A scrubbing solution for removing contaminants, including particularly hydrogen sulfide, from a fluid. The scrubbing solution includes at least one scrubbing reagent which has a primary or secondary amine and an acid, which may be phosphoric acid. The fluid being scrubbed is passed through the scrubbing solution. The contaminants react with the scrubbing reagent securing them in the scrubbing solution. The fluid being scrubbed and the scrubbing solution are then separated. The scrubbing solution is heated and, if the scrubbing solution is under pressure, the pressure is reduced. The acid facilitates thorough removal of the contaminants, and especially the hydrogen sulfide, from the scrubbing solution. The scrubbing solution is then ready for reuse. Because the scrubbing solution is rendered substantially free of hydrogen sulfides, it can absorb other sulfide contaminants that might not otherwise be absorbed.
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
characterised in that the hydrogen concentration in the reactor is changed and the change is effected at least in part by changing the V/L ratio by at least 10% and/or by changing the volume, X.
The present invention relates to the polymerisation of one or more monomers in a gas phase reactor, and in particular provides a process for from the polymerisation of one or more monomers in a horizontal stirred bed gas phase reactor, wherein the process comprises: a. Polymerising a mixture comprising one or more monomers and hydrogen in the reactor to produce the polymer, b. Withdrawing from the reactor a gaseous stream, c. Passing the gaseous stream to a condenser in which it is partly condensed to produce a liquid phase and a remaining vapour phase, d. Passing the mixture of liquid phase and remaining vapour from the condenser to a separator in which there is maintained a liquid phase and a vapour phase, the volume of the liquid phase in the separator being a percentage, X, which is between 10 and 80% of the total volume of the separator..
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
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
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
A scrubbing solution for removing contaminants, including particularly hydrogen sulfide, from a fluid. The scrubbing solution includes at least one scrubbing reagent which has a primary or secondary amine and an acid, which may be phosphoric acid. The fluid being scrubbed is passed through the scrubbing solution. The contaminants react with the scrubbing reagent securing them in the scrubbing solution. The fluid being scrubbed and the scrubbing solution are then separated. The scrubbing solution is heated and, if the scrubbing solution is under pressure, the pressure is reduced. The acid facilitates thorough removal of the contaminants, and especially the hydrogen sulfide, from the scrubbing solution. The scrubbing solution is then ready for reuse. Because the scrubbing solution is rendered substantially free of hydrogen sulfides, it can absorb other sulfide contaminants that might not otherwise be absorbed.
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
The present invention relates to a process for supply of a polymerization catalyst component to a polymerization reactor which comprises: a. Providing a first stream comprising the catalyst component, b. Providing a diluent stream in a second line, c. Contacting the first stream and the diluent stream to form a mixed stream and passing the mixed stream to a polymerization reactor, and further characterised in that at least one of the following applies: i) the volume of the mixing chamber is less than 150 ml, ii) the volume of the mixing chamber is such that the residence time, based on the total volumetric flow rate of the mixed stream, is less than 5 seconds, iii) the mixing chamber is not mechanically agitated, the mixing chamber has a cover which can be removed to allow cleaning of the mixing chamber in situ.
C08F 210/16 - Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
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
The present invention relates to a process for polymerization of a monomer, and in particular whereby polymer particles are transferred from an upstream polymerization reactor, which process comprises: (a) discharging a mixture comprising polymer particles and reactive gases, which reactive gases comprise hydrogen, from the upstream reactor, (b) transferring the polymer particles and reactive gases into a first chamber which is in open communication with a second chamber, (c) keeping the first and second chamber in open communication for a time period, t, after completing transfer of the polymer particles to the second chamber, and (d) subsequently isolating the second chamber from the first chamber and transferring the polymer particles from the second chamber into a downstream vessel.
C08F 210/16 - Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
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
characterised in that the mixing of the first stream and the diluent stream takes place by providing the first stream from the first line and the diluent stream from the second line separately to a mixing chamber which has an enlarged cross-section compared to the first and second lines.
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
B01J 8/36 - 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 with fluidised bed through which there is an essentially horizontal flow of particles
A scrubbing solution for removing contaminants, including particularly hydrogen sulfide, from a fluid. The scrubbing solution includes at least one scrubbing reagent which has a primary or secondary amine and an acid, which may be phosphoric acid. The fluid being scrubbed is passed through the scrubbing solution. The contaminants react with the scrubbing reagent securing them in the scrubbing solution. The fluid being scrubbed and the scrubbing solution are then separated. The scrubbing solution is heated and, if the scrubbing solution is under pressure, the pressure is reduced. The acid facilitates thorough removal of the contaminants, and especially the hydrogen sulfide, from the scrubbing solution. The scrubbing solution is then ready for reuse. Because the scrubbing solution is rendered substantially free of hydrogen sulfides, it can absorb other sulfide contaminants that might not otherwise be absorbed.
