C07C 7/09 - Purification, separation or stabilisation of hydrocarbonsUse of additives by fractional condensation
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
2.
MULTI-METAL OXIDE CATALYSTS FOR OXIDATIVE DEHYDROGENATION
abcdlexx. In this formula, a is 1.0, b is about 0.01 to about 1.0, c is about 0.01 to about 0.5, d is about 0.01 to about 0.5, e is about 0.005 to about 0.1, and x is the number of oxygen atoms necessary to render the catalyst electrically neutral, wherein the values a, b, c, d, and e are determined based on the amount of each starting material used to form the catalyst. The catalyst is used for the oxidative dehydrogenation of ethane to ethylene.
B01J 23/31 - Chromium, molybdenum or tungsten combined with bismuth
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
A burner and associated methods are disclosed. The burner comprises a housing and a heat shield. The housing comprises an inlet for receiving gas, one or more outlets for expelling gas, and walls forming a gas cavity for directing the gas from the inlet to the outlet. The heat shield comprises a shield layer configured to cover at least a portion of at least one of the walls to thermally insulate the at least one of the walls from heat outside the gas cavity.
The present disclosure describes ethylene/α-olefin copolymer products with a density from 0.865 to 0.905 g/cm3 characterized as having unique rheological fingerprint during their transition from a solid state into a fully molten state. The ethylene/α-olefin copolymer products comprise a first high-density fraction and optionally a second high-density fraction. wherein said first and said optional second high-density fractions have distinct chemical compositions from that of the overall ethylene/α-olefin copolymer products. The first high-density fraction further has a weight-average molecular weight Mw,1HD, wherein Mw,1HD and the weight average molecular weight of the overall ethylene/α-olefin copolymer product Mw satisfy the inequality of Mw,1HD/Mw>2.
C08F 4/6592 - Component covered by group containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
A process for purifying a recycled polyethylene is disclosed. The process includes dissolving recycled polyethylene in a solvent with a boiling point higher than 70°C and a relative energy difference between the solvent and the polyethylene in the recycled polyethylene, as calculated using Hansen Solubility Parameters, less than or equal to 0.8 to provide a first polyethylene-containing solution, and contacting the first polyethylene-containing solution with an adsorption media to obtain a second polyethylene-containing solution. The second polyethylene-containing solution is separated to provide a purified recycled polyethylene.
ab1c2dx122 is Ta, Nb, or a mixture thereof; a is 1.0; b is 0.01 to 0.5; c is 0.005 to 0.2; d is 0.005 to 0.1; and x is the number of oxygen atoms necessary to render the catalyst electrically neutral. The values a, b, c, and d are determined based on the amount of each starting material used to form the catalyst. The catalyst material has a PXRD pattern including peaks at 2θ values of 12.6° ± 0.2°, 18.0° ± 0.2°, 27.9° ± 0.2°, and 29.1° ± 0.2°, wherein the PXRD pattern is obtained using Cu Kα radiation.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
8.
DEVOLATILIZATION OF ETHYLENE/a-OLEFIN COPOLYMER PELLETS
Pellets of ethylene/a-olefin copolymer are devolatilized using nitrogen in a devolatilization bin via a multistep process. Said multistep process, among other things, comprises providing nitrogen gas to the devolatilization bin at a first nitrogen inlet temperature (I) less than VICAT softening temperature of the ethylene/α-olefin copolymer for a first period of time t1 to form a new peak melting peak (II) greater than (I) and smaller than a highest peak melting temperature Tm of the ethylene/α-olefin copolymer. The devolatilization process is continued by raising and holding the nitrogen gas temperature provided to said devolatilization bin at a second nitrogen inlet temperature (III) for a second period of time t2 subsequent to the first period of time t1, wherein (III) is greater than (I) and less than (II).
The present disclosure provides a method to improve the optical properties of an ethylene copolymer composition which is made in a multi reactor solution phase polymerization process. A single site catalyst is employed in a first polymerization reactor and a multi-site catalyst is employed in a second polymerization reactor arranged in series with the first polymerization reactor. The method involves increasing the amount of alpha olefin fed to a second polymerization reactor relative to the amount of alpha olefin fed to a first polymerization reactor, and if desired, optimizing other process conditions across the two reactors, such as the overall alpha-olefin to ethylene ratio, the polymerization temperature of the reactors, and the amount of hydrogen fed to each reactor, in order to maintain the density and the melt index of the ethylene copolymer composition.
Provided herein is a laminate comprising first and second film layers prepared primarily, if not entirely, using polyethylene resins. The first film possesses a low level of surface roughness and a continuous coating, comprising an aqueous dispersion of a clay mineral, that becomes contained at the interface between the first and second film layers following lamination. The laminate is suitable for use in packaging applications that require optimal oxygen barrier performance, and since the laminate is prepared primarily from polyethylene it is accompanied by the benefit of being amenable to recycling.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
A pyrolysis oil is contacted with a hydrocracking catalyst disposed within a hydrocracking unit to convert at least a portion of the pyrolysis oil into a lower alkane to produce a hydrocracking product stream. The hydrocracking product stream is separated into an ethane feed stream comprising ethane and a C3+ feed stream comprising at least one of a C3 alkane, a C4 alkane, or a higher alkane. The C3+ feed stream is diluted with steam to form a steam cracking feed stream. The steam cracking feed stream is heated in a steam cracker to convert at least a portion of the C3+ feed stream to ethylene. The ethane feed stream is diluted with an oxidant to form an oxidative dehydrogenation (ODH) feed stream. The ODH feed stream is contacted with an ODH catalyst disposed within an ODH reactor to convert at least a portion of the ethane to ethylene.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
C10G 69/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
12.
NON-FLUORINATED POLYMER PROCESSING AIDS FOR DIE LIP BUILD-UP MITIGATION IN EXTRUSION OF COMPOSITIONS CONTAINING RECYCLED POLYETHYLENE
An extrudable polymeric composition and methods of making and using the extrudable polymeric composition are disclosed. The composition can include 5 wt.% to 99 wt.% of a recycled polyethylene, and 500 ppm to 5,000 ppm, based on the weight of the extrudable polymeric composition, of added polyether block amide. Also disclosed is a method of reducing die lip build-up during extrusion of polymeric compositions including recycled polyethylene.
