The present disclosure relates to bis(heterocyclic-olate) 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(heterocyclic-olate) Lewis base catalysts, can be 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 or polymers having low to very 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.
Exemplary embodiments of the present technological advancement include pyridine-2,6-bis(phenylenephenolate) complexes that are useful as catalyst components for olefin polymerization and have improved solubility in non-aromatic hydrocarbons (e.g. isohexane). The improved solubility of these complexes was accomplished by the modification of the ligand framework at a specific position that led to improved solubility, but did not adversely affect the performance of the complex when used as a catalyst for olefin polymerizations.
A polyethylene copolymer may comprise about 90 wt % to about 99.99 wt % ethylene and about 0.01 wt % to about 10 wt % an alpha-olefin that is not ethylene, wherein the polyethylene has: a density of about 0.930 g/cm3 to about 0.955 g/cm3, a melt flow index (2.16 kg at 190°° C.) of about 10 g/10 min to about 50 g/10 min, a melt flow index ratio (MIR) of about 15 to about 25, a weight average molecular weight to number average molecular weight ratio (Mw/Mn) of about 2 to about 4, a wt % of TREF elution at 90° C. and less of about 10 wt % to about 80 wt %, and a wt % of TREF elution at 95° C. and greater of about 3 wt % or more. Said polyethylene may be especially well-suited for making bicomponent fibers, which may be useful producing in nonwoven fabrics.
D01F 8/10 - Filaments, ou similaires, faits par l’homme, conjugués, c.-à-d. à plusieurs composantsLeur fabrication à partir de polymères synthétiques avec au moins un autre composé macromoléculaire obtenu par des réactions faisant intervenir uniquement des liaisons non saturées carbone-carbone comme constituant
D01F 8/14 - Filaments, ou similaires, faits par l’homme, conjugués, c.-à-d. à plusieurs composantsLeur fabrication à partir de polymères synthétiques avec au moins un polyester comme constituant
D01G 1/04 - Découpage des filaments continus ou des fibres longues, p. ex. mise sous forme de fibres coupées pour former des fibres coupées non livrées sous forme de brins par sectionnement
D04H 1/541 - Fibres composites, p. ex. âme-gaine, mer-île ou côte à côteFibres mixtes
4.
Integration of Polymeric Waste Co-Processing in Cokers to Produce Circular Chemical Products from Coker Gas Oil
Systems and methods are provided for integration of polymeric waste co-processing in cokers to produce circular chemical products from coker gas oil, including a method of producing circular chemical products comprising: providing a coker gas oil that is at least partially derived from polymeric waste, wherein the coker gas oil has a paraffin content of about 5 wt % to about 50 wt %, a sulfur content of about 0.1 wt % to about 7 wt %, and a halide content of about 0.1 wppm to about 5 wppm; and converting the coker gas oil into at least a polymer.
C10G 65/10 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série ne comprenant que des étapes de craquage
C10B 49/22 - Distillation destructive des matières carbonées solides par chauffage direct au moyen d'agents porteurs de chaleur, y compris la combustion partielle de la matière à traiter avec des porteurs de chaleur solides, mobiles, sous forme divisée sous forme dispersée selon la technique du "lit fluidisé"
5.
POLYETHYLENE COMPOSITIONS AND PROCESSES FOR THEIR PRODUCTION
Provided are polyethylene copolymers with an improved balance of melt strength and processability and methods for making such polyethylene copolymers. In some embodiments, the polyethylene copolymers include from 9 to 11 weight percent of at least one comonomer having 4 to 8 carbon atoms, and have a density in the range of from 0.908 to 0.916 g/cm3, a melt index I2 in the range of 0.10 to 0.60 g/10 min., and a melt index ratio I21/I2 greater than or equal to 46.9−(33.3×(I2)), wherein I2 is provided in g/10 min. In some embodiments, the polyethylene copolymer is produced in a dry mode gas phase process using a metallocene catalyst.
Compositions, methods, and molded articles including a bimodal molecular weight ethylene/propylene random copolymer comprising a high molecular weight component having a melt flow rate at 230° C. of from about 0.02 g/10 min to about 0.5 g/10 min and a low molecular weight component having a melt flow rate at 230° C. of from about 1 g/10 min to about 10 g/10 min, and an ethylene content of from about 0.40 wt. % to about 0.60 wt. %.
A variety of systems and methods are disclosed, including, in one embodiment, a method of needle coke production. The method includes hydro-processing a hydrocarbon liquid by contacting the hydrocarbon liquid with at least one hydro-processing catalyst in one or more hydro-processing stages to form a hydro-processed product, wherein the hydro-processing of the hydrocarbon liquid in at least one of the one or more hydro-processing stages is performed in the presence of a utility fluid. The hydrocarbon liquid includes an initial boiling point at atmospheric pressure of about 200° C. or greater in accordance with ASTM 7500. The hydrocarbon liquid includes an aromatic content of about 50 wt. % or greater. The method further includes coking at least a portion of the hydro-processed product to form a coker effluent and coke, wherein the coke comprises needle coke.
C10B 55/02 - Cokéfaction des huiles minérales, bitumes, goudrons ou analogues, ou de leurs mélanges, avec des matières carbonées solides avec des matières solides
C10G 45/00 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène
8.
Integration of Polymeric Waste Co-Processing in Cokers to Produce Circular Chemical Products from Coker Gas
Systems and methods are provided for integration of polymeric waste co-processing in cokers to produce circular chemical products from coker gas, including a method of producing circular chemical products comprising: providing a coker gas that is at least partially derived from polymeric waste, wherein the coker gas has an olefin content of about 10 wt % to about 30 wt %, a sulfur content of about 0.5 wt % to about 5 wt %, and a total halide content of about 1 wppm to about 150 wppm; and oxygen-containing compounds in an amount of about 0.5 wt % to about 15 wt %; and converting the coker gas into at least a polymer.
C10B 57/04 - Autres procédés de carbonisation ou de cokéfactionCaractéristiques générales des procédés de distillation destructive utilisant des charges de composition spéciale
C10B 57/00 - Autres procédés de carbonisation ou de cokéfactionCaractéristiques générales des procédés de distillation destructive
C10B 57/02 - Procédés de carbonisation ou de cokéfaction à phases multiples
9.
Low Cost Processes of In-Situ MAO Supportation and the Derived Finished Polyolefin Catalysts
The present disclosure provides methods for preparing a catalyst system comprising contacting in an organic solvent at a temperature of from less than −6° C. to −60° C. at least one support material having absorbed water and trimethylaluminum (TMA) to form a supported MAO (catalyst precursor) in-situ and contacting the supported MAO with at least one catalyst precursor compound having a Group 3 through Group 12 metal atom or lanthanide metal atom, wherein the TMA to water ratio and the in-situ sMAO formation temperature are so controlled that the supemate after the in-situ supported MAO formation with optional heating or after the finished catalyst formation contains no NMR detectable TMA or no more than 500 ppm TMA.
Processes and systems for fractionating a pyrolysis effluent. The effluent can be separated into a first liquid and a first vapor within a flash zone of a primary' fractionator. A pyrolysis tar can be recovered from the flash zone. The first vapor can flow into a quench zone and can be contacted with a first quench medium to produce a. second liquid and a second vapor. A pyrolysis quench oil can be recovered from the quench zone. The second vapor can flow into a fractionation zone and can be contacted with a second quench medium. A pyrolysis gas oil and a process gas can be recovered from the fractionation zone. Heat can be indirectly transferred from the pyrolysis quench oil to a heat transfer medium to produce a cooled pyrolysis quench oil. The first quench medium can include at least a portion of the cooled pyrolysis quench oil.
Exemplary embodiments of the present technological advancement include pyridine-2,6-bis(phenylenephenolate) complexes that are useful as catalyst components for olefin polymerization and have improved solubility in non-aromatic hydrocarbons (e.g., isohexane). The improved solubility of these complexes was accomplished by the modification of the ligand framework at a specific position that led to improved solubility, but did not adversely affect the performance of the complex when used as a catalyst for olefin polymerizations.
The present disclosure relates to bis(aryl phenolate) Lewis base transition metal complexes, catalyst systems including bis(aryl phenolate) Lewis base transition metal complexes, and polymerization processes to produce polyolefin polymers such as polyethylene based polymers and polypropylene based polymers.
The present disclosure relates to polyethylene compositions, articles including such polyethylene compositions, and methods of making polyethylene compositions and articles (e.g., films) thereof. In some embodiments, a method of making a polyethylene composition includes introducing ethylene, an optional comonomer, a diluent, a catalyst, and 30 ppm to 500 ppm of a cocatalyst to a loop reactor under conditions sufficient to produce a slurry comprising the polyethylene composition. The method includes continuously discharging a portion of the slurry from the loop reactor as effluent comprising the polyethylene composition. The method includes flashing the effluent to vaporize diluent and form a concentrated effluent comprising the polyethylene composition. The method includes condensing the vaporized diluent. The polyethylene composition comprises 80 wt % or greater ethylene-derived units and has a density within the range from 0.935 to 0.975 g/cm3; and a melt index (I2.16) of 2 g/10 min to 4 g/10 min.
Processes for steam cracking hydrocarbons. The process can include introducing a hydrocarbon that can include ethane, propane, or a mixture thereof into radiant coils under steam cracking conditions that produce a steam cracker effluent and deposit coke on an inner surface thereof. An ethane conversion can be ≤75% or a. propane conversion can be ≤93%. Introduction of the hydrocarbon into at least one of the radiant coils can be periodically stopped. A decoking feed can be introduced into the at least one of the radiant coils under decoking process conditions that can include: (i) a decoking effluent that can have a coil outlet temperature of >900° C. (ii) introducing the decoking feed at a. mass flux rate at the quench exchanger inlet of >39 kg m−2 second−1, and/or (iii) introducing the decoking feed while maintaining introduction of the first hydrocarbon feed into one or more of the radiant coils in the plurality of radiant coils.
A variety of systems and methods are disclosed, including, in one embodiment, a method of performing coking on a combined feed, comprising: combining a resin feedstock with a coker feedstock comprising a T10 distillation point of about 343° C. or higher to form a combined feedstock, wherein the resin feedstock comprises a thermoset resin having a median particle size of about 5 mm or less; and exposing at least a portion of the combined feedstock to coking conditions in a coking reactor to form at least coke and a coker effluent.
