HERSTELLUNG VON VINYL ENTHALTENDEN POLYMEREN

Production of cyclohexylbenzene hydroperoxide

In a process for producing cyclohexylbenzene hydroperoxide, cyclohexylbenzene is contacted with oxygen to produce a reaction product comprising cyclohexylbenzene hydroperoxide and unreacted cyclohexylbenzene. The reaction product is then maintained under conditions such that crystals of cyclohexylbenzene hydroperoxide form and separate from the reaction product. The cyclohexylbenzene hydroperoxide crystals are then recovered from the reaction product.

Protective pipe and tank linings

Protective liners or coatings for metal conduits, pipes and tanks subjected to corrosive liquids are disclosed. The liners comprise a composition containing a silylated copolymer of, for example, isobutylene and para-methylstyrene, which are curable by contact with moisture.

Dynamic vulcanization process for preparing thermoplastic elastomers

Described in one aspect is a process for preparing a low durometer thermoplastic vulcanizate composition comprising melt blending one or more thermoplastic polymer(s) with a cross-linkable elastomer under conditions of dynamic vulcanization; adding at or after the start of the melt blending at least one curative agent for the elastomer so as to cross-link the elastomer during the melt blending; introducing process oil into the melt blending before, during and/or after the addition of the curative agent; and, extruding a fully crosslinked thermoplastic vulcanizate having a Shore A Hardness of less than 25.

Process for methane conversion

A process for converting methane to higher hydrocarbon(s) including aromatic hydrocarbon(s) in a reaction zone comprises providing to a hydrocarbon feedstock containing methane and a catalytic particulate material to the reaction zone and contacting the catalytic particulate material and the hydrocarbon feedstock in a substantially countercurrent fashion in the reaction zone, while operating the reaction zone under reaction conditions sufficient to convert at least a portion of said methane to a first effluent having said higher hydrocarbon(s).

Continuous slurry polymerization process and apparatus

A process of converting a loop reactor into multiple loop reactors comprising starting with a loop reactor comprising at least 8 vertical legs, at least two non-vertical conversion runs, each non-vertical run connected in fluid flow communication with two vertical legs; at least two feed inlets; and at least two continuous discharge conduits; disconnecting at least one connection of each conversion run; and reconnecting each conversion run in fluid flow communication with a different vertical leg in such a manner to form multiple loop reactors each having at least one feed inlet and at least one continuous discharge conduit.

Thermoplastic polyolefin compositions

This invention relates to a thermoplastic polyolefin composition with (a) a polypropylene having a melting point of greater than 130° C. and a melt flow rate from 10 to 80 g/10 min; (b) an ethylene-propylene copolymer with 40 wt % to 80 wt % ethylene derived units and a Mooney Viscosity (1+4, 125° C.) of greater than 20 Mooney units, a Mw/Mn of from 1.8 to 4.0, and a weight average molecular weight of 50,000 to 300,000 g/mole; and (c) a propylene-based elastomer having 5 wt % to 25 wt % ethylene derived units and having a melting point of less than 110° C. and a Mw/Mn from 2.0 to 4.0; wherein the room temperature notch impact of the thermoplastic polyolefin composition is at least four times greater than the room temperature notch impact of a composition without the propylene-based elastomer.

Hydrocarbon upgrading

Aspects of the invention provide a process for upgrading a hydrocarbon feed. The process includes providing a hydrocarbon feed and a utility fluid. Then selectively extracting from the feed at least a portion of particulates to produce a raffinate and an extract. Third hydroprocessing at least a portion of the raffinate.

Supported transition metal bis(phenolate) complexes and their use as catalysts for olefin polymerization

This invention relates to supported catalyst compositions of transition metal complexes of a dianionic, tridentate ligand that features a central neutral heterocyclic Lewis base and two phenolate donors, where the tridentate ligand coordinates to the metal center to form two eight-membered rings. Preferably the bis(phenolate) complexes are represented by Formula (I): where M, L, X, m, n, E, E′, Q, R1, R2, R3, R4, R1′, R2′, R3′, R4′, A1, A1′, A3 A2, and A2′ A3′ are as defined herein, where A1QA1′ are part of a heterocyclic Lewis base containing 4 to 40 non-hydrogen atoms that links A2to A2′ via a 3-atom bridge with Q being the central atom of the 3-atom bridge.

Burner with high capacity venturi

An improved burner and a method for combusting fuel in burners used in furnaces, such as those used in steam cracking, are disclosed. The burner includes a burner tube having an upstream end, a downstream end and a venturi intermediate said upstream and downstream ends, the venturi including a throat portion having substantially constant internal cross-sectional dimensions such that the ratio of the length to maximum internal cross-sectional dimension of the throat portion is at least 3. A burner tip is mounted on the downstream end of the burner tube adjacent a first opening in the furnace, so that combustion of the fuel gas takes place downstream of said burner tip.

Macrostructures of porous inorganic material and process for their preparation

There is provided macrostructures of porous inorganic material which can have controlled size, shape, and/or porosity and a process for preparing the macrostructures. The macrostructures comprise a three-dimension network of particles of porous inorganic materials. The process for preparing the macrostructures involves forming an admixture containing a porous organic ion exchanger and a synthesis mixture capable of forming the porous inorganic material and then converting the synthesis mixture to the porous inorganic material. After formation of the composite material, the porous organic ion exchanger can be removed from the composite material to obtain the macrostructures.

Hydrogenation catalyst, its method of preparation and use

A method of preparing a hydrogenation catalyst, for example, a phthalate hydrogenation catalyst, comprising contacting a silica support having a median pore size of at least about 10 nm with a silylating agent to form an at least partially coated silica support, calcining said coated silica support to form a treated silica support, and depositing a noble metal, preferably ruthenium, on the treated silica support, and optionally contacting the treated silica support with an optional chelating agent to form the hydrogenation catalyst; a hydrogenation catalyst prepared by that method; and a method of hydrogenating unsaturated hydrocarbons, such as phthalates, in which an unsaturated hydrocarbon is contacted with hydrogen gas in the presence of the hydrogenation catalyst of the invention.

Polyolefin-based elastomer modified polyethylene terephthalate blends with enhanced notched impact strength

A thermoplastic polymer blend having improved impact performance includes from about 50 wt % to about 98 wt % polyethylene terephthalate (PET), a polymeric toughening agent and a compatibilizer. The compatibilizer is a functionalized polyolefin, a thermoplastic copolymer or a thermoplastic terpolymers. The ratio of wt % compatibilizer to wt % polymeric toughening agent, based on the total weight of the thermoplastic polymer blend, is from about 0.1 to about 0.4.

Apparatus and method of cleaning a transfer line heat exchanger tube

An apparatus for on-line cleaning and maintaining the cleanliness of a transfer line exchanger tube is provided. In one embodiment, the apparatus includes a housing having a first end, a second end and a longitudinal axis, the housing further including a first inlet for introducing a flushing fluid to the transfer line exchanger tube, the first inlet disposed proximate the first end of the housing, a second inlet for providing a product effluent comprising hydrocarbons and an outlet for placing in fluid communication with an inlet of the transfer line exchanger tube and a critical flow nozzle or flow control orifice, the critical flow nozzle or flow control orifice in fluid communication with the first inlet of the housing. Systems and processes for cleaning and maintaining the cleanliness of a transfer line exchanger are also disclosed.

Composites comprising elastomer, layered filler and tackifier

The invention relates to rubber nanocomposites particularly suitable for innerliners and other tire applications. The uncured nanocomposite comprises an elastomer, tackifier and nanoclay.

Process for selectively producing high octane naphtha

This invention is related to a catalytically cracked or thermally cracked naphtha stream. The naphtha stream is contacted with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures from about 500° C. to about 650° C. and a hydrocarbon partial pressure from about 10 to 40 psia. The resulting product is a high octane naphtha.

Soluble late transition metal catalysts for olefin oligomerizations III

A This invention relates to a composition comprising a catecholate ligand, palladium or nickel, and an ancillary ligand with the following structure: where Pn is a Group-15 element; H is hydrogen; R⁷ and R⁸ are independently hydrogen or C₁-C₃₀ hydrocarbyl radicals, or both are C₁-C₃₀ hydrocarbyl radicals that form a ring structure comprising one or more aromatic or non-aromatic rings; and R¹³-R¹⁸ are, independently, hydrogen or C₁-C₃₀ hydrocarbyl radicals. The composition can be used to oligomerize ethylene.

Polyethylene compositions comprising cyclic-olefin copolymers

A composite comprising a polyethylene and within a range from 1 wt % to 25 wt % of at least one cyclic-olefin copolymer by weight of the composition, where the polyethylene may have a density of at least 0.90 g/cm3, and where the cyclic-olefin copolymer has a glass transition temperature (Tg) of at least 30° C. Disclosed also is the feature of orienting the composite to form an oriented article, wherein the article comprises rods having an average length of at least 1 μm, and at least 5 nm in average diameter.

Polyethylene and cyclic olefin copolymer blend compositions with oxygen barrier properties and articles made therefrom

In an embodiment, a monolayer, sealable film includes polyethylene; and between about 0.2 wt % and about 10 wt % of a branched cyclic olefin copolymer (bCOC) comprising: between about 50 wt % to about 98 wt % ethylene; and between about 2 wt % and about 50 wt % cyclic olefin derived monomer units. In another embodiment, a receptacle for containing organic material (such as food), gas, and/or fluent material includes a storage zone; a sealing zone extending around at least a portion of the storage zone; and a film structure having an exterior surface and a storage side surface facing the storage zone, wherein the film structure comprises a gas barrier film, comprising: polyethylene; and between about 0.2 wt % and about 10 wt % of a branched cyclic olefin copolymer (bCOC) comprising: between about 50 wt % and about 98 wt % ethylene; and between about 2 wt % and about 50 wt % cyclic olefin derived monomer units.

Stabilization of acid catalysts

The invention is directed to a method of stabilizing metalloaluminophosphate molecular sieves and catalysts derived therefrom. In particular, the invention is directed to a method of treating such molecular sieves with chemisorbed ammonia, which may be easily desorbed before or during use and after storage. The invention is also directed to formulating the molecular sieve into a catalyst useful in a process for producing olefin(s), preferably ethylene and/or propylene, from a feedstock, preferably an oxygenate containing feedstock.

Process for cracking synthetic crude oil-containing feedstock

A process for steam cracking liquid hydrocarbon feedstocks containing synthetic crude oil comprises i) hydroprocessing a wide boiling range aliquot containing a) normally liquid hydrocarbon portion substantially free of resids and b) thermally cracked hydrocarbon liquid, boiling in a range from about 600° to about 1050° F., to provide a synthetic crude oil substantially free of resids; ii) adding to the synthetic crude oil a normally liquid hydrocarbon component boiling in a range from about 100° to about 1050° F.; and iii) cracking the mixture resulting from ii) in a cracker furnace comprising a radiant coil outlet to provide a cracked effluent, wherein the cracking is carried out under conditions sufficient to effect a radiant coil outlet temperature which is greater than the optimum radiant coil outlet temperature for cracking the synthetic crude oil separately. A method for upgrading synthetic crude for use in cracking is also provided, as well as a feedstock for cracking.

Process for making phenol and/or cyclohexanone

Disclosed is (i) a process of making phenol and/or cyclohexanone from cyclohexylbenzene including a step of removing methylcyclopentylbenzene from (a) the cyclohexylbenzene feed supplied to the oxidation step and/or (b) the crude phenol product (ii) a phenol composition and (iii) a cyclohexylbenzene composition that can be made using the process.

Air barrier composition for innerliners

According to the invention, a processing aid is used to improve processing in a green (uncured) rubber composition, such as in downstream in-plant processing of an innerliner compound, and maintaining, or more preferably, reducing the air permeability of the cured composition, e.g., innerliner compound. In embodiments, another of the advantages of the present invention is that the processing aid according to the invention can be used in very low levels relative to the other processing aids and oils.

Propylene elastomers for electrical wire and cable compounds

The present disclosure is directed to an electrical device comprising a propylene-alpha olefin polymer, wherein the propylene-alpha olefin polymer comprises from about 5 to about 25 wt % alpha olefin, from about 75 to about 95 wt % propylene and optionally 10 wt % diene, wherein the propylene-alpha olefin polymer has a MWD of from about 1 to about 5, a heat of fusion less than or equal to 75 J/g and a Tm105° C.

Vaporisation in oxidation to phthalic anhydride

In the production of phthalic anhydride by the oxidation of ortho-xylene with air, the ortho-xylene loading is increased without increasing the likelihood of explosion by insulating the system to avoid cold spots to keep the ortho-xylene at a temperature above its dew point; in addition the system may be electrically interconnected and grounded to reduce the risk of spark initiated explosions or deflagrations.

Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks

Hydrocarbon feedstock containing resid is cracked by a process comprising: (a) heating the hydrocarbon feedstock; (b) mixing the heated hydrocarbon feedstock with steam and optionally water to form a mixture stream; (c) introducing the mixture stream to a flash/separation apparatus to form i) a vapor phase at its dew point which partially cracks and loses/or heat causing a temperature decrease and partial condensation of the vapor phase in the absence of added heat to provide coke precursors existing as uncoalesced condensate, and ii) a liquid phase; (d) removing the vapor phase as overhead and the liquid phase as bottoms from the flash/separation apparatus; (e) treating the overhead by contacting with a hydrocarbon-containing nucleating liquid substantially free of resid and comprising components boiling at a temperature of at least about 260° C. (500° F.) under conditions sufficient to at least partially coalesce the coke precursors to provide coke precursor liquid, in the form of hydrocarbon ...

Polymer blend, method for making the same and roofing membrane containing the same

A polymer blend comprising 10 to 90 parts by weight of a propylene-based polymer component having a weight average molecular weight of at least 200 kg·mol−1; and 20 to 80 parts by weight of a propylene-based elastomer component comprising structural units derived from propylene and at least one of ethylene and C4-C12 alpha-olefins having a weight average molecular weight in the range from 5 to 50 kg·mol−1, method for making a membrane comprising the same and roofing membrane comprising the same. The polymer blend is particularly suitable for making roofing membrane due to advantageous elastic modulus in broad temperature ranges.

Process for producing olefins

A process is described for producing an olefins stream from a first vapor effluent stream from an oxygenate to olefin conversion reaction, said first vapor effluent stream comprising C₂ and C₃ olefins, C₄ hydrocarbons, and C₂ to C₆ carbonyl compounds. In the process, the temperature and pressure of the first vapor effluent stream are adjusted to produce a second vapor effluent stream having a pressure ranging from about 100 psig to about 350 psig (790 to 2514 kPa) and a temperature ranging from about 70° F. to about 120° F. (21 to 49° C.), said second vapor effluent stream containing about 50 wt. % or more C₄ hydrocarbons based upon the total weight of C₄ hydrocarbons in the first vapor effluent stream. The second vapor effluent stream is then washed with a liquid alcohol-containing stream to produce a third vapor effluent stream, whereafter the third vapor effluent stream is washed with liquid water to provide ...

Production of xylenes from syngas

This disclosure relates to the production of xylenes from syngas, in which the syngas is converted to an aromatic product by reaction with a Fischer-Tropsch catalyst and an aromatization catalyst. The Fischer-Tropsch catalyst and aromatization catalyst may be different catalysts or combined into a single catalyst. The aromatic product is then subjected to selective alkylation with methanol and/or carbon monoxide and hydrogen to increase its p-xylene content.

Рrосеss fоr mеthаnе соnvеrsiоn

А prосеss fоr соnvеrting mеthаnе tо highеr hуdrосаrbоn(s) inсluding аrоmаtiс hуdrосаrbоn(s) in а rеасtiоn zоnе соmprisеs prоviding tо а hуdrосаrbоn fееdstосk соntаining mеthаnе аnd а саtаlуtiс pаrtiсulаtе mаtеriаl tо thе rеасtiоn zоnе аnd соntасting thе саtаlуtiс pаrtiсulаtе mаtеriаl аnd thе hуdrосаrbоn fееdstосk in а substаntiаllу соuntеrсurrеnt fаshiоn in thе rеасtiоn zоnе, whilе оpеrаting thе rеасtiоn zоnе undеr rеасtiоn соnditiоns suffiсiеnt tо соnvеrt аt lеаst а pоrtiоn оf sаid mеthаnе tо а first еffluеnt hаving sаid highеr hуdrосаrbоn(s).

Рrосеss fоr mеthаnе соnvеrsiоn

А prосеss fоr соnvеrting mеthаnе tо highеr hуdrосаrbоn(s) inсluding аrоmаtiс hуdrосаrbоn(s) in а rеасtiоn zоnе соmprisеs prоviding tо а hуdrосаrbоn fееdstосk соntаining mеthаnе аnd а саtаlуtiс pаrtiсulаtе mаtеriаl tо thе rеасtiоn zоnе аnd соntасting thе саtаlуtiс pаrtiсulаtе mаtеriаl аnd thе hуdrосаrbоn fееdstосk in а substаntiаllу соuntеrсurrеnt fаshiоn in thе rеасtiоn zоnе, whilе оpеrаting thе rеасtiоn zоnе undеr rеасtiоn соnditiоns suffiсiеnt tо соnvеrt аt lеаst а pоrtiоn оf sаid mеthаnе tо а first еffluеnt hаving sаid highеr hуdrосаrbоn(s).

High stiffness polypropylene impact copolymer

Disclosed is a polypropylene with an MFR of at least 20 g/10 min comprising a homopolypropylene and optionally within a range from 2 wt % to 30 wt % of an propylene-α-olefin copolymer by weight of the polypropylene; wherein the homopolypropylene has a MFR within a range from 30 g/10 min to 200 g/10 min, an Mw/Mn within a range from 7 to 16, and comprising 1.1 wt % or less atactic polypropylene based on the total weight of the homopolypropylene and atactic polypropylene, where the propylene-α-olefin copolymer has within a range from 30 wt % to 50 wt % α-olefin derived units by weight of the propylene-α-olefin copolymer, and an intrinsic viscosity within a range from 4 to 8 dL/g. The impact copolymer may be obtained by combining a Ziegler-Natta catalyst having at least two different internal electron donors with propylene in reactors in series to produce the homopolypropylene followed by a gas phase reactor to produce a propylene-α-olefin copolymer.

Production of gradient copolymers using monomer and comonomer concentration gradients in a loop reactor

A method for producing gradient copolymers can include polymerizing a reaction mixture comprising a monomer and a comonomer in the presence of a metallocene catalyst in a loop reactor, wherein in the loop reactor a gradient monomer weight percent in the reaction mixture is about 3 wt % to about 50 wt %, thereby forming a gradient copolymer.

Dual metallocene catalyst copolymer compositions

Processes are provided which include copolymerization using two different metallocene catalysts, one capable of producing high Mooney-viscosity polymers and one suitable for producing lower Mooney-viscosity polymers having at least a portion of vinyl terminations. The two catalysts may be used together in polymerization to produce copolymer compositions of particularly well-tuned properties. For instance, polymerizations are contemplated to produce high-Mooney metallocene polymers that exhibit excellent processability and elasticity, notwithstanding their high Mooney viscosity. Other polymerizations are also contemplated in which lower-Mooney metallocene polymers are produced, which also exhibit excellent processability and elasticity, while furthermore having excellent cure properties suitable in curable elastomer compound applications. Many of the contemplated polymerizations include controlling the ratio of the two metallocene catalysts used in the polymerization so as to obtain the ...

Ethylene propylene copolymer compounds for use in layered articles

A multilayer structure can include at least one layer that comprises an ethylene propylene diene copolymer compound that comprises: 60 parts per hundred rubber (phr) to 95 phr of a first ethylene propylene diene copolymer (EP(D)M) having an ethylene content of 62 wt % to 90 wt % based on the first EP(D)M and a heat of fusion (Hf) of 15 J/g or greater; 5 phr to 40 phr of an second EP(D)M having an ethylene content of 40 wt % to 60 wt % based on the second EP(D)M and a Hfof 0 J/g to 14 J/g, wherein the Hfof the first EP(D)M minus the Hfof the second EP(D)M is 5 J/g or greater; wherein the first EP(D)M and second EP(D)M combined are 100 parts; a filler at 40 phr to 500 phr; and a curing agent at 0.5 phr to 20 phr.

A METHANOL, OLEFIN, AND HYDROCARBON SYNTHESIS PROCESS

PROCESS FOR PREPARING DIALKYLBIPHENYL ISOMER MIXTURES

PROCESS FOR PRODUCING CYCLOHEXYLBENZENE

SOFT POLYPROPYLENE-BASED NONWOVENS

PHASE SEPARATOR AND MONOMER RECYCLE FOR SUPERCRITICAL POLYMERIZATION PROCESS

OLEFIN POLYMERIZATION PROCESS TO PRODUCE BRANCHED POLYMER COMPOSITIONS

OLEFIN POLYMERIZATION CATALYST SYSTEM USEFUL FOR POLAR MONOMERS

PROCESS FOR MAINTAINING ACID CATALYST SITES IN SAPO MOLECULAR SIEVES

METHOD FOR PRODUCING PHENOL AND/OR CYCLOHEXANONE

MULTISTAGE METHOD FOR MANUFACTURING POLYOLEFINS

Oligomerization reactor wash process using by-product solvent recovered using a thin film evaporator

A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.