C08L 87/00 - Compositions of unspecified macromolecular compounds, obtained otherwise than by polymerisation reactions only involving unsaturated carbon-to-carbon bonds
C08J 3/20 - Compounding polymers with additives, e.g. colouring
C08J 3/22 - Compounding polymers with additives, e.g. colouring using masterbatch techniques
13.
A PROCESS AND SYSTEM INTEGRATING HYDROCRACKING WITH HYDROCARBON DEHYDROGENATION
A pyrolysis oil is contacted with a hydrocracking catalyst to convert at least a portion of the pyrolysis oil into a hydrocracking product stream comprising a lower alkane and residual hydrogen. An oxidative dehydrogenation (ODH) feed stream comprising ethane is contacted with an ODH catalyst to convert at least a portion of the ODH feed stream to produce an ODH product stream comprising ethylene and residual oxygen. At least a portion of the hydrocracking product stream is combined with at least a portion of the ODH product stream to produce a mixed stream. The residual hydrogen from the portion of the hydrocracking product stream reduces at least a portion of the mixed stream, or the residual oxygen from the portion of the ODH product stream oxidizes at least a portion of the mixed stream. An ethylene stream and a liquefied petroleum gas (LPG) stream are separated from the mixed stream.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 27/04 - Refining of hydrocarbon oils, in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
C10G 69/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
C10G 69/14 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural parallel stages only
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
Large volumes of recycled polyethylenes are available for reuse. It would be desirable to prepare films from recycled polyethylene, however, the technical demands for many types of films can make this very difficult. Provided herein are films, for example, stretch films; shrink films; films for vacuum packages and films for dunnage packaging, that may be prepared from a blend of recycled polyethylene with “virgin” polyethylene.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
An anti-coking surface having a thickness up to 15 microns comprising from 15 to 50 wt. % of MnCr2O4 (for example manganochromite); from 15 to 25 wt. % of Cr0.23Mn0.08Ni0.69 (for example chromium manganese nickel); from 10 to 30 wt. % of Cr1.3Fe0.7O3 (for example chromium iron oxide); from 12 to 20 wt. % of Cr2O3 (for example eskolaite); from 4 to 20 wt. % of CuFe5O8 (for example copper iron oxide); and less than 5 wt. % of one or more compounds chosen from FeO(OH), CrO(OH), CrMn, Si and SiO2 (either as silicon oxide or quartz) and less than 0.5 wt. % of aluminum in any form provided that the sum of the components is 100 wt. % is provided on steel.
C23C 8/16 - Oxidising using oxygen-containing compounds, e.g. H2O, CO2
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique
B01J 19/02 - Apparatus characterised by being constructed of material selected for its chemically-resistant properties
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C23C 8/60 - Solid state diffusion of only non-metal elements into metallic material surfacesChemical surface treatment of metallic material by reaction of the surface with a reactive gas, leaving reaction products of surface material in the coating, e.g. conversion coatings, passivation of metals using solids, e.g. powders, pastes
C23C 30/00 - Coating with metallic material characterised only by the composition of the metallic material, i.e. not characterised by the coating process
16.
OXIDATIVE DEHYDROGENATION WITH WATER-GAS SHIFT REACTION
The present disclosure relates to hydrocarbon production processes including oxidative dehydrogenation of ethane-containing feed streams and reaction of carbon monoxide produced thereby with water to produce hydrogen and carbon dioxide.
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
When added to a linear polyethylene in relatively small amounts (fewer than about 5,000 parts per million), an ethylene vinyl alcohol copolymer (EVOH) reduces melt defects during extrusion processes, even in the absence of fluoropolymers.
A system and method including an oxidative dehydrogenation (ODH) reactor system, feeding ethane and oxygen to an ODH reactor having ODH catalyst, and dehydrogenating ethane to ethylene via the ODH catalyst in presence of the oxygen in the ODH reactor, thereby forming acetic acid in the ODH reactor. The ODH reactor effluent is discharged through a quench heat exchanger, thereby cooling the effluent via the quench heat exchanger to below a temperature threshold, the effluent including ethylene, acetic acid, water, carbon dioxide, carbon monoxide, and unreacted ethane, wherein residence time of the effluent from the ODH reactor to effluent discharge outlet of the quench heat exchanger is less than a specified upper limit.
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 4/00 - Feed devicesFeed or outlet control devices
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
A polymeric composition and methods of making and using the same that includes a polyolefin polymer and 100 ppm to 10,000 ppm of a polyamide is disclosed. The composition can be substantially free of a polyolefin polymer/polyamide compatibilizer.
An olefin polymerization process is carried out in the presence of a catalyst system comprising a pre-polymerization catalyst, a boron-based catalyst activator, an alkylaluminoxane co-catalyst, and a hindered phenol compound. The pre-polymerization catalyst is a titanium complex and has an indenoindolyl ligand bridged to a phenoxy ligand via a silyl group. The catalyst system is effective at polymerizing ethylene with alpha-olefins in a solution phase polymerization process at high temperatures and produces ethylene copolymers with high molecular weight and high degrees of alpha-olefin incorporation.
C08F 4/6592 - Component covered by group containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
A system and method for oxidative dehydrogenation including a first reactor having a first ODH catalyst to dehydrogenate an alkane to a corresponding alkene at a first temperature and facilitate generation of steam, a second reactor having a second ODH catalyst to dehydrogenate alkane in a first-reactor effluent to the corresponding alkene at a second temperature that may be greater than the first temperature and facilitate generation of steam, and a third reactor having a third ODH catalyst to dehydrogenate alkane in a second-reactor effluent to the corresponding alkene at a third temperature that may be greater than the first temperature or the second temperature and facilitate generation of steam.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
A solution phase polymerization process utilizes multiple reactors connected in series to make a polyethylene composition. Two different single site catalysts are fed to a first upstream reactor and a Ziegler-Natta catalyst is fed to a second downstream reactor. Optionally, a third polymerization reactor, also connected in series is employed. The single site catalysts fed to the first reactor include a metallocene catalyst and a phosphinimine catalyst. The solution phase polymerization process affords a polyethylene composition comprising a first polyethylene, a second polyethylene, and optionally a third polyethylene.
