ineos Sales (Uk) Limited | Apparatus and process for the polymerisation of olefins |
WO2012072417A1 (en) | 2010-11-29 | 2012-06-07 | Ineos Commercial Services Uk Limited | Polymerisation control process |
US9394381B2 (en) | 2010-11-29 | 2016-07-19 | Ineos Sales (Uk) Limited | Polymerisation control process |
US9708423B2 (en) * | 2010-12-20 | 2017-07-18 | Ineos Sales (Uk) Limited | Process and apparatus for the polymerisation of olefins |
US20160289348A1 (en) * | 2010-12-20 | 2016-10-06 | Ineos Sales (Uk) Limited | Process and apparatus for the polymerisation of olefins |
US9139673B2 (en) | 2012-03-16 | 2015-09-22 | Ineos Europe Ag | Process for introduction of liquid feeds to a polymerization process |
US9567411B2 (en) | 2012-03-16 | 2017-02-14 | Ineos Europe Ag | Polymerisation process |
US9175120B2 (en) | 2012-03-16 | 2015-11-03 | Ineos Europe Ag | Polymerisation process |
WO2013135564A1 (en) * | 2012-03-16 | 2013-09-19 | Ineos Europe Ag | Process |
US9328183B2 (en) | 2012-03-16 | 2016-05-03 | Ineos Europe Ag | Polymerization process |
US9605091B2 (en) | 2012-03-16 | 2017-03-28 | Ineos Europe Ag | Separation of monomer components from light components |
WO2013156491A1 (en) | 2012-04-19 | 2013-10-24 | Ineos Europe Ag | Catalyst for the polymerisation of olefins, process for its production and use |
US9540467B2 (en) | 2013-08-14 | 2017-01-10 | Ineos Europe Ag | Polymerization process |
US9663590B2 (en) | 2013-09-10 | 2017-05-30 | Ineos Europe Ag | Process for the (co-)polymerisation of olefins |
EP2848635A1 (en) | 2013-09-16 | 2015-03-18 | Ineos Europe AG | Polymerization process |
WO2015097012A1 (en) * | 2013-12-23 | 2015-07-02 | Ineos Europe Ag | Scavenger injection |
US9683063B2 (en) | 2013-12-23 | 2017-06-20 | Ineos Europe Ag | Process |
US9688799B2 (en) | 2013-12-23 | 2017-06-27 | Ineos Europe Ag | Scavenger injection |
WO2015097013A1 (en) | 2013-12-23 | 2015-07-02 | Ineos Europe Ag | Process |
WO2016182920A1 (en) | 2015-05-08 | 2016-11-17 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US10377841B2 (en) | 2015-05-08 | 2019-08-13 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US10584196B2 (en) | 2015-06-23 | 2020-03-10 | Borealis Ag | Process for producing LLDPE resins |
US10975183B2 (en) | 2016-09-09 | 2021-04-13 | Exxonmobil Chemical Patents Inc. | Pilot plant scale semi-condensing operation |
WO2018048472A1 (en) * | 2016-09-09 | 2018-03-15 | Exxonmobil Chemical Patents Inc. | Pilot plant scale semi-condensing operation |
US11041036B2 (en) | 2016-09-27 | 2021-06-22 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018063764A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US11192970B2 (en) | 2016-09-27 | 2021-12-07 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US11274170B2 (en) | 2016-09-27 | 2022-03-15 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018063767A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018063765A1 (en) | 2016-09-27 | 2018-04-05 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US10899942B2 (en) | 2016-09-28 | 2021-01-26 | Borealis Ag | Process for producing a coated pipe |
US11180586B2 (en) | 2016-11-25 | 2021-11-23 | Borealis Ag | Process for producing polyolefin film composition and films prepared thereof |
US10982025B2 (en) | 2016-11-25 | 2021-04-20 | Borealis Ag | Process for producing polyolefin film composition and films prepared thereof |
WO2018118155A1 (en) | 2016-12-20 | 2018-06-28 | Exxonmobil Chemical Patents Inc. | Polymerization process |
US11142591B2 (en) | 2016-12-20 | 2021-10-12 | Exxonmobil Chemical Patents Inc. | Polymerization process |
WO2018170248A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170227A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170056A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170208A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
WO2018170138A1 (en) | 2017-03-15 | 2018-09-20 | Dow Global Technologies Llc | Catalyst system for multi-block copolymer formation |
US11254809B2 (en) | 2017-06-21 | 2022-02-22 | Borealis Ag | Polymer composition and a process for production of the polymer composition |
WO2022010622A1 (en) | 2020-07-07 | 2022-01-13 | Exxonmobil Chemical Patents Inc. | Processes for making 3-d objects from blends of polyethylene and polar polymers |
Also Published As
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0699213B1 (en) | Polymerisation process | |
US6096839A (en) | Atomizer nozzle | |
US6214943B1 (en) | Nozzle for atomizing a fluid in a fluidized bed | |
US5898053A (en) | Polymerisation process | |
US6001938A (en) | Polymerization process | |
US6225422B1 (en) | Gas fluidized bed polymerization process for olefins | |
EP0825204B1 (en) | Polymerisation process | |
EP0813555B1 (en) | Polymerisation process | |
EP0824117B1 (en) | Polymerisation process | |
EP0803519A1 (en) | Polymerisation process | |
EP0824114A1 (en) | Polymerisation process | |
AU694924C (en) | Polymerisation process | |
EP0814100A1 (en) | Polymerisation process | |
EP0824118B1 (en) | Polymerisation process | |
AU701999B2 (en) | Polymerisation process |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 94192172.7 Country of ref document: CN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 08256052 Country of ref document: US |
|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AT AU BB BG BR BY CA CH CN CZ DE DK ES FI GB GE HU JP KG KP KR KZ LK LU LV MD MG MN MW NL NO NZ PL PT RO RU SD SE SI SK TJ TT UA US UZ VN |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN ML MR NE SN TD TG |
|
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) |
Free format text: US |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 1994915621 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 266173 Country of ref document: NZ |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2161432 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 95-01861 Country of ref document: RO |
|
WWE | Wipo information: entry into national phase |
Ref document number: PV1995-2940 Country of ref document: CZ |
|
WWE | Wipo information: entry into national phase |
Ref document number: 143395 Country of ref document: SK Ref document number: 1019950705119 Country of ref document: KR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 955561 Country of ref document: FI |
|
WWP | Wipo information: published in national office |
Ref document number: PV1995-2940 Country of ref document: CZ |
|
WWP | Wipo information: published in national office |
Ref document number: 1994915621 Country of ref document: EP |
|
REG | Reference to national code |
Ref country code: DE Ref legal event code: 8642 |
|
EX32 | Extension under rule 32 effected after completion of technical preparation for international publication | ||
LE32 | Later election for international application filed prior to expiration of 19th month from priority date or according to rule 32.2 (b) | ||
ENP | Entry into the national phase |
Ref document number: 1996 677123 Country of ref document: US Date of ref document: 19960709 Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 1997 987155 Country of ref document: US Date of ref document: 19971208 Kind code of ref document: A |
|
WWG | Wipo information: grant in national office |
Ref document number: 1994915621 Country of ref document: EP |
|
WWG | Wipo information: grant in national office |
Ref document number: PV1995-2940 Country of ref document: CZ |
|
WWG | Wipo information: grant in national office |
Ref document number: 955561 Country of ref document: FI |