Ru-containing polyoxotungstates and process for their preparation

The invention relates to polyoxometalates represented by the formula (An)m+ [Ru2L2(XW11O39)2WO2]m or solvates thereof, wherein A is a cation, n is the number of the cations, m is the charge of the polyanion, L is a ligand bound to ruthenium and is independently selected from group consisting of water, unsubstituted or substituted arenes, unsubstituted or substituted heteroarenes, unsaturated hydrocarbons, ethers, unsubstituted or substituted allyl, unsubstituted or substituted alkanes, nitriles, carboxylates, peroxides, peracids, phosphines, phosphanes, CO, OH, peroxo, carbonate, NO3, NO2, NO, NH3, amines, F, Cl, Br, I, SCN, NCS, NCO and mixtures thereof and X is a heteroatom selected from Si, Ge, B and mixtures thereof, a process for their preparation and their use for the catalytic oxidation of organic molecules.

Mixed metal oxide catalysts and use thereof

Disclosed herein are catalyst compositions useful in selective decomposition of organic oxygenates. A feed comprising an organic oxygenate may be contacted with a catalyst comprising (a) at least 0.1 wt % of an oxide of an element selected from Group 3 of the Periodic Table of Elements, wherein Group 3 includes the Lanthanide series; (b) at least 0.1 wt % of an oxide of an element selected from Group 6 of the Periodic Table of Elements; and (c) at least 0.1 wt % of an oxide of at least one element selected from Group 4 of the Periodic Table of Elements, wherein the wt % s are based upon the total combined weight of the oxides in (a) through (c) and excludes any other components.

Thermoplastic vulcanizates comprising broad molecular weight distribution polypropylene

Provided herein are thermoplastic vulcanizates that comprise rubber, broad molecular weight distribution polypropylene, and oil, where the rubber forms a rubber phase that is dispersed and at least partially cross-linked within a continuous thermoplastic component that comprises the broad molecular weight distribution polypropylene. The broad molecular weight distribution polypropylene preferably has a molecular weight distribution (Mw/Mn) of greater than 4; a melt flow rate of greater than 1 g/10 min; and a weight average molecular weight (Mw) of greater than 380,000 daltons.

Methyl-substituted biphenyl compounds, their production and their use in the manufacture of plasticizers

In a process for producing methyl-substituted biphenyl compounds, a feed comprising at least one aromatic hydrocarbon selected from the group consisting of toluene, xylene and mixtures thereof is contacted with hydrogen in the presence of a hydroalkylation catalyst under conditions effective to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluenes and/or (dimethylcyclohexyl)xylenes. At least part of the hydroalkylation reaction product is then dehydrogenated in the presence of a dehydrogenation catalyst under conditions effective to produce a dehydrogenation reaction product comprising a mixture of methyl-substituted biphenyl compounds.

Halogenated isobutylene-based copolymers having enhanced viscosity and thermoplastic compositions thereof

The invention provides a method for increasing the viscosity of halogenated (brominated) elastomeric copolymers of a C₄ to C₇ isomonoolefin (isobutylene) and a para-alkylstryrene (p-methylstyrene) by mixing the copolymer with a silica or clay particulate filler which has been contacted with an aminosilane containing at least one C₁ to C₄ alkoxy group and at least one primary, secondary or tertiary amine group. The resulting elastomer compositions are used to prepare thermoplastic elastomer blend compositions, containing more finely dispersed elastomers which results in compositions having improved mechanical properties.

Fuel spud for high temperature burners

An improved burner and a method for combusting fuel in a burner used in furnaces such as those found in steam cracking. The burner includes a burner tube having a downstream end and an upstream end, the burner tube having a venturi therein; a fuel spud located adjacent the upstream end of the burner tube, for introducing fuel gas into the burner tube; a burner tip mounted on the downstream end of the burner tube adjacent a first opening in the furnace; at least one passageway having a first end and a second end adjacent the upstream end of the burner tube; means for drawing flue gas from the furnace, through the passageway, in response to an inspirating effect of uncombusted fuel gas exiting the fuel spud, the uncombusted fuel gas flowing through the burner tube from its upstream end towards its downstream end; and means for increasing the inspirating effect of uncombusted fuel gas exiting the fuel spud. The means for increasing the inspirating effect of uncombusted fuel gas exiting the ...

Method and apparatus for treating oxygenate-containing feeds and their use in conversion of oxygenates to olefins

A feed vaporization process and apparatus for oxygenate to olefin conversion is provided which uses a vapor-liquid disengaging drum to separate non-volatiles and/or partial non-volatiles from volatiles in the oxygenate feed and produce a vaporized effluent that is reduced in non-volatiles and/or partial non-volatiles while at the same time maintaining the effluent at optimal temperature and pressure as a feed for oxygenate to olefin conversion.

Supported late transition metal catalyst systems

A late transition metal catalyst system for polymerization of olefin monomers is a Group 9, 10 or 11 metal complex stabilized by a bidentate ligand immobilized on a solid support where the late transition metal loading is less than 100 micromoles transition metal compound per gram of solid support. The bidentate ligand has the formula:wherein A is a bridging group containing a Group 13-15 element; each E is independently a Group 15 or 16 element bonded to M; each R is independently a C1-C30 containing radical or diradical group which is a hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, hydrocarbyl-substituted organometalloid, halocarbyl-substituted organometalloid, m and n are independently 1 or 2 depending on the valency of E; and p is the charge on the bidentate ligand.

Hydrocarbon conversion process using a zeolite bound zeolite catalyst

There is provided a process for converting hydrocarbons which utilizes a zeolite bound zeolite catalyst that has enhanced performance when utilized in hydrocarbon conversion processes, e.g., catalytic cracking, alkylation, disproportionation of toluene, isomerization, and transalkylation reactions. The catalyst comprises a first zeolite having particles of greater than about 0.1 micron average particle size and a binder comprising second zeolite particles having an average particle size less than said first particles.

Molecular sieve catalyst composition, its making and use in conversion processes

A catalyst composition that comprises an over flocculated molecular sieve and optionally, a phosphorous compound and, optionally, a non-over flocculated molecular sieve. A method of preparing a catalyst composition that comprises mixing an over flocculated molecular sieve and optionally, a phosphorous compound and, optionally, a non-over flocculated molecular sieve.

Polyolefin adhesive compositions

A multi-modal polymer blend for use in an adhesive composition comprising at least two compositionally different propylene-based polymers. The multi-modal polymer blend has a Mw of about 10,000 g/mol to about 150,000 g/mol. When subjected to Temperature Rising Elution Fractionation, the multi-modal polymer blend exhibits a first fraction that is soluble at 15° C. in a hydrocarbon solvent, such as xylene or ortho-dichlorobenzene, the first fraction having an isotactic (mm) triad tacticity of about 70 mol % to about 90 mol %; and a second fraction that is insoluble or less soluble than the first fraction at 15° C. in the hydrocarbon solvent, the second fraction having an isotactic (mm) triad tacticity of about 85 mol % to about 98 mol %.

Elastomer nanocomposites comprising isobutylene and multifunctional oligomers

The present invention provides a nanocomposite of an elastomer, a polymer or oligomer functionalized with a polar group, and a clay. The nanocomposite can be a mixture of a halogenated elastomer, an acid or acid anhydride modified polymer, and a clay, desirably an exfoliated clay, suitable for use as an air barrier. Also disclosed is a nanocomposite that can be a mixture of a halogenated elastomer, a polymer modified with a carboxylic acid, and an organoclay.

Elastomeric blend for air barriers comprising grafted resin components

A composition suitable for an air barrier such as an automotive tire innertube, innerliner, and aircraft tire innertube or innerliner, curing bladders, and other pneumatic devices is disclosed. The composition comprises an elastomer, a processing oil, and a grafted resin component.

Polymerization processes and polymers made therefrom

The present disclosure provides processes for polymerizing olefin(s). Methods can include contacting a first composition and a second composition in a line to form a third composition. The first composition can include a contact product of a first catalyst, a second catalyst, a support, a first activator, a mineral oil. The second composition can include a contact product of an activator, a diluent, and the first catalyst or the second catalyst. Methods can include introducing the third composition from the line into a gas-phase fluidized bed reactor, introducing a condensing agent to the line and/or the reactor, exposing the third composition to polymerization conditions, and/or obtaining a polyolefin. Polyethylene compositions including at least 65 wt % ethylene derived units, based upon the total weight of the polyethylene composition, are provided.

Method for converting oxygenates to olefins

The present invention provides a method for converting a feed containing oxygenates to olefins and comprises the following steps: providing a feed including an oxygenate; contacting the feed in a reactor apparatus with a catalyst including a molecular sieve, the contacting taking place under conditions effective to convert the oxygenate to a product including a light olefin, the conditions including a gas superficial velocity of at least two meters per second at at least one point in the reaction zone; and recirculating a first portion of the catalyst to recontact the feed.

Compositions suitable for elastomeric membranes

This invention relates generally to polymers suitable for making elastomeric films, membranes or sheets. More specifically, this invention is directed to polymers of the ethylene, alpha-olefin, diene terpolymer type that are reactor blends of two components, an amorphous major component and semicrystalline minor component, wherein the viscosity of the major component is less than one fourth the viscosity of minor component. These polymers are particularly suitable for elastomeric membranes such as roofing membranes.

Powder, compositions thereof, processes for making the same, and articles made therefrom

Provided herein is a powder comprising at least one of: (a) a propylene-based elastomer comprising, based on the total weight of said propylene-based elastomer, (i) at least about 60 wt % of propylene-derived units, (ii) about 5 wt % to about 35 wt % of units derived from at least one of ethylene and a C4-C10 alpha-olefin, and said propylene-based elastomer having a heat of fusion, as determined by DSC, of about 75 J/g or less; and (b) a polyolefin-based elastomer having a Shore A hardness, as determined by ISO 868, of less than 95; wherein the powder has an average particle size of from about 30 mum to about 850 mum. The powder is useful for rotational molding and for making articles having unique combination of elasticity, flexibility, and toughness.

Process for nitrile removal from hydrocarbon feeds

A process is described, such process comprising i) contacting a hydrocarbon feed with a heterogeneous catalyst under conditions suitable to hydrolyze nitriles present in the feed to form a nitrile hydrolysis product comprising ammonia, carboxylic acid and carboxylate salts or a mixture thereof; and ii) removing the nitrile hydrolysis product from the feed. In an embodiment, the hydrocarbon feed comprises olefins and is intended for use in an olefin oligomerization process.

Olefin oligomerization

A process for producing a hydrocarbon composition that comprises contacting a feed stream, that comprises at least one C3 to C8 olefin, and an olefinic recycle stream, that comprises a first olefinic recycle stream and no more than 10 wt % of C10+ non-normal olefins, with a molecular sieve catalyst in a reaction zone under olefin oligomerization conditions producing an oligomerization effluent stream; separating the oligomerization effluent stream to produce a first olefinic stream, that has a weight ratio of C4/(C5-C8) molecules from about 0.8 to about 1.2 times the weight ratio of C4/(C5-C8) molecules found in the oligomerization effluent stream, and a first hydrocarbon product stream, that comprises at least 1 wt % and no more than 30 wt % of C9 non-normal olefin; and splitting the first olefinic stream to produce the first olefinic recycle stream and a first purge stream.

Method of Making Catalyst, Catalyst Made Thereby and Use Thereof

The invention concerns a method of making a catalyst adapted for isomerization of xylenes. 1. In the method of making a metal-containing zeolite catalyst by competitive ion exchange , the improvement comprising preparation of said metal-containing zeolite catalyst by competitive ion exchange in the presence of ammonium acetate.2. The method according to claim 1 , wherein said zeolite is selected from at least one of ZSM-5 claim 1 , ZSM-11 claim 1 , ZSM-12 claim 1 , ZSM-18 claim 1 , MCM-68 claim 1 , MCM-22 claim 1 , Beta claim 1 , mordenite claim 1 , and mixtures thereof.3. The method according to claim 1 , wherein the metal in said metal-containing zeolite comprises at least one metal from Groups 8-10 of the Periodic Table.4. The method according to claim 1 , wherein said metal-containing zeolite includes at least one of platinum or rhenium dispersed in the amount of from 0.01 wt % to 1.20 wt % claim 1 , preferably 0.01 wt % to less than 1.00 wt % claim 1 , more preferably 0.01 wt % to 0.50 wt % claim 1 , based on the weight of said metal-containing zeolite.5. The method according to claim 1 , wherein said metal-containing zeolite is silicone-selectivated.6. The method according to claim 1 , wherein said catalyst includes a support selected from alumina claim 1 , silica claim 1 , clay claim 1 , aluminosilicates claim 1 , and mixtures thereof.7. A catalyst made by the process according to .8. The catalyst made by the process of claim 7 , further comprising an acetate moiety.9. A catalyst system including a first bed comprising a first metal-containing zeolite catalyst adapted for dealkylation of ethylbenzene and ethylene saturation claim 7 , and a second bed comprising a second metal-containing zeolite catalyst claim 7 , different from said first catalyst and adapted for xylene isomerization claim 7 , wherein at least one of said first catalyst and said second catalyst is prepared by competitive ion exchange in the presence of ammonium acetate.10. The catalyst system ...

Process for the purification of paraxylene

The proposed process uses crystallization technology to purify paraxylene simultaneously of large concentrations of C8 aromatics and also small concentrations of oxygenated species.

Molecular sieve catalyst composition, its making and use in conversion processes

The invention relates to a molecular sieve catalyst composition, to a method of making or forming the molecular sieve catalyst composition, and to a conversion process using the catalyst composition. In particular, the invention is directed to making a formulated molecular sieve catalyst composition from a slurry of formulation composition of a synthesized molecular sieve that has not been fully dried, a binder and an optional matrix material. In a more preferred embodiment, the weight ratio of the binder to the molecular sieve and/or the solid content of the slurry is controlled to provide an improved attrition resistant catalyst composition, particularly useful in a conversion process for producing olefin(s), preferably ethylene and/or propylene, from a feedstock, preferably an oxygenate containing feedstock.

Process for continuous solution polymerization

Described herein are methods for continuous solution polymerization. The method may comprise polymerizing one or more monomers and comonomers in the presence of a solvent in a polymerization reactor to produce a polymer solution; determining the composition of the polymer solution exiting the polymerization reactor in an on-line fashion; determining at least one of the critical pressure or critical temperature; comparing the critical pressure and/or critical temperature to the actual temperature of the polymer solution and the actual pressure of the polymer solution; heating or cooling the polymer solution to a temperature within 50° C. of the critical temperature; and passing the polymer solution through a pressure letdown valve into a liquid-liquid separator, where the pressure of the polymer solution is reduced or raised to a pressure within 50 psig of the critical pressure to induce a separation of the polymer solution into two liquid phases.

Рrосеss fоr mеthаnе соnvеrsiоn

А prосеss fоr соnvеrting mеthаnе tо highеr hуdrосаrbоn(s) inсluding аrоmаtiс hуdrосаrbоn(s) in а rеасtiоn zоnе соmprisеs prоviding tо а hуdrосаrbоn fееdstосk соntаining mеthаnе аnd а саtаlуtiс pаrtiсulаtе mаtеriаl tо thе rеасtiоn zоnе аnd соntасting thе саtаlуtiс pаrtiсulаtе mаtеriаl аnd thе hуdrосаrbоn fееdstосk in а substаntiаllу соuntеrсurrеnt fаshiоn in thе rеасtiоn zоnе, whilе оpеrаting thе rеасtiоn zоnе undеr rеасtiоn соnditiоns suffiсiеnt tо соnvеrt аt lеаst а pоrtiоn оf sаid mеthаnе tо а first еffluеnt hаving sаid highеr hуdrосаrbоn(s).

Рrосеss аnd аppаrаtus fоr upgrаding stеаm сrасkеd tаr

А prосеss аnd аppаrаtus аrе prоvidеd fоr upgrаding stеаm сrасkеd tаrs. Тhе invеntiоn аlsо rеlаtеs tо а stеаm сrасking prосеss аnd аppаrаtus fоr rеduсing thе уiеlds оf tаrs prоduсеd frоm stеаm сrасking whilе inсrеаsing уiеlds оf highеr vаluе prоduсts, hеаting сооlеd stеаm сrасkеr tаr соntаining аsphаltеnеs, tо а tеmpеrаturе, е.g., аbоvе аbоut 300° С., whiсh is suffiсiеnt tо соnvеrt аt lеаst а pоrtiоn оf thе stеаm сrасkеd tаr tо lоwеr bоiling mоlесulеs. Тhе rеsulting hеаt-trеаtеd tаr саn bе sеpаrаtеd intо gаs оil, fuеl оil аnd tаr strеаms.

Polymeric coating compositions and articles coated with the same

Polymeric coating compositions and articles coated with the polymeric coating compositions are provided. The polymeric coating composition can include an ethylene-based polymer that exhibits desirable melting properties and molecular weight distribution. The polymeric coating composition can provide a thin coating layer on an article while still providing advantageous properties, such as seal strength.

HIGH-PRESSURE VALVE

METHOD OF PREPARATION OF CROSSLINKED BLENDS OF AMORPHOUS AND CRYSTALLINE POLYMERS

IMPROVED LIQUID PHASE ALKYLATION PROCESS

HETEROCYCLIC AMIDO TRANSITION METAL COMPLEXES, PRODUCTION AND USE THEREOF

COPOLYMERIZATION PROCEEDING OF 1-DECENE AND 1-DODECENE

EXPANSIBLE BARRIER FILM ASSEMBLIES

AN APPARATUS FOR THE PRODUCTION OF POLYETHYLENE AND ETHYLENE COPOLYMERS

PROCESS FOR PRODUCING POLYOLEFIN

POLYMERIZATION CATALYST SYSTEMS, THEIR PRODUCTION AND USE

PROCESSES AND SYSTEMS FOR THE CONVERSION OF HYDROCARBONS

DEVICE AND RELATED METHOD FOR PROCESSING POLYMERS

Bis(aryl phenolate) lewis base catalysts and methods thereof

The present disclosure relates to bis(aryl phenolate) Lewis base catalysts. Catalysts, catalyst systems, and processes of the present disclosure can provide high temperature ethylene polymerization, propylene polymerization, or copolymerization as the bis(aryl phenolate) Lewis base catalysts are stable at high polymerization temperatures and have good activity at the high polymerization temperatures. The stable catalysts with good activity can provide formation of polymers having high molecular weights and the ability to make an increased amount of polymer in a given reactor, as compared to conventional catalysts. Hence, the present disclosure demonstrates highly active catalysts capable of operating at high reactor temperatures while producing polymers with controlled molecular weights and or robust isotacticity.

Transparent and colorable elastomeric compositions

Transparent and colorable elastomeric compositions are provided. The transparent elastomeric compositions can be covulcanized with rubbers such as polybutadiene, polyisoprene, styrene-butadiene rubber, styrene-isoprene-butadiene rubber, isoprene-butadiene rubber, ethylene-propylene diene rubber or natural rubber. The colorable rubber compositions have sufficient properties to function as a reinforcing member in an automobile tire. Preferably, both the transparent and colorable elastomeric compositions include at least one copolymer of a C4 to C7 isoolefin and a para-alkylstyrene, silica and a coupling agent.

Method of separating dimethyl ether from an olefin stream

This invention is directed to a method of removing dimethyl ether from an olefin stream. Dimethyl ether is removed from the olefin stream by first separating the olefin stream into a first stream comprising dimethyl ether and lighter boiling point compounds, and a second stream comprising C4+ olefin and higher boiling point hydrocarbons. The dimethyl ether is then separated from the first stream using extractive distillation.

Transition metal bis(phenolate) complexes and their use as catalysts for olefin polymerization

This invention relates to transition metal complexes of a dianionic, tridentate ligand that features a central neutral heterocyclic Lewis base and two phenolate donors, where the tridentate ligand coordinates to the metal center to form two eight-membered rings. Preferably the bis(phenolate) complexes are represented by Formula (I): where M, L, X, m, n, E, E′, Q, R1, R2, R3, R4, R1′, R2′, R3′, R4′, A1, A1′, are as defined herein, where A1QA1′are part of a heterocyclic Lewis base containing 4 to 40 non-hydrogen atoms that links A2to A2′ via a 3-atom bridge with Q being the central atom of the 3-atom bridge.

Production of light olefins from oxygenate using framework gallium-containing medium pore molecular sieve

A method is provided for converting oxygenates, e.g., methanol, to olefins, e.g., ethylene and propylene, comprising contacting said oxygenates and an aromatics co-feed, e.g., xylenes, with a framework gallium-containing molecular sieve catalyst comprising pores having a size ranging from about 5.0 Angstroms to about 7.0 Angstroms, e.g., ZSM-5, under production conditions effective to produce olefins. A catalyst composition is also provided, comprising a ZSM-5 zeolite-bound ZSM-5 zeolite having a bound zeolite of framework Ga-containing zeolite having a Si/Ga molar ratio ranging from 5 to 500 and a binder of Ga-modified, e.g., Ga-exchanged and/or Ga-impregnated, zeolite having a Si/Ga molar ratio ranging from 5 to ∞.

Reactor wall coating and processes

Reactor wall coatings for polymerization reactors and processes for forming such coatings are disclosed. The reactor wall coatings can have a thickness of at least 100 mum and a molecular weight distribution including a major peak having one or more of an Mw/Mn ratio of less than 10; an Mz/Mw ratio of less than 7; and a maximum value of d(wt %)/d(log MW) at less than 25,000 daltons in a plot of d(wt %)/d(log MW), where MW is the molecular weight in daltons. The reactor wall coatings can be formed in-situ during polymerization, on reactor walls initially free of a reactor wall coating, or having a pre-existing reactor wall coating.