C08F 210/16 - Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
C08F 4/659 - Component covered by group containing a transition metal-carbon bond
C08F 4/6592 - Component covered by group containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
A system and methods for integrating a small modular nuclear reactor into a steam cracking process are provided. An exemplary system provides a steam cracking system that includes a small modular reactor (SMR) to provide a heat exchange stream and a steam heat exchanger to use the heat exchange stream to generate a steam stream from a water stream, wherein the steam stream is provided to a steam-cracking furnace. A feed heat exchanger uses the heat exchange stream to generate a hot feed stream, wherein the hot feed stream is provided to the steam -cracking furnace. The steam -cracking furnace to generate a product stream including an olefin.
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
G21C 1/32 - Integral reactors, i.e. reactors wherein parts functionally associated with the reactor but not essential to the reaction, e.g. heat exchangers, are disposed inside the enclosure with the core
The present disclosure describes a continuous solution-phase polymerization process to provide an ethylene polymer product comprising a first ethylene polymer and a second ethylene polymer. The continuous solution-phase polymerization process is carried out by injecting a bridged metallocene catalyst formulation, ethylene and process solvent in a first reactor, and by injecting a first heterogenous catalyst formulation and a second combined feed stream comprising ethylene and process solvent in a second reactor. The second feed stream is injected into the second reactor at defined ethylene concentration and temperature ranges resulting in reduced frequency of occurrence of non-oxidized polyethylene defects in the final ethylene polymer product.
A biaxially oriented polyethylene film structure comprises at least three layers, at least one layer comprising a polyethylene composition, the polyethylene composition having a density of from 0.941 to 0.962 g/cm3; a melt index, I2 of from 0.5 to 5.0 g/10 min; and a molecular weight distribution Mw/Mn, of from 3.0 to 8.0. The biaxially oriented film has good optical properties.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
A method and a system for converting ethane to ethylene are provided. An exemplary method includes providing a feed stream including the ethane and oxygen to an oxidative dehydrogenation reactor and converting at least a portion of the ethane to ethylene in the oxidative dehydrogenation reactor to provide a reactor effluent stream including ethane, ethylene, and oxygen, acetylene, or both. The method includes cooling the reactor effluent stream to form a cooled effluent stream and providing the cooled effluent stream to an oxygen removal reactor including an ODH catalyst bed. A deoxygenation stream including water and an alcohol is provided to the oxygen removal reactor to form a deoxygenated effluent.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 7/148 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound
27.
LINEAR HIGH-DENSITY POLYETHYLENE COMPOSITION AND ROTOMOLDED ARTICLE
A solution phase polymerization process employing a metallocene catalyst in a first reactor and a Ziegler-Natta catalyst in a second reactor affords polyethylene compositions which have a density of ≥ 0.940 g/cm3, and a melt index, I2 of less than 3.0 g/10min. When made into a plaque, the polyethylene compositions have a 5 good combination of environmental stress crack resistance, IZOD impact strength and stiffness. The polyethylene compositions which comprise a first ethylene copolymer and a second ethylene copolymer also have a good processing window when making rotomolded specimens.
2 2 of greater than 5.0 g/10min. When made into a plaque the high density polyethylene resin has environmental stress crack resistance, ESCR of greater than 1000 hours as determined by ASTM D1693 in 100% IGEPAL CO-630 under condition B and an IZOD Impact strength of ≥ 10 foot.pound/inch. The polyethylene composition which comprises a first ethylene copolymer and a second ethylene copolymer is relatively easy to process and may be used to make molded articles.
A solution phase polymerization process employing a metallocene catalyst in a first reactor and a Ziegler-Natta catalyst in a second reactor affords polyethylene compositions which have a density of ≥ 0.940 g/cm3, and a melt index, I2 of from 3.0 to 5.0 g/10min. When made into a plaque, the polyethylene compositions have a good combination of 5 environmental stress crack resistance, IZOD impact strength and stiffness. The polyethylene compositions which comprise a first ethylene copolymer and a second ethylene copolymer also have a good processing window when making rotomolded specimens.
A multilayer film structure comprising a sealant layer with a defined compositions and packages prepared from the multilayer film structure are disclosed. The sealant layer comprising from 5% to 65%, based on the total weight of the sealant layer, of a first ethylene copolymer composition; from 20% to 90%, based on the total weight of the sealant layer, of a second ethylene copolymer composition; and from 5% to 30%, based on the total weight of the sealant layer, of a polybutene-1 resin; wherein the first ethylene copolymer composition has a density of from greater than 0.910 g/cm3to less than or equal to 0.940 g/cm322 of from 3.0 dg/min to 7.0 dg/min, and wherein the second ethylene copolymer composition has a density of from greater than or equal to 0.865 g/cm3to less than or equal to 0.910 g/cm3.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
B32B 27/18 - Layered products essentially comprising synthetic resin characterised by the use of special additives
A feed stream including ethane is flowed to a purification unit that includes a first oxidative dehydrogenation catalyst. The feed stream is contacted with the first oxidative dehydrogenation catalyst at a first temperature to reduce a concentration of impurities in the feed stream to produce a purified feed stream. The purified feed stream is flowed to an oxidative dehydrogenation unit that includes a second oxidative dehydrogenation catalyst. The purified feed stream is contacted with the second oxidative dehydrogenation catalyst in the presence of oxygen at a second temperature greater than the first temperature to dehydrogenate ethane to produce a product stream that includes ethylene.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
32.
LOW CONVERSION START-UP OF A HYDROCARBON CRACKING FURNACE
144 alkane, wherein the first conversion level is less than or equal to 60% conversion, and maintaining the first conversion level for a predetermined interval.
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
G05D 21/00 - Control of chemical or physico-chemical variables, e.g. pH-value
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. The polymer processing aid comprises a polyalkylene glycol such as a polyethylene glycol together with a high pressure low density polyethylene (LDPE) and reduces melt defects well in a thermoplastic polyolefin such as a linear low density polyethylene (LLDPE).
Provided herein is a reactor blend ethylene polymer composition comprising at least two identifiable components with distinct structural and compositional characteristics; namely: a first ethylene polymer and a second ethylene interpolymer. The ethylene polymer composition is produced in a continuous solution polymerization process in which the first ethylene polymer is formed in a first solution polymerization reactor by polymerizing ethylene and optionally at least one α-olefin with a first homogenous catalyst formulation; and the second ethylene interpolymer is formed in a second solution polymerization reactor by polymerizing ethylene and at least one α-olefin with a second homogeneous catalyst formulation. The provided ethylene polymer compositions can advantageously be used in applications where easy-opening, mono-material packaging systems are desired.