C10B 55/10 - Cokéfaction des huiles minérales, bitumes, goudrons ou analogues, ou de leurs mélanges, avec des matières carbonées solides avec des matières solides avec des matières solides en mouvement sous forme dispersée selon la technique du "lit fluidisé"
C10B 53/07 - Distillation destructive spécialement conçue pour des matières premières solides particulières ou sous forme spéciale de matières polymères synthétiques, p. ex. pneumatiques
C10B 57/04 - Autres procédés de carbonisation ou de cokéfactionCaractéristiques générales des procédés de distillation destructive utilisant des charges de composition spéciale
16.
Contaminant Removal During Integrated Plastic Recycle
Systems and methods are provided for conversion of polymers (such as plastic waste) to olefins and/or feedstocks that can be further processed for formation of olefins, fuels, and/or other products. The systems and methods can include an optional thermal dehalogenation stage followed by an initial pyrolysis stage where a plastic feedstock is at least partially converted to lower boiling products. Prior to, during, and/or after the pyrolysis stage, one or more contaminant removal stages can be used in order to reduce the content of halides and/or other contaminants in the pyrolysis effluent. This can allow at least a portion of the pyrolysis effluent, such as a gas phase portion and/or a liquid phase portion of the pyrolysis effluent, to have a sufficiently low contaminant content to be used as part of a feed to a conventional petrochemical process.
C10G 1/02 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par distillation
B01D 53/02 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par adsorption, p. ex. chromatographie préparatoire en phase gazeuse
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
C08J 11/12 - Récupération ou traitement des résidus des polymères par coupure des chaînes moléculaires des polymères ou rupture des liaisons de réticulation par voie chimique, p. ex. dévulcanisation uniquement par traitement à la chaleur sèche
C10B 49/22 - Distillation destructive des matières carbonées solides par chauffage direct au moyen d'agents porteurs de chaleur, y compris la combustion partielle de la matière à traiter avec des porteurs de chaleur solides, mobiles, sous forme divisée sous forme dispersée selon la technique du "lit fluidisé"
C10B 53/07 - Distillation destructive spécialement conçue pour des matières premières solides particulières ou sous forme spéciale de matières polymères synthétiques, p. ex. pneumatiques
C10B 57/14 - Caractéristiques des procédés de carbonisation à basse température
17.
EWT FRAMEWORK MOLECULAR SIEVES, MANUFACTURING PROCESSES AND USES THEREOF
Modified EWT framework zeolites are provided, including processes for making such modified EWT framework zeolites and uses of such modified EWT framework zeolites. The modified EWT framework zeolites can be formed based on contacting a EWT framework zeolite with an aqueous solution of an aluminum salt multiple times, such as performing the contacting 2 to 10 times.
C01B 39/02 - Zéolites aluminosilicates cristallinesLeurs composés isomorphesLeur préparation directeLeur préparation à partir d'un mélange réactionnel contenant une zéolite cristalline d'un autre type, ou à partir de réactants préformésLeur post-traitement
B01J 29/70 - Zéolites aluminosilicates cristallinesLeurs composés isomorphes de types caractérisés par leur structure spécifique non prévus dans les groupes
C01B 39/48 - Autres types caractérisés par leur diagramme de diffraction des rayons X et par leur composition définie utilisant au moins un agent structurant organique
18.
Phosphine-borane Catalyst Compounds and Use Thereof
Embodiments described herein relate to tethered phosphine-borane catalyst complexes for the polymerization of one or more epoxides and one or more of CO2, COS, and CS2. The catalysts can also polymerize cyclic monomers such as lactones and lactide.
This disclosure relates to polyethylene polymers, polymerization processes for making such polyethylene polymers, and films made therefrom. In some embodiments, a polyethylene copolymer includes ethylene units; and 1 wt % to 8 wt % of Cs-Cs alpha-olefin comonomer units. The polyethylene copolymer has a density of 0.914 g/cm3 to 0.925 g/cm3 and a melt index (MI, determined per ASTM D1238 at 190° C. and 2.16 kg loading) greater than 1 g/10 min and less than or equal to 2.5 g/10 min. The polyethylene copolymer has a composition distribution breadth index of 75% or greater and a molecular weight distribution (Mw/Mn) of 2 to 8.
Embodiments described herein relate to tertiary pnictogenium-borane catalyst complexes for the polymerization of one or more epoxides and one or more of CO2, COS, and CS2. The catalysts can also polymerize cyclic monomers such as lactones and lactide.
B01J 31/14 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant des composés organiques ou des hydrures métalliques contenant des composés organométalliques ou des hydrures métalliques d'aluminium ou de bore
C08G 64/34 - Procédés généraux de préparation utilisant du dioxyde de carbone et de éthers cycliques
C08G 65/26 - Composés macromoléculaires obtenus par des réactions créant une liaison éther dans la chaîne principale de la macromolécule à partir d'éthers cycliques par ouverture d'un hétérocycle à partir d'éthers cycliques et d'autres composés
21.
Metal-Containing Bis(Imino) per-Substituted Aryl Compounds and Methods Thereof
The present disclosure related to metal-containing compounds that, in some embodiments, are compounds represented by Formula (I). M is Fe or Co. Each of R8, R9, R10, R13, R14, and R15 is independently C1-C40 hydrocarbyl, —OR16, —NR172, halogen, or five-, six-, or seven-membered heterocyclic ring comprising at least one atom selected from the group consisting of N, P, O and S. Each of R6, R7, R11, and R12 is independently C1-C40 hydrocarbyl, a heteroatom or a heteroatom-containing group. Each of X1 and X2 is independently an anionic ligand.
Alkylated naphthalene compositions are usually formed by reacting naphthalene with an electrophilic agent under acid-catalyzed conditions to afford a mixture of monoalkylated naphthalenes, dialkylated naphthalenes, and sometimes polyalkylated naphthalenes. Reaction conditions are usually chosen to change the product distribution for purposes of modifying lubricant properties such as viscosity or volatility. Rarely does the product distribution exceed 90 wt. % monoalkylated naphthalenes. Viscosity and volatility may alternately be modified by obtaining a first fraction enriched in monoalkylated naphthalenes and a second fraction enriched in dialkylated naphthalenes and combining the first fraction and the second fraction in a specified ratio to produce a modified alkylated naphthalene composition having a targeted value of one of the viscosity or the volatility. The first fraction and the second fraction may be obtained by fractional distillation of a first alkylated naphthalene composition to afford an overhead fraction and a bottoms fraction.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C10M 177/00 - Méthodes particulières de préparation des compositions lubrifiantesModification chimique par post-traitement des constituants ou de la composition lubrifiante elle-même, non couverte par d'autres classes
C10N 30/00 - Propriétés physiques ou chimiques particulières améliorées par l'additif caractérisant la composition lubrifiante, p. ex. additifs multifonctionnels
C10N 30/02 - Point d'écoulementIndice de viscosité
C10N 40/04 - Bains d'huileBoîtes de vitessesTransmissions automatiquesMécanismes de traction
Provided herein is an agrochemical composition suitable for use as an emulsifiable concentrate, comprising one or more active ingredients; one or more alkylated aromatic solvents, and optionally, one or more surfactants.
A01N 25/02 - Biocides, produits repoussant ou attirant les animaux nuisibles, ou régulateurs de croissance des végétaux, caractérisés par leurs formes, ingrédients inactifs ou modes d'applicationSubstances réduisant les effets nocifs des ingrédients actifs vis-à-vis d'organismes autres que les animaux nuisibles contenant des liquides comme supports, diluants ou solvants
Catalyst compositions and processes for making and using same. The catalyst composition can include 0.001 wt % to 6 wt % of a Group 8-10 element disposed on a support, based on the weight of the support. The support can include Al and at least 0.5 wt % of a Group 2 element, based on the weight of the support. The catalyst composition can be free of Si or can contain <0.5 wt % of Si, based on the weight of the support.
B01J 23/02 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe des métaux alcalins ou alcalino-terreux ou du béryllium
B01J 23/58 - Métaux du groupe du platine avec des métaux alcalins ou alcalino-terreux ou du béryllium
B01J 23/96 - Régénération ou réactivation de catalyseurs contenant des métaux, oxydes ou hydroxydes des métaux nobles
B01J 37/00 - Procédés de préparation des catalyseurs, en généralProcédés d'activation des catalyseurs, en général
B01J 37/02 - Imprégnation, revêtement ou précipitation
B01J 37/10 - Traitement thermique en présence d'eau, p. ex. de vapeur d'eau
B01J 38/12 - Traitement avec un gaz contenant de l'oxygène libre
25.
Metal Bis(Imino) Aryl Compounds and Methods Thereof
The present disclosure related to metal-containing compounds that, in some embodiments, are alkane-soluble non-metallocene iron compounds having a multidentate ligand chelated to iron, where the multidentate ligand contains at least one nitrogen or phosphorus atom and at least one silyl or germyl group of the formula A(Ra)(Rb)(Rc) where A is Si or Ge and Ra, Rb, or Rc (such as each of Ra, Rb, and Rc) are independently C4-C40 alkyl containing a linear or branched chain at least four carbon atoms in length terminally bound to A.
The 5-OMe-6-tBu substitution of the indenyl fragment of C1 symmetric catalysts is critical for improvements in EP molecular weight capability. The catalysts described in this document are also capable of producing other ordinary polyolefins such as iPP, PE and EO copolymers. The added capability of high molecular weight EP copolymers may expand the potential of C1 symmetric systems in the area of RCPs and ICPs where such capability is necessary.
Methods and compositions for processing polymers with fluorine-free polymer processing aids (PPAs) are described. The methods can include extruding a polymer composition, the polymer composition optionally containing polyethylene glycol (PEG) polymer processing aid, to make a polymeric film; developing one or more melt fractures in the polymeric film; and in response to developing the one or more melt fractures, feeding a masterbatch of polymer processing agent. The masterbatch can include, and preferably can consist essentially of, 1 to 50 wt % PEG having weight average molecular weight (Mw) less than 10,000 g/mol; a carrier resin; and, optionally, one or more non-PPA additives.