Self-sulfiding of guard reactor catalyst for solvent assisted tar conversion processes

The present disclosure provides methods for hydroprocessing of heavy oils, such as pyrolysis tars. For example, a process for preparing a liquid hydrocarbon product includes providing a first process stream comprising a reduced reactivity tar, and blending the first process stream with a utility fluid to produce a second process stream comprising solids and a reduced reactivity, lower viscosity tar. The method can includes introducing the second process stream into a guard reactor without sulfiding the guard reactor catalyst(s) prior to introducing the second process stream into the guard reactor. The method includes hydroprocessing the second process stream in the guard reactor under mild hydroprocessing conditions to produce a third process stream. The method includes hydroprocessing the third process stream to produce a fourth process stream having a bromine number (BN) lower than 12 and comprising the liquid hydrocarbon product and the utility fluid.

Process for producing cycloalkylaromatic compounds

In a process for producing a cycloalkylaromatic compound, an aromatic compound and a cyclic olefin are contacted with a first catalyst under conditions effective to produce a reaction product comprising the cycloalkylaromatic compound and at least one non-fused bicyclic by-product. The at least one non-fused bicyclic by-product is then contacted with a second catalyst under conditions effective to convert at least a portion of the at least one non-fused bicyclic by-product to a converted by-product.

Methods and systems for treating a hydrocarbon feed

The invention relates to methods and systems for treating heavy hydrocarbon by cavitation and hydroprocessing. The invention also relates to systems and methods for such treating, to equipment useful for such treating, and to cavitated, hydroprocessed products.

Hydrocarbon conversion process using molecular sieve of MFS framework type

A crystalline molecular sieve of MFS framework type manufactured by the method disclosed herein. A hydrocarbon conversion process using the crystalline molecular sieve is disclosed.

Propylene-based impact copolymers

An impact copolymer comprising a polypropylene comprising at least 50 mol % propylene, and having a molecular weight distribution (MwMALLS/Mn) greater than 10, a branching index (g′) of less than 0.97, and a melt strength greater than 40 cN, and an elastomer. Also disclosed is a method of making an impact copolymer composition comprising melt-blending the components, sequentially or simultaneously a polypropylene resin comprising at least 50 mol % propylene, and having a molecular weight distribution (Mw/Mn) greater than 6, a branching index (g′) of at least 0.97, and a melt strength greater than 10 cN determined using an extensional rheometer at 190° C.; and within the range from 0.01 to 3 wt % of at least one organic peroxide; and an elastomer.

Transparent and translucent crosslinked propylene-based elastomers, and their production and use

The present invention provides a crosslinked propylene-based elastomer having an isotactic propylene triad tacticity of from 65 to 95%, a melting point by DSC equal to or less than 110° C., a heat of fusion of from 5 J/g to 50 J/g, and a haze % per 100 mil thickness of 95 or less, and comprising at least 75 wt % propylene-derived units, at least 5 wt % ethylene-derived units, and optionally 10 wt % or less of diene-derived units. In an embodiment, the present invention is a blend of a continuous phase of the crosslinked propylene-based elastomer and a dispersed phase of a crystalline polymeric compound. The present invention also provides elastomeric compositions comprising a crosslinked propylene-based elastomer as described herein and 100 parts by weight or less of a pigment per 100 parts of polymer. The present invention also provides films, fibers, nonwovens, molded objects, and extruded forms which include any of the inventive compositions described herein.

Process for hydroformylation of propylene

Increasing the propylene content of the propylene feed delivered to a continuous hydroformylation process from the 95 mole % maximum level that is usual in typical chemical grade propylene to at least 97 mole %, for example to the 97.5% level obtainable from the conversion of oxygenates to olefins or the 99.5% level of polymer grade propylene, enables adjustments to be made in the syngas feed to the process. This leads to surprising improvements in hydroformylation product yield, in reactor capacity utilization and in the reduction of amounts of waste gases.

Fast fluid bed methanol synthesis

This invention is directed to a process for making a methanol product from a synthesis gas (syngas) feed using a fast fluid bed reactor. The reactor is operated at substantially plug flow type behavior. The heat from circulated catalyst is sufficient to initiate the reaction process with little to no preheating of feed required. In addition, little if any internal reactor cooling is needed.

Processes for the production of esters

A process for production of C4 to C15 esters by the esterification of a carboxylic acid or anhydride with a C4 to C15 alcohol including forming a reaction mixture of the acid or anhydride and the C4 to C15 alcohol including a stoichiometric excess of the alcohol is provided.

Method of preparing group 14 bridged biscyclopentadienyl ligands

The present invention relates to ligands and the synthesis of those ligands for use in metallocene complexes. More particularly, the present invention relates to the synthesis of diarylsilyl bridged biscyclopentadienes using diarylsilyldisulfonates. Even more particularly, the present invention describes Group IV metallocenes containing diarylsilyl bridged bis-cyclopentadienyl ligands prepared from contacting a diarylsilyldisulfonate with an organometallic indenyl reagent.

Polyethylene and process for production thereof

This invention relates to a process for polymerizing olefins in which the amount of trimethylaluminum in a methylalumoxane solution is adjusted to be from 1 to 25 mol %, prior to use as an activator, where the mol % trimethylaluminum is determined by 1H NMR of the solution prior to combination with any support. This invention also relates to a process for polymerizing olefins in which the amount of an unknown species present in a methylalumoxane solution is adjusted to be from 0.10 to 0.65 integration units prior to use as an activator, where the amount of the unknown species is determined by the 1H NMR spectra of the solution performed prior to combination with any support. Preferably, the methylalumoxane solution is present in a catalyst system also comprising a metallocene transition metal compound.

Thermoplastic Elastomer Compositions, Articles Made Therefrom, and Methods for Making Such Articles

Provided are TPV formulations having beneficial properties, such as scratch resistance, improved bondability, e.g., nylon bondability, and improved processability. Preferred TPVs provide lower density, lower cost, and good extrusion capabilities compared to conventional formulations. Sealing systems may be prepared with the TPVs described above. An exemplary automotive sealing system includes a sealant foot and a sealant lip.

Olefinic Copolymer Compositions for Viscosity Modification of Motor Oil

Lube oil compositions and methods for making the same are provided. The lubricating oil composition can include at least one propylene-based polymer comprising 60 wt % to 98 wt % propylene derived units, other units derived from one or more other alpha olefins, and a base oil. The propylene-based polymer can have a triad tacticity of 90% or more, a heat of fusion of less than 80 J/g, and a weight average molecular weight (Mw) as measured by GPC of from 70,000 to 250,000.

Viscosity Modifiers Comprising Blends of Ethylene-Based Copolymers

The present invention is directed to polymer blend compositions for use as viscosity modifiers comprising at least two ethylene-based copolymer components. The viscosity modifiers described herein comprise a first ethylene-based copolymer having an ethylene content of from about 44 to about 52 wt % and/or a heat of fusion of from about 0 to about 15 J/g and a second ethylene-based copolymer having an ethylene content of from about 68 to about 75 wt % and/or a heat of fusion of from about 40 to about 65 J/g. The invention is also directed to lubricant compositions comprising a lubricating basestock and a polymer blend of the invention.

Purification of Aromatic Feedstock

The invention is a process for removing impurities from an aromatics stream and apparatus for the practice thereof, whereby trace olefins and dienes are removed from aromatic plant feedstocks using a reactor design that enables the product to be backmixed with the feedstock and that enables a feed/effluent heat exchanger.

Functionalizable Synthetic Hydrocarbon Fluids and Integrated Method for Production Thereof

This invention relates to a process to produce a poly(alpha-olefin)(alpha, internally unsaturated, nonconjugated olefin) comprising: contacting at least one renewable feedstream with at least one lower olefin in the presence of a metathesis catalyst, wherein a mixture of at least one C 4 to C 40 linear alpha-olefin and at least one alpha, internally unsaturated, nonconjugated olefin is produced; and contacting the mixture with a metallocene catalyst system, wherein a poly(alpha-olefin)(alpha, internally unsaturated, nonconjugated olefin) is produced.

Process And Apparatus For Co-Production Of Olefins And Electric Power

A method and system are disclosed for co-production of olefins and electric power. The method includes determining a separation level, separating a hydrocarbon feed into a light fraction stream and a heavy fraction stream based on the determined separation level; generating electric power from the heavy fraction stream; and cracking the light fraction stream in a pyrolysis unit to produce an effluent comprising olefins. The separation level may be based on olefin production requirements and electric power requirements or specific split of the hydrocarbon feed to be utilized for power generation and olefin production.

Crosslinked Polyolefin Polymer Blends

Crosslinked polyolefin blends, methods for their production, and articles made of the same are provided. In at least one specific embodiment, the polyolefin blends comprise a first polymer formed in a first reactor and a second polymer formed in a second reactor. The first and second polymers, as well as the resulting blend, may comprise units derived from propylene, ethylene, and a diene. The blended composition can then be compounded with one or more coagents, antioxidants, UV sensitizers, and/or other additives and crosslinked, preferably by exposure to UV radiation and/or energetic photons. The crosslinked polymers are particularly useful for making fibers, films, and nonwovens.

Polyketone Plasticizers

The invention relates to polyketone compounds and the at least partially hydrogenated products thereof, the use of said polyketone compounds and/or the at least partially hydrogenated products thereof as plasticizers, processes of making polyketone compounds and the at least partially hydrogenated products thereof, compositions comprising the polyketone compounds and/or the at least partially hydrogenated products thereof, and to articles formed from products of the invention.

Process for the Production of Purified Xylene Isomers

The invention is directed to a process to produce paraxylene and orthoxylene, including reducing the amount of isomerate recycle from vapor phase xylenes isomerization by providing a parallel configuration of vapor phase and liquid phase isomerization units.

Plasticiser Alcohol And Production Improvement

Embodiments of the invention disclosed herein relate to a process for the production of a C 6 -C 15 alcohol mixture comprising the steps of: hydroformylating an olefin mixture comprising a branched C 5 -C 14 olefin to form a hydroformylation product comprising aldehydes and formate esters, whereby the hydroformylation product has a net cold sap number from 15 to 38 mg KOH/g, and converting the aldehydes and formate esters to alcohols in a hydrogenation step comprising at least one first hydrogenation reactor comprising a fixed bed of a heterogeneous sulphided bimetallic catalyst.

Method and Apparatus for Obtaining Aromatics from Diverse Feedstock

The process relates to the use of any naphtha-range stream containing a portion of C8+ aromatics combined with benzene, toluene, and other non-aromatics in the same boiling range to produce toluene. By feeding the A8+ containing stream to a dealkylation/transalkylation/cracking reactor to increase the concentration of toluene in the stream, a more suitable feedstock for the methylation reaction can be produced. This stream can be obtained from a variety of sources, including the pygas stream from a steam cracker, “cat naphtha” from a fluid catalytic cracker, or the heavier portion of reformate.

Process For Producing Cyclohexylbenzene

In a process for producing cyclohexylbenzene, benzene and hydrogen are contacted under hydroalkylation conditions with a catalyst system comprising a MCM-22 family molecular sieve and at least one hydrogenation metal. The conditions comprise a temperature of about 140° C. to about 175° C., a pressure of about 135 psig to about 175 psig (931 kPag to 1207 kPag), a hydrogen to benzene molar ratio of about 0.30 to about 0.65 and a weight hourly space velocity of benzene of about 0.26 to about 1.05 hr −1 .

Slit Film Tape Compositions For Improved Tenacity And Methods For Making Same

Slit film tapes comprising (i) 1 to 50 wt % of a propylene elastomer based upon the total weight of the blend comprising 70 wt % to 95 wt % propylene and about 5 wt % to about 30 wt % alpha-olefin comonomer based upon total weight of the propylene elastomer. The propylene elastomer has a melt flow rate of 1 to 35 dg/min, a peak melting point of less than 115° C., and an mm triad tacticity of at least 70%; (ii) about 50 to about 99 wt % of a polypropylene based upon total weight of the blend comprising about 90 to about 100 mol % propylene wherein the polypropylene has a melt flow rate of 2 to 35 dg/min and a peak melting point of at least 130° C.; and (iii) 0.1 to 50 wt % of filler based upon the total weight of the blend.

Elastomeric Nanocomposites, Nanocomposite Compositions, and Methods of Manufacture

An elastomeric nanocomposite contains: (a) at least one elastomer comprising units derived from isoolefins having from 4 to 7 carbon atoms; (b) at least 10 phr of a carbon black; and (c) at least 1 phr of a nanoclay; wherein when the nanocomposite is used in an article, the article has a gas permeation coefficient of 80.0 cc*mm/[m 2 -day] at 40° C. The carbon black may be graphitized to reduce interactions between the carbon black and the nanoclays. The elastomeric nanocomposite may, with or without the use of the graphitized carbon black, may calendared or extruded in such a manner as to orient the nanoclay platelets within the composition such that the oriented nanoclay elastomer nanocomposite has an orientation parameter of greater than 0.15.

Molecular Sieve Of MFS Framework Type With Controllable Average Size, Its Method of Making And Use

A method of making a crystalline molecular sieve of MFS framework type, preferably ZSM-57, from a synthesis mixture comprising at least one source of tetravalent element (Y), at least one source of trivalent element (X), at least one source of alkali metal hydroxide (MOH), at least one structure-directing-agent (R) and water, said alkali metal (M) comprising potassium, and having the following mole composition (expressed in terms of oxide): YO 2 :( p )X 2 O 3 :( q )OH − :( r )R:( s )H 2 O, wherein (p) is in the range from 0.005 to 0.05, (q) is in the range from 0.01 to 3, (r) is in the range from 0.03 to 2 and (s) is in the range from 10 to 75 (based on total weight of said synthesis mixture); wherein the crystals of molecular sieve formed having an average diameter (D) of less than or equal to 1.5 micron and an average thickness (T) of less than or equal to 300 nanometers.

Halogen Substituted Heteroatom-Containing Metallocene Compounds for Olefin Polymerization

Halogen substituted metallocene compounds are described and comprise one or more monocyclic or polycyclic ligands that are pi-bonded to the metal atom and include at least one halogen substituent directly bonded to an sp 2 carbon atom at a bondable ring position of the ligand, wherein the or at least one ligand has one or more ring heteroatoms in its cyclic structure. When combined with a suitable activator, these compounds show activity in the polymerization of olefins, such as ethylene and propylene.

Oxidation Of Hydrocarbons

In a process for oxidizing a hydrocarbon, the hydrocarbon is contacted with oxygen in the presence of an N-substituted cyclic imide and under conditions to oxidize the hydrocarbon to produce an oxidized hydrocarbon product and at least one decomposition product of the N-substituted cyclic imide. At least a portion of the at least one decomposition product is contacted with hydroxylamine or a salt thereof under conditions to convert the at least one decomposition product back to said imide. 1. A process for oxidizing a hydrocarbon the process comprising:(a) contacting a hydrocarbon with oxygen in the presence of an N-substituted cyclic imide and under conditions to oxidize said hydrocarbon to produce an oxidized hydrocarbon product and at least one decomposition product of the N-substituted cyclic imide; and(b) contacting at least a portion of the at least one decomposition product with a first reactant selected from hydroxylamine or a salt thereof under conditions to convert at least a portion of the at least one decomposition product back to said imide.2. The process of claim 1 , further comprising contacting at least a portion of the at least one decomposition product with a second reactant selected from an acid or anhydride thereof.3. The process of claim 1 , wherein the contacting (a) further forms unreacted N-substituted cyclic imide and the process further comprises:(i) treating the oxidized hydrocarbon product, unreacted N-substituted cyclic imide and at least one decomposition product of the N-substituted cyclic imide with a base prior to the contacting (b) to convert at least a portion of said unreacted imide and said decomposition product to an adduct or salt; and(ii) removing at least a portion of the adduct or salt from the oxidized hydrocarbon product.4. The process of claim 2 , wherein the acid or anhydride thereof is a polycarboxylic acid or anhydride thereof and wherein the polycarboxylic acid or anhydride thereof reacts with said hydroxylamine or ...

Molecular Sieve Composition (EMM-10), Its Method of Making, and Use for Hydrocarbon Conversions

This invention relates to a process for hydrocarbon conversion comprising contacting a hydrocarbon feedstock with a crystalline molecular sieve, in its ammonium exchanged form or in its calcined form, under conversion conditions to form a conversion product, said crystalline molecular sieve comprising unit cells with MWW topology and is characterized by diffraction streaking from the unit cell arrangement in the c direction as evidenced by the arced hk0 patterns of electron diffraction pattern.

Dehydrogenation Process

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a dehydrogenation catalyst produced by a method comprising treating the support with a liquid composition comprising the dehydrogenation component or a precursor thereof and at least one organic dispersant selected from an amino alcohol and an amino acid. The contacting is conducted under conditions effective to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to benzene and to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to paraffins. 1. A dehydrogenation process comprising:(a) providing a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound; and(b) producing a dehydrogenation reaction product stream comprising the step of contacting at least a portion of the hydrocarbon stream with a dehydrogenation catalyst comprising a support and a metal component under conditions effective to convert at least a portion of the at least one non-aromatic six-membered ring compound to benzene and to convert at least a portion of the at least one five-membered ring compound to at least one paraffin,wherein the dehydrogenation catalyst is produced by a method comprising treating the support with a liquid composition comprising the metal component or a precursor thereof and at least one organic dispersant selected from an amino alcohol and an amino acid.2. The process of claim 1 , wherein the dehydrogenation catalyst has an alpha value from about 0 to about 20.3. The process of claim 1 , wherein the dehydrogenation catalyst has an alpha value from about 0 to about 5.4. The process of claim 1 , wherein the dehydrogenation catalyst has an alpha value from about 0 to about 1.5. The process of claim 1 , wherein the ...

Dehydrogenation Process

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a dehydrogenation catalyst comprising: (i) a support; (ii) a first component comprising at least one metal component selected from Group 1 and Group 2 of the Periodic Table of Elements; and (iii) a second component comprising at least one metal component selected from Groups 6 to 10 of the Periodic Table of Elements, wherein the catalyst composition exhibits an oxygen chemisorption of greater than 50%. The contacting is conducted under conditions effective to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to benzene and to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to paraffins. 1. A dehydrogenation process comprising:(a) providing a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound; and(b) producing a dehydrogenation reaction product stream comprising the step of contacting at least a portion of the hydrocarbon stream with a dehydrogenation catalyst under conditions effective to convert at least a portion of the at least one non-aromatic six-membered ring compound to benzene and to convert at least a portion of the at least one five-membered ring compound to at least one paraffin;wherein the dehydrogenation catalyst comprises: (i) a support; (ii) a first component comprising at least one metal component selected from Group 1 and Group 2 of the Periodic Table of Elements wherein the first component is present in an amount of at least 0.1 wt %; and (iii) a second component comprising at least one metal component selected from Groups 6 to 10 of the Periodic Table of Elements and wherein the catalyst composition has an oxygen chemisorption of greater than 50%.2. The process of claim 1 , wherein ...

System and Method for Providing a Continuous Flow of Catalyst Into a Polyolefin Reactor

Both a catalyst feed system and a method are provided for providing a flow, of a mud-like catalyst slurry into a polyolefin reactor. The system includes a pressurized reservoir of the catalyst having an outlet, and a progressive cavity pump including a stator and a rotor. The pump stator has an inlet connected to the reservoir outlet, and an outlet leading to the polyolefin reactor. In operation, the reservoir is first pressurized to a level a little higher than the pressure of the reactor. The outlet of the reservoir is opened and the progressive cavity pump is actuated. The pressure drop generated across the catalyst slurry contained in the reservoir by the pump causes the slurry diluent to flow between the interstices of the particles of catalyst. The thick, mud-like catalyst slurry is quickly transformed into a much less viscous, syrup-like slurry that flows from the reservoir outlet to the inlet of the pump stator. The progressive cavity pump then continuously conveys the catalyst through the stator outlet and into the reactor. 139-. (canceled)41. The system defined in claim 40 , wherein the progressive cavity pump produces a controlled flow of slurry catalyst to the polyolefin reactor.42. The system defined in claim 41 , wherein the controlled flow is a continuous flow.43. The system defined in claim 40 , further comprising a catalyst agitator provided between the reservoir outlet and the stator inlet that lowers the viscosity of the catalyst slurry flowing into said pump stator.44. The system defined in claim 43 , wherein said catalyst agitator is formed from a distal portion of said rotor that extends beyond said stator.45. The system defined in claim 40 , wherein said progressive cavity pump further includes a motor having an output shaft claim 40 , and a drive train connected to said motor output shaft that provides a drive torque to a proximal end of said rotor.46. The system defined in claim 45 , wherein said drive train is incapable of rotating in ...

Fluid Separation Systems And Methods

Systems and methods for separating particles from fluids are provided. The system comprises a vessel with a fluid inlet and a fluid outlet and a baffle assembly located within the vessel. The baffle assembly has a plurality of baffles that can provide a change in direction to fluid entering the vessel thereby separating particles. During shut-down of a polymerization reactor, reaction mixture is discharged to a separation system where polymer particles are removed from the mixture prior to being released into the atmosphere.

Dehydrogenation Process

In a dehydrogenation process a hydrocarbon stream comprising at least one non-aromatic six-membered ring compound and at least one five-membered ring compound is contacted with a first catalyst comprising at least one metal component and at least one support and a second catalyst. The first catalyst is utilized to convert at least a portion of the at least one non-aromatic six-membered ring compound in the hydrocarbon stream to at least one aromatic compound and the second catalyst is utilized to convert at least a portion of the at least one five-membered ring compound in the hydrocarbon stream to at least one paraffin.