Methods for preparing a catalyst are provided. An exemplary method includes forming a slurry including metal oxides, a reducing agent, and water; and heating the slurry to form the catalyst. The metal oxides include an oxide of molybdenum; an oxide of vanadium; an oxide of tellurium or an oxide of antimony, or both; and an oxide of tantalum 5 or an oxide of niobium, or both. A ratio of the water in the slurry to amount of catalyst formed is between 0.1 mL water per gram of catalyst and 10 mL water per gram of catalyst.
A catalyst and methods for making the catalyst are provided. An exemplary catalyst includes the formula: MoaVbBicMdOx. In this formula, M is Ta or Nb, a is 1.0, b is 0.01 to 0.5, c is 0.005 to 0.2, d is 0.005 to 0.1, and x is the number of oxygen atoms necessary to render the catalyst electrically neutral. The values a, b, c, and d are determined based on the 5 amount of each starting material used to form the catalyst. The catalysts provided herein may be suitable as catalyst in oxidative dehydrogenation reactions, such as in the oxidative dehydrogenation of ethane.
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
A polyethylene composition has a density of from 0.941 to 0.962 g/cm3; a melt index, I2 of from 0.5 to 5.0 g/10 min; a melt flow ratio, I21/I2 of ≥40; a Z-average molecular weight distribution, Mz/Mw of ≥2.5; a comonomer distribution breadth index, CDBI50 of >50 wt %; and a long chain branching factor, LCBF of >0.0010. In a temperature rising elution fractionation (CTREF) analysis, the polyethylene composition has greater than 70 weight percent of material eluting at a temperature of greater than 90° C.
A bimodal polyethylene composition has a density of from 0.940 to 0.949 g/cm3, a melt index, I2 of greater than 5 g/10 min and an environmental stress crack resistance, ESCR of greater than 1000 hours as determined by ASTM D1693 in 100% IGEPAL CO-630 under condition B. The bimodal polyethylene composition which comprises a first ethylene copolymer and a second ethylene copolymer is relatively easy to process and may be used to make molded articles.
Organometallic complexes are described which are useful as pre-polymerization catalysts which may form part of olefin polymerization catalyst systems. The catalyst systems find use in the polymerization of ethylene, optionally with one or more C3-12 alpha-olefin comonomers. The organometallic complexes are broadly represented by formula I:
Organometallic complexes are described which are useful as pre-polymerization catalysts which may form part of olefin polymerization catalyst systems. The catalyst systems find use in the polymerization of ethylene, optionally with one or more C3-12 alpha-olefin comonomers. The organometallic complexes are broadly represented by formula I:
Organometallic complexes are described which are useful as pre-polymerization catalysts which may form part of olefin polymerization catalyst systems. The catalyst systems find use in the polymerization of ethylene, optionally with one or more C3-12 alpha-olefin comonomers. The organometallic complexes are broadly represented by formula I:
wherein L is a bridging group containing a contiguous chain of atoms connecting P with Cy, wherein the contiguous chain contains 2 or 3 atoms and wherein Cy is a cyclopentadienyl-type ligand. The olefin polymerization catalyst system is effective at polymerizing ethylene with alpha-olefins in a solution phase polymerization process at high temperatures and produces ethylene copolymers with high molecular weight and high degrees of alpha-olefin incorporation. Pre-metallation compounds, metallation processes and synthetic methods to make the organometallic complexes as well as polymerization processes are also described.
This document relates to oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and iron; oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and aluminum; and oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, iron, and aluminum.
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
41.
MULTI-STAGE HYDROCRACKING OF PYROLYSIS OIL WITH INTERMEDIATE QUENCHING
C10G 65/10 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
C10G 69/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
A method and a system for devolatilizing a polymer are provided. An exemplary method includes flashing a polymer solution across a first pressure control valve into a first low-pressure separation vessel to form a more concentrated polymer solution from the first low-pressure separation vessel, and flashing the more concentrated polymer solution across a second pressure control valve into a second low-pressure separation vessel to form an outlet stream from the second low-pressure separation vessel.
This document relates to oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and iron; oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, and aluminum; and oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, oxygen, iron, and aluminum.
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
A system and method for producing ethylene, including dehydrogenating ethane to ethylene via an ODH catalyst in an ODH reactor, discharging an effluent from the ODH reactor, heating feed including ethane to the ODH reactor with the effluent, recovering acetic acid from the effluent as acetic acid product, and forwarding a process gas including ethylene from the effluent for further processing to give ethylene product. The technique involves energy integration including with respect to the processing of the effluent. Water may be recovered from the effluent as recycle water for addition of the recycle water to the feed.
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
B01D 11/04 - Solvent extraction of solutions which are liquid
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/48 - SeparationPurificationStabilisationUse of additives by liquid-liquid treatment
46.
INTEGRATION FOR FEED DILUTION IN OXIDATIVE DEHYDROGENATION (ODH) REACTOR SYSTEM
A system and method for producing ethylene, including dehydrogenating ethane to ethylene via an ODH catalyst in the presence of oxygen in an ODH reactor, discharging an effluent (including at least ethylene, water, and acetic acid) from the ODH reactor, recovering heat from the effluent for processing feed including ethane for the ODH reactor, recovering water from the effluent as recycle water for addition to the feed in performing water dilution of the feed, and adding oxygen to the feed to give a mixed feed including ethane, oxygen, and recycle water to the ODH reactor.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
The present disclosure relates to hydrocarbon treatments including oxidative dehydrogenation of ethane-containing feed streams and extraction of contaminants from pyrolysis oil.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 21/02 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
C10G 53/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
C10G 67/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
48.
NONLINEAR RHEOLOGY OF ETHYLENE INTERPOLYMER COMPOSITIONS
This disclosure relates to ethylene interpolymer compositions, films prepared therefrom and a nonlinear rheology method capable of determining presence of long-chain branched structures in these ethylene interpolymer compositions. Ethylene interpolymer compositions disclosed herein specifically relates to ethylene interpolymer products having: a dimensionless nonlinear rheology network parameter, Δint., greater than or equal to 0.01, satisfying 0.01×(Z−48)0.78≤Δint≤0.01×(Z−60)0.78 inequality wherein Z is a normalized molecular weight defined by (I) where Mw and Me are the weight average and entanglement molecular weights; and a residual catalytic metal of from ≥0.03 to ≤5 ppm of hafnium. The disclosed ethylene interpolymer products have a melt index from about 0.3 to about 500 dg/minute, a density from about 0.855 to about 0.975 g/cc, a polydispersity, Mw/Mn, from about 1.7 to about 25 and a Composition Distribution Breadth Index (CDBI50) from about 1% to about 98%.