A variety of methods and systems that include water washing of a recycle pyrolysis oil for feed to a cracker are disclosed, including, in one embodiment, a method including: contacting a recycle pyrolysis oil with water to produce a purified pyrolysis oil; and cracking the purified pyrolysis oil to produce a product.
C10G 55/04 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique
C10G 1/10 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon à partir de caoutchouc ou de déchets de caoutchouc
29.
Compositions Containing Tri-Cyclopentadiene and Processes for Making Same
Compositions containing tri-cyclopentadiene and processes for making same. In some embodiments, the composition can include 1 wt % to 6 wt % of TCPD-7; 5 wt % to 25 wt % of TCPD-3; 15 wt % to 30 wt % of TCPD-5; and 55 wt % to 75 wt % of TCPD-1, where all wt % values are based on the combined weight of TCPD-7, TCPD-3, TCPD-5, and TCPD-1 in the composition. In some embodiments, the composition can further include di-cyclopentadiene. In other embodiments, the composition can further include di-cyclopentadiene, tetra-cyclopentadiene, and optionally one or more oligomers heavier than tetra-cyclopentadiene. In some embodiments, the composition can be made via a continuous process.
C07C 13/68 - Hydrocarbures polycycliques ou leurs dérivés hydrocarbonés acycliques à cycles condensés à plus de trois cycles condensés le système cyclique condensé ne contenant que quatre cycles à système cyclique ponté
Methods and compositions for processing polymers with fluorine-free polymer processing aids (PPAs) are described. The methods can include continuously extruding a polymer composition through an extruder to form a polymer product, and during at least a portion of the extruding, continually feeding a polyethylene glycol (PEG) composite to the extruder so that the PEG composite and polymer composition are coextruded through the extruder at conditions sufficient to melt blend the PEG composite and the polymer composition. The PEG composite can comprise or consist essentially of PEG (preferably PEG having weight average molecular weight less than 10,000 g/mol) and one or more non-PPA additives having melting point at 1 atm greater than that of the PEG.
Die plates for polymer extrusion may include a die plate having an entrance face for accepting a polymer flow and an exit face for extruding one or more polymer strands, wherein the exit face including at least one element constructed from polycrystalline diamond. Systems for extruding polymer may include: an extruder, a die plate attached to an outlet of the extruder and having (i) an entrance face for accepting a polymer flow and (ii) an exit face for extruding one or more polymer strands; an array of blades configured to rotate so as to contact and slide along the surface of the die exit face, thereby cutting the one or more polymer strands extruded therethrough; wherein (a) the exit face, (b) the blade array, or (c) each of the exit face and the blade array comprises at least one element constructed from polycrystalline diamond.
B29C 48/345 - Filières d’extrusion comprenant au moins deux orifices disposés de manière adjacente, pour extrusion simultanée de fils multiples, p. ex. pour faire des boulettes
EXXONMOBIL TECHNOLOGY AND ENGINEERING COMPANY (USA)
Inventeur(s)
Ruocco, Nino
Leaf, Michael A.
Van Hoyweghen, Danny
Dehlinger, Stephen E.
Abrégé
Methods and compositions for processing polymers with fluorine-free polymer processing aids (PPAs) are described. The methods can include continuously extruding a polymer composition through an extruder to form a polymer product, and during at least a portion of the extruding, continually feeding a polyethylene glycol (PEG) composite to the extruder so that the PEG composite and polymer composition are coextruded through the extruder at conditions sufficient to melt blend the PEG composite and the polymer composition. The PEG composite can comprise or consist essentially of PEG (preferably PEG having weight average molecular weight less than 10,000 g/mol) and one or polymers having melting point at 1 atm greater than that of the PEG.
The present invention relates to a functional cyclic olefin polymer obtained from hydrogenation of a cyclic olefin polymer, wherein the cyclic olefin polymer comprises at least a monomeric unit A′ derived from a monomer A having a norbornene ring and a polar functional group, wherein the amount of the monomeric unit A′ is in the range of from 20% to 100% by mole, 50% to 100% by mole, from 60% to 100% by mole, or from 70% to 100% by mole, based on the total amount of the monomeric units of the cyclic olefin polymer. The present invention further relates to a process for producing the functional cyclic olefin polymer, a composition comprising the functional cyclic olefin polymer, and the use of the functional cyclic olefin polymer. The functional cyclic olefin polymer of the present invention exhibits improved properties, especially in terms of mechanical properties and barrier properties.
The present disclosure relates to methods of constructing a furnace facility including determining transport parameters including vessel parameters. The method can include determining operating site parameters of an operating site and designing one or more modules based on the vessel and operating site parameters. The modules can be sized to provide length, width, height, weight of the modules within allowance of the vessel and operating site parameters. The modules can be constructed at a module fabrication site before transporting to the operating site via a vessel. One or more modules can have one or more furnace components, and/or one or more modules can have one or more furnace.
Catalyst compositions and processes for making and using same. The catalyst composition can include up to 0.025 wt % of Pt and up to 10 wt % of a promoter that can include Sn, Cu, Au, Ag, Ga, a combination thereof, or a mixture thereof disposed on a support. The support can include at least 0.5 wt % of a Group 2 element. All weight percent values are based on the weight of the support.
Processes for venting gas phase olefin polymerization systems are provided. A portion of the reactor overhead can be withdrawn from the reactor to a vent column and contacted with a liquid stripping medium (L) within the vent column to remove at least a portion of the olefin monomer to produce a vent column overhead (G) and a vent column bottoms; recycling the vent column bottoms (rich in the olefin monomer and lean in the carrier gas) to the reactor; determining a L*N to C*G ratio, wherein L is total liquid stripping medium flow to the vent column, N is carrier gas concentration in the reactor overhead, C is the monomer concentration in the reactor overhead, and G is the vent column overhead gas flow. One or more of these flow streams (L, N, C, G) can then be controlled based on the calculated L*N to C*G ratio.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
The present disclosure provides processes and apparatuses for cracking a hydrocarbon-containing feed. The process includes introducing the hydrocarbon-containing feed to a desalter preheat train having an effluent interchanger. The process includes directing a portion of the hydrocarbon-containing feed from in the desalter preheat train to a feed inlet of a convection section of a steam cracking furnace. The process includes combusting fuel proximate to a plurality of burners that provide thermal energy to a radiant section and a convection section of the steam cracking furnace. The hydrocarbon-containing feed is in an operating mode in the convection section to obtain a heated feed mixture. The process includes separating a bottoms effluent from the heated feed mixture of the convection section in a separator. The process includes cooling the bottoms effluent in a heat exchanger using boiler feed water.
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
38.
Hydrocarbon Polymer Modifiers Having High Aromaticity and Low Molecular Weight and Uses Thereof
Described herein are hydrocarbon polymer modifiers for use in various applications. The hydrocarbon polymer modifier comprises a cyclic component, and has a glass transition temperature and Mn defined by the following two equations: (1) Tg≥95−2.2*(% H Ar), and (2) Tg≥−53+(0.265*Mn); an aromatic proton content (% H Ar) of from 12 mole % to 19 mole %; and an Mn of from 300 g/mole to 450 g/mole, wherein Tg is glass transition temperature as expressed in ° C. of the modifier, the % H Ar represents the content of aromatic protons in the hydrocarbon polymer modifier, Mn represents the number average molecular weight of the hydrocarbon polymer modifier, and the cyclic component is selected from the group of a distillation cut from a petroleum refinery stream, and/or C4, C5 or C6 cyclic olefins and mixtures thereof. Further, the hydrocarbon polymer modifier may be characterized by a Tg of from 70° C. to 95° C. and/or a z-average molecular weight (Mz) of the hydrocarbon polymer modifier of less than 1000 g/mole. The hydrocarbon modifiers are particularly useful in high Tg applications where low molecular weight resin is desirable.
Processes for upgrading a hydrocarbon for a predetermined period of time. The process can include determining an amount of one or more contaminant-containing compositions that will be present in a pyrolysis effluent based, at least in part, on a composition of a hydrocarbon feed to be steam cracked, a temperature the hydrocarbon feed will be heated at during steam cracking, a residence time the hydrocarbon feed will be heated at the temperature during steam cracking, or a combination thereof. In some examples, the process can also include taking one or more steps to allow the hydrocarbon feed to be steam cracked for at least as long as a predetermined period of time, controlling process conditions within one or more separation stages to favor certain product compositions, introducing a predetermined amount of one or more agents into various locations of the process, or any combination thereof.
C10G 55/04 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique
C10G 25/00 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, au moyen d'absorbants ou d'adsorbants solides
40.
Polypropylene viscosity modifiers and lubricating oils thereof
In some embodiments, a lubricating oil includes at least 50 wt % of a base oil, based on total weight of the lubricating oil. The lubricating oil includes at least 0.1 wt % of a polypropylene homopolymer having a racemic dyad content of about 60% to about 99% and a number average molecular weight (by GPC DRI) of about 10,000 g/mol to about 250,000 g/mol, wherein a total amount of the base oil and the polypropylene homopolymer does not exceed 100 wt %.
C10M 143/04 - Compositions lubrifiantes caractérisées en ce que l'additif est un hydrocarbure macromoléculaire ou un tel hydrocarbure modifié par oxydation contenant du propène
C10M 157/00 - Compositions lubrifiantes caractérisées en ce que l'additif est un mélange d'au moins deux composés macromoléculaires couverts par plus d'un des groupes principaux , chacun de ces composés étant un composé essentiel
C10M 169/04 - Mélanges de matériaux de base et d'additifs
C10M 171/02 - Valeurs particulières de la viscosité ou de l'indice de viscosité
C10N 20/04 - Poids moléculaireRépartition du poids moléculaire
C10N 30/00 - Propriétés physiques ou chimiques particulières améliorées par l'additif caractérisant la composition lubrifiante, p. ex. additifs multifonctionnels
C10N 30/02 - Point d'écoulementIndice de viscosité
Provided herein are polymer compositions comprising a polymer and polymer processing aid (PPA) comprising a blend of at least two of: (i) a polyethylene glycol; (ii) a surfactant comprising a sorbitan ester or a polysorbate; and (iii) a metal salt of a fatty acid. The polymer can be a C2-C6 olefin homopolymer or a copolymer of two or more C2-C20 α-olefins. and the polymer composition can take the form of polymer pellets; a polymer melt; reactor-grade polymer granules and/or polymer slurries; or other form of polymer composition containing the PPA and optionally one or more other additives. The polymer composition is preferably free or substantially free of fluorine, including fluoropolymer-based PPAs.