Processes Utilizing Switch Condensers

Processes for controlling the operation of switch condensers are provided. 2. The process of claim 1 , wherein n is a number from 1-15.3. The process of claim 1 , wherein n is a number from 1-10.4. The process of claim 1 , further comprising switching the plurality of switch condensers to operate in an x−n′/y−n cycle; wherein n′ is independently a number from 1-20.5. The process of claim 1 , further comprising switching the plurality of switch condensers to operate in an x+n″/y−n cycle; wherein n″ is independently a number from 1-20.6. The process of claim 1 , wherein the switching is controlled by a process control application.7. The process of claim 6 , wherein the process control application comprises a distributed control software program.8. The process of claim 6 , wherein the process control application comprises at least one of the abilities to control the operating modes claim 6 , to monitor the condition of the switching valves claim 6 , to regulate the temperature of the switch condensers claim 6 , and any combination thereof.9. The process of claim 1 , wherein after the switching claim 1 , the gas rate through the switch condensers remains substantially the same.10. The process of claim 1 , wherein after the switching claim 1 , the gas rate through the switch condensers is increased by no more than 10%.11. The process of claim 1 , wherein after the switching claim 1 , the gas rate through the switch condensers is increased by no more than 5%.12. The process of claim 1 , wherein the loss of heat exchanger capacity of the plurality of the switch condensers after switching cycles is 15% or less.13. The process of claim 1 , wherein the loss of heat exchanger capacity of the plurality of the switch condensers after switching cycles is 10% or less.14. The process of claim 1 , wherein the loss of heat exchanger capacity of the plurality of the switch condensers after switching cycles is 5% or less.15. A continuous process for the recovery of phthalic anhydride ...

CONSTRUCTION COMPRISING TIE LAYER

A vulcanizable layered composition comprising at least two layers and at least one tie layer. The first layer of the two layers comprises an fluid permeation prevention layer, the second layer of the two layers comprises at least one high diene rubber, and the tie layer comprises about 50 to about 100 weight % of at least one halogenated isobutylene containing elastomer; up to about 50 weight % of at least one high diene elastomer; about 20 to about 50 weight % of at least one filler; up to about 30 weight % of at least one processing oil; about 1 to about 20 parts per hundred (phr) of at least one tackifier; and about 0.2 to about 15 parts per hundred of rubber (phr) of a curing system for the elastomers. The fluid permeation prevention layer preferably comprises a thermoplastic engineering resin component and an elastomer component. 1. A pneumatic tire , the tire comprising a vulcanizable layered composition and an adjacent carcass layer , said vulcanizable layer composition comprising a fluid permeation prevention layer and a tie layer ,wherein the tie layer comprises a mixture of:(1) 100 weight % of at least one halogenated isobutylene containing elastomer based upon the weight of elastomer present in the tie layer;(2) about 20 to about 50 weight % of at least one filler;(3) about 0 to about 30 weight % of at least one processing oil;(4) about 1 to about 20 parts per hundred rubber (phr) of a mixture of at least two tackifiers, wherein the tackifiers are selected from the group consisting of rosin, rosin derivatives, condensate of tert-butyl phenol and acetylene, and mixtures thereof; and(5) about 0.2 to about 15 parts per hundred of rubber (phr) of a curing system for the elastomers;wherein said fluid permeation prevention layer comprises a polymer composition having a Young's modulus of 1 to 500 MPa, said polymer composition comprising:(A) at least 10% by weight, based on the total weight of the polymer composition of at least one thermoplastic engineering ...

Vinyl Terminated Higher Olefin Polymers and Methods to Produce Thereof

This invention relates to higher olefin vinyl terminated polymers having an Mn of at least 200 g/mol (measured by H NMR) including of one or more Cto Chigher olefin derived units, where the higher olefin vinyl terminated polymer comprises substantially no propylene derived units; and wherein the higher olefin polymer has at least 5% allyl chain ends and processes for the production thereof. These vinyl terminated higher olefin polymers may optionally include ethylene derived units. 1. A higher olefin vinyl terminated polymer having an Mn (measured by H NMR) of at least 160 g/mol comprising at least 15 mol % of one or more Cto Chigher olefin derived units , where the higher olefin polymer comprises substantially no propylene derived units; and wherein the higher olefin polymer has at least 20% allyl chain ends , provided however that if the polymer consists essentially of octene and tetradecene then the polymer has at least 45% allyl chain ends (relative to total unsaturation).2. The higher olefin polymer of claim 1 , wherein the higher olefin polymer has an Mn in the range of 200 to 100 claim 1 ,000 g/mol.3. The higher olefin polymer of claim 1 , wherein the Cto Chigher olefin is selected from butene claim 1 , pentene claim 1 , hexene claim 1 , heptene claim 1 , octene claim 1 , nonene claim 1 , decene claim 1 , undecene claim 1 , dodecene claim 1 , norbornene claim 1 , norbornadiene claim 1 , dicyclopentadiene claim 1 , cyclopentene claim 1 , cycloheptene claim 1 , cyclooctene claim 1 , cyclooctadiene claim 1 , cyclododecene claim 1 , 7-oxanorbornene claim 1 , 7-oxanorbornadiene claim 1 , substituted derivatives thereof claim 1 , and isomers thereof.4. The higher olefin polymer of claim 1 , further comprising at least 5 mol % ethylene derived units.5. The higher olefin polymer of claim 1 , wherein the higher olefin polymer has an allyl chain end to vinylidene chain end ratio of 1:1 or greater.6. The higher olefin polymer of claim 1 , wherein the higher olefin ...

Thermoplastic Polyolefin Blends and Films Therefrom

This invention relates to a film comprising a blend composition comprising: 1) a linear ethylene containing polymer, such as a LLDPE, a HDPE or the like; and at least 1 weight percent of an in-reactor polymer blend comprising: (a) a first ethylene containing polymer having a density of greater than 0.90 g/cmand a Mof more than 20,000 g/mol; and (b) a second ethylene containing polymer having a density of less than 0.90 g/cm, wherein the polymer blend has a Tof at least 90° C. (DSC second melt), a density of less than 0.92 g/cm, and the densities of the first and second polymers differ by at least 1%. 1. A film comprising a composition comprising:{'sup': '3', '1) a linear ethylene containing polymer having a density of at least 0.910 g/cm; and'}{'sup': 3', '3', '3, 'sub': w', 'm, '2) an in-reactor polymer blend comprising: (a) a first ethylene containing polymer having a density of greater than 0.90 g/cmand a Mof more than 20,000 g/mol and (b) a second ethylene containing polymer having a density of less than 0.90 g/cm, wherein the densities of the first and second polymers differ by at least 1%, and wherein the in-reactor polymer blend has a Tof at least 90° C. (DSC second melt), a density of less than 0.92 g/cm, and contains at least 78 wt % ethylene.'}2. The film of claim 1 , wherein the linear ethylene containing polymer has a CDBI of 60% or more.3. The film of claim 1 , wherein the linear ethylene containing polymer is an LLDPE or an HDPE.4. The film of claim 1 , wherein the linear ethylene containing polymer has an Mof 50 claim 1 ,000 g/mol or more claim 1 , a g′ of 0.95 or more and an M/Mof from greater than 1 to 10 and comprises from 50 mole % to 100 mole % ethylene and from 0 mole % to 50 mole % of Cto Ccomonomer.5. The film of claim 1 , wherein the linear ethylene containing polymer is a polymer of an ethylene and at least one alpha olefin having 5 to 20 carbon atoms claim 1 , where the linear ethylene containing polymer has a melt index (190° C./2.16 kg) ...

Olefin Functionalization By Metathesis Reaction

This invention relates to a process to functionalize propylene co-oligomer comprising contacting an alkene metathesis catalyst with a heteroatom containing alkene, and a propylene a co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends, where: 1) X=(−0.94 (mol % ethylene incorporated)+100), when 10 to 60 mol % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mol % ethylene is present in the co-oligomer, and 3) X=(1.83*(mol % ethylene incorporated)−83), when 70 to 90 mol % ethylene is present in the co-oligomer. This invention also relates to a process to functionalize propylene homo-oligomer comprising contacting an alkene metathesis catalyst with a heteroatom containing alkene, and a propylene homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 100 ppm aluminum. 1. A process to functionalize propylene co-oligomer comprising contacting an alkene metathesis catalyst with a heteroatom containing alkene , and a propylene co-oligomer having an Mn of 300 to 30 ,000 g/mol (as measured by H NMR) comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene , wherein the oligomer has at least X % allyl chain ends (relative to total unsaturations) , where: 1) X=(−0.94*(mol % ethylene incorporated)+100) , when 10 to 60 mol % ethylene is present in the co-oligomer , and 2) X=45 , when greater than 60 and less than 70 mol % ethylene is present in the co-oligomer , and 3) X=(1.83*(mol % ethylene incorporated)-83) , when 70 to 90 mol % ethylene is present in the co-oligomer.2. The process of wherein the oligomer has more than 90% allyl chain ends (relative to total unsaturations).3. The process of wherein the oligomer comprises 15 to 95 wt % ethylene ...

Vinyl-Terminated Macromonomer Oligomerization

Vinyl-terminated macromonomer oligomerization, namely, a process to produce polymacromonomers comprising contacting a vinyl-terminated macromonomer with a catalyst system capable of oligomerizing vinyl-terminated macromonomer, in the presence of an aluminum containing compound, a zinc containing compound, or a combination thereof, under polymerization conditions to produce a polymacromonomer, and polymacromonomers produced thereby. Also, polymacromonomers having a degree of polymerization greater than 10, a glass transition temperature Tg of less than 60° C., and an Mn of greater than or equal to about 5000 Da. 1. A process to produce polymacromonomers comprising contacting (1) a vinyl-terminated macromonomer having an Mn of 125 Da or more and at least 70% vinyl termination (as measured by H NMR) relative to total unsaturations , and (2) up to 40 wt % of Cto Ccomonomer , with (3) a catalyst system capable of oligomerizing vinyl-terminated macromonomer , in the presence of a chain transfer agent , under polymerization conditions at a temperature from 20° C. to 180° C. and a reaction time of 1 min to 24 hours to produce a polymacromonomer having a degree of polymerization greater than 10 , a branching index g′() less than 0.9 , a Tg from −10° C. to 40° C. , and an Mn of greater than or equal to about 5000 Da.2. The process of claim 1 , wherein the vinyl-terminated macromonomer claim 1 , prior to polymerization claim 1 , is one or more of:(i) a vinyl-terminated polymer having at least 5% allyl chain ends;{'sup': '1', 'sub': 4', '40, '(ii) a vinyl-terminated polymer having an Mn of at least 200 g/mol (measured by H NMR) comprising one or more Cto Chigher olefin derived units, where the higher olefin polymer comprises substantially no propylene derived units; and wherein the higher olefin polymer has at least 5% allyl chain ends;'}{'sup': '1', 'sub': 5', '40, '(iii) a copolymer having an Mn of 300 g/mol or more (measured by H NMR) comprising (a) from about 20 mol % to ...

Process for Forming Polymer Blends

A method for forming a fiber, the method comprising charging to a reactive extruder a first polymer and a second polymer to form an initial blend, where the first polymer is a propylene-based elastomer including up to 35% by weight ethylene-derived units and a heat of fusion, as determined according to DSC procedures according to ASTM E-793, of less than 80 J/g and a melt temperature of less than 110° C., where the second polymer is a propylene-based polymer having a melt temperature in excess of 110° C. and a heat of fusion in excess of 80 J/g, and introducing the reactive blend to a spinneret to form a fiber or extruding the reacted blend through a plurality of die capillaries to form molten threads or filaments which are attenuated in a gas stream to form meltblown fibers. 1. A method for forming one or more fibers , the method comprising:(i) charging to a reactive extruder a first polymer and a second polymer to form an initial blend, where the first polymer is a propylene-based elastomer including up to 35% by weight ethylene-derived units and a heat of fusion, as determined according to DSC procedures according to ASTM E-793, of less than 80 J/g and a melt temperature of less than 110° C., where the second polymer is a propylene-based polymer having a melt temperature in excess of 110° C. and a heat of fusion in excess of 80 J/g;(ii) after said step of charging, charging a peroxide to the initial blend to thereby form a reactive blend;(iii) conducting the reactive blend at a flow rate through a series of barrels within the extruder;(iv) subjecting the reactive blend, in one or more barrels, to high shear mixing;(v) maintaining the temperature of the reactive blend at a temperature sufficient to decompose at least 50% of the peroxide and thereby form a reacted blend;(vi) restricting flow rate of the reacted blend through one or more barrels to increase the time that the reactive blend is subjected to the high shear mixing;(vii) increasing flow rate of the ...

High Vinyl Terminated Propylene Based Oligomers

This invention relates to a co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends, where: 1) X=(−0.94 (mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer. This invention also relates to a homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 100 ppm aluminum. This invention also relates to a process of making homo-oligomer, comprising propylene, wherein the productivity is greater than 4500 g/mmol Hf (or Zr)/hour. 1. A co-oligomer having an Mn of 300 to 30 ,000 g/mol (measured by H NMR) comprising 10 to 50 mol % propylene and 50 to 90-mol % of ethylene , wherein the co-oligomer has at least X % allyl chain ends (relative to total unsaturations) , where: 1) X=1.20*(−0.94*(mole % ethylene incorporated)+100) , when 50 to 60 mole % ethylene is present in the co-oligomer , and 2) X=45 , when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer , and 3) X=(1.83* (mole % ethylene incorporated)−83) , when 70 to 90 mole % ethylene is present in the co-oligomer.2. The co-oligomer of claim 1 , wherein the co-oligomer has more than 90% allyl chain ends (relative to total unsaturations).3. The co-oligomer of claim 1 , wherein the co-oligomer has more than 80% allyl chain ends (relative to total unsaturations).4. The co-oligomer of claim 1 , wherein the co-oligomer has more than 70% allyl chain ends (relative to total unsaturations).5. The co-oligomer of claim 1 , wherein the co-oligomer has more than 95% allyl chain ends ( ...

High Vinyl Terminated Propylene Based Oligomers

This invention relates to a co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends, where: 1) X=(−0.94(mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer. This invention also relates to a homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 100 ppm aluminum. This invention also relates to a process of making homo-oligomer, comprising propylene, wherein the productivity is greater than 4500 g/mmol Hf (or Zr)/hour.

Monoalkylated Aromatic Compound Production

A process for producing a monoalkylated aromatic compound in an alkylation reaction zone, said process comprising the steps of: 1. A process for producing a monoalkylated aromatic compound in an alkylation reaction zone , said process comprising the steps of:{'sup': '−1', '(a) providing a first catalytic particulate material which comprises MCM-56 and having a ratio of surface area over surface volume ratio in the range of 241 to 2867 cm;'}(b) providing said alkylation reaction zone with an alkylatable aromatic compound, an alkylating agent, and said first catalytic particulate material; and whereby the molar ratio of said polyalkylated aromatic compound(s) over said monoalkylated aromatic compound produced by said first catalytic particulate material is less than the molar ratio of polyalkylated aromatic compound(s) over monoalkylated aromatic compound produced by a second catalytic particulate material and said alkylation reaction zone is operated under the same alkylation conditions,', {'sup': '−1', 'wherein at least 51 wt. % of said second catalytic particulate material having a ratio of surface area over surface volume between 78 and 79 cm.'}], '(c) contacting said alkylatable aromatic compound and said alkylating agent with said catalytic particulate material in said alkylation reaction zone maintained under alkylation conditions, to form a product comprised of said monoalkylated aromatic compound and polyalkylated aromatic compound(s);'}2. The process of claim 1 , wherein the moles of said monoalkylated aromatic compound produced by said first catalytic particulate material is greater than the moles of monoalkylated aromatic compound produced by said second catalytic particulate material when said alkylation reaction zone is operated under the same alkylation conditions for the same amount of time with the same mass of said first and second catalytic particulate material claim 1 ,{'sup': '−1', 'wherein at least 51 wt. % of said second catalytic particulate ...

Dynamic Modulation of Metallocene Catalysts

This invention relates to a process to alter comonomer distribution in a copolymer (as compared to a copolymer made absent the Lewis base modifier) comprising contacting ethylene and one or more C 3 to C 40 comonomers; with a catalyst system comprising: 1) a Lewis base modifier; 2) an activator; and 3) a bridged bisindenyl group 4 transition metal metallocene catalyst compound having a hydrogen atom at least one 2 position.

Modified Polyethylene Compositions

The present invention relates to a branched modifier and a composition comprising more than 25 wt % (based on the weight of the composition) of one or more linear ethylene polymers having a g′of 0.97 or more and an Mof 20,000 g/mol or more and at least 0.1 wt % of a branched modifier where the modifier has a g′of less than 0.97, wherein the ethylene polymer has a g′of at least 0.01 units higher than the g′of the branched modifier. 1. A branched polyethylene modifier comprising at least 50 mol % ethylene , one or more Cto Ccomonomers , and a polyene having at least two polymerizable bonds , wherein said branched polyethylene modifier: a) has a g′of less than 0.97; b) is essentially gel free; c) has an Mw of 100 ,000 g/mol or more; and d) has an Mw/Mn of 4.0 or more.2. The modifier of claim 1 , wherein the comonomer is present at from 0.5 mol % to 30 mol %.3. The modifier of claim 1 , wherein the polyene is present at from 0.001 mol % to 10 mol %.4. The modifier of claim 1 , wherein the modifier has a g′of 0.90 or less.5. The modifier of claim 1 , wherein the modifier has a strain-hardening ratio of 2 or greater.6. The modifier of claim 1 , wherein the Cto Ccomonomers are one or more Cto Calpha olefin comonomers.7. The modifier of claim 1 , wherein the modifier has 5 wt % or less of xylene insoluble material.8. The modifier of claim 1 , wherein the Cto Ccomonomers are one or more of hexene claim 1 , butene claim 1 , or octene.9. The modifier of claim 1 , wherein the polyene is selected from the group consisting of: 1 claim 1 ,4-pentadiene claim 1 , 1 claim 1 ,5-hexadiene claim 1 , 1 claim 1 ,6-heptadiene claim 1 , 1 claim 1 ,7-octadiene claim 1 , 1 claim 1 ,8-nonadiene claim 1 , 1 claim 1 ,9-decadiene claim 1 , 1 claim 1 ,10-undecadiene claim 1 , 1 claim 1 ,11-dodecadiene claim 1 , 1 claim 1 ,12-tridecadiene claim 1 , 1 claim 1 ,13-tetradecadiene claim 1 , tetrahydroindene claim 1 , norbornadiene also known as bicyclo-(2.2.1)-hepta-2 claim 1 ,5-diene claim 1 , ...

Elastic Film Compositions with Improved Tear Resistance

A film composition comprising one or more propylene-based polymers and one or more hydrocarbon resins, and methods for making the same are provided. The propylene-based polymer may have (i) 60 wt % or more units derived from propylene, (ii) isotactically arranged propylene derived sequences, and (iii) a heat of fusion less than 65 J/g. The hydrocarbon resin may have a glass transition temperature greater than 20° C. 19-. (canceled)10. A method for making a film composition , comprising:admixing one or more propylene-based polymers and one or more miscible hydrocarbon resins in an amount sufficient to form a blend which provides a film having an increase in intrinsic tear by at least 5% compared to a film without either the one or more propylene-based polymers or the one or more miscible hydrocarbon resins,the propylene-based polymers each having (i) 60 wt % or more units derived from propylene, (ii) isotactically arranged propylene derived sequences, and (iii) a heat of fusion less than 45 J/g; and the hydrocarbon resins each having a glass transition temperature greater than 20° C.11. The method of claim 10 , wherein the blend further comprises polypropylene or one or more thermoplastic resins.12. The method of claim 10 , wherein the propylene-based polymer is present in the film in an amount of from 80 to 99 wt % and the hydrocarbon resin is present in an amount of from 1 to 20 wt % claim 10 , based on the total weight of the film.13. The method of claim 10 , wherein the intrinsic tear of the film is at least 1.5 gm/micron.14. The method of claim 10 , further comprising one or more styrenic block copolymers.15. The method of claim 10 , wherein the propylene-based polymer has a melt flow rate (230° C./2.16 Kg) of at least 3.0 g/10 min.16. The method of claim 10 , wherein the propylene-based polymer has a density of at least 0.80 g/cm.17. The method of claim 10 , wherein the propylene-based polymer has a melt temperature of less than 110° C.18. The method of claim ...

High-Pressure Valve

Disclosed in one aspect is a valve comprising (a) a valve body having a poppet valve chamber with an axis running there through; (b) a seat having a seat sealing surface, and a outer-seat surface, the seat located axially within the poppet valve chamber; and (c) a poppet having a poppet sealing surface, the poppet being located axially within the poppet valve chamber; wherein a poppet-seat interface is created between at least a portion of the seat sealing surface and at least a portion of the poppet sealing surface, the poppet-seat interface being at an angle β of from 20 to 90° to the axis. In one embodiment the seat is removable, allowing the geometry of at least the poppet head surface and/or the seat inside surface, which defines a fluid flow-path cross-section, to be tailored. 123-. (canceled)24. A valve comprising:(a) a valve body having a poppet valve chamber and an axis running there through;(b) a removable seat having a seat inside surface, the seat located within the poppet valve chamber; and(c) a poppet having a poppet head surface, the poppet being located within the poppet valve chamber, the poppet head surface comprising two surfaces that form an intersection that is operable to removably contact the seat inside surface, and wherein the location of the poppet is dependent on the flow rate of a fluid through the valve.25. The valve of claim 24 , wherein the poppet head surface and the seat inside surface are operable to form a flow restriction zone.26. The valve of claim 24 , wherein the seat inside surface has a seat sealing surface claim 24 , and a poppet-seat interface is created between the seat sealing surface and at least one of the two surfaces of the poppet head surface claim 24 , the poppet-seat interface being at an angle β of from 20° to 90° to the axis.27. A valve comprising:(a) a valve body having a poppet valve chamber with an axis running there through and a valve inside surface;(b) a removable seat having a seat sealing surface, a flow ...