C08F 4/6592 - Component covered by group containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. The polymer processing aid comprises a block copolymer having polyamide blocks and polyether blocks and reduces melt defects well in a thermoplastic polyolefin such as a linear low density polyethylene (LLDPE).
C08G 81/02 - Macromolecular compounds obtained by interreacting polymers in the absence of monomers, e.g. block polymers at least one of the polymers being obtained by reactions involving only carbon-to-carbon unsaturated bonds
C08L 23/26 - Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bondCompositions of derivatives of such polymers modified by chemical after-treatment
50.
CONCENTRATION OF AQUEOUS ACETIC ACID BY CLATHRATE HYDRATE FORMATION
A method and a system for concentrating an acetic acid solution are provided An exemplary system includes a hydrate reactor to form solid hydrates in the acetic acid solution, a filtration system to remove the solid hydrates formed in the hydrate reactor, and a drying system to separate ethane from water.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/43 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation
C07C 51/47 - SeparationPurificationStabilisationUse of additives by solid-liquid treatmentSeparationPurificationStabilisationUse of additives by chemisorption
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C25B 3/00 - Electrolytic production of organic compounds
52.
FLAMELESS COMBUSTION HEATING OF OXYGEN SEPARATION MEMBRANE
Systems and methods for heating an oxygen transport membrane in an oxygen separation module are provided. An exemplary oxygen separation module includes an oxygen transport membrane housed inside a sealed vessel and having a retentate side and a permeate side, a first inlet for introducing feed from the distillation top outlet, combustible fuel, or both into the retentate side. The oxygen separation module has a second inlet for introducing feed from a distillation top outlet, combustible fuel, or both into the permeate side, an air inlet for introducing air into the retentate side. The oxygen separation module includes a flameless combustor to heat the oxygen transport membrane, an exhaust for discharge of oxygen depleted air, combustion products from the retentate side, or both, and an outlet for removing oxygen enriched gas and combustion products from the permeate side.
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
53.
PROCESS AND SYSTEM FOR PRODUCING ETHYLENE FROM PYROLYSIS OIL
A process for producing ethylene includes contacting a feed stream including pyrolysis oil with a hydrocracking catalyst disposed within a hydrocracking unit to convert, in the presence of hydrogen, at least a portion of the pyrolysis oil into one or more C2-C4 alkanes to produce a yield in a range of from about 40 wt.% to about 100 wt.% of the one or more C2-C4 alkanes. A hydrocracking product stream is removed from the hydrocracking unit. The hydrocracking product stream is diluted with steam to form a steam cracking feed stream. The steam cracking feed stream is heated in a steam cracker to convert at least a portion of the one or more C2-C4 alkanes to ethylene.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 47/18 - Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
54.
VERY LOW DENSITY POLYETHYLENE WITH RAPID CRYSTALLIZATION RATES
Ethylene copolymer compositions having a density of from 0.860 to 0.910 g/cm3 exhibit rapid crystallization behavior. The ethylene copolymer compositions comprise a first ethylene copolymer, a second ethylene copolymer and a third ethylene copolymer, where the number average molecular weight of the first ethylene copolymer is greater than the number average molecular weight of the second ethylene copolymer and the third ethylene copolymer. The ethylene copolymer compositions are useful in the formation of monolayer and multilayer films.
C08F 4/76 - MetalsMetal hydridesMetallo-organic compoundsUse thereof as catalyst precursors selected from metals not provided for in group selected from refractory metals selected from titanium, zirconium, hafnium, vanadium, niobium, or tantalum
A biaxially oriented polyethylene film structure comprises at least three layers, including a core layer, wherein the core layer comprises: i) from 50 to 99.5 weight percent of a first polyethylene which is an ethylene copolymer having a density of greater than 0.940 g/cm3: and ii) from 0.5 to 50 weight percent of a second polyethylene which is a polyethylene homopolymer composition having a density of at least 0.950 g/cm3: wherein the polyethylene homopolymer composition further comprises a nucleating agent or a mixture of nucleating agents. The biaxially oriented film has very good optical properties.
An apparatus for hydrocarbon conversion, the apparatus including a reactor and a reactor insert secured and disposed within an interior cavity of the reactor, is described. The reactor is configured to permit addition of a feed stream comprising a hydrocarbon at an upstream end of the reactor and to permit discharge of a product stream at a downstream end of the reactor. The reactor insert is configured to provide heat to the interior cavity to promote conversion of hydrocarbons as the feed stream moves from the upstream end of the reactor to the downstream end of the reactor. The products of the conversion reaction are discharged at the downstream end as part of the product stream. A method for hydrocarbon conversion using the apparatus is also described.
B01J 19/24 - Stationary reactors without moving elements inside
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
Decoking a coil of a cracking furnace includes firing one or more burners of the cracking furnace at a burner fuel rate, providing a flow of superheated steam to the coil, wherein the coil comprises a layer of coke extending from an inner surface of the coil and along a length of the coil, providing a flow of air to the coil, thereby initiating a bum of the layer of coke and converting at least some of the coke to carbon dioxide, and adjusting a flow rate of the air relative to a flow rate of the superheated steam to advance a peak tube metal temperature of the coil from a region proximate a first end of the coil to a region proximate a second end of the coil until a compression strength of the furnace coil exceeds a hoop strength of the layer of coke.
A polyethylene composition has a density of ≥0.945 g/cm3, a melt index. I2 of from 0.8 to 4.0 g/10 min. an environmental stress crack resistance, an ESCR of greater than 400 hours as determined by ASTM D1693 in 100% IGEPAL CO-630 under conditions A or B. and a melt strength of ≥3.0 cN.
Methods are provided for preparing a catalyst for oxidative dehydrogenation of ethane. An exemplary method includes forming a slurry including oxides of molybdenum, tantalum, vanadium, and tellurium. Citric acid, oxalic acid, and ethylene glycol are added to the slurry. A chemically compatible carrier (CCC) is added to the slurry. The slurry is transferred to a hydrothermal synthesis vessel, and the hydrothermal synthesis vessel is heated to form a catalyst material precursor. The catalyst material precursor formed in the hydrothermal synthesis vessel is isolated and calcined to form the catalyst material.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
60.