Provided herein are polymer compositions comprising a polymer and a surfactant. The surfactant can serve as a polymer processing aid (PPA), and can include a sorbitan ester and/or a polysorbate, preferably a polysorbate. The polymer composition can optionally include other additives, as well. The polymer can be a C2-Ce olefin homopolymer or a copolymer of two or more C2-C20 a-olefins, and the polymer composition can take the form of polymer pellets; a polymer melt; reactor-grade polymer granules and/or polymer slurries; or other form of polymer composition containing the PPA and optionally one or more other additives. The polymer composition is preferably free or substantially free of fluorine, including fluoropoly mer-based PPAs.
Provided herein are polymer compositions comprising a polymer and polyethylene glycol (PEG)-based polymer processing aid (PPA) compositions. The polyethylene glycol can have molecular weight less than 40,000 g/mol. The polymer can be a C2-C6 olefin homopolymer or a copolymer of two or more C2-C20 α-olefins, and can have melt index ratio (MIR) of 20 or less. The polymer composition can further include a metal salt of a fatty acid. The polymer composition is preferably free or substantially free of fluorine, including fluoropolymer-based PPAs.
Processes for upgrading a hydrocarbon for a predetermined period of time. The process can include determining an amount of one or more contaminant-containing compositions that will be present in a pyrolysis effluent based, at least in part, on a composition of a hydrocarbon feed to be steam cracked, a. temperature the hydrocarbon feed will be heated at during steam cracking, a residence time the hydrocarbon feed will be heated at the temperature during steam cracking, or a combination thereof. In some examples, the process can also include taking one or more steps to allow the hydrocarbon feed to be steam cracked for at least as long as a predetermined, period of time, such as controlling process conditions within one or more separation stages to favor certain product compositions and/or introducing a predetermined amount of one or more materials into various locations of the process, or any combination thereof.
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
C01B 3/56 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés
C10G 55/04 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique
C10K 3/04 - Modification de la composition chimique des gaz combustibles contenant l'oxyde de carbone en vue de produire un carburant amélioré, p. ex. un carburant de pouvoir calorifique différent qui peut ne pas contenir d'oxyde de carbone par traitement catalytique réduisant le taux d'oxyde de carbone
45.
Processes and Systems for Steam Cracking Hydrocarbon Feeds
Processes and systems for steam cracking hydrocarbons. Liquid water can be combined with a preheated hydrocarbon feed to produce a mixture, which can be heated to produce a heated mixture. At least a portion of the heated mixture can be steam cracked to produce an effluent. A process gas, a steam cracker naphtha, a condensed process water, and one or more heavy steam cracker products can be separated from the effluent. The condensed process water can include entrained hydrocarbons and at least a portion of the entrained hydrocarbons can be separated therefrom to produce a purified process water. At least a portion of the purified process water can be heated to produce dilution steam. The liquid water combined with the preheated hydrocarbon feed can include a portion of the condensed process water, a portion of the purified process water, condensed dilution steam, or a mixture thereof.
C10G 47/32 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur en présence de composés donneurs d'hydrogène
Embodiments described herein relate to polyhdroxyalkanoate (PHA) copolymers and methods for their preparation utilizing ring-opening polymerization of lactones. Variations of the monomer composition, % of alternation, tacticity, and/or microstructure allow for tailoring of mechanical properties that fall into the elastomer, plastomer, and thermoplastic range.
Provided herein are polymer compositions comprising a Ziegler Natta-catalyzed polymer and polymer processing aid (PPA) compositions. The PPA composition comprises a polyethylene glycol, and optionally a sorbitan ester or polysorbate. The polyethylene glycol can have molecular weight less than 40,000 g/mol. The polymer can have melt index ratio (MIR) of 20 or greater. The polymer composition is preferably free or substantially free of fluorine, including fluoropolymer-based PPAs.
C08L 67/08 - Polyesters modifiés soit par des huiles d'acides gras supérieurs ou leurs acides, soit par des résines naturelles ou des acides résiniques
The present disclosure provides a catalyst feeder for a polymerization process that uses a solid catalyst. A catalyst feeder includes a housing, a plug disposed radially inside the housing and rotatable relative to the housing, and an end plate coupled to the housing. If the plug is in a first rotational position, each one of a first plurality of magnets coupled, to an axial end of the plug is axially aligned with one of a. second plurality of magnets coupled to a surface of the end plate facing towards the axial end of the plug, thereby moving the plug towards a first seated position in relation to the housing. If the plug is in a second rotational position, the plurality of first magnets and the plurality of second magnets are axially offset from each other, thereby moving the plug towards an unseated position in relation to the housing.
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 4/00 - Dispositifs d'alimentationDispositifs de commande d'alimentation ou d'évacuation
B01J 8/08 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles
B01J 8/10 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules mobiles mues par des agitateurs ou par des tambours rotatifs ou par des récipients tournants
The present disclosure generally relates to methods for reducing fouling in tar upgrading processes and to apparatus for carrying out such processes. In some embodiments, a method is provided that includes providing a first tar stream, combining the first tar stream with a utility fluid to form a first process stream having a viscosity lower than that of the first tar stream, and heating the first process stream in a pre-heater under liquid phase conditions without feeding molecular hydrogen gas into the pre-heater to form a second process stream exiting the pre-heater.
C10G 9/16 - Prévention ou enlèvement des incrustations
C10G 49/00 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou
C10G 69/06 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique en l'absence d'hydrogène
Methods for cleaning a die face for an extruder include: positioning an articulating tool adjacent the die face while the die face is installed on the extruder, the die face defining a plurality of die orifices; triggering operation of the articulating tool and thereby articulating an end effector coupled to the articulating tool; and contacting the end effector against one or more surfaces of the die face and thereby removing fouling from the die plate. Methods may include: pausing production of a polymer pellet product from the extruder when at least one of the pressure at the die or a polymer pellet product properties indicates fouling at the die; removing a polymer residue from one or more orifices in the die with an articulating tool equipped with an end effector while the die is mounted on the extruder; and resuming production of the polymer pellet product.
B29C 48/27 - NettoyagePurgeÉvitement de la contamination
B29C 48/00 - Moulage par extrusion, c.-à-d. en exprimant la matière à mouler dans une matrice ou une filière qui lui donne la forme désiréeAppareils à cet effet
51.
Methods for Preparing Polyhydroxyalkanoate Polymer Compositions
A method for preparing a polyhydroxyalkanoate (PHA) polymer by ring-opening polymerization, comprising: polymerizing a lactone in a presence of a solvent and a catalyst with a yttrium metal center under reaction conditions; controlling the polymerization to derive a polymer from the lactone with the polymer having predetermined tensile properties, wherein a Tm of the polymer ranges from 90 to 170° C. and the tensile properties are determined by a ligand of the catalyst, the solvent, and a temperature of the reaction conditions; and recovering the polymer.
Systems and methods are provided for integration of a reactor for polyolefin pyrolysis with the effluent processing train for a steam cracker. The polyolefins can correspond to, for example, polyolefins in plastic waste. Integrating a process for polyolefin pyrolysis with a steam cracker processing train can allow a mixture of polymers to be converted to monomer units while reducing or minimizing costs and/or equipment footprint. This can allow for direct conversion of polyolefins to the light olefin monomers in high yield while significantly lowering capital and energy usage due to integration with a steam cracking process train. The integration can be enabled in part by selecting feeds with appropriate mixtures of various polymer types and/or by limiting the volume of the plastic waste pyrolysis product relative to the volume from the steam cracker(s) in the steam cracking process train. By selecting plastic waste and/or other polyolefin sources with an appropriate mixture of polyolefins as the feedstock, the resulting polyolefin pyrolysis product can be separated in a steam cracking process train to produce separate fractions for various polymer grade small olefin products.
C10G 1/10 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon à partir de caoutchouc ou de déchets de caoutchouc
C10B 49/22 - Distillation destructive des matières carbonées solides par chauffage direct au moyen d'agents porteurs de chaleur, y compris la combustion partielle de la matière à traiter avec des porteurs de chaleur solides, mobiles, sous forme divisée sous forme dispersée selon la technique du "lit fluidisé"
C10B 53/07 - Distillation destructive spécialement conçue pour des matières premières solides particulières ou sous forme spéciale de matières polymères synthétiques, p. ex. pneumatiques
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
An ethylene recycle method may include: obtaining an overheads stream comprising ethylene in a first gaseous state from an ethylene purification column; heating the overheads stream in a first heat exchanger to produce a heated overheads stream comprising the ethylene in a second gaseous state; compressing the heated overheads stream to yield a compressed ethylene stream comprising the ethylene in a first supercritical state; cooling the compressed ethylene stream to produce a cooled, compressed ethylene stream comprising the ethylene in a first liquid state, wherein the cooling comprises passing the compressed ethylene through the first heat exchanger; reducing the pressure of the cooled, compressed ethylene stream to produce a first recycle stream comprising the ethylene in a second liquid state and optionally a third gaseous state; and introducing the first recycle stream into the ethylene purification column.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
B01D 1/28 - Évaporation avec compression de vapeur
B01J 3/00 - Procédés utilisant une pression supérieure ou inférieure à la pression atmosphérique pour obtenir des modifications chimiques ou physiques de la matièreAppareils à cet effet
54.
Systems and Methods for Measuring Polymer Additive Dispensation
Methods may include dispensing an additive from a secondary feeder to a primary feeder: dispensing the additive from the primary feeder to a mixing device: obtaining a primary measurement: obtaining a secondary measurement from the secondary feeder that feeds the primary feeder: comparing the primary measurement and the secondary measurement; and continuing (i-a) dispensing the additive from the primary feeder to the mixing device or (i-b) dispensing the additive from the secondary feeder to the primary feeder: or (ii) when the difference between the primary measurement and the secondary measurement is greater than the selected threshold, halting (ii-a) dispensing the additive from the primary feeder to the mixing device or (ii-b) dispensing the additive from the secondary feeder to the primary feeder, and further recalibrating at least one of the primary feeder or the secondary feeder.