Hydrocarbon Pyrolysis Process

Disclosed is a pyrolysis process that is capable of being with reduced coke and/or tar formation. The process can pyrolyze hydrocarbon feed that contains low- to mid-range levels of non-volatiles. Pyrolysis is carried out with a predetermined amount of the feed being in the liquid phase so as to minimize coke and/or tar formation in the pyrolysis reactor. The pyrolysis feed may also include a diluent, such as molecular hydrogen, that further acts to minimize coke and/or tar formation in the pyrolysis reactor. The amount of diluent in the pyrolysis feed can be adjusted to adjust or control dry point of the hydrocarbon in the pyrolysis feed. 1. A method for pyrolyzing a pyrolysis feed in a thermal pyrolysis regenerative reactor to produce a pyrolyzed hydrocarbon product , comprising the steps of:providing a pyrolysis feed having (i) a liquid portion and (ii) a vapor portion, the pyrolysis feed comprising a hydrocarbon component containing greater than 0.010 wt % of a non-volatile component based on total weight of the pyrolysis feed, and wherein the liquid portion is sufficient to maintain the non-volatile component in the liquid portion;passing the pyrolysis feed to a first end of a regenerative reactor;vaporizing at least a portion of the liquid portion of the pyrolysis feed at the first end of the regenerative reactor;pyrolyzing at least a portion of the hydrocarbon component to produce the pyrolyzed hydrocarbon product that comprises acetylene;conducting away the pyrolyzed hydrocarbon product from a second end of the regenerative reactor; andremoving from the regenerative reactor at least a portion of the non-volatile component via the first end of the regenerative reactor.2. The method of claim 1 , wherein the non-volatile component comprises a combustible non-volatile component and a non-combustible non-volatile component.3. The method of claim 2 , wherein the ratio of combustible non-volatile component to non-combustible non-volatile component is in the range ...

Adhesive Composition

A composition comprising a hot melt pressure-sensitive adhesive comprising a propylene-based polymer component having a melting point less than or equal to about 130° C. and a triad tacticity greater than about 75%, and free of or having a low block copolymer content. Also, an adhesive article comprising the composition. 1. A hot melt pressure-sensitive adhesive composition comprising a propylene-based polymer component comprising from about 60 to about 98 wt % propylene and from about 2 to about 40 wt % of one or more of ethylene and C-Calpha-olefins , based on the weight of the propylene-based polymer component , the propylene-based polymer component having a melting point less than or equal to about 130° C. and a triad tacticity greater than about 75%; the hot melt pressure-sensitive adhesive composition free of or comprising not more than about 30 wt % of a block copolymer based on the weight of the hot melt pressure sensitive adhesive composition.2. The hot melt pressure-sensitive adhesive composition of claim 1 , wherein the propylene-based polymer component comprises from about 75 to about 98 wt % propylene and from about 2 to about 25 wt % of one or more of ethylene and C-Calpha-olefins claim 1 , and wherein the propylene-based polymer component has a melting point less than or equal to about 120° C.3. The hot melt pressure-sensitive adhesive composition of claim 1 , wherein the propylene-based polymer component further has a heat of fusion less than about 90 J/g.4. The hot melt pressure-sensitive adhesive composition of claim 1 , wherein the propylene-based polymer component has a melt flow rate (MFR) of from about 1 to about 900 g/10 min claim 1 , as measured according to ASTM D-1238 at 230° C. claim 1 , 2.16 kg.5. The hot melt pressure-sensitive adhesive composition of claim 1 , having a viscosity of less than or equal to about 150 claim 1 ,000 mPa-s at 175° C. determined according to ASTM D 3236 claim 1 , or an equivalent thereof.6. The hot melt pressure ...

Polymeric Compositions Useful as Rheology Modifiers and Methods for Making Such Compositions

Disclosed are rheology modifiers comprising compositionally disperse polymeric compositions and/or crystallinity disperse polymeric compositions that may be useful in modifying the rheological properties of lubrication fluids, and methods for making such compositions. The compositionally disperse polymeric composition are formed from at least two discrete compositions of ethylene copolymers. The crystallinity disperse polymeric composition are formed from ethylene copolymers having at least two discrete values of residual crystallinity. 113.-. (canceled)14. A polymeric composition comprising: [{'sub': 'A', 'i. an Hin the range from greater than or equal to 0 to less than or equal to 30; and'}, {'sub': 'A', 'ii. a Mwof less than 130,000; and'}], '(a) a first ethylene copolymer having [{'sub': 'B', 'i. an Hin the range from greater than 30 to less than or equal to 60; and'}, {'sub': 'B', 'ii. a Mwof less than 70,000.'}], '(b) a second ethylene copolymer having15. The polymeric composition of claim 14 , wherein the first ethylene copolymer and/or the second ethylene copolymer have a substantially linear structure.16. The polymeric composition of claim 14 , wherein the first ethylene copolymer and/or the second ethylene copolymer have a MWD of about 2.4 or less.17. The polymeric composition of claim 14 , wherein MWD of the first ethylene copolymer is in the range from greater than or equal to 1.80 to less than or equal to 1.95 claim 14 , and/or wherein MWD of the second ethylene copolymer is in the range from greater than or equal to 1.80 to less than or equal to 1.95.18. The polymeric composition of claim 14 , wherein His less than Hfor the polymeric composition.19. The polymeric composition of claim 14 , wherein His in the range from greater than or equal to 0 to less than or equal to 10.20. The polymeric composition of claim 14 , wherein MI/MIis less than or equal to 3.0.21. The polymeric composition of claim 14 , wherein the weight percent of the first ethylene ...

Process for Producing Novel Synthetic Basestocks

This disclosure relates to a liquid syndiotactic polyalphaolefin, sPAO, comprising one or more Cto Cmonomers, said sPAO having: a) an rr triad content of 5 to 50% as measured by C NMR; b) an mr triad content of 25 to 60% as measured by C NMR, where the mr to mm triad ratio is at least 1.0; c) a pour point of Z ° C. or less, where Z=0.0648X−51.2, where X=kinematic viscosity at 100° C. as reported in centistokes (cSt); d) a kinematic viscosity at 100° C. of 100 cSt or more (alternatively 200 cSt or more); e) a ratio of mr triads to rr triad (as determined by C NMR) of less than 9; f) a ratio of vinylidene to 1,2-disubstituted olefins (as determined by H NMR) of less than 8; g) a viscosity index of 120 or more; and h) an Mn of 40,000 or less. This disclosure further relates to processes to make and use sPAOs, including those having any combination of characterics a) to h). 16.-. (canceled)9. The process of claim 7 , wherein the sPAO has the following characteristics:{'sup': '13', 'a) an rr triad content of 25 to 60%, as measured by C NMR;'}{'sup': '13', 'b) an mr triad content of at least 45%, as measured by C NMR, where % mr triad is greater than the % mm triad content by at least 50%;'}c) a pour point of Z ° C. or less, where Z=0.0648X−51.2, where X=kinematic viscosity at 100° C. as reported in centistokes (cSt);d) a kinematic viscosity at 100° C. of 100 cSt or more;{'sup': '13', 'e) a ratio of mr triads to rr triad, as determined by C NMR, of less than 9;'}{'sup': '1', 'f) a ratio of vinylidene to 1,2-disubstituted olefins, as determined by H NMR, of less than 8;'}g) a viscosity index of 120 or more; andh) an Mn of 40,000 or less.10. The process of claim 7 , further comprising1) optionally treating the sPAO to reduce heteroatom containing compounds to less than 600 ppm; and or2) optionally separating the sPAO from solvents or diluents; and or3) contacting the sPAO with hydrogen and a hydrogenation catalyst; and or4) obtaining a sPAO having a Bromine number less than ...

Nonwoven Fabrics Made From Polymer Blends And Methods For Making Same

The present invention is directed to polymer blends for use in nonwoven fabric applications, and to fabrics formed from the polymer blends. In one or more embodiments, the polymer blends comprise from about 70 to about 99.9 wt %, based on the total weight of the composition, of a first propylene-based polymer and from about 0.1 to about 30 wt % of a second propylene-based polymer. The first polymer has a melt flow rate of from about 100 to about 5,000 g/10 min, and the second polymer has a melt flow rate of from about 1 to about 500 g/min, and the second polymer has either a lower melt flow rate or a higher triad tacticity than the first polymer.

Functionalization of Vinyl Terminated Polymers by Ring Opening Cross Metathesis

This invention relates to a polymer of a cyclic olefin and a vinyl terminated macromonomer, and processes for the production thereof.

Functionalized High Vinyl Terminated Propylene Based Oligomers

This invention relates to a functionalized co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends, where: 1) X=(−0.94 (mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer. This invention also relates to a functionalized homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 100 ppm aluminum. This invention also relates to a process of making functionalized homo- or co-oligomer, comprising propylene, wherein the productivity is greater than 4500 g/mmol Hf (or Zr)/hour.

Alkylation Process

The present invention provides an improved process for the catalytic conversion of a feedstock comprising an alkylatable aromatic compound and an alkylating agent to form a conversion product comprising the desired alkylaromatic compound by contacting said feedstock in at least partial liquid phase under catalytic conversion conditions with a catalyst composition comprising a porous crystalline material having a structure type of FAU, BEA* or MWW, or a mixture thereof, wherein the porous crystalline material has a Relative Activity measured at 220° C. as an RAof at least 7.5 or measured at 180° C. as RAof at least 2.5, allowing operation at lower reaction pressures, e.g., a reaction pressure of about 450 psig (3102 kPa) or less, and lower alkylating agent feed supply pressure of 450 psig (3102 kPa) or less. 1. In a process for catalytic conversion of a feedstock comprising at least one alkylatable aromatic compound and an alkylating agent to form a conversion product comprising an alkylaromatic compound , the process comprising the step of contacting said feedstock in at least partial liquid phase under catalytic conversion conditions including a molar ratio of alkylatable aromatic compound to alkylating agent of from about 0.1:1 to about 100:1 , and a feed weight hourly space velocity (WHSV) based on the alkylating agent of from about 0.1 to about 500 hr , with a catalyst composition comprising a porous crystalline material having a structure type of FAU , *BEA or MWW , or a mixture thereof , the improvement comprising modifying said catalyst composition to have a Relative Activity measured as an RAat 220° C. of at least 7.5 or RAat 180° C. of at least 2.5 , wherein said catalytic conversion conditions include a temperature of less than about 270° C. and a pressure of about 450 psig (3102 kPa) or less , and wherein said alkylating agent feed supply pressure is 450 psig (3102 kPa) or less , wherein said Relative Activity is the percent temperature rise in an ...

Aromatics Production Process and Apparatus

In a process for producing para-xylene, a naphtha feed is reformed under conditions effective to convert at least 50 wt % of the naphthenes in the naphtha feed to aromatics, but to convert no more than 25 wt % of the paraffins in the naphtha feed, and thereby produce a reforming effluent. A first stream containing benzene and/or toluene is removed from the reforming effluent and is fed to a xylene production unit under conditions effective to convert benzene and/or toluene to xylenes. In addition, a second stream containing C8 aromatics is removed from the reforming effluent and is fed, together with at least part of the xylenes produced in the xylene production unit, to a para-xylene recovery unit to recover a para-xylene product stream and leave a para-xylene-depleted C8 stream. At least part of para-xylene-depleted C8 stream is then fed to a xylene isomerization unit effective to isomerize xylenes in para-xylene-depleted stream back towards an equilibrium mixture of xylenes and thereby produce an isomerization effluent. The isomerization effluent is then recycled to the para-xylene extraction unit. 1. A process for producing para-xylene , the process comprising:(a) reforming a naphtha feed under reforming conditions effective to convert at least 50 wt % of the naphthenes in the naphtha feed to aromatics, but to convert no more than 25 wt % of the paraffins in the naphtha feed, and thereby produce a reforming effluent;(b) removing at least a first stream containing benzene and/or toluene and a second stream containing C8 aromatics from the reforming effluent;(c) feeding at least part of the benzene and/or toluene from the first stream to a xylene production unit under conditions effective to convert benzene and/or toluene to xylenes;(d) feeding at least part of the C8 aromatics from the second stream and at least part of the xylenes produced in (c) to a para-xylene recovery unit to recover a para-xylene product stream and leave a para-xylene-depleted C8 stream;(e) ...

Process for Producing Para-Xylene

A process for producing a PX-rich product, the process comprising: (a) providing a PX-depleted stream; (b) isomerizing at least a portion of the PX-depleted stream to produce an isomerized stream having a PX concentration greater than the PX-depleted stream and a benzene concentration of less than 1,000 ppm and a C+ hydrocarbons concentration of less than 5,000 ppm; and (c) separating the isomerized stream by selective adsorption. 115.-. (canceled)16. A process for producing a PX-rich product , the process comprising:{'sub': 8', '8, '(a) separating a feedstock containing Chydrocarbons to produce a Chydrocarbons rich stream;'}{'sub': '8', '(b) separating at least a portion of the Chydrocarbons rich stream to produce a first PX-rich stream and a first raffinate stream;'}(c) isomerizing at least a portion of the first raffinate stream to produce a first isomerized stream having a higher PX concentration than the first raffinate stream;{'sub': '8', '(d) separating the first isomerized stream to produce a second Chydrocarbons rich stream;'}{'sub': '8', '(e) separating the second Chydrocarbons rich stream to produce a second PX-rich stream and a second raffinate stream;'}(f) isomerizing, at least partially in the liquid phase, at least a portion of the second raffinate stream to produce a second isomerized stream having a higher PX concentration than the second raffinate stream; and(g) providing at least a portion of the second isomerized stream to the separating (a).17. The process of claim 16 , comprising providing at least a portion of said second raffinate stream in the separating (e) to the separating (b).18. The process of claim 16 , comprising providing at least a portion of said second isomerized stream in the isomerizing (f) to the separating (b).19. The process of claim 16 , further comprising:(h) separating at least a portion of said second isomerized stream in the isomerizing (f) to produce a benzene-depleted stream and a benzene-rich stream; and(i) providing ...

Powder, Compositions Thereof, Processes for Making the Same, and Articles Made Therefrom

Provided herein is a powder comprising at least one of: (a) a propylene-based elastomer comprising, based on the total weight of said propylene-based elastomer, (i) at least about 60 wt % of propylene-derived units, (ii) about 5 wt % to about 35 wt % of units derived from at least one of ethylene and a C 4 -C 10 alpha-olefin, and said propylene-based elastomer having a heat of fusion, as determined by DSC, of about 75 J/g or less; and (b) a polyolefin-based elastomer having a Shore A hardness, as determined by ISO 868, of less than 95; wherein the powder has an average particle size of from about 30 μm to about 850 μm. The powder is useful for rotational molding and for making articles having unique combination of elasticity, flexibility, and toughness.

Vinyl Terminated Higher Olefin Copolymers and Methods to Produce Thereof

This invention relates to a vinyl terminated higher olefin copolymer having an Mn of 300 g/mol or more (measured by H NMR) comprising: (i) from about 20 to about 99.9 mol % of at least one Cto Chigher olefin monomer; and (ii) from about 0.1 to about 80 mol % of propylene; wherein the higher olefin copolymer has at least 40% allyl chain ends. The copolymer may also have an isobutyl chain end to allyl chain end ratio of less than 0.7:1 and/or an allyl chain end to vinylidene chain end ratio of greater than 2:1. 2. The process of claim 1 , wherein the copolymer has an isobutyl chain end to allyl chain end ratio of less than 0.7:1.3. The process of claim 1 , wherein the copolymer has an allyl chain end to vinylidene chain end ratio of more than 2:1.4. The process of claim 1 , wherein the Cto Chigher olefin is selected from pentene claim 1 , hexene claim 1 , heptene claim 1 , octene claim 1 , nonene claim 1 , decene claim 1 , undecene claim 1 , dodecene claim 1 , norbornene claim 1 , norbornadiene claim 1 , dicyclopentadiene claim 1 , cyclopentene claim 1 , cycloheptene claim 1 , cyclooctene claim 1 , cyclooctadiene claim 1 , cyclododecene claim 1 , 7-oxanorbornene claim 1 , 7-oxanorbornadiene claim 1 , substituted derivatives thereof claim 1 , and isomers thereof.5. The process of claim 1 , wherein the higher olefin copolymer has a viscosity at 60° C. of greater than 1000 cP.6. (canceled)8. The process of claim 7 , wherein the copolymer has an isobutyl chain end to allyl chain end ratio of less than 0.7:1.9. The process of claim 7 , wherein the copolymer has an allyl chain end to vinylidene chain end ratio of more than 2:1.10. The process of claim 7 , wherein the higher olefin copolymer comprises at least 50 wt % claim 7 , based upon the weight of the copolymer composition claim 7 , of olefins having at least 36 carbon atoms claim 7 , as measured by H NMR claim 7 , assuming one unsaturation per chain.11. (canceled)13. The process of claim 12 , wherein the Cto Chigher ...

Reactor Components

The present disclosure relates to reactor components and their use, e.g., in regenerative reactors. A process and apparatus for utilizing different wetted areas along the flow path of a fluid in a pyrolysis reactor, e.g., a thermally regenerating reactor, such as a regenerative, reverse-flow reactor, is described. 1. A hydrocarbon conversion method comprising: {'sub': v1', 'v2', 'v2', 'v1, 'the regenerative reactor has a first portion having a first plurality of flow passages with a wetted area aand a second portion having a second plurality of flow passages with a second wetted area a, wherein the ratio of the second wetted area ato the first wetted area ais ≦0.75; and'}, 'passing a first mixture comprising hydrocarbons to a regenerative reactor, wherein'}{'sub': '2', 'reacting at least a portion of the hydrocarbons within the regenerative reactor to produce a second mixture comprising Cunsaturates.'}2. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais ≦0.5.3. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.05 to 0.75.4. The method of claim 1 , wherein the ratio of the second wetted area ato the first wetted area ais in the range of 0.1 to 0.5.5. The method of claim 1 , comprising: [{'br': None, 'i': R', '=a', '/a', '=X, 'sub': 21', 'v2', 'v1, 'sup': (T', {'sub2': '2'}, '-T', {'sub2': '1'}, ')/300}, {'sub': 21', '2', '1, 'wherein Ris the ratio, Tis the zone temperature of the second portion in units of ° C., Tis the zone temperature of the first portion in units of ° C., and the X parameter is between 0.1 and 0.9;'}], 'calculating the ratio by the following equation{'sub': '21', 'obtaining the first portion and the second portion based on the determined ratio R; and'}disposing the first portion and second portion within the regenerative reactor.6. The method of claim 5 , wherein the X parameter is in the range of 0.25 to 0.75.7. The method of claim 1 ...

Integrated Process For Steam Cracking

This invention relates to a process and system for cracking hydrocarbon feedstock containing vacuum resid comprising: (a) subjecting a vacuum resid to a first thermal conversion in a thermal conversion reactor (such as delayed coker, fluid coker, Flexicoker™, visbreaker and catalytic hydrovisbreaker) where at least 30 wt % of the vacuum resid is converted to material boiling below 1050° F. (566° C.); (b) introducing said thermally converted resid to a vapor/liquid separator, said separator being integrated into a steam cracking furnace, to form a vapor phase and liquid phase; (c) passing said vapor phase to the radiant furnace in said steam cracking furnace; and (d) recovering at least 30 wt % olefins from the material exiting the radiant furnace (based upon the weight of the total hydrocarbon material exiting the radiant furnace). 135.-. (canceled)36. A system for cracking hydrocarbon feedstock containing vacuum resid comprising:a) a first thermal conversion zone operating at a temperature of less than 649° C. selected from the group consisting of: a delayed coker, a fluid coker, a Flexicoker™, a visbreaker or a catalytic hydrovisbreaker, said first thermal conversion zone in fluid communication with b) a steam cracking furnace having a vapor/liquid separator in fluid communication with said furnace.37. The system of claim 36 , further comprising a second a vapor/liquid separator in fluid communication with said thermal conversion zone.38. The system of claim 36 , wherein the first thermal conversion zone is a fluidized coker comprising:i) a fluidized bed gasifier,ii) a transfer line reactor comprising a hydrocarbon feed inlet in fluid communication with a lower portion of said separator, and a pyrolysis product outlet line,iii) a solids conduit connecting a lower portion of said fluidized bed gasifier with said transfer line reactor, andiv) at least one cyclone separator having an inlet connected to said pyrolysis product outlet line, a cracked product outlet at a ...