LARGE SCALE SYNTHESIS OF OXIDATIVE DEHYDROGENATION CATALYST
Catalysts and Methods for large-scale production of the catalysts are provided. An exemplary catalyst composition includes molybdenum, vanadium, tellurium, niobium, oxygen. In the catalyst composition, the molar ratio of molybdenum to vanadium is from 1:0.05 to 1:0.60, the molar ratio of molybdenum to tellurium is from 1:0.01 to 1:0.30, and the molar ratio of molybdenum to niobium is from 1:0.01 to 1:0.40. Oxygen is present at least in an amount to satisfy the valency of any present metal oxides, and composition includes less than 1.0 wt. % of sulfur.
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. The polymer processing aid comprises a polyalkylene glycol such as a polyethylene glycol together with a high pressure low density polyethylene (LDPE) and reduces melt defects well in a thermoplastic polyolefin such as a linear low density polyethylene (LLDPE).
3-12 alpha-olefin comonomers. The organometallic complexes are broadly represented by formula I:
wherein L is a bridging group containing a contiguous chain of atoms connecting P with Cy, wherein the contiguous chain contains 2 or 3 atoms and wherein Cy is a cyclopentadienyl-type ligand. The olefin polymerization catalyst system is effective at polymerizing ethylene with alpha-olefins in a solution phase polymerization process at high temperatures and produces ethylene copolymers with high molecular weight and high degrees of alpha-olefin incorporation. Pre-metallation compounds, metallation processes and synthetic methods to make the organometallic complexes as well as polymerization processes are also described.
A process and a system for oxidative dehydrogenation ("ODH") of hydrocarbons are provided. An exemplary process includes contacting an ethane feed with an oxidant in the presence of an oxidative dehydrogenation catalyst in an oxidative dehydrogenation reactor under oxidative dehydrogenation conditions to produce an output stream. The ethane feed includes ethane. The output stream includes ethylene, acetic acid, and residual ethane from the ethane feed. The process includes contacting the output stream with an acetate in an absorber to separate a product stream from a residual ethane stream. The product stream includes the ethylene. The residual stream includes the residual ethane from the ethane feed.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
C07C 7/152 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound by forming adducts or complexes
C07C 7/156 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound by forming adducts or complexes with solutions of copper salts
C07C 51/25 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
C07C 51/44 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation by distillation
C07C 51/48 - SeparationPurificationStabilisationUse of additives by liquid-liquid treatment
A catalyst material includes molybdenum (Mo): vanadium (V). the molar ratio of Mo:V being between 1:0.12 and 1:0.49; tellurium (Te), the molar ratio of Mo:Te being between 1:0.01 and 1:0.30; niobium (Nb), the molar ratio of Mo:Nb being between 1:0.01 and 1:0.30; and beryllium (Be), the molar ratio of Mo:Be being from 1:1 to 1:50.
B01J 35/70 - Catalysts, in general, characterised by their form or physical properties characterised by their crystalline properties, e.g. semi-crystalline
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. The polymer processing aid comprises a monovalent metal salt of a carboxylic acid and reduces melt defects well in a thermoplastic polyolefin such as a linear low density polyethylene (LLDPE).
A biaxially oriented polyethylene film structure comprises at least three layers, including a core layer, wherein the core layer comprises: i) from 50 to 99.5 weight percent of a first polyethylene which is an ethylene copolymer having a density of greater than 0.940 g/cm3; and ii) from 0.5 to 50 weight percent of a second polyethylene which is a polyethylene homopolymer composition having a density of at least 0.950 g/cm3; wherein the polyethylene homopolymer composition further comprises a nucleating agent or a mixture of nucleating agents. The biaxially oriented film has very good optical properties.
The present invention provides an ethylene copolymer composition, which comprises at least two ethylene copolymers and which is suitable for use in a film layer. The invention also relates to film layers and to multilayer film structures comprising such layers. These structures are particularly useful in cling or stretch wrap film applications, to which the invention further relates.
Polyethylene blends made from recycled polyethylene and a bimodal polyethylene composition are disclosed. The polyethylene blends are suitable for compression molding or injection molding applications and are particularly useful in the manufacture of caps and closures for bottles.
Ethylene copolymer compositions having a density of 0.902 g/cm3 or less exhibit rapid crystallization behavior. The ethylene copolymer compositions comprise a first ethylene copolymer, a second ethylene copolymer and optionally a third ethylene copolymer, where the number average molecular weight of the first ethylene copolymer is greater than the number average molecular weight of the second ethylene copolymer. The ethylene copolymer compositions are useful in the formation of monolayer and multilayer films.
C08F 4/76 - MetalsMetal hydridesMetallo-organic compoundsUse thereof as catalyst precursors selected from metals not provided for in group selected from refractory metals selected from titanium, zirconium, hafnium, vanadium, niobium, or tantalum
The copolymerization of ethylene with a cyclic mono olefin (such as norbornene) is conducted in the presence of a catalyst system comprising a bridged hafnocene catalyst and a three part activator. The catalyst system provides excellent activity at high polymerization temperatures. Copolymers produced according to this invention have unique microstructure (with methyl branching being observed) and unique rheology.
C08F 4/642 - Component covered by group with an organo-aluminium compound
C08F 4/659 - Component covered by group containing a transition metal-carbon bond
C08F 4/6592 - Component covered by group containing a transition metal-carbon bond containing at least one cyclopentadienyl ring, condensed or not, e.g. an indenyl or a fluorenyl ring
C08F 232/04 - Copolymers of cyclic compounds containing no unsaturated aliphatic radicals in a side chain, and having one or more carbon-to-carbon double bonds in a carbocyclic ring system having no condensed rings having one carbon-to-carbon double bond
A catalyst, useful for oxidative dehydrogenation of ethane, comprising molybdenum, vanadium, tellurium, tantalum, and oxygen, prepared using a stage hydrothermal synthesis procedure, is provided. The catalyst comprises from 30 to 50 wt. % amorphous content and may be combined with a support/carrier material to form a catalyst material. The described catalysts and catalyst materials demonstrate high selectivity for ethylene at higher temperatures, show little to no decline in conversion and selectivity over time, and do not appear to be sensitive to low residual oxygen concentrations.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
The copolymerization of ethylene with vinylcyclohexane (VCH) is carried out with a catalyst system comprising a bridged hafnocene. High levels of vinylcyclohexane incorporation can be achieved affording ethylene-vinylcyclohexane copolymers having low degrees of crystallinity as measured by differential scanning calorimetry (Xc in %). These copolymers have good barrier properties when made into film.