A hydrocarbon feed can be contacted with dehydrogenation catalyst particles to produce a conversion effluent that includes coked catalyst particles and dehydrogenated hydrocarbon(s). The coked catalyst particles can be contacted with an oxidant and a fuel to produce a combustion effluent that can include catalyst particles lean in coke and a combustion gas. The catalyst particles lean in coke can be contacted with an oxidative gas at an oxidizing temperature for a duration of at least 30 seconds to produce conditioned catalyst particles that can have an activity that can be less than the coked catalyst particles. The conditioned catalyst particles can be contacted with a reducing gas to produce regenerated catalyst particles that can have a dehydrogenation activity that can be greater than the coked catalyst particles. The dehydrogenated hydrocarbon(s) can be cooled, compressed, and a plurality of products can be separated from the compressed gaseous stream.
Processes for regenerating an at least partially deactivated catalyst that can include a Group (10) element, an inorganic support, and a contaminant. The Group (10) element can have a concentration of from 0.06 wt % to 6 wt %, based on the weight of the inorganic support. The process can include (I) heating the deactivated catalyst using a heating gas mixture that includes H2O at a concentration >5 mol %, based on the total moles in the mixture to produce a precursor catalyst. The process can also include (II) providing an oxidative gas that includes ≤5 mol % of H2O, based on the total moles in the oxidative gas, and (III) contacting the precursor catalyst at an oxidizing temperature with the oxidative gas for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process can also include (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.
C07C 5/32 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par déshydrogénation avec formation d'hydrogène libre
57.
POLYMERS OF VINYLCYCLOBUTANE AND PROCESSES FOR MAKING SAME
Vinylcyclobutane (VCB) homopolymers, VCB copolymers and processes for making same. The VCB homopolymers and copolymers have a polydispersity (PDI) of less than 3.0 and are made by contacting VCB monomer in the presence of a single-site metallocene, post metallocene, or half metallocene, and an activator, under sufficient reaction conditions to produce a VCB (co)polymer having the narrow PDI of less than 3.0. The resulting poly(vinylcyclobutane) polymers have increased crystallinity and melting point properties (Tm of 165° C. to 246° C.) that are comparable to conventional polyolefins such as polyethylene (typical Tm <135° C.) and polypropylene (typical Tm <165° C.).
C08F 10/14 - Monomères contenant au moins cinq atomes de carbone
C08F 4/659 - Composant couvert par le groupe contenant une liaison métal de transition-carbone
C08F 4/6592 - Composant couvert par le groupe contenant une liaison métal de transition-carbone contenant au moins un cycle cyclopentadiényle, condensé ou non, p. ex. un cycle indényle ou fluorényle
Processes and systems for upgrading a hydrocarbon. In some embodiments, the process for upgrading a hydrocarbon, can include contacting a gas that can include one or more C1-C4 hydrocarbons and carbonyl sulfide with a sorbent under conditions sufficient to cause at least a portion of the carbonyl sulfide to sorb onto the sorbent to produce a treated gas lean in carbonyl sulfide and a sorbent rich in carbonyl sulfide. The process can also include contacting the sorbent rich in carbonyl sulfide with a regenerating gas that can include molecular hydrogen, one or more C1-C4 hydrocarbons, or a mixture thereof to produce a regenerated sorbent and a desorb effluent that can include a sulfur-based contaminant. The process can also include introducing at least a portion of the desorb effluent into a pyrolysis zone of a steam cracker and recovering a steam cracker effluent from the pyrolysis zone.
C10G 70/04 - Post-traitement de mélanges non définis normalement gazeux obtenus par des procédés couverts par les groupes , , , , par des procédés physiques
B01D 53/04 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
C10G 70/06 - Post-traitement de mélanges non définis normalement gazeux obtenus par des procédés couverts par les groupes , , , , par des procédés physiques par mise en contact gaz-liquide
59.
Method and System for Light Olefin Generation with High Yields and Selectivity
A method for forming an olefin, the method including: introducing a hydrocarbon feed stream into a reactor including a dehydrogenation catalyst; reacting the hydrocarbon feed stream with a dehydrogenation catalyst in the reactor to form a high temperature dehydrogenated product, the high temperature dehydrogenated product including at least a portion of the dehydrogenation catalyst; separating at least a portion of the dehydrogenation catalyst from the high temperature dehydrogenated product in a primary separation device and a secondary separation device downstream of and in fluid communication with the primary separation device; following the exit of high temperature dehydrogenation product from the secondary separation device, combining the high temperature dehydrogenation product with a quench stream to cool the high temperature dehydrogenation product and form an intermediate temperature dehydrogenation product, wherein the quench stream includes a hydrocarbon; and cooling the intermediate temperature dehydrogenation product to form a cooled dehydrogenation product.
C07C 5/32 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par déshydrogénation avec formation d'hydrogène libre
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
B01J 23/02 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe des métaux alcalins ou alcalino-terreux ou du béryllium
B01J 23/62 - Métaux du groupe du platine avec du gallium, de l'indium, du thallium, du germanium, de l'étain ou du plomb
B01J 35/30 - Catalyseurs caractérisés par leur forme ou leurs propriétés physiques, en général caractérisés par leurs propriétés physiques
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
60.
Processes for Dehydrogenating Alkanes and Alkyl Aromatic Hydrocarbons
A hydrocarbon can be contacted with dehydrogenation catalyst particles to produce an effluent that can include coked catalyst particles and dehydrogenated hydrocarbon(s). A first stream rich in coked catalyst particles and a second stream rich in dehydrogenated hydrocarbon(s) and containing entrained catalyst particles can be separated from the effluent. The second stream can be contacted with a first quench medium to produce a cooled stream. The cooled stream can be contacted with a second quench medium within a quench tower. A gaseous stream that includes the dehydrogenated hydrocarbon(s), a first quench medium stream, and a slurry stream that includes the second quench medium and the entrained catalyst particles can be separated from the tower. The first quench medium can be recycled. The entrained catalyst particles can be separated from the slurry to provide recovered second quench medium and recovered entrained catalyst particles. The recovered second quench medium can be recycled.
C07C 5/32 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par déshydrogénation avec formation d'hydrogène libre
61.
PROCESSES TO PRODUCE POLY ALPHA-OLEFIN TRIMER AND APPARATUS THEREFOR
In at least one embodiment, a process to produce a poly alpha-olefin (PAO) includes introducing a first alpha-olefin to a first catalyst system comprising activator and a metallocene compound into a continuous stirred tank reactor or a continuous tubular reactor under first reactor conditions to form a first reactor effluent. The first alpha-olefin is introduced to the reactor at a flow rate of about 100 g/hr or more. The first reactor effluent includes at least 60 wt % of PAO dimer and 40 wt % or less of higher oligomers, where the higher oligomers are oligomers that have a degree of polymerization of 3 or more. The process includes introducing the first reactor effluent and a second alpha-olefin to a second catalyst composition including an acid catalyst in a second reactor to form a second reactor effluent comprising PAO trimer.
C08F 210/16 - Copolymères de l'éthylène avec des alpha-alcènes, p. ex. caoutchoucs EP
C07C 2/30 - Procédés catalytiques avec des hydrures ou des composés organiques comportant une liaison métal-carboneHydrures métalliques
C07C 2/32 - Procédés catalytiques avec des hydrures ou des composés organiques sous forme de complexes, p. ex. des acétyl-acétonates
C08F 4/659 - Composant couvert par le groupe contenant une liaison métal de transition-carbone
C08F 4/6592 - Composant couvert par le groupe contenant une liaison métal de transition-carbone contenant au moins un cycle cyclopentadiényle, condensé ou non, p. ex. un cycle indényle ou fluorényle
Hydrocarbon conversion processes. The process can include providing a gas oil feed that can include a gas oil and an olefin. A reactivity R(go) of the gas oil feed can be determined. The R(go) can be compared to a predetermined reference reactivity R(ref). If R(go)>R(ref), the gas oil feed can be heated to a temperature in a range of from 200° C. to 400° C. for a residence time in a range of from 1 minute to 45 minutes to produce a heat-treated gas oil feed having a reactivity R(ht-go), until R(ht-go)≤R(ref). A hydroprocessor feed that includes the gas oil feed if R(go)≤R(ref) or the heat-treated gas oil feed can be fed to a hydroprocessor. The hydroprocessor feed can be hydroprocessed in the hydroprocessor to produce a hydroprocessor effluent that can include a hydroprocessed gas oil.
C10G 65/12 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série comprenant des étapes de craquage et d'autres étapes d'hydrotraitement
63.
Membrane-Based Separation Processes Enhanced with an Absorption Device
A salt ion membrane may be paired with an absorption device to provide advantaged separation processes comprising: introducing a first aqueous salt stream and a mixed feed stream comprising at least one olefin and at least one paraffin to a salt ion membrane under conditions effective to form at least two phases; obtaining an olefin-rich permeate stream and an olefin-lean retentate stream from the salt ion membrane, in which the olefin-rich permeate stream and/or the olefin-lean retentate stream further comprises a salt ion membrane aqueous salt phase; introducing at least a portion of the olefin-lean retentate stream and a second aqueous salt stream to an absorption device under conditions effective to promote olefin extraction; obtaining an olefin-rich aqueous salt stream from the absorption device; and providing at least a portion of the olefin-rich aqueous salt stream as at least a portion of the first aqueous salt stream.
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
64.
Method to Activate Carbene and Carbyne Complexes and Their Use in Metathesis Polymerization
A method, including: contacting a carbene or carbyne precatalyst with a first co-catalyst, under reaction conditions sufficient to cause the first-co-catalyst to activate the carbene or carbyne precatalyst, wherein the first co-catalyst is selected from the group consisting of an aluminum activator, a Br2-1,4-dioxane complex, I2, PhICl2, and PCl5.
B01J 27/135 - HalogènesLeurs composés avec du titane, du zirconium, de l'hafnium, du germanium, de l'étain ou du plomb
B01J 31/02 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant des composés organiques ou des hydrures métalliques
65.