Mixer/Flow Distributors

The invention relates mixer/flow distributors and their use, e.g., in regenerative reactors. The invention encompasses a process and apparatus for controlling oxidation, e.g., for thermally regenerating a reactor, such as a regenerative, reverse-flow reactor. 1. A regeneration method , comprising:(a) conducting fuel through at least one first conduit and oxidant through at least one second conduit, the first and second conduits being located in a recuperation zone of a reactor system;(b) combining and reacting at least a portion of the fuel with at least a portion of the oxidant in a mixing-distributing zone to produce heat and a first reaction product, the mixing-distributing zone being located (i) in the reactor system and (ii) downstream of the recuperation zone and upstream of a reaction zone, the mixing-distributing zone comprising a mixer-distributor having a Maldistibution ≦15.0%, a pressure drop ≦0.3 bar, and a combined fuel-oxidant flow rate ≧10.0 kg/hr; and(c) conducting the reaction product through the reaction zone and transferring at least a portion of the heat from the reaction product to the reaction zone.2. The method of claim 1 , wherein the mixer-distributor has a Maldistribution ≦10.0% claim 1 , a pressure drop ≦0.1 bar claim 1 , and a combined fuel-oxidant flow rate ≧100.0 kg/hr.3. The method of claim 1 , wherein the mixer-distributor has a Mixing Efficiency ≧75.0 Wt. %.4. The method of claim 1 , wherein the mixer-distributor has a Temperature Variability ≦60.0° C.5. The method of claim 1 , wherein the mixer-distributor includes swirling means having a swirl number in the range of from 0.1 to 1.3.6. The method of claim 1 , wherein the mixer-distributor comprises a plurality of first orifices in a first location; at least one second orifice at a second location claim 1 , the first location being upstream of the second location with respect to the fuel-oxidant flow; and means for substantially preventing fuel-oxidant flow through the mixer- ...

Molecular Sieve Composition From Pre-Formed Extrudates and Process of Use

This disclosure provides a molecular sieve composition having a first and second crystalline molecular sieve, made by the method comprising: (a) providing a reaction mixture comprising at least one source of ions of tetravalent element Y, at least one source of alkali metal hydroxide, water, optionally at least one seed crystal, and optionally at least one source of ions of trivalent element X, the reaction mixture having the following molar composition: 1. A molecular sieve composition having at least one first crystalline molecular sieve and a second crystalline molecular sieve prepared by a method comprising the steps of: [{'br': None, 'sub': '2', 'Y:X=2 to infinity'}, {'br': None, 'sup': '−', 'OH:Y=0.001 to 2'}, {'br': None, 'sup': '+', 'M:Y=0.001 to 2'}, 'wherein M is an alkali metal and the amount of water is at least sufficient to permit extrusion of said reaction mixture, wherein said reaction mixture is substantially free of a crystalline molecular sieve (not including the optional seed crystals);, 'a. providing a reaction mixture comprising at least one source of ions of tetravalent element Y, at least one source of alkali metal hydroxide, water, optionally at least one seed crystal, and optionally at least one source of ions of trivalent element X, said reaction mixture having the following molar compositionb. extruding said reaction mixture to form a pre-formed extrudate of said first crystalline molecular sieve; andc. crystallizing said pre-formed extrudate and said second crystalline molecular sieve in a liquid medium comprising water under liquid phase conditions to form said molecular sieve composition having said first crystalline molecular sieve and said second crystalline molecular sieve;wherein said second crystalline molecular sieve is different from said first crystalline molecular sieve.2. The molecular sieve composition of claim 1 , characterized by said pre-formed extrudate comprising a structure directing agent R.3. The molecular sieve ...

Film Composition and Method of Making the Same

Films including at least one layer of a blend of a cyclic olefin copolymer and a hydrocarbon wax are described. Particularly, films including 75.0 wt % to 99.9 wt % of a copolymer of a cyclic olefin monomer and an acyclic olefin and 0.1 wt % to 25.0 wt % of a hydrocarbon wax are described. Methods of making such films are also disclosed. 1. A film comprising at least a first layer , the first layer , comprising:{'sub': 'g', 'a) 75.0 wt % to 99.9 wt % of a copolymer of a cyclic olefin monomer and an acyclic olefin, the copolymer having a glass transition temperature, T; and'}b) 0.1 wt % to 25.0 wt % of a hydrocarbon wax.2. The film of claim 1 , wherein Tis ≦ is the melting point claim 1 , mp claim 1 , of the hydrocarbon wax.3. The film of claim 2 , wherein T≦mp≦T+20.0° C.4. The film of claim 2 , wherein mp is T≦mp≦T+10.0° C.5. The film of any previous claim claim 2 , wherein the cyclic olefin monomer has 4 to 12 carbon atoms.6. The film of any previous claim claim 2 , wherein cyclic olefin monomer is a norbornene.7. The film of any previous claim claim 2 , wherein the acyclic olefin is selected from the group consisting of ethylene claim 2 , propylene claim 2 , butylene claim 2 , and mixtures thereof.8. The film of any previous claim claim 2 , wherein hydrocarbon wax is a microcrystalline wax.9. The film of any previous claim claim 2 , wherein the first layer comprises less than 2.0 wt % to about 0.5 wt % of the hydrocarbon wax.10. The film of any previous claim claim 2 , wherein the first layer is substantially free of a polyethylene.11. The film of any previous claim claim 2 , wherein the first layer comprises less than 2.0 wt % polyethylene and has a haze value of 1.0% or less according to ASTM D 1003.12. The film according to any previous claim claim 2 , wherein the defect number of the film is at least 70% less than the defect number of a comparative film that lacks the hydrocarbon wax.13. The film according to any previous claim claim 2 , wherein the defect ...

Fluid Bed Reactor with Staged Baffles

The invention relates to a process of alkylating aromatic hydrocarbons, and more particularly a process of making paraxylene by alkylation of benzene and/or toluene with methanol and/or dimethyl ether, and to an apparatus for carrying out said process, the improvement comprising staged injection of one of the reactants, with the stages separated by structured packing so as to minimize at least one of gas phase back-mixing, by-pass phenomena, and gas bubble size.

System and Method for Monitoring Bubble Formation Within A Reactor

Bubble formation is monitored in a reactor such as a loop polymerization reactor which effectively operates at pressures above or near the vapor pressure of a circulating slurry liquid. The method measures a property of the reactor composition at a first location within the reactor, and then at a second location within the reactor. The process is repeated, followed by determining if the difference in measured property varies from a reference difference, derived under bubble-free conditions. When the difference in measured physical property has changed relative to the reference difference, an effect may be implemented, e.g., increase of reactor pressure, decrease of composition vapor pressure, and decrease of reactor temperature, to an extent sufficient to reduce or eliminate bubbling. 1. A method for monitoring bubble formation within a reactor comprising:a) measuring a property of a composition within the reactor at a first location to obtain a first measured value;b) measuring the property at a second location to obtain a second measured value;c) determining a measured difference between the first measured value in (a) and the second measured value in (b); andd) comparing the measured difference in (c) with a reference difference to monitor bubble formation.2. The method of claim 1 , wherein the reference difference is equal to the difference between the value of the property at the first location and the value of the property at the second location determined under substantially bubble-free conditions.3. The method of claim 1 , further comprising:e) repeating steps (a) through (d).4. The method of claim 1 , further comprising implementing an effect when the measured difference in (c) diverges from the reference difference by a predetermined amount.5. The method of claim 4 , wherein the effect is at least one of: (i) notifying a reactor operator; (ii) increasing the operating pressure of the reactor; (iii) decreasing the vapor pressure of the composition; and (iv) ...

"process for producing cycloalkylaromatic compounds"

In a process for producing a cycloalkylaromatic compound, an aromatic compound, hydrogen and at least one diluent are supplied to a hydroalkylation reaction zone, such that the weight ratio of the diluent to the aromatic compound supplied to the hydroalkylation reaction zone is at least 1:100. The aromatic compound, hydrogen and the at least one diluent are then contacted under hydroalkylation conditions with a hydroalkylation catalyst in the hydroalkylation reaction zone to produce an effluent comprising a cycloalkylaromatic compound.

Extractive Distillation Controls

The invention concerns an improvement in the monitoring and control systems used in a liquid-liquid extraction unit or an extractive distillation unit for the separation of aromatic hydrocarbons from non-aromatic hydrocarbons. 1. In a process for separating aromatics from a hydrocarbon mixture feed comprising aromatics and non-aromatics by use of a solvent which preferentially absorbs aromatics , in a system comprising a liquid-liquid extraction (LLE) unit or an extractive distillation (ED) unit , wherein said solvent is mixed with said hydrocarbon mixture and said solvent preferentially absorbs said aromatics to provide a first aromatics-depleted hydrocarbon stream , relative to said hydrocarbon mixture feed , and a first aromatics-enriched solvent stream , relative to said hydrocarbon mixture , and wherein both said first aromatics-depleted hydrocarbon stream and said first aromatics-enriched solvent stream are further processed in said LLE unit or ED unit to produce a final aromatics-depleted stream and a product comprising at least one of the aromatics selected from the group consisting of benzene , toluene , and xylene , the improvement comprising:(a) controlling process variables and calculations of those process variables using at least one of levels, temperatures, analyzers, pressures, and flows to optimize product specifications including non-aromatics in the aromatics product, aromatics in the aromatics depleted hydrocarbon stream, flow rates, and energy usage and to improve reliability for LLE and ED units; and (I) a set of rules identifying an abnormal condition in the aromatic system, and a message;', '(II) receiving data from the aromatics system;', '(III) evaluating on-line process calculations for the aromatics system from the data;', '(IV) evaluating the on-line calculation results against the set of rules identifying an abnormal condition;', '(V) identifying each of the set of rules as true or false; and', '(VI) displaying a message if appropriate ...

High Strength Presulfied Catalyst for Hydrogenating Hydrocarbon Resins

High strength presulfided catalyst for hydrogenating hydrocarbon resins without an in situ sulfiding step. The catalyst particles have a supported metal catalyst structure with presulfided interstitial surfaces with about 20 weight percent of a low molecular weight hydrocarbon resin, based on the weight of the porous supported metal catalyst structure, filling from 90 to 95 percent of the pore volume to improve a crush strength of the catalyst particles. The presulfided catalyst can be stored and/or shipped in an airtight container with an inert atmosphere. The catalyst particles are made by preparing the oxidized catalyst, presulfiding the catalyst, contacting the catalyst with the low molecular weight hydrocarbon resin in an inert atmosphere, sealing the catalyst in a storage/shipping container, loading the reactor with the presulfided, filled catalyst, and contacting the catalyst with an unsaturated hydrocarbon resin under hydrogenation conditions. 1. A packaged , presulfided catalyst useful to hydrogenate hydrocarbon resin without an in situ sulfiding step , comprising:porous catalyst particles comprising a supported metal catalyst structure comprising an internal pore volume with presulfided interstitial surfaces;about 20 wt. % of a low molecular weight hydrocarbon resin, based on the weight of the supported metal catalyst structure, filling from 90 to 95 percent of the pore volume to improve a crush strength of the catalyst particles; andan air-tight, transportable container housing the discrete catalyst particles in an inert atmosphere.2. A method to hydrogenate hydrocarbon resin , comprising:preparing catalyst particles comprising a supported metal catalyst structure comprising an internal pore volume with oxidized interstitial surfaces;sulfiding the supported metal catalyst structure to form presulfided interstitial surfaces;in an inert atmosphere, contacting the presulfided catalyst particles with about 20 wt. % percent of a low molecular weight ...

Enhanced Catalyst Performance for Production of Vinyl Terminated Propylene and Ethylene/Propylene Macromers

This invention relates to a transition metal catalyst compound represented by the structure: 132.-. (canceled)33. A polymer of propylene having an Mn of more than 30 ,000 g/mol and at least 30% allyl chain ends (relative to total unsaturation).34. The polymer of claim 33 , where the polymer has an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.3:1.0 claim 33 , optionally less than 1400 ppm aluminum.35. The polymer of claim 33 , wherein the polymer has at least 50% allyl chain ends (relative to total unsaturation).36. The polymer of claim 33 , wherein the polymer has at least 70% allyl chain ends (relative to total unsaturation).37. The polymer of claim 33 , wherein the polymer has at least 90% allyl chain ends (relative to total unsaturation).38. The polymer of claim 33 , wherein the polymer has at least 95% allyl chain ends (relative to total unsaturation).39. The polymer of claim 33 , wherein the polymer has an Mn of more than 30 claim 33 ,000 g/mol up to 100 claim 33 ,000 g/mol.40. The polymer of claim 33 , wherein the polymer has an Mn of more than 30 claim 33 ,000 g/mol up to 60 claim 33 ,000 g/mol.41. The polymer of claim 33 , wherein the polymer has an Mn of more than 30 claim 33 ,000 g/mol up to 40 claim 33 ,000 g/mol.42. The polymer of claim 33 , wherein the polymer has an Mn of more than 30 claim 33 ,000 g/mol up to 60 claim 33 ,000 g/mol and comprises 90 to 40 mol % propylene and 10 to 60 mol % of ethylene claim 33 , wherein the copolymer has at least X % allyl chain ends (relative to total unsaturations) claim 33 , where: 1) X=(−0.94 (mol % ethylene incorporated)+100).43. The polymer of claim 33 , wherein the polymer has an Mn of more than 30 claim 33 ,000 g/mol up to 60 claim 33 ,000 g/mol and comprises less than 40 and greater than 30 mol % propylene and greater than 60 and less than 70 mol % of ethylene claim 33 , wherein the copolymer has at least 45% allyl chain ends (relative to total unsaturations).44. The polymer of claim 33 , ...

Extraction Towers And Processes For Using The Same

The disclosure relates to processes and systems utilizing one or more extraction towers in the recovery and recycle of acid catalysts used in the production of carboxylic acids. The carboxylic acids may be neo-acids produced through the hydrocarboxylation of olefins or olefin mixtures. 1. A process comprising:obtaining a reactor effluent from one or more reactors comprising a mixture of a neo-acid, and one or more of a catalyst, a catalyst salt, and a complex of a catalyst and a neo-acid;passing the reactor effluent through at least one extraction tower;contacting at least a portion of the reactor effluent with water;separating at least a portion of the neo-acid from the reactor effluent; andrecovering the separated neo-acid; wherein the at least one extraction tower comprises two or more phases operating at least two extractions; wherein the at least one tower comprises water and the water concentration is the molar equivalent to the at least one neo-acid from the reactor effluent.2. The process of claim 1 , wherein the at least two extractions are liquid/liquid extractions and the at least one extraction tower comprises two or more phases in mixing mode or four or more phases in quiescent mode.3. The process of claim 1 , wherein the at least one extraction tower is a York-Scheibel tower.4. The process of claim 1 , wherein the at least one tower comprises from 20 to 40 alternating mixing and settling stages.5. The process of claim 1 , wherein the at least one separated neo-acid is substantially free of the at least one catalyst and/or the at least one catalyst salt.6. The process of claim 1 , wherein the at least one separated neo-acid is free of the at least one catalyst and/or the at least one catalyst salt.7. The process of claim 1 , wherein at least a portion of the catalyst is recycled to the one or more reactors.8. The process of claim 1 , wherein the at least one extraction tower comprises a top section claim 1 , a bottom section claim 1 , and an interface.9 ...

Dehydrogenation Process

In a process for the dehydrogenation of at least one dehydrogenatable hydrocarbon, at least one dehydrogenatable hydrocarbon selected from an oxygen-containing six-membered carbon ring compound is supplied to a first dehydrogenation reaction zone together with at least one stabilizing compound selected from a non-oxygen-containing six membered carbon ring compound to the first dehydrogenation reaction zone, such that the weight ratio of the stabilizing compound to the dehydrogenatable hydrocarbon supplied to the first dehydrogenation reaction zone is in the range of from 1:200 to 200:1. The dehydrogenation feed stream and the at least one stabilizing compound are contacted with a first dehydrogenation catalyst in the first dehydrogenation reaction zone under dehydrogenation conditions to convert at least a portion of the dehydrogenatable hydrocarbon into an unsaturated six-membered carbon ring compound and hydrogen. 1. A process for the dehydrogenation of at least one dehydrogenatable hydrocarbon , the process comprising:(a) supplying a dehydrogenation feed stream comprising at least one dehydrogenatable hydrocarbon to a first dehydrogenation reaction zone wherein the at least one dehydrogenatable hydrocarbon is an oxygen-containing six-membered carbon ring compound;(b) supplying at least one stabilizing compound to the first dehydrogenation reaction zone, such that the weight ratio of the stabilizing compound to the dehydrogenatable hydrocarbon supplied to the first dehydrogenation reaction zone is in the range of from 1:200 to 200:1 wherein the stabilizing compound is a non-oxygen-containing six membered carbon ring compound; and(c) contacting the at least one dehydrogenatable hydrocarbon and the at least one stabilizing compound with a first dehydrogenation catalyst in the first dehydrogenation reaction zone under dehydrogenation conditions to convert at least a portion of the dehydrogenatable hydrocarbon into an unsaturated six-membered carbon ring compound and ...

Regeneration of Oligomerisation Catalysts and Their Use

Deactivation of a zeolite catalyst during its use to catalyse the oligomerisation of olefins, is often believed to be a result of the formation of high boiling polymers as by-products. These by-products can remain on the catalyst and undergo further conversion to higher molecular weight polymers, which resemble heavy tars and in some cases even have the appearance of coke-like material. These materials can coat the catalyst particles and plug pores in the catalyst, thereby causing catalyst deactivation. The invention relates to an improved method for regenerating such a catalyst. 1. A process for the regeneration of a catalyst selected from ZSM-22; ZSM-57 , or mixtures thereof wherein the catalyst has been used for the oligomerisation of olefins comprising the following steps:i) heating the catalyst to a temperature in the range from 300° C. to 450° C. under an inert dry atmosphere; andii) heating the catalyst to a temperature in the range from 450° C. to 500° C. in a dry oxygen-containing atmosphere.2. The process according to in which the total time for regeneration is no more that 100 hours.3. The process according to in which the second step is performed in less than 68 hours.4. The process according to in which the inert atmosphere employed in the first step is a nitrogen atmosphere.5. The process according to in which the dry oxygen containing atmosphere employed in the second step is air having a dew point of −10° C. or below.6. The continuous process for the oligomerisation of olefins employing a zeolite catalyst that has been regenerated according to .7. The process according to wherein an olefin containing hydrocarbon feed is passed over a bed of the regenerated zeolite catalyst in a tubular reactor wherein the shell side of the reactor is cooled by a temperature control fluid and the temperature of the reaction is monitored and the space velocity of the olefin stream fed to the reactor is adjusted according to the temperature measured.8. The continuous ...

Secondary Alcohols and Esters Made Therefrom

The invention relates to secondary alcohols produced by contacting an olefin and a carboxylic acid with a zeolite, esters made therefrom, and to plasticizer compositions comprising the esters. 1. A process comprising reacting an olefin with a carboxylic acid in the presence of a zeolite under predetermined conditions , said zeolite and said conditions suitable to produce a product comprising a mixture of alkyl carboxylate esters , including an α-methylalkyl carboxylate ester and other isomers of said alkyl carboxylate esters , wherein the ratio of said α-methylalkyl carboxylate ester to said other isomers is greater than 1 , followed by converting at least a portion of the mixture of the alkyl carboxylate esters to a high C—OH content secondary alcohol mixture by a method selected from hydrolysis , hydrogenation , and chemical reduction , with subsequent reaction of the secondary alcohol mixture with dicarboxylic acids or tricarboxylic acids or their anhydrides to produce plasticizing esters.2. The process of claim 1 , wherein said carboxylic acid is selected from C-Ccarboxylic acids.3. The process of claim 1 , wherein said carboxylic acid includes acetic acid.4. The process of claim 1 , wherein said olefin is selected from C-Calpha olefins or C-Colefin mixtures containing greater than 50% linear alpha olefins.5. The process of claim 1 , wherein said zeolite is selected from at least one of ZSM-12 and ZSM-5.6. The process of claim 1 , wherein said zeolite is ZSM-12.7. The process of claim 1 , wherein said ratio is greater than 3.8. The process of claim 1 , wherein said ratio is greater than 15.9. The process of claim 1 , wherein said dicarboxylic acid or tricarboxylic acid is selected from adipic acid claim 1 , phthalic acid claim 1 , phthalic anhydride claim 1 , terephthalic acid claim 1 , dimethyl terephthalic acid claim 1 , trimellitic acid claim 1 , trimellitic anhydride claim 1 , citric acid claim 1 , hexahydrophthalic acid claim 1 , hexahydrophthalic anhydride ...

System for Alcohol Production

The invention concerns a system and process for alcohol production. 1. In a system for acid catalyzed hydration of at least one olefin to at least one alcohol , said system comprising a rich stage absorber distillation column in combination with plural reactor loops fluidly connected with said rich stage absorber and wherein said olefin is contacted in a mixed phase with said acid to produce an extract , the improvement comprising the use of plural inverted conical baffles in said rich stage absorber distillation column.2. The system according to claim 1 , wherein said acid is sulfuric acid claim 1 , said olefin is propylene claim 1 , and said alcohol is isopropyl alcohol (IPA).3. The system according to claim 1 , wherein said acid is sulfuric acid claim 1 , said olefin is butene claim 1 , and said alcohol is secondary-butyl alcohol (SBA).4. The system according to claim 1 , wherein said rich stage absorber is defined by a top portion claim 1 , a middle portion claim 1 , and a bottom portion claim 1 , the top portion including an inlet for said acid and an outlet for gaseous olefin claim 1 , the middle portion including said plural inverted conical baffles claim 1 , and the bottom portion including at least one de-entrainment device for de-entrainment of sulfuric acid from said rich stage absorber into said plural reactor loops and an outlet for extract claim 1 , wherein said at least one de-entrainment device provides a fluid connection between said rich stage absorber and each of said plural reactor loops claim 1 , and wherein each of said plural reactor loops is also fluidly connected with said middle portion of said rich stage absorber.5. The system according to claim 4 , comprising a single de-entrainment device fluidly connected to each of said plural reactor loops and a separate fluid connection for each of said plural reactor loops with said rich stage absorber.6. The system according to claim 5 , including a reservoir comprising olefin claim 5 , said ...