The copolymerization of ethylene with vinylcyclohexane is carried out with a catalyst system comprising a bridged hafnocene. When relatively low levels of vinylcyclohexane are incorporated, the ethylene-vinylcyclohexane copolymers have high degrees of crystallinity as measured by differential scanning calorimetry (Xc in %). These copolymers have good thermoformability.
A polymer processing aid (PPA) reduces die lip build up during the extrusion of a thermoplastic polyolefin in the absence of fluoropolymers. The polymer processing aid comprises a block copolymer having polyamide blocks and polyether blocks.
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. A polymer processing aid comprising a block copolymer having polyamide blocks and polyether blocks reduces melt defects well in a thermoplastic polyolefin such as a linear low density polyethylene (LLDPE). Inclusion of an adjuvant PPA comprised of polycaprolactone, or polycaprolactone diol polymer further improves the melt fracture behavior in a thermoplastic and in the absence of fluoropolymers.
A polymer processing aid (PPA) reduces melt defects in extruded polyolefins in the absence of fluoropolymers. A polymer processing aid comprising a block copolymer having polyamide blocks and polyether blocks reduces melt defects well in a ther¬ moplastic polyolefin such as a linear low density polyethylene (LLDPE). Inclusion of an adjuvant PPA comprised of polycaprolactone, or polycaprolactone diol polymer further improves the melt fracture behavior in a thermoplastic and in the absence of fluoropolymers.
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
79.
CATALYSTS AND RELATED METHODS OF MAKING AND USING THE SAME
Syngas conversion catalysts are H-MOR catalysts including iron and zinc. The catalysts can be made using a solid-state ion exchange process. The catalysts can be used in DSTO processes.
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
The present invention provides a polymer blend, which comprises a low- density polyethylene and an ethylene copolymer composition and which is suitable for use in a film layer. The invention also relates to film layers and to multilayer film structures comprising such film layers, which structures are particularly useful in collation shrink packaging applications.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
C08F 210/16 - Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
The present invention provides a polymer blend, which comprises a lowdensity polyethylene and an ethylene copolymer composition and which is suitable for use in a film layer. The invention also relates to film layers and to multilayer film structures comprising such film layers, which structures are particularly useful in collation shrink packaging applications.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
C08F 4/659 - Component covered by group containing a transition metal-carbon bond
C08F 210/16 - Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
A fixed bed reactor system for the oxidative dehydrogenation of ethane, comprising a catalyst bed wherein the catalyst capacity profile increases along the length of catalyst bed from the upstream end to the downstream end. The catalyst bed may include one or more sections, across one or more fixed bed reactors, that are identified by a change in catalyst capacity. Catalyst capacity, or the ability to convert ethane into ethylene, may be altered by changing the dilution ratio, void fraction, and or the 35% conversion temperature. A method for loading a fixed bed reactor with an increasing catalyst capacity is also described.
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
85.
REACTOR SYSTEMS FOR OXIDATIVE DEHYDROGENATION (ODH) OF ETHANE
An oxidative dehydrogenation (ODH) reactor system and a method of operating the ODH reactor system, including providing feed having ethane, oxygen, and diluent to give a reaction mixture flowing through the tube side of the ODH reactor, and converting ethane into ethylene with ODH catalyst on the tube side. Coolant is routed through the shell side of the ODH reactor to maintain the tube side at a first temperature in a first cooling section and at a second temperature in a second cooling section, wherein the first temperature is lower than the second temperature. The ODH reactor system may include more than one ODH reactor. For ODH reactor systems having more than one ODH reactor is series, oxygen gas may be injected between ODH reactors.
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
An oxidative dehydrogenation (ODH) reactor system and a method of operating the ODH reactor system, including providing feed having ethane, oxygen, and diluent to give a reaction mixture flowing through the tube side of the ODH reactor, and converting ethane into ethylene with ODH catalyst on the tube side. Coolant is routed through the shell side of the ODH reactor to maintain the tube side at a first temperature in a first cooling section and at a second temperature in a second cooling section, wherein the first temperature is lower than the second temperature. The ODH reactor system may include more than one ODH reactor. For ODH reactor systems having more than one ODH reactor is series, oxygen gas may be injected between ODH reactors.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
An oxidative dehydrogenation (ODH) reactor system and a method of operating the ODH reactor system, including providing feed having ethane, oxygen, and diluent to give a reaction mixture flowing through the tube side of the ODH reactor, and converting ethane into ethylene with ODH catalyst on the tube side. Coolant is routed through the shell side of the ODH reactor to maintain the tube side at a first temperature in a first cooling section and at a second temperature in a second cooling section, wherein the first temperature is lower than the second temperature. The ODH reactor system may include more than one ODH reactor. For ODH reactor systems having more than one ODH reactor is series, oxygen gas may be injected between ODH reactors.
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
This disclosure relates to a process of converting one or more alkanes to one or more alkenes that includes providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation process which converts at least a portion of the one or more alkanes to one or more alkenes in an oxidative dehydrogenation reactor, a second stream exiting the oxidative dehydrogenation process comprising one or more alkanes, and one or more alkenes; and providing at least a portion of the alkanes in the second stream to a catalytic membrane dehydrogenation process containing a catalyst loaded into a catalytic dehydrogenation membrane reactor which converts at least a portion of the alkanes to the corresponding alkenes and hydrogen.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
B01J 29/89 - Silicates, aluminosilicates or borosilicates of titanium, zirconium or hafnium
C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
89.
REACTOR SYSTEMS FOR OXIDATIVE DEHYDROGENATION (ODH) OF ETHANE
An oxidative dehydrogenation (ODH) reactor system and a method of operating the ODH reactor system, including providing feed having ethane, oxygen, and diluent to give a reaction mixture flowing through the tube side of the ODH reactor, and converting ethane into ethylene with ODH catalyst on the tube side. Coolant is routed through the shell side of the ODH reactor to maintain the tube side at a first temperature in a first cooling section and at a second temperature in a second cooling section, wherein the first temperature is lower than the second temperature. The ODH reactor system may include more than one ODH reactor. For ODH reactor systems having more than one ODH reactor is series, oxygen gas may be injected between ODH reactors.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
abcdxx. In this formula, a is 1.0, b is about 0.01 to about 0.3, c is about 0.01 to about 0.09, d is about 0.01 to about 0.05, and x is the number of oxygen atoms necessary to render the catalyst electronically neutral.