Processes for Dehydrogenating Alkane and Alkyl Aromatic Hydrocarbons
Processes for converting an alkane to an alkene. In some embodiments, the process can include contacting a hydrocarbon-containing feed with a first catalyst that can include Pt or a second catalyst that can include Cr within a conversion zone to effect dehydrogenation of at least a portion of the hydrocarbon-containing feed to produce an effluent that can include one or more dehydrogenated hydrocarbons and molecular hydrogen. The process can also include contacting the effluent with a solid oxygen carrier disposed within the conversion zone to effect combustion of at least a portion of the molecular hydrogen to produce a conversion product that can include the one or more dehydrogenated hydrocarbons and water. In some embodiments, contacting the feed with the first or second catalyst can occur in a first conversion zone and contacting the effluent with the solid oxygen carrier can occur in a second conversion zone.
Catalyst compositions and processes for making and using same. The catalyst composition can include catalyst particles. The catalyst particles can include 0.001 wt % to 6 wt % of Pt and up to 10 wt % of a promoter that can include Sn, Cu, Au, Ag, Ga, or a combination thereof, or a mixture thereof disposed on a support. The support can include at least 0.5 wt % of a Group 2 element. All weight percent values are based on the weight of the support. The catalyst particles can have a median particle size in a range from 10 μm to 500 pm. The catalyst particles can have an apparent loose bulk density in a range from 0.3 g/cm3 to 2 g/cm3, as measured according to ASTM D7481-18 modified with a 10, 25, or 50 mL graduated cylinder instead of a 100 or 250 mL graduated cylinder.
B01J 23/02 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe des métaux alcalins ou alcalino-terreux ou du béryllium
B01J 37/10 - Traitement thermique en présence d'eau, p. ex. de vapeur d'eau
C07C 5/32 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par déshydrogénation avec formation d'hydrogène libre
Provided herein is an agrochemical composition suitable for use as an emulsifiable concentrate, comprising one or more active ingredients; one or more solvents selected from specific amides and esters; and optionally, one or more surfactants.
A01N 31/04 - Biocides, produits repoussant ou attirant les animaux nuisibles, ou régulateurs de croissance des végétaux, contenant des composés organiques de l'oxygène ou du soufre l'atome d'oxygène ou de soufre étant lié à une chaîne latérale aliphatique d'un système cyclique carbocyclique
A01N 25/02 - Biocides, produits repoussant ou attirant les animaux nuisibles, ou régulateurs de croissance des végétaux, caractérisés par leurs formes, ingrédients inactifs ou modes d'applicationSubstances réduisant les effets nocifs des ingrédients actifs vis-à-vis d'organismes autres que les animaux nuisibles contenant des liquides comme supports, diluants ou solvants
The present disclosure relates to a process including introducing a feed to a catalyst and an activator to provide a solution in a continuous or semi-continuous reactor. The feed can include a solvent, and a first monomer that is propylene. The reactor can include polymerization conditions including a pressure of about 1 MPa to about 5 MPa and/or a temperature of about 60° C. to about 120° C. The solution can be circulated to form a biphasic product including a first portion and a second portion, the first portion having a propylene based polymer having a polydispersity index of about 1.5 to about 15, and weight average molecular weight (Mw) of about 50,000 g/mol or greater, according to GPC-4D.
A feed mixture comprising at least one C3 olefin and/or at least one C4 olefin may be contacted with a zeolite catalyst under oligomerization reaction conditions to form a product mixture comprising a plurality of olefin oligomers. The zeolite catalyst, optionally with one or more further modifications, may be selected for operability at high WHSV values that may produce at least C12 olefins in the product mixture having an average branching index of about 2.2 or less. Under suitable conditions, C10-C13 olefins may comprise at least about 25% of the product mixture, M based on total olefin oligomers. Percentage conversion of the at least one C3 olefin and/or at least one C4 olefin may impact the average branching index of at least C12 olefin oligomers and selectivity for C10-C13 olefin oligomers. An amount of C4 olefin in the feed mixture may produce a targeted selectivity for at least C1 olefins.
Methods and systems for analyzing the carbon number distribution of distillation fractions may utilize a fast gas chromatograph. For example, methods may comprise: distilling a hydrocarbon feed to provide a plurality of distillation fractions using a distillation column; obtaining a draw stream from one or more of the plurality of distillation fractions; and analyzing the draw stream with a fast gas chromatograph to directly determine a carbon number distribution of the draw stream, the fast gas chromatograph having a cycle time that is less than a residence time of a specified component of the draw stream within the distillation column, and the fast gas chromatograph being in-line with or in parallel with the draw stream.
Provided herein are substantially all-poly ethylene films, and in particular blown biaxially oriented all-polyethylene films. The films can be multi-layer, and can be produced using a double bubble process. Particular multi-layer films include at least two skin layers, and al least one core layer disposed directly or indirectly between the at least two skin layers. The film composes: a narrow-composition-distribution metallocene linear low density′ polyethylene (narrow-CD mLLDPE), a long-chain-branched metallocene linear low density′ polyethylene (LCB mLLDPE), and, optionally, either or both of a low density polyethylene (LDPE) and high density polyethylene (HDPE).
B32B 27/32 - Produits stratifiés composés essentiellement de résine synthétique comprenant des polyoléfines
B29C 48/00 - Moulage par extrusion, c.-à-d. en exprimant la matière à mouler dans une matrice ou une filière qui lui donne la forme désiréeAppareils à cet effet
B29C 48/08 - Moulage par extrusion, c.-à-d. en exprimant la matière à mouler dans une matrice ou une filière qui lui donne la forme désiréeAppareils à cet effet caractérisées par la forme à l’extrusion de la matière extrudée plate, p. ex. panneaux flexible, p. ex. pellicules
B29C 48/21 - Articles comprenant au moins deux composants, p. ex. couches coextrudées les composants étant des couches les couches étant jointes à leurs surfaces
B29K 23/00 - Utilisation de polyalcènes comme matière de moulage
B32B 7/02 - Propriétés physiques, chimiques ou physicochimiques
B32B 27/08 - Produits stratifiés composés essentiellement de résine synthétique comme seul composant ou composant principal d'une couche adjacente à une autre couche d'une substance spécifique d'une résine synthétique d'une sorte différente
B32B 27/18 - Produits stratifiés composés essentiellement de résine synthétique caractérisée par l'emploi d'additifs particuliers
72.
ETHYLENE-PROPYLENE BRANCHED COPOLYMERS AS VISCOSITY MODIFIERS
The present disclosure relates to lubricant compositions comprising a branched copolymer and methods for making such compositions. Lubricant compositions of the present disclosure comprise an oil and a copolymer and have a high temperature high shear (HTHS) viscosity of about 5 or less, shear stability index (30 cycles) of from about 2% to about 80%, a ratio of thickening efficiency to shear stability index (30 cycles) of from about 1:2 to about 1:30, a kinematic viscosity at 100° C. of from about 3 cSt to about 30 cSt, and a thickening efficiency of about 1 or more. In another class of embodiments, the present disclosure provides a lubricant composition comprising a first and a second copolymers wherein the first copolymer has an ethylene content higher than that of the second copolymer, and wherein at least one of the two copolymers is a long chain branched ethylene copolymer.
C10M 169/02 - Mélanges de matériaux de base et d'épaississants
C10N 20/00 - Propriétés physiques particulières des constituants des compositions lubrifiantes
C10N 20/04 - Poids moléculaireRépartition du poids moléculaire
C10N 30/00 - Propriétés physiques ou chimiques particulières améliorées par l'additif caractérisant la composition lubrifiante, p. ex. additifs multifonctionnels
C10N 30/02 - Point d'écoulementIndice de viscosité
73.
Hydrocarbon Extraction Processes Utilizing a Cleansing Bed
Hydrocarbon extraction processes utilizing a cleansing bed to cleanse at least a portion of a lean-solvent stream are disclosed. The cleansing bed can preferentially include abed of activated carbon, abed of alumina, and/or a bed of an ion-exchange resin. The extraction process can use a liquid/liquid extraction column or an extraction distillation column. The process can be particularly advantageous for removing C10-C20 contaminants, among others, from the lean-solvent stream.
Apparatuses for maintaining a solid as a melt (e.g., for storage or transport) may comprise: a closed vessel having an upper section and a lower section; a pool of a heat-receiving fluid located in the lower section; at least one product circulation conduit located in the lower section and at least partially immersed in the pool of the heat-receiving fluid; and a cooling fluid conduit located in the upper section and spaced apart from the pool of the heat-receiving fluid, the cooling fluid conduit being in thermal communication with vapor produced from the heat-receiving fluid; wherein a cooling fluid is present in the cooling fluid conduit.
F28D 20/02 - Appareils ou ensembles fonctionnels d'accumulation de chaleur en généralAppareils échangeurs de chaleur de régénération non couverts par les groupes ou utilisant la chaleur latente
F28D 7/06 - Appareils échangeurs de chaleur comportant des ensembles de canalisations tubulaires fixes pour les deux sources de potentiel calorifique, ces sources étant en contact chacune avec un côté de la paroi d'une canalisation les canalisations ayant une courbure en U unique
F28D 20/00 - Appareils ou ensembles fonctionnels d'accumulation de chaleur en généralAppareils échangeurs de chaleur de régénération non couverts par les groupes ou
75.
Processes for Regenerating Catalysts and for Upgrading Alkanes and/or Alkyl Aromatic Hydrocarbons
Processes for regenerating an at least partially deactivated catalyst that can include a Group (10) element, an inorganic support, and a contaminant. The Group (10) element can have a concentration of from 0.001 wt % to 6 wt %, based on the weight of the inorganic support. The process can include (I) heating the deactivated catalyst using a heating gas mixture that includes H2O at a concentration >5 mol %, based on the total moles in the mixture to produce a precursor catalyst. The process can also include (II) providing an oxidative gas that includes ≤5 mol % of H2O, based on the total moles in the oxidative gas, and (III) contacting the precursor catalyst at an oxidizing temperature with the oxidative gas for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process can also include (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.