Cyclohexylbenzene Compositions

In a process for producing phenol and cyclohexanone, a feed comprising cyclohexylbenzene is oxidized to produce an oxidation reaction product comprising cyclohexyl-1-phenyl-1-hydroperoxide. At least a portion of the oxidation reaction product is then cleaved to produce a cleavage reaction product comprising phenol, cyclohexanone, and at least one contaminant At least a portion of the cleavage reaction product is contacted with an acidic material to convert at least a portion of the at least one contaminant to a converted contaminant and thereby produce a modified reaction product. The composition comprising cyclohexylbenzene may have at least 10 wt % of cyclohexylbenzene; 1 wppm to 1 wt % of bicyclohexane; 1 wppm to 1 wt % of biphenyl; and 1 wppm to 2 wt % of methylcyclopentylbenzene, wherein the wt % s and wppms are based upon total weight of the composition. 1. A composition comprising:a. at least 10 wt % of cyclohexylbenzene;b. 1 wppm to 1 wt % of bicyclohexane;c. 1 wppm to 1 wt % of biphenyl; and 'wherein the wt % s and wppms are based upon total weight of the composition.', 'd. 1 wppm to 2 wt % of methylcyclopentylbenzene,'}2. The composition of claim 1 , wherein the composition is a feed.3. The composition of claim 1 , wherein the composition comprises 10 wppm to 8000 wppm of bicyclohexane.4. The composition of claim 1 , wherein the composition comprises 10 wppm to 8000 wppm of biphenyl.5. The composition of claim 1 , wherein the composition comprises 10 wppm to 1 wt % of methylcyclopentylbenzene.6. The composition of claim 1 , wherein the composition comprises less than 1000 wppm of phenol claim 1 , olefins or alkylene benzenes claim 1 , individually or in any combination.7. The composition of claim 1 , wherein the composition comprises less than 100 wppm of phenol claim 1 , olefins or alkylene benzenes claim 1 , individually or in any combination.8. The composition of claim 1 , wherein the composition comprises less than 100 wppm of cyclohexenyl benzene.9. ...

Hydrocarbon Pyrolysis Method

Disclosed is a pyrolysis reaction process. The process can be advantageously accomplished using a pyrolysis reactor that has a primary reaction zone comprised of bed packing having multiple passages through the bed packing and a secondary reaction zone having an open flow arrangement. The process includes a step of injecting a pyrolysis feed comprising a first hydrocarbon into the primary reaction zone to produce a primary pyrolysis product containing unsaturated hydrocarbon. A reactive feed comprising a second hydrocarbon is injected into the secondary reaction zone to mix with the primary pyrolysis product and produce a secondary pyrolysis product.

Hydrocarbon Conversion Process

The invention relates to a process for converting hydrocarbons into unsaturated products such as acetylene and/or ethylene. The invention also relates to converting acetylene to olefins such as ethylene and/or propylene, to polymerizing the olefins, and to equipment useful for these processes.

"PROCESSES FOR PRODUCING PHENOL"

In a process for producing phenol and cyclohexanone, a feed comprising cyclohexylbenzene is oxidized to produce an oxidation reaction product comprising cyclohexyl-1-phenyl-1-hydroperoxide. At least a portion of the oxidation reaction product is then cleaved to produce a cleavage reaction product comprising phenol, cyclohexanone, and at least one contaminant. At least a portion of the cleavage reaction product is contacted with an acidic material to convert at least a portion of the at least one contaminant to a converted contaminant and thereby produce a modified reaction product. 1. A process for producing phenol comprising:(a) oxidizing at least a portion of a feed comprising cyclohexylbenzene to produce an oxidation composition comprising cyclohexyl-1-phenyl-1-hydroperoxide;(b) cleaving at least a portion of the oxidation composition to produce a cleavage reaction mixture comprising phenol, cyclohexanone and at least one contaminant; and(c) contacting at least a portion of the cleavage reaction mixture with an acidic material to convert at least a portion of the contaminant to a converted contaminant, thereby producing a modified reaction mixture.2. The process of claim 1 , wherein the contaminant is one or more of an acyclic aliphatic hexanal claim 1 , an acyclic aliphatic hexanone claim 1 , a cyclohexenone claim 1 , a cyclohexyldione claim 1 , a hydroxycyclohexanone claim 1 , benzoic acid claim 1 , a benzoic ester claim 1 , a cyclohexenyl cyclohexanone claim 1 , a methylcyclopentenyl cyclohexanone claim 1 , 1-phenyl-6-hydroxyhexan-1-one claim 1 , 1-cyclohexyl-6-hydroxyhexan-1-one and a bicyclic twelve carbon hydroperoxide.3. The process of claim 1 , wherein the acidic material comprises at least one of a microporous acid material claim 1 , a cation exchange resin claim 1 , a Bronsted acid claim 1 , and sulfurous acid or acid salt.4. The process of claim 1 , wherein the acidic material is a solid acid catalyst.5. The process of claim 1 , wherein the acidic ...

Polypropylene-Based Adhesive Compositions

The present invention is related to adhesive compositions and their applications. In particular, the adhesive compositions described herein comprise a two or more propylene-based copolymers with varying comonomer content.

Plasticizer

The liquid volume resistivity of plasticiser esters is improved by purifying the ester with an adsorbent having a pH in the range 6 to 11. It is preferable to use a mixture of a filtration aid and an adsorbent. A plasticiser having a desirable combination of high liquid volume resistivity, low amount of light ends and low carbonyl number is obtained. 1. A process for the production of a plasticiser ester consisting essentially of:(i) esterifying an acid or an anhydride with an alcohol containing from 6 to 13 carbon atoms to form a crude ester;(ii) treating the crude ester with a base to form a treated ester;(iii) filtering the treated ester to separate a liquid product;(iv) stripping the liquid product to form a stripped material;(v) treating the stripped material with an adsorbent; and(vi) filtering the product of step (v), optionally in the presence of a filter aid, to remove the adsorbent from the plasticiser ester.2. The process according to wherein the base is an alkali metal salt.3. The process according to wherein the base is selected from the group consisting of sodium hydroxide and sodium carbonate.4. The process according to comprising removing water from the treated ester before filtering step (iii).5. The process according to wherein the water is removed by flashing or steam stripping.6. The process according to wherein the acid or anhydride is selected from the group consisting of aromatic monocarboxylic acids and anhydrides claim 1 , and polybasic aromatic carboxylic acids and anhydrides.7. The process according to wherein the anhydride is phthalic anhydride.8. The process according to wherein the alcohol is a Cto Calcohol.9. The process according to wherein the alcohol is selected from the group consisting of a Calcohol and a Calcohol.10. The process according to wherein the combined amount of adsorbent and the filter aid employed is from about 0.01 to about 5 wt % claim 1 , based on the weight of the plasticiser ester.11. The process according to ...

Phenol and Cyclohexanone Mixtures

In a process for producing phenol and cyclohexanone, a feed comprising cyclohexylbenzene is oxidized to produce an oxidation reaction product comprising cyclohexyl-1-phenyl-1-hydroperoxide. At least a portion of the oxidation reaction product is then cleaved to produce a cleavage reaction product comprising phenol, cyclohexanone, and at least one contaminant. At least a portion of the cleavage reaction product is contacted with an acidic material to convert at least a portion of the at least one contaminant to a converted contaminant and thereby produce a modified reaction product. The cleavage reaction product may comprise 1 wt %-30 wt % phenol; 1 wt %-30 wt % cyclohexanone; and 0.1 wt % to 10 wt % of at least one of water, bicyclohexane, cyclohexenylbenzene, methylcyclopentanone, 1-phenylhexan-1-one, cyclohexyldione, cyclohexanol, cyclohexenone, hydroxycyclohexanone, benzoic acid, phenyl cyclohexanol, hexanal and 1-phenyl-6-hydroxyhexan-1-one, wherein the wt % s are based upon the total weight of the mixture. 1. A mixture comprising:(a) 1 wt %-30 wt % phenol;(b) 1 wt %-30 wt % cyclohexanone; and(c) 0.1 wt %-10 wt % of at least one of water, bicyclohexane, cyclohexenylbenzene, methylcyclopentanone, 1-phenylhexan-1-one, cyclohexyldione, cyclohexanol, cyclohexenone, hydroxycyclohexanone, benzoic acid, phenyl cyclohexanol, hexanal and 1-phenyl-6-hydroxyhexan-1-one,wherein the wt % s are based upon the total weight of the mixture.2. The mixture of claim 1 , the mixture further comprising 50 wppm to 3000 wppm of at least one of Bronsted acids claim 1 , Lewis acids claim 1 , sulfonic acids claim 1 , perchloric acid claim 1 , phosphoric acid claim 1 , hydrochloric acid claim 1 , p-toluene sulfonic acid claim 1 , aluminum chloride claim 1 , oleum claim 1 , sulfur trioxide claim 1 , ferric chloride claim 1 , boron trifluoride claim 1 , sulfur dioxide and sulfur trioxide claim 1 , wherein the wppms are based upon the total weight of the mixture.3. The mixture of claim 1 , ...

Bimetallic Catalyst and Use in Xylene Production

The invention is directed to a bimetallic catalyst system adapted for the manufacture of xylenes, a process for making said catalyst system, and to the process of manufacture of xylenes using said catalyst system, providing, in embodiments, improved selectivity by at least one of higher ethylene saturation and low xylene loss, decreased susceptibility to poisoning from feedstream impurities, and ability to operate at less severe conditions. 1. A catalyst system comprising a first bed including at least one first metal selected from Groups 7-10 , and at least one second metal selected from silver , copper , ruthenium , indium and tin , dispersed on ZSM-5 , and a second bed including at least one first metal selected from Groups 7-10 , and at least one second metal selected from silver , copper , ruthenium , indium and tin , dispersed on ZSM-5 , further characterized in that ZSM-5 in the first bed is silicon-selectivated and ZSM-5 in the second bed is not silicon-selectivated.2. The catalyst system according to claim 1 , wherein at least one of said first bed and said second bed further comprises a support selected independently from at least one of alumina claim 1 , silica claim 1 , aluminosilicates claim 1 , clay claim 1 , and combinations thereof3. The catalyst system according to claim 1 , further characterized as including a first bed comprising a catalyst made by adding at least one first metal selected from Groups 7-10 and at least one second metal selected from silver claim 1 , copper claim 1 , ruthenium claim 1 , indium and tin by the incipient wetness technique to a silicone-selectivated ZSM-5 claim 1 , followed by drying and calcination claim 1 , and a second bed comprising a catalyst made by combining a metal solution comprising at least one first metal selected from Groups 7-10 and at least one second metal selected from silver claim 1 , copper claim 1 , ruthenium claim 1 , indium and tin claim 1 , and water and a non-selectivated ZSM-5 molecular sieve ...

Stabilized Ceramic Composition, Apparatus and Methods of Using the Same

In one aspect, the invention includes a refractory material, said material comprising: (i) at least 20 wt. % of a first grain mode stabilized zirconia based upon the total weight of said material, said first grain mode having a D50 grain size in the range of from 5 to 2000 μm, said stabilized zirconia including a matrix oxide stabilizer; (ii) at least 1 wt. % of a second grain mode having a D50 grain size in the range of from 0.01 μm up to not greater than one-fourth the D50 grain size of said first grain mode zirconia, based upon the total weight of said material; and (iii) at least 1 wt. % of a preservative component within at least one of said first grain mode stabilized zirconia, said second grain mode stabilized zirconia, and an optional another grain mode; wherein after sintering, said material has porosity at 20° C. in the range of from 5 to 45 vol %. 127.-. (canceled)28. A method of preparing a ceramic composition comprising the steps of:a) preparing a granular ceramic composition including at least:(i) at least 20 wt. % of a first grain mode based upon the total weight of said ceramic composition, said first grain mode comprising stabilized zirconia having a D50 grain size in the range of from 5 to 2000 μm, said stabilized zirconia including a matrix oxide stabilizer; and(ii) at least 1 wt. % of a second grain mode having a D50 grain size in the range of from 0.01 μm up to not greater than one-fourth the D50 grain size of said first grain mode based upon the total weight of said ceramic composition,{'sub': 2', '3', '2, '(iii) at least 1 wt. % of a preservative component within the ceramic composition, based upon the total weight of said ceramic composition, said preservative component selected from at least one of an yttrium-containing compound, CaO, MgO, YO, CeO, and mixtures thereof;'}b) combining said first grain mode, said second grain mode, and said preservative component to form a dispersed composition; andc) sintering said dispersed composition at a ...

Phenol and Cyclohexanone Mixtures

Disclosed herein is a process for producing phenol. The process includes oxidizing at least a portion of a feed comprising cyclohexylbenzene to produce an oxidation composition comprising cyclohexyl-1-phenyl-1-hydroperoxide. The oxidation composition may then be cleaved in the presence of an acid catalyst to produce a cleavage reaction mixture comprising the acid catalyst, phenol and cyclohexanone. At least a portion of the cleavage reaction mixture may be neutralized with a basic material to form a treated cleavage reaction mixture. In various embodiments, the cleavage reaction mixture contains 1 wt % to 30 wt % phenol, 1 wt % to 30 wt % cyclohexanone and a complexation product. 1. A mixture comprising:(a) 1 wt % to 30 wt % phenol;(b) 1 wt % to 30 wt % cyclohexanone; and(c) a complexation product,wherein the wt % s are based upon total weight of the mixture.2. The mixture of claim 1 , wherein the complexation product is a salt of sodium sulfate.3. The mixture of claim 1 , wherein the mixture further comprises water.4. The mixture of claim 1 , wherein the complexation product is a complex of (CHNH).HSO.5. The mixture of claim 1 , wherein the complexation product is a complex of (HN(CH)NH).HSO.6. The mixture of claim 1 , wherein the complexation product has a normal boiling above phenol.7. The mixture of claim 1 , wherein the complexation product is soluble in the mixture.8. The mixture of claim 1 , wherein the complexation product does not decompose at temperatures above 200° C.9. The mixture of claim 1 , wherein the complexation product is substantially inert to other components in the mixture.10. The mixture of claim 1 , wherein the mixture comprises 5 wt % to 15 wt % cyclohexanone claim 1 , based upon the total weight of the treated mixture.11. The mixture of claim 1 , wherein the mixture comprises 5 wt % to 15 wt % phenol claim 1 , based upon the total weight of the mixture.12. The mixture of claim 1 , wherein the mixture comprises 5 wt % to 15 wt % of phenol ...

Upgrading Hydrocarbon Pyrolysis Products

The invention relates to upgraded pyrolysis products, processes for upgrading products obtained from hydrocarbon pyrolysis, equipment useful for such processes, and the use of upgraded pyrolysis products.

Reactor Components

The present disclosure relates to insulation components and their use, e.g., in regenerative reactors. Specifically, a process and apparatus for managing temperatures from oxidation and pyrolysis reactions in a reactor, e.g., a thermally regeneratating reactor, such as a regenerative, reverse-flow reactor is described in relation to the various reactor components.

Selecting an Improved Catalyst Composition and Hydrocarbon Conversion Process Using Same

The present invention provides a method for selecting an improved catalyst composition comprising a crystalline molecular sieve material having a structure and properties whereby the catalyst composition has at least one active catalytic site with a Mono Alkylation Selectivity Factor (MASF) greater than or equal to 0 kcal/mol±0.5 kcal/mol, and optionally further at least one active catalytic site with an Olefin Oligomerization Suppression Factor (OOSF) greater than or equal to 5 kcal/mol±0.5 kcal/mol. Further, there is provided an improved process for conversion of hydrocarbon feedstock in the presence of said selected catalyst composition. 1. A method for selecting a catalyst composition comprising a porous crystalline material for use in a hydrocarbon conversion process , said method comprising steps of determining a Mono Alkylation Selectivity Factor of one or more catalyst compositions , and selecting a catalyst composition which has at least one active catalytic site with said Mono Alkylation Selectivity Factor greater than or equal to 0 kcal/mol±0.5 kcal/mol.2. The method of claim 1 , wherein said selected catalyst composition has at least one active catalytic site with a Mono Alkylation Selectivity Factor greater than or equal to 3 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 7 kcal/mol±0.5 kcal/mol.3. The method of claim 1 , further comprising steps of determining a Olefin Oligomerization Suppression Factor of one or more catalyst compositions claim 1 , and selecting a catalyst composition which has at least one active catalytic site with said Olefin Oligomerization Suppression Factor greater than or equal to 5 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 7 kcal/mol±0.5 kcal/mol claim 1 , or greater than or equal to 10 kcal/mol±0.5 kcal/mol.4. The method of claim 1 , wherein said Mono Alkylation Selectivity Factor (MASF) is defined by the formula:{'br': None, 'sup': T', 'Olefin+MonoAlkylated Aromatics', 'T', 'Olefin+Aromatics, ' ...

Flange Joint and Method for Preventing a Fluid from Leaking Out Through a Flange Joint

A method comprising forming a partial barrier in an outer part of a flange joint, applying a sealant to the outside of the flange joint, and supplying a safe sealing fluid to an inner part of the flange joint, prevents a process fluid from leaking out through a flange joint, advantageously without having to dismantle the flange joint. 1. A method for preventing a process fluid from leaking out through a flange joint , the method comprising:a. forming a partial barrier in an outer part of the flange joint;b. applying a sealant to the outside of the flange joint, the partial barrier restricting ingress of the sealant into the flange joint; andc. supplying a safe sealing fluid, at a pressure higher than the pressure of the process fluid, to an inner part of the flange joint, such that the safe sealing fluid prevents the process fluid from leaking out through the flange joint and prevents contact between the process fluid and the sealant, wherein the safe sealing fluid is supplied through a slotted stud in the flange joint.2. A method according to claim 1 , wherein the sealant is a solid sealant.3. A method according to claim 1 , wherein the safe sealing fluid is also supplied through a hole in the flange joint.4. A method according to claim 1 , wherein the partial barrier is a peened wire.5. A method according to claim 1 , wherein a clamp is attached to the flange joint and the solid sealant is injected into a cavity between the clamp and the partial barrier.6. A method according to claim 1 , wherein the safe sealing fluid is supplied from an intrinsically safe source.7. A method according to claim 1 , wherein the safe sealing fluid is selected from a group consisting of air claim 1 , water claim 1 , nitrogen claim 1 , helium claim 1 , carbon dioxide or combinations thereof.8. A flange joint comprising:a. a partial barrier in an outer part of the flange joint;b. a clamp attached to the flange joint so as to form a cavity between the clamp and the partial barrier;c. a ...

Polymers, Polymer Blends, and Articles Made Therefrom

Polymer compositions including an ethylene-based polymer having a melt index of from about 0.1 g/10 min to about 5.0 g/10 min; a melt index ratio of from about 15 to about 30; a weight average molecular weight (Mw) of from about 20,000 to about 200,000; a molecular weight distribution (Mw/Mn) of from about 2.0 to about 4.5; and a density of from 0.900 to 0.920 g/cm 3 . Films having a thickness of 1 mil show a difference between the maximum seal strength and the minimum seal strength over the ranges of temperatures between 95.0° C. and 140.0° C. of ≦1.00×10 2 grams/cm.

Catalyst Regeneration Process

This disclosure relates to a process for regenerating a catalyst composition to improve the aging rate in subsequent cycles. 1. In a process for conversion of an aromatic hydrocarbon feed stream , including contacting said feed stream with a molecular sieve and carrying out said contacting for a cycle time , whereby coke deposits on said catalyst during at least a portion of said cycle time and wherein the reactor temperature is increased and/or through-put is decreased over at least a portion of said cycle time in order to meet at least one predetermined indicia of conversion efficiency , the improvement comprising determining the end of cycle time by at least one of (i) wt % coke deposits on said molecular sieve , and (ii) H/C ratio of the coke deposits on said molecular sieve.2. The process of claim 1 , including determining end of cycle conditions of said molecular sieve claim 1 , said end of cycle conditions selected from (i) wt % coke deposits on said molecular sieve claim 1 , and (ii) H/C ratio of the coke deposits on said molecular sieve; then regenerating or rejuvenation said molecular sieve and carrying out said contacting for another cycle time claim 1 , with the proviso that said end of cycle conditions change from the previous cycle time; then making a determination of appropriate end of cycle conditions and operating said process based on said determination claim 1 , wherein the improvement is further characterized by a decrease in molecular sieve aging rate claim 1 , expressed as the rate of increase in temperature required to maintain at least one indicia of conversion efficiency constant.3. The process of claim 1 , including regenerating or rejuvenating said catalyst by treatment under oxidative conditions claim 1 , reductive conditions claim 1 , treatment with steam claim 1 , and combinations thereof.4. The process of claim 1 , wherein said conversion process is selected from transalkylation claim 1 , disproportionation claim 1 , comproportionation ...