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
Methods are provided provides a method for preparing a catalyst for oxidative dehydrogenation. An exemplary method includes forming a slurry including oxides of molybdenum, tantalum oxide, and tellurium and adding VOSO4 to the slurry. Citric acid, oxalic acid, and ethylene glycol are added to the slurry. The slurry is transferred to an autoclave, and the autoclave is heated to form a catalyst precursor. The catalyst precursor formed in the autoclave is isolated and calcined to form the catalyst.
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
In some embodiments a Stand Up Pouch (SUP) is prepared using a polyethylene structure having a first web and a second web. The webs are laminated together to form the polyethylene structure that is used to prepare the SUP. One web contains a layer of recycled polyethylene (r.PE). In some instances, the use of r.PE has been observed to reduce the effectiveness of the sealant layer of the overall structure. In some embodiments, the SUP disclosed herein has a two layer sealant system to mitigate this problem.
B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
B65D 75/00 - Packages comprising articles or materials partially or wholly enclosed in strips, sheets, blanks, tubes or webs of flexible sheet material, e.g. in folded wrappers
B65D 75/26 - Articles or materials wholly enclosed in laminated sheets or wrapper blanks
93.
ETHYLENE INTERPOLYMER PRODUCTS HAVING UNIQUE MELT FLOW-INTRINSIC VISCOSITY (MFIVI) AND HIGH UNSATURATION
This disclosure relates to ethylene interpolymer products comprising a Melt Flow-Intrinsic Viscosity Index value, MFIVI, from ≥0.05 to ≤0.80; a first derivative of a melt flow distribution function, formula (I) at a loading of 4000 g, from >−1.51 to ≤−1.15; a sum of unsaturation, SUMU, from ≥0.005 to <0.047 unsaturations per 100 carbon atoms; and a residual catalytic metal from ≥0.03 to ≤5 ppm of hafnium. Ethylene interpolymer products comprise at least two ethylene interpolymers. Ethylene interpolymer products are characterized by a melt index (I2) from 0.3 to 500 dg/minute, a density from 0.855 to 0.975 g/cc and from 0 to 25 mole percent of one or more a-olefins. Ethylene interpolymer products have polydispersity, Mw/Mn, from 1.7 to 25; and CDBI50 values from 1% to 98%. These ethylene interpolymer products have utility in flexible as well as rigid applications.
This disclosure relates to ethylene interpolymer products comprising a Melt Flow-Intrinsic Viscosity Index value, MFIVI, from ≥0.05 to ≤0.80; a first derivative of a melt flow distribution function, formula (I) at a loading of 4000 g, from >−1.51 to ≤−1.15; a sum of unsaturation, SUMU, from ≥0.005 to <0.047 unsaturations per 100 carbon atoms; and a residual catalytic metal from ≥0.03 to ≤5 ppm of hafnium. Ethylene interpolymer products comprise at least two ethylene interpolymers. Ethylene interpolymer products are characterized by a melt index (I2) from 0.3 to 500 dg/minute, a density from 0.855 to 0.975 g/cc and from 0 to 25 mole percent of one or more a-olefins. Ethylene interpolymer products have polydispersity, Mw/Mn, from 1.7 to 25; and CDBI50 values from 1% to 98%. These ethylene interpolymer products have utility in flexible as well as rigid applications.
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B32B 27/08 - Layered products essentially comprising synthetic resin as the main or only constituent of a layer next to another layer of a specific substance of synthetic resin of a different kind
2 yield; and have negligible effect on ethane conversion. The feed ethanol is converted to carbonaceous products without negatively effecting the catalyst activity.
A four component additive package that contains a first phosphite, a second phosphite, a primary antioxidant and an optical brightener is used in combination with a polyethylene that is polymerized with a mixed catalyst system that contains two different types of catalysts. The stabilized polyethylene exhibits improved color performance.
A chemical complex to perform oxidative dehydrogenation of C2-C4 alkanes, to C2-C4 alkenes, the chemical complex involving at least one oxidative dehydrogenation reactor containing one or more mixed metal oxide catalysts and designed to accept, optionally in the presence of a heat removal diluent gas, an oxygen containing gas and a C2-C4 alkane containing gas, and to produce a product stream including a corresponding C2-C4 alkene and one or more of: an unreacted C2-C4 alkane; oxygen; heat removal diluent gas; carbon oxides, including carbon dioxide and carbon monoxide; oxygenates, including but not limited to, one or more of acetic acid, acrylic acid and maleic acid; and water; and involving a combustion chamber for combusting a product stream and at least one fuel stream and optionally at least one stream including oxygen, the combustion chamber producing a flue gas at a temperature of 850° C. to 1500° C.
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
B01J 27/057 - Selenium or telluriumCompounds thereof
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
An apparatus for hydrocarbon cracking includes a reactor and a heating component. The reactor has an interior cavity configured to receive a feed stream. The feed stream includes a hydrocarbon. The heating component surrounds the reactor. The heating component is configured to provide heat to an external surface of the reactor to crack the hydrocarbon and produce a product stream. The product stream includes a C2-C4 alkene, syngas, or a combination thereof. The reactor is configured to discharge the product stream. The heating component can include an electrical resistor, a combustion chamber, or both.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
An apparatus for hydrocarbon cracking includes a reactor and a heating component. The reactor has an interior cavity configured to receive a feed stream. The feed stream includes a hydrocarbon. The heating component surrounds the reactor. The heating component is configured to provide heat to an external surface of the reactor to crack the hydrocarbon and produce a product stream. The product stream includes a C2-C4 alkene, syngas, or a combination thereof. The reactor is configured to discharge the product stream. The heating component can include an electrical resistor, a combustion chamber, or both.
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
Disclosed herein are the design and construction methods for a specialized structure, or “cabinet”, to house compressed gas cylinders such that they may be kept within an ordinary building.
Compositions for forming rotationally molded (rotomolded) parts, methods for forming the rotomolded parts, and the rotomolded parts are provided. An exemplary rotomolding composition includes a virgin resin, including a polyethylene polymer, and a postconsumer recycle (PCR) resin.