B01J 38/12 - Traitement avec un gaz contenant de l'oxygène libre
B01J 23/89 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe du cuivre ou des métaux du groupe du fer combinés à des métaux nobles
B01J 23/96 - Régénération ou réactivation de catalyseurs contenant des métaux, oxydes ou hydroxydes des métaux nobles
A feed mixture comprising at least one C3 olefin and/or at least one C4 olefin may be contacted with a zeolite catalyst under oligomerization reaction conditions to form a product mixture comprising a plurality of olefin oligomers comprising C12 olefin oligomers having an average branching index, as measured by gas chromatography, of about 2.2 or less, such as about 1.3 to about 2.0. The olefin oligomers may be contacted with a syngas mixture comprising carbon monoxide and hydrogen in the presence of a hydroformylation catalyst to form a hydroformylation reaction product, which may be subsequently reduced to form a plurality of branched alcohols. The branched alcohols, in turn, may be converted into an amphiphilic compound, such as a plurality of branched alcohol sulfates.
C07C 29/141 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par réduction d'un groupe fonctionnel contenant de l'oxygène de groupes contenant C=O, p. ex. —COOH d'un groupe —CHO avec de l'hydrogène ou des gaz contenant de l'hydrogène
B01J 29/70 - Zéolites aluminosilicates cristallinesLeurs composés isomorphes de types caractérisés par leur structure spécifique non prévus dans les groupes
C07C 2/12 - Procédés catalytiques avec des alumino-silicates cristallins, p. ex. avec des tamis moléculaires
C07C 303/24 - Préparation d'esters ou d'amides d'acides sulfuriquesPréparation d'acides sulfoniques ou de leurs esters, halogénures, anhydrides ou amides d'esters d'acides sulfuriques
77.
Guaiazulene-Based Metallocene Catalysts for Olefin Polymerization
Catalyst compositions are disclosed herein, as well as embodiments of catalyst systems and their use in the production of olefin polymers. The catalysts disclosed herein are simple organometallic, metallocene complexes having at least one guaiazulene-based ligand (e.g., guaiazulene or a guaiazulene derivative). Additionally, the catalyst can be combined with an activator, such as methyl alumoxane and/or a non-coordinating anion to provide a catalyst system. Either the catalyst or the catalyst system can be combined with a support, such as silica and/or alumina. The catalyst system, supported or unsupported, can be used to polymerize olefins, such as propylene or ethylene.
A process for producing mesophase pitch, the process including: providing a feedstock having a T5≥400° F. (204° C.) and a T95≤1,400° F. (760° C.); heating the feedstock at a temperature of at least 450° C. to produce a heat treated product including mesophase pitch, wherein the heating is conducted under reaction conditions sufficient to have an equivalent reaction time greater than or equal to 1,000 seconds; and recovering the mesophase pitch.
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
79.
ENHANCED PRODUCTION OF LIGHTLY BRANCHED OLEFIN OLIGOMERS THROUGH OLEFIN OLIGOMERIZATION
A feed mixture comprising at least one C3 olefin and/or at least one C4 olefin may be contacted with a zeolite catalyst under oligomerization reaction conditions to form a product mixture comprising a plurality of olefin oligomers. The zeolite catalyst, optionally with one or more further modifications, may be selected for operability at high WHSV values that may produce at least C12 olefins in the product mixture having an average branching index of about 2.2 or less, such as about 1.3 to about 2.0. Under suitable conditions, C10-C13 olefins may comprise at least about 25% of the product mixture, based on total olefin oligomers. Percentage conversion of the at least one C3 olefin and/or at least one C4 olefin may impact the average branching index of C12 olefin oligomers and selectivity for C10-C13 olefin oligomers. An amount of C4 olefin in the feed mixture may produce a targeted selectivity for C12 olefins.
C07C 2/12 - Procédés catalytiques avec des alumino-silicates cristallins, p. ex. avec des tamis moléculaires
B01J 29/70 - Zéolites aluminosilicates cristallinesLeurs composés isomorphes de types caractérisés par leur structure spécifique non prévus dans les groupes
The present disclosure also relates to lubrication compositions comprising a long branched ethylene copolymer and methods for making compositions. Compositions of the present disclosure can be a composition including an oil and a ethylene copolymer, the copolymer having one or more of an MWD from about 2.0 to about 6.5; an Mw(LS) from about 30,000 to about 300,000 g/mol; a g′vis of from about 0.5 to about 0.97; an ethylene content of about 40 wt % to less than 80 wt %. The compostion has a shear stability index (30 cycles) of from about 1% to about 60%; and a kinematic viscosity at 100° C. of from about 3 cSt to about 25 cSt. A method of making a composition includes blending an oil with a copolymer is also disclosed. Additionally, provided are novel long chain branched ethylene propylene copolymers and methods to produce such copolymers.
C10M 143/04 - Compositions lubrifiantes caractérisées en ce que l'additif est un hydrocarbure macromoléculaire ou un tel hydrocarbure modifié par oxydation contenant du propène
C08F 210/16 - Copolymères de l'éthylène avec des alpha-alcènes, p. ex. caoutchoucs EP
C10M 169/04 - Mélanges de matériaux de base et d'additifs
C10N 20/00 - Propriétés physiques particulières des constituants des compositions lubrifiantes
C10N 20/04 - Poids moléculaireRépartition du poids moléculaire
C10N 30/00 - Propriétés physiques ou chimiques particulières améliorées par l'additif caractérisant la composition lubrifiante, p. ex. additifs multifonctionnels
C10N 30/02 - Point d'écoulementIndice de viscosité
81.
ENHANCED POLYMER DEVOLATILIZATION VIA CONTROLLED FOAMING
Systems and methods for devolatilizing a low viscosity polymer. The method comprises providing a reaction mixture comprising polymer and one or more volatiles, wherein the one or more volatiles comprises one or more unreacted monomers and at least one hydrocarbon solvent; separating the reaction mixture, within a first separator, into a polymer-rich phase and a polymer-lean phase; separating the polymer-rich phase, within a second separator, into a vapor hydrocarbon phase and a concentrated polymer phase; removing at least a portion of the volatiles from the concentrated polymer phase, within a third separator, to provide a devolatilized polymer; and providing a residence time of about 0.2 seconds to 10 seconds within a separator conduit located between the second separator and the third separator.
The invention relates to a method of preparing a polymer, preferably polyethylene, in a polymerization reactor system comprising an initiator injection line. The method comprises operating a back-pressure valve of the initiator injection line to maintain a pressure upstream of the back -pressure valve and downstream of an initiator pump. The invention also concerns an initiator injection line comprising a back-pressure valve and a polymerization reactor system comprising said initiator injection line.
B01J 3/02 - Dispositifs d'alimentation ou d'évacuation appropriés
B01J 4/00 - Dispositifs d'alimentationDispositifs de commande d'alimentation ou d'évacuation
F15B 11/042 - Systèmes comportant essentiellement des moyens particuliers pour commander la vitesse ou la puissance d'un organe de sortie pour commander la vitesse par des moyens de commande situés dans le circuit d'alimentation
B01J 3/04 - Récipients sous pression, p. ex. autoclaves
B01J 19/24 - Réacteurs fixes sans élément interne mobile
Provided is a method for restarting a. gas phase polymerization reactor after operational interruption to a portion of the feed and/or product withdrawal systems while producing a first polyethylene under a first set of operating conditions. The method comprises terminating the polymerization reaction using a polymerization neutralizer and terminating the addition of catalyst and monomer feed to the reactor and/or the withdrawal of the first polyethylene. The reactor is then idled by maintaining recirculation of cycle fluid to maintain fluidization of the fluidized bed. Restart is effected by adding the catalyst and monomer feed to the fluidized bed under a transitional set of polymerization conditions, and withdrawing a. transitional polyethylene for a threshold number of bed. turnovers. Rates of addition of the catalyst and monomer feed to the fluidized bed are adjusted, and a. second polyethylene is withdrawn from the reactor under a second set of operating conditions.
Processes for transitioning from a first catalyst to a second catalyst in a gas phase polymerization reactor. In some embodiments, the processes relate to transitioning from a metallocene catalyst to a Ziegler-Natta catalyst. In other embodiments, the processes relate to transitioning from a first Ziegler-Natta catalyst to a second Ziegler-Natta catalyst.
The present invention relates to tubular reactors, optionally in combination with autoclave reactors, for high pressure polymerization of a monomer, preferably ethylene. Tire tubular reactor comprises at least one thermocouple device for measuring a temperature within the reactor. The invention also concerns a polymerization reactor system comprising said tubular reactor and methods of preparing a polymer in said polymerization reactor system.
Elastomer blends may comprise about 25 wt% or above of a brominated isobutylene-p-methylstyrene copolymer, based on total polymer mass and a non-zero amount of a companion elastomer. The companion elastomer is not a bromobutyl rubber, and the brominated isobutylene-p-methylstyrene copolymer is free of a diene comonomer. Suitable companion elastomers may include, but are not limited to, bromobutyl rubber and natural or synthetic polyisoprene. Advantaged properties may be realized with specified amounts of each companion elastomer. The elastomer blends may be utilized in various locations within tires or components used for making tires.
B60C 1/00 - Pneumatiques caractérisés par la composition chimique, la disposition ou le mélange physique de la composition
C08L 23/22 - Copolymères de l'isobutylèneCaoutchouc butylHomopolymères ou copolymères d’autres iso-oléfines
C08L 23/28 - Compositions contenant des homopolymères ou des copolymères d'hydrocarbures aliphatiques non saturés ne possédant qu'une seule liaison double carbone-carboneCompositions contenant des dérivés de tels polymères modifiées par post-traitement chimique par réaction avec les halogènes ou des composés contenant des halogènes
Systems and methods are provided for reducing or minimizing the chloride content of products generated during co-processing of a plastic feedstock (such as plastic waste) in a refinery process. The reduction in chloride is achieved by mixing the plastic feedstock with one or more additional feedstocks for co-processing in a mixing and/or holding vessel that is maintained at a dechlorination temperature that allows for decomposition of chlorine from the plastic feedstock to form HCl, while reducing or minimizing other conversion of the plastic feedstock and/or the additional feedstock. A purge gas can be passed through the mixing/holding vessel to remove the evolved HCl from the vessel. Because the dechlorination temperature is selected to reduce or minimize conversion of the feedstocks in the mixture, the amount of carbon-containing products that are removed with the purge gas can be reduced or minimized. The dechlorinated mixture of plastic feedstock and additional feedstock(s) can then be processed in a convenient refinery process, such as a thermal cracking process (e.g., coking, visbreaking, other types of pyrolysis) or a catalytic conversion process (e.g., fluid catalytic cracking).