Liquid Phase Isomerization Process

Liquid phase isomerization technology is employed in a manner to increase efficiency and reduce energy in paraxylene recovery. 1. In a process for the production of paraxylene from a feedstream comprising a mixture of C8 aromatic hydrocarbons , comprising a xylene separation step , including the separation of paraxylene from its C8 aromatic isomers to provide a paraxylene-enriched stream and a paraxylene-depleted stream , and a liquid-phase isomerization step , including the isomerization of said paraxylene-depleted stream to produce an equilibrium xylenes stream , the improvement characterized in that the paraxylene-depleted stream is used directly as feed to said liquid-phase isomerization step , without an intervening separation step.2. In a process for the production of paraxylene from a feedstream comprising a mixture of C8 aromatic hydrocarbons , comprising:(a) separation of said feedstream into a first product enriched in C8+ species relative to said feedstream and a second product enriched in C7− aromatic species relative to said feedstream;(b) passing said first product to a fractionation tower to provide a third product enriched in xylenes relative to said first product and a fourth product depleted in xylenes relative to said first product;(c) passing the third product to a xylene separation step to provide a product enriched in paraxylene when compared with said third product, and a raffinate product, characterized as depleted of paraxylene when compared with said third product; and(d) passing said raffinate product directly, without a fractionation step, to a liquid phase isomerization unit, to provide a product enriched in paraxylene when compared with said raffinate.3. The process of claim 2 , further comprising:(e) treating said second product by at least one separation step to provide a product enriched in C7+ species when compared with said second product; and(f) providing said product enriched in C7+ species from step (e) and the product enriched ...

Lubricant Compositions Comprising Ethylene Propylene Copolymers and Methods for Making Them

Lubricant compositions, as well as processes for their formulation, are provided. The lubricant compositions comprise an oil basestock and one or more blocky ethylene propylene copolymers. The copolymers are preferably prepared using metallocene catalyst systems but without using a chain shuttling agent. 1. A lubricant composition comprising:a. an oil basestock; andb. from about 0.5 to about 2.5 wt. %, based on the total weight of the lubricant composition, of a copolymer of propylene and ethylene, wherein the copolymer comprises from about 50 to about 95 wt. % ethylene, the copolymer has a melting point greater than about 90° C., and less than about 5 wt. % of the copolymer, based upon the total weight of the copolymer, is soluble in xylene or ortho-dichlorobenzene.2. The lubricant composition of claim 1 , wherein the copolymer comprises from about 65 to about 90 wt. % ethylene.3. The lubricant composition of claim 1 , wherein the copolymer has a melting point greater than about 100° C.4. The lubricant composition of claim 1 , wherein the melting point of the soluble fraction of the copolymer is greater than about 100° C.5. The lubricant composition of claim 1 , wherein the lubricant composition has a thickening efficiency from about 1.5 to about 3.5.6. The lubricant composition of claim 1 , wherein the lubricant composition has a shear stability index from about 15% to about 25%.7. The lubricant composition of claim 1 , wherein the lubricant composition has a shear stability index greater than or equal to about 24%.8. The lubricant composition of claim 1 , wherein the copolymer is not synthesized in the presence of a chain shuttling agent.9. A lubricant composition comprising:a. an oil basestock; andb. from about 7.5 to about 15.0 wt. %, based on the total weight of the lubricant composition, of a copolymer of propylene and ethylene, wherein the copolymer comprises from about 50 to about 95 wt. % ethylene, the copolymer has a melting point greater than about 90° C ...

Methods and Apparatus for Forming Blends of Polyolefin and Resin Modifier

A process for preparing a blend of thermoplastic polymer and resin modifier within a single-screw extruder, wherein the resin modifier is a hydrocarbon resin. 1. A process for preparing a blend of thermoplastic polymer and resin modifier , the process comprising the steps of:(i) charging neat thermoplastic polymer to a single-screw extruder;(ii) charging neat resin modifier to the extruder;(iii) conveying the polyolefin and resin modifier through a feed section of the extruder to form a blend, where the feed section has an average channel depth;(iv) conveying the blend through a compression section of the extruder to thereby form a molten blend;(v) mixing the molten blend after said step of conveying the blend through the compression section to thereby impart positive pressure on the molten blend in a downstream direction;(vi) conveying the molten blend through a metering section, where the metering section has an average channel depth; and(vii) extruding the molten blend, wherein the blend or molten blend is subjected to a compression ratio that is at least 1.2, where the compression ratio is the ratio of the feed section average channel depth to the metering section average channel depth.2. The process of claim 1 , where the blend includes a thermoplastic polymer to resin modifier weight ratio of 95:5 to 5:95.3. The process of claim 1 , where said step of extruding includes forming a film.4. The process of claim 1 , where said step of charging neat thermoplastic polymer includes charging thermoplastic polymer pellets comprising at least 95 wt % of the thermoplastic polymer claim 1 , and where said step of charging neat resin modifier includes charging resin pellets comprising at least 95 wt % of the resin modifier.5. The process of claim 1 , where the thermoplastic polymer is a polyolefin selected from the group consisting of polypropylene and polyethylene.6. The process of claim 1 , where the resin modifier is an amorphous hydrocarbon resin.7. The process of ...

Blocky Ethylene Propylene Copolymers and Methods for Making Them

Copolymers comprising ethylene and propylene and methods for producing such polymers are provided. The polymers are blocky copolymers having semicrystalline ethylene sequences and amorphous or low crystallinity propylene sequences. The polymers are preferably prepared using metallocene-based catalyst systems but without the use of a chain shuttling agent. The polymers may have higher melting temperatures than previously known random copolymers or blocky copolymers prepared with chain shuttling agents having similar comonomer contents. The polymers include both ethylene-rich and propylene-rich copolymers. 1. A process for preparing a copolymer comprising:polymerizing propylene and ethylene in a solution process and in the presence of a catalyst system comprising a catalyst and an activator;a. wherein the catalyst comprises a metallocene compound;b. wherein the activator comprises a cationic component and an anionic component; [{'sup': 1', '2', '3', '+', '1', '2', '1', '2', '3, 'sub': 2', 'a', '1', '5, 'i. [RRRNH], where Rand Rare together a —(CH)— group, where a is 3, 4, 5, or 6 and Rand Rform a 4-, 5-, 6-, or 7-membered non-aromatic ring together with the nitrogen atom to which one or more aromatic or heteroaromatic rings may optionally be fused via adjacent ring carbon atoms; and Ris a C-Calkyl group; or'}, {'sub': 3', '1', '3, 'sup': '+', 'ii. [RNH], where all R are identical and are C-Calkyl groups; and'}], 'c. wherein the cationic component of the activator corresponds to the formula{'sup': 4', '−', '4, 'sub': '4', 'd. wherein the anionic component of the activator corresponds to the formula [B(R)], where Ris an aryl group or a substituted aryl group having one or more substituents, wherein the one or more substituents are identical or different and are selected from alkyl, aryl, halogenated aryl, or haloalkylaryl groups or a hydrogen atom.'}2. The process of claim 1 , wherein the copolymer is prepared in the absence of a chain shuttling agent.3. The process of ...

Polyethylene and Process for Production Thereof

This invention relates to a process for polymerizing olefins in which the amount of trimethylaluminum in a methylalumoxane solution is adjusted to be from 1 to 25 mol %, prior to use as an activator, where the mol % trimethylaluminum is determined by 1 H NMR of the solution prior to combination with any support. This invention also relates to a process for polymerizing olefins in which the amount of an unknown species present in a methylalumoxane solution is adjusted to be from 0.10 to 0.65 integration units prior to use as an activator, where the amount of the unknown species is determined by the 1 H NMR spectra of the solution performed prior to combination with any support. Preferably, the methylalumoxane solution is present in a catalyst system also comprising a metallocene transition metal compound.

Copolymer Production System and Process

In a process for making a copolymer, a first product stream comprising a semi-crystalline polymer and a chain terminating agent is produced in a first reactor system. The first product is provided to a second reactor system wherein a low crystallinity polymer is produced in the presence of the semi-crystalline polymer. At least a portion of the chain terminating agent is removed from the second reactor system by an in-situ process. 1. A process for making a copolymer , the process comprising:a. producing in a first reactor system a first product stream comprising a semi-crystalline polymer and a chain terminating agent;b. providing at least a portion of the first product stream to a second reactor system;c. producing in the second reactor system a low crystallinity polymer in the presence of the semi-crystalline polymer; andd. removing at least a portion of the chain terminating agent introduced with the first product stream from the second reactor system by an in-situ process.2. The process of claim 1 , wherein the in-situ process comprises a catalytic hydrogenation reactor to consume hydrogen via reaction with monomer claim 1 , or a membrane unit to selectively remove the chain terminating agent from the reaction system.3. The process of claim 1 , wherein the copolymer has an intrinsic viscosity ratio (IVR) of greater than 4.4. The process of claim 1 , wherein the chain terminating agent is hydrogen.5. The process of claim 1 , wherein the monomer is selected from ethylene and propylene.6. The process of claim 1 , wherein the semi-crystalline polymer has a matrix claim 1 , and at least a portion of the low crystallinity polymer is formed within the pores of the matrix.7. The process of claim 1 , wherein the semi-crystalline polymer is polypropylene homopolymer and the low crystallinity polymer is ethylene propylene rubber (EPR).8. The process of claim 1 , wherein the first reactor system comprises a slurry loop reactor or a plurality of slurry loop reactors in ...

Dehydrogenation Processes and Phenol Compositions

Described herein is a process for producing phenol in which (a) benzene and hydrogen are contacted with a hydroalkylation catalyst under hydroalkylation conditions to produce cyclohexylbenzene; (b) the cyclohexylbenzene is contacted with an oxidation catalyst under oxidation conditions to produce cyclohexylbenzene hydroperoxide; (c) the cyclohexylbenzene hydroperoxide is contacted with a cleavage catalyst under cleavage conditions to produce a cleavage effluent comprising phenol and cyclohexanone; (d) the cyclohexanone is contacted with a dehydrogenation catalyst under dehydrogenation conditions to produce a dehydrogenation effluent having at least a portion of the cyclohexanone and a first contaminant; and (e) the first contaminant is contacted with an acidic material under contaminant treatment conditions to convert at least a portion of the first contaminant into a converted first contaminant. Phenol compositions made from the above-described process are also described herein. 1. A process for producing phenol comprising:(a) contacting benzene and hydrogen with a hydroalkylation catalyst under hydroalkylation conditions to produce cyclohexylbenzene;(b) contacting at least a portion of the cyclohexylbenzene with an oxidation catalyst under oxidation conditions to produce cyclohexylbenzene hydroperoxide;(c) contacting at least a portion of the cyclohexylbenzene hydroperoxide with a cleavage catalyst under cleavage conditions to produce a cleavage effluent comprising phenol and cyclohexanone;(d) contacting at least a portion of the cyclohexanone from the cleavage effluent with a dehydrogenation catalyst under dehydrogenation conditions to produce a dehydrogenation effluent having at least a portion of the cyclohexanone converted to phenol, wherein the dehydrogenation effluent further comprises a first contaminant; and(e) contacting at least a portion of the first contaminant from the dehydrogenation effluent with an acidic material under contaminant treatment ...

Hydrocarbon Conversion Process

The invention relates to processes for converting a mixture of hydrocarbon and oxygenate into products containing acetylene and carbon monoxide. The invention also relates to utilizing at least a portion of the acetylene and carbon monoxide for producing xylenes such as p-xylene, utilizing at least a portion of xylenes for producing polymeric fibers, and to equipment useful for these processes. 1. A hydrocarbon conversion process , comprising:(a) providing a first mixture, the first mixture comprising ≧10.0 wt. % hydrocarbon and ≧1.0 wt. % oxygenate, the weight percents being based on the weight of the first mixture;(b) exposing the first mixture a temperature ≧700° C. in a first region under pyrolysis conditions to produce a second mixture, the second mixture comprising molecular hydrogen, carbon monoxide, and ≧1.0 wt. % of acetylene based on the weight of the second mixture, wherein the second mixture has a molecular hydrogen:carbon monoxide molar ratio ≧2.0 and a carbon monoxide:acetylene molar ratio ≧0.1;(c) converting at least a portion of the second mixture's acetylene to produce a first intermediate mixture comprising ≧10.0 wt. % aromatic hydrocarbon based on the weight of the intermediate mixture;(d) reacting at least a portion of the second mixture's carbon monoxide with at least a portion of the second mixture's molecular hydrogen to produce a second intermediate mixture comprising ≧10.0 wt. % alcohol based on the weight of the second intermediate mixture; and(e) reacting at least a portion of the first intermediate mixture's aromatics with at least a portion of the second intermediate mixture's alcohol to produce a product comprising water and ≧10.0 wt. % p-xylene based on the weight of the product.2. The process of claim 1 , wherein the first mixture comprises ≧25.0 wt. % of hydrocarbon and ≧10.0 wt. % of oxygenate claim 1 , the oxygenate having an Effectiveness Factor ≧0.05 claim 1 , and further comprises ≧5.0 wt. % molecular hydrogen claim 1 , the ...

Process for the Production of Xylenes and Light Olefins

In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of C 4 + olefinic and aromatic hydrocarbons is recovered from the first stream and is fed together with a methylating agent to a reaction zone containing a catalyst under reaction conditions including a temperature of about 450° C. to about 700° C., such that aromatics components in the second stream undergo dealkylation, transalkylation and/or methylation and aliphatic components undergo cracking and aromatization to produce a third stream having an increased xylene content compared with said second stream and a C 3 − olefin by-product. The C 3 − olefin by-product is recovered and para-xylene is removed from at least part of said third stream.

Process for the Production of Xylenes and Light Olefins

In a hydrocarbon upgrading process, a hydrocarbon feed is treated in at least one of a steam cracker, catalytic cracker, coker, hydrocracker, and reformer under suitable conditions to produce a first stream comprising olefinic and aromatic hydrocarbons. A second stream composed mainly of C 4 to C 12 + olefinic and aromatic hydrocarbons is recovered from the first stream and blended said second stream with a residual fraction from a steam cracker or an atmospheric or vacuum distillation unit to produce a third stream. The third stream is then catalytically pyrolyzed in a reactor under conditions effective to produce a fourth stream having an increased benzene and/or toluene content compared with said second stream and a C 3 -olefin by-product. The C 3 -olefin by-product is recovered and benzene and/or toluene are recovered from the fourth stream.

Hydrocarbon Conversion Process

The invention relates to processes for converting hydrocarbons to phthalic acids such as terephthalic acid. The invention also relates to polymerizing phthalic acid derivatives to produce, e.g., synthetic fibers.

Manganese Oxides and Their Use in the Oxidation of Alkanes

Catalytic structures are provided comprising octahedral tunnel lattice manganese oxides ion-exchanged with metal cations or mixtures thereof. The structures are useful as catalysts for the oxidation of alkanes and may be prepared by treating layered manganese oxide under highly acidic conditions, optionally drying the treated product, and subjecting it to ion exchange.

Hydrocarbon Conversion Process Using a High Throughpout Process for Manufacturing Molecular Sieves

A method of crystallizing a crystalline molecular sieve having a pore size in the range of from about 2 to about 19 Å, said method comprising the steps of (a) providing a mixture comprising at least one source of ions of tetravalent element (Y), at least one hydroxide source (OH − ), and water, said mixture having a solid-content in the range of from about 15 wt. % to about 50 wt. %; and (b) treating said mixture to form the desired crystalline molecular sieve with stirring at crystallization conditions sufficient to obtain a weight hourly throughput from about 0.005 to about 1 hr −1 , wherein said crystallization conditions comprise a temperature in the range of from about 200° C. to about 500° C. and a crystallization time less than 100 hr.

Process for Producing Para-Xylene

A process for producing a PX-rich product, the process comprising: (a) providing a PX-depleted stream; (b) isomerizing at least a portion of the PX-depleted stream to produce an isomerized stream having a PX concentration greater than the PX-depleted stream and a benzene concentration of less than 1,000 ppm and a C 9 + hydrocarbons concentration of less than 5,000 ppm; and (c) separating the isomerized stream by selective adsorption.

Synthesis and Use of M41S Family Molecular Sieves

A process is described for producing an M41S family molecular sieve. The process comprises preparing a synthesis mixture capable of forming said molecular sieve in a reactor, which is equipped with a mixer having a Froude number of at least 1, said synthesis mixture having a solids content of at least 20 wt %. The synthesis mixture is heated in the reactor while agitating the mixture with said mixer to form a product mixture comprising water and crystals of said molecular sieve material. Thereafter at least part of the water is removed from the product mixture in the reactor so as to decrease the water content of the product mixture inside the reactor by at least 5 wt %. 1. A process for producing a molecular sieve material having an X-ray diffraction pattern with at least one peak at a position greater than about 18 Angstrom Units d-spacing with a relative intensity of 100 , and a benzene adsorption capacity of greater than about 15 grams benzene per 100 grams anhydrous crystal at 50 torr and 25° C. , said process comprising the steps of:{'sub': 1', '2', '3', '4', '1', '2', '3', '4', '1', '2', '3', '4, 'sup': '+', '(a) preparing a synthesis mixture capable of forming said molecular sieve material by combining in a reactor equipped with a mixer having a Froude number of at least 1, at least water, a source of at least one oxide selected from the group consisting of divalent element W, trivalent element X, tetravalent element Y and pentavalent element Z, a source of an alkali or alkaline earth metal M, and an organic directing agent (R) having the formula RRRRQ, wherein Q is nitrogen or phosphorus and wherein at least one of R, R, Rand Ris selected from the group consisting of aryl of from 6 to about 36 carbon atoms, alkyl of from 6 to about 36 carbon atoms and combinations thereof and the remainder of R, R, Rand Ris selected from the group consisting of hydrogen, alkyl of from 1 to 5 carbon atoms and combinations thereof, said synthesis mixture having a solids ...

THERMOPLASTIC ELASTOMER COMPOSITION

In order to improve fatigue durability of a thermoplastic elastomer composition composed of a matrix phase of a thermoplastic resin and dispersed phases of a rubber, the thermoplastic elastomer composition comprises (A) 100 parts by weight of a halogenated poly(isoolefin-co-p-alkylstyrene) rubber, (B) 40 to 120 parts by weight of a polyamide resin, and (C) 0.5 to 10 parts by weight of an amine having at least one hydroxyl group. The amine (C) having at least one hydroxyl group is preferably a compound represented by formula (1): 1. A thermoplastic elastomer composition comprising (A) 100 parts by weight of a halogenated poly(isoolefin-co-p-alkylstyrene) rubber , (B) 40 to 120 parts by weight of a polyamide resin , and (C) 0.5 to 10 parts by weight of an amine having at least one hydroxyl group.3. A thermoplastic elastomer composition according to claim 2 , wherein Ris —(CHO)—H claim 2 , where n is an integer of 1 to 30; and each of Rand Rindependently is —(CHO)—H claim 2 , where m is an integer of 1 to 30 claim 2 , a Calkyl claim 2 , or hydrogen.4. A thermoplastic elastomer composition according to claim 3 , wherein Ris a Calkyl; Ris —(CHO)—H claim 3 , where n is an integer of 1 to 30; and Ris —(CHO)—H claim 3 , where m is an integer of 1 to 30 claim 3 , a Calkyl claim 3 , or hydrogen.5. A thermoplastic elastomer composition according to claim 4 , wherein Ris a Calkyl; Ris —(CHO)—H claim 4 , where n is an integer of 1 to 30; and Ris —(CHO)—H claim 4 , where m is an integer of 1 to 30 claim 4 , or a Calkyl.6. A thermoplastic elastomer composition according to claim 5 , wherein Ris a Calkyl; Ris —(CHO)—H claim 5 , where n is an integer of 1 to 30; and Ris —(CHO)—H claim 5 , where m is an integer of 1 to 30.7. A thermoplastic elastomer composition according to claim 2 , wherein the total number of oxyethylene repeating unit (CHO) in one molecule of the amine (C) having at least one hydroxyl group is 1 to 30.8. A thermoplastic elastomer composition according to claim 3 ...

Dehydrogenation Catalyst and Process

A catalyst composition comprises (i) a support; (ii) a dehydrogenation component comprising at least one metal or compound thereof selected from Groups 6 to 10 of the Periodic Table of Elements; and (iii) tin or a tin compound, wherein the tin is present in an amount of 0.01 wt % to about 0.25 wt %, the wt % based upon the total weight of the catalyst composition. 1. A catalyst composition comprising: (i) a support; (ii) a dehydrogenation component comprising at least one metal or compound thereof selected from Groups 6 to 10 of the Periodic Table of Elements; and (iii) tin or a tin compound , wherein the tin is present in an amount of 0.01 wt % to about 0.25 wt % , the wt % based upon the total weight of the catalyst composition.2. The catalyst composition of claim 1 , wherein the tin is present in an amount of about 0.05 wt % to about 0.25 wt % claim 1 , based upon the total weight of the catalyst composition.3. The catalyst composition of claim 1 , wherein the tin is present in an amount of about 0.05 wt % to about 0.15 wt % of tin based upon the total weight of the catalyst composition.4. The catalyst composition of claim 1 , wherein the support is selected from the group consisting of silica claim 1 , a silicate claim 1 , an aluminosilicate claim 1 , zirconia claim 1 , carbon claim 1 , and carbon nanotubes.5. The catalyst composition of claim 1 , wherein the dehydrogenation component comprises at least one of platinum claim 1 , palladium and compounds thereof.6. The catalyst composition of claim 1 , wherein the dehydrogenation component is present in an amount of greater than 0.01 wt % to about 2 wt % claim 1 , based upon the total weight of the catalyst composition.7. The catalyst composition of claim 1 , wherein the composition provides a reduced selectivity to one or more of pentane claim 1 , pentene and carbon monoxide.8. A method for preparing a catalyst composition claim 1 , the method comprising:(a) treating a support with tin or a compound thereof;(b) ...

Branched Polyethylenes by Hydrosilation Grafting to Improve Processability of Polyethylene

This invention relates to blends of polyalphaolefins (PAOs) and polyhydrosilane-modified polyolefins, methods to prepare the blends and methods to prepare polyhydrosilane-modified polyolefins.