C10G 55/06 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage catalytique
C08J 11/10 - Récupération ou traitement des résidus des polymères par coupure des chaînes moléculaires des polymères ou rupture des liaisons de réticulation par voie chimique, p. ex. dévulcanisation
88.
Methods of Recycling End-of-Life Rubber and Oil-Fouled Plastics
Methods for absorbing residual hydrocarbon liquids from plastic waste including obtaining hydrocarbon liquid-fouled plastic waste shreds, wherein the plastic waste shreds have a particle size of about 0.1 inches to about 3 inches; admixing the hydrocarbon liquid-fouled plastic waste shreds with absorbent elastomer granules, wherein the absorbent elastomer granules have a particle size of about 0.05 inches to about 2 inches; wherein the ratio of absorbent elastomer to hydrocarbon liquid-fouled plastic is about 1:4 to about 4:1 by weight; and agitating the mixture for a period of time.
C10G 55/04 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique
C10B 53/07 - Distillation destructive spécialement conçue pour des matières premières solides particulières ou sous forme spéciale de matières polymères synthétiques, p. ex. pneumatiques
89.
Processes and Systems for Analyzing a Sample Separated from a Steam Cracker Effluent
Processes and systems for analyzing a composition of a C3− component separated from a steam cracker effluent. The process can include steam cracking a hydrocarbon feed to produce a steam cracker effluent. The effluent can be cooled to produce a cooled effluent and a sample can be separated therefrom. Heat can be indirectly exchanged from the sample to a heat transfer medium to produce a gas phase product that can include C3− compounds and a first liquid phase product that can include C4+ compounds. The gas phase product can flow through a flow restricting line and into a transport line. The flow restricting line can have an inner cross-sectional area that is <50% of an inner cross-sectional area of the transport line. The gas phase product can flow through the transport line and into an analyzer. An at least partial composition of the gas phase product can be determined.
G01N 1/10 - Dispositifs pour prélever des échantillons à l'état liquide ou fluide
C10G 9/00 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
Processes and systems for steam cracking hydrocarbon feeds. The process can include introducing a first hydrocarbon feed into radiant coil(s) disposed within a first segment of a firebox to produce a first steam cracker effluent having a first coil outlet temperature. A second hydrocarbon feed can be introduced into radiant coil(s) disposed within a second segment of the firebox to produce a second steam cracker effluent having a second coil outlet temperature. The first and second segments can each include one or more burners providing heat thereto. The burner(s) in each segment can be operated at substantially the same firing rate such that an amount of heat produced by each burner can be substantially the same. A feed rate of the first hydrocarbon feed can be controlled based, at least in part, on a composition of the first hydrocarbon feed and the first coil outlet temperature.
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
91.
ETHYLENE POLYMER LAYERS AND LAYERED FILMS MADE THEREFROM
Ethylene polymer and copolymer layered greenhouse film compositions comprising thermoexpandable microcells exhibiting enhanced thermicity and manufacturing methods related thereto. A greenhouse film composition including at least one foamable film layer composition comprising a thermal expandable microsphere masterbatch component and an ethylene-based polymer component, wherein the greenhouse film comprises less than 20% by weight of a total of one or both of ethylene vinyl acetate or ethylene acetyl acetate.
C08J 9/04 - Mise en œuvre de substances macromoléculaires pour produire des matériaux ou objets poreux ou alvéolairesLeur post-traitement utilisant des gaz de gonflage produits par un agent de gonflage introduit au préalable
C08J 9/14 - Mise en œuvre de substances macromoléculaires pour produire des matériaux ou objets poreux ou alvéolairesLeur post-traitement utilisant des gaz de gonflage produits par un agent de gonflage introduit au préalable par un agent physique de gonflage organique
Olefin separation processes may comprise: introducing a first aqueous salt stream and a mixed feed stream comprising at least one olefin to a salt ion membrane; obtaining an olefin-rich permeate stream and an olefin-lean retentate stream from the salt ion membrane, at least the olefin-lean retentate stream comprising a salt ion membrane aqueous salt phase; introducing the olefin-lean retentate stream to a separation device to obtain a first portion comprising a hydrocarbon stream and a second portion comprising the salt ion membrane aqueous salt phase; introducing to an absorption device the hydrocarbon stream and a second aqueous salt stream under conditions effective to promote olefin extraction, in which the salt ion membrane aqueous salt phase is provided as a portion of the second aqueous salt stream; and obtaining an olefin-rich aqueous salt stream from the absorption device that is provided as at least a portion of the first aqueous salt stream.
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
B01D 69/02 - Membranes semi-perméables destinées aux procédés ou aux appareils de séparation, caractérisées par leur forme, leur structure ou leurs propriétésProcédés spécialement adaptés à leur fabrication caractérisées par leurs propriétés
93.
LANTHANIDE COMPLEXES OF CONSTRAINED GEOMETRY LIGANDS AND USE THEREOF IN RING-OPENING POLYMERIZATION OF CYCLIC ESTERS
Metal-ligand complexes may comprise a lanthanide metal atom and a ligand having a structure represented by Formula (I) in which R1, R2, R6, and R711414hydrocarbyl; R3and R411414hydrocarbyl, or R3and R4are joined together to form an optionally substituted 6-membered aromatic ring; R5114 in situin situ when producing a polyester by ring-opening polymerization of at least one cyclic ester under suitable polymerization reaction conditions. The metal-ligand complexes may be effective to polymerize cyclic esters containing a 7-membered ring, such as ε-decalactone, which are otherwise difficult to polymerize by ring-opening polymerization.
Compositions, methods, and molded articles including a bimodal molecular weight ethylene/propylene random copolymer comprising a high molecular weight component having a melt flow rate at 230 °C of from about 0.02 g/10 min to about 0.5 g/10 min and a low molecular weight component having a melt flow rate at 230 °C of from about 1 g/10 min to about 10 g/10 min, and an ethylene content of from about 0.40 wt.% to about 0.60 wt.%.
The embodiments described herein pertain to constrained geometry catalyst (CGC)-type titanium catalyst compounds with an amido moiety that features asymmetric substituents that give rise to diastereomerism in new catalysts. Catalyst compounds embodying the present technological advancement are excellent catalysts for variety of transformations including homopolymers of propylene (P), ethylene (E), ethylene-propylene (EP)-copolymers and ethylene-octene (EO) copolymers.
C08F 4/76 - MétauxHydrures métalliquesComposés organiques de métalLeur utilisation comme précurseurs de catalyseurs choisis parmi les métaux non prévus dans le groupe choisis parmi les métaux réfractaires choisis parmi le titane, le zirconium, le hafnium, le vanadium, le niobium ou le tantale
The present disclosure relates to molybdenum and/or tungsten complexes, catalyst systems including molybdenum and/or tungsten complexes, and polymerization processes to produce polyalkenamers such as polypentenamers and polycyclooctenamers.
C08F 4/78 - MétauxHydrures métalliquesComposés organiques de métalLeur utilisation comme précurseurs de catalyseurs choisis parmi les métaux non prévus dans le groupe choisis parmi les métaux réfractaires choisis parmi le chrome, le molybdène ou le tungstène
C08F 4/16 - Composés métalliques autres que les hydrures et autres que les composés organiques de métalComplexes d'halogénures de bore ou d'halogénures d'aluminium avec des composés organiques contenant de l'oxygène de silicium, de germanium, d'étain, de plomb, de titane, de zirconium ou de hafnium
97.
Processes and systems for quenching pyrolysis effluents
Processes and systems for quenching an effluent. In certain embodiments, the process can include contacting a pyrolysis effluent and a first quench medium to produce a first quenched effluent. A bottoms stream that can include tar and an overhead stream that can include ethylene and propylene can be obtained from the first quenched effluent. The first quench medium can include a first portion of the bottoms stream that can include a first portion of the tar. In certain embodiments, the process can also include hydroprocessing a second portion of the bottoms stream that can include a second portion of the tar to produce a hydroprocessed product. A hydroprocessed bottoms stream can be obtained from the hydroprocessed product. In certain embodiments, the process can also include contacting at least a portion of the hydroprocessed bottoms stream and the first portion of the bottoms stream to produce the first quench medium.
C10G 70/04 - Post-traitement de mélanges non définis normalement gazeux obtenus par des procédés couverts par les groupes , , , , par des procédés physiques
C10G 69/06 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique en l'absence d'hydrogène
98.
FOAMABLE BRANCHED POLYPROPYLENE COMPOSITIONS AND FOAMED PRODUCTS THEREFROM
visvis value of about 0.5 to about 0.95, and a foaming agent blended with the branched polypropylene. The foamable compositions may be free of a phenolic stabilizer, such as Vitamin E or a Vitamin E derivative, but may optionally comprise a non-phenolic stabilizer. The foamable compositions may be free of stabilizer in some instances. The branched polypropylenes may be formed by irradiation of a substantially linear polypropylene with ionizing radiation, either in an absence of stabilizer or a non-phenolic stabilizer.
C08J 9/12 - Mise en œuvre de substances macromoléculaires pour produire des matériaux ou objets poreux ou alvéolairesLeur post-traitement utilisant des gaz de gonflage produits par un agent de gonflage introduit au préalable par un agent physique de gonflage
Compositions, methods, and molded articles including an ethylene/propylene random copolymer composition comprising an ethylene content of from about 0.1 wt.% to about 0.47 wt.%, a molecular weight distribution of from about 5 to about 20, a plaque haze of from about 10% to about 35%, and a flexural modulus of from ab out 250 kpsi to about 350 kpsi.
A method for steam cracking a plastic-derived liquid feedstock can comprise: steam cracking a plastic-derived liquid feedstock in a steam cracker to produce a cracked product, wherein the plastic-derived liquid feedstock has a final boiling point of about 550° C. or less and an olefin content of about 40 wt % or less; quenching the cracked product from a temperature of about 750° C. or greater to a temperature of about 350° C. or less with a quench oil; and wherein the method does not comprise hydrotreating and/or fractionating the plastic-derived liquid feedstock before steam cracking.
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
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