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
C10K 1/12 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids alkaline-reacting
C10K 1/14 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids alkaline-reacting organic
A scrubbing solution for removing contaminants, including particularly hydrogen sulfide, from a fluid. The scrubbing solution includes at least one scrubbing reagent which has a primary or secondary amine and an acid, which may be phosphoric acid. The fluid being scrubbed is passed through the scrubbing solution. The contaminants react with the scrubbing reagent securing them in the scrubbing solution. The fluid being scrubbed and the scrubbing solution are then separated. The scrubbing solution is heated and, if the scrubbing solution is under pressure, the pressure is reduced. The acid facilitates thorough removal of the contaminants, and especially the hydrogen sulfide, from the scrubbing solution. The scrubbing solution is then ready for reuse. Because the scrubbing solution is rendered substantially free of hydrogen sulfides, it can absorb other sulfide contaminants that might not otherwise be absorbed.
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
C10K 1/12 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids alkaline-reacting
C10K 1/14 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids alkaline-reacting organic
A scrubbing solution for removing contaminants, including particularly hydrogen sulfide, from a fluid. The scrubbing solution includes at least one scrubbing reagent which has a primary or secondary amine and an acid, which may be phosphoric acid. The fluid being scrubbed is passed through the scrubbing solution. The contaminants react with the scrubbing reagent securing them in the scrubbing solution. The fluid being scrubbed and the scrubbing solution are then separated. The scrubbing solution is heated and, if the scrubbing solution is under pressure, the pressure is reduced. The acid facilitates thorough removal of the contaminants, and especially the hydrogen sulfide, from the scrubbing solution. The scrubbing solution is then ready for reuse. Because the scrubbing solution is rendered substantially free of hydrogen sulfides, it can absorb other sulfide contaminants that might not otherwise be absorbed.
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
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
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
C10L 3/10 - Working-up natural gas or synthetic natural gas
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
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
C10L 3/10 - Working-up natural gas or synthetic natural gas
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
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
18.
METHOD AND APPARATUS FOR RECOVERING ABSORBING AGENTS IN ACID GAS TREATMENT
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
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
19.
METHOD AND APPARATUS FOR RECOVERING ABSORBING AGENTS IN ACID GAS TREATMENT
A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream.
Drilling fluids and processes for making drilling fluids for use in environmentally sensitive areas are provided. The environmentally friendly drilling fluid includes a linear olefin portion that includes linear alpha olefins and/or linear internal olefins with carbon numbers of about 6 carbons to about 30 carbons; and an oligomer portion comprising dimers, trimers, tetramers, and/or heavier oligomers of olefins, wherein the olefins have a carbon number of between about 4 carbons and about 24 carbons, and the oligomer portion includes at least about 50 mole percent of trisubstituted olefin. The drilling fluid has a pour point of about -10 °C or lower, a biodegradation ratio of about 1.0 or less, a toxicity ratio of about 1.0 or less, a Marine Bodis of at least about 60%, a flash point of about 110 °C or higher, a viscosity less than about 4 cSt at 40 °C, a density of about 0.78 to about 0.83 gram/ml, and a log Pow of greater than about 3.
Drilling fluids and processes for making drilling fluids for use in environmentally sensitive areas are provided. The environmentally friendly drilling fluid includes a linear olefin portion that includes linear alpha olefins and/or linear internal olefins with carbon numbers of about 6 carbons to about 30 carbons; and an oligomer portion comprising dimers, trimers, tetramers, and/or heavier oligomers of olefins, wherein the olefins have a carbon number of between about 4 carbons and about 24 carbons, and the oligomer portion includes at least about 50 mole percent of trisubstituted olefin. The drilling fluid has a pour point of about -10 .degree.C or lower, a biodegradation ratio of about 1.0 or less, a toxicity ratio of about 1.0 or less, a Marine Bodis of at least about 60%, a flash point of about 110 .degree.C or higher, a viscosity less than about 4 cSt at 40 .degree.C, a density of about 0.78 to about 0.83 gram/ml, and a log Pow of greater than about 3.
A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer and an empirical model. During a transition, the empirical model predicts a required amount based upon an initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed.
A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer and an empirical model. During a transition, the empirical model predicts a required amount based upon an initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed.
A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a steady-state control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer, an online analyzer and an empirical model. During a transition, the on-line analyzer measures an initial concentration of a reaction component, the empirical model predicts a required amount based upon the measured initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed.
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a steady-state control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer, an online analyzer and an empirical model. During a transition, the on-line analyzer measures an initial concentration of a reaction component, the empirical model predicts a required amount based upon the measured initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed.
G05D 11/08 - Controlling ratio of two or more flows of fluid or fluent material with auxiliary non-electric power by sensing concentration of mixture, e.g. by measuring pH-value
G06F 9/455 - EmulationInterpretationSoftware simulation, e.g. virtualisation or emulation of application or operating system execution engines
26.
Pre calcination additives for mixed metal oxide ammoxidation catalysts
A process for preparation of catalysts for the production of acrylonitrile, acetonitrile and hydrogen cyanide comprising contacting at an elevated temperature, propylene, ammonia and oxygen in the vapor phase in the presence of a catalyst, said catalyst comprising a complex of metal oxides wherein a heat-decomposable nitrogen containing compound is added during the process for the preparation of the catalyst.
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
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 45/35 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
A process for preparation of catalysts for the production of acrylonitrile, acetonitrile and hydrogen cyanide comprising contacting at an elevated temperature, propylene, ammonia and oxygen in the vapor phase in the presence of a catalyst, said catalyst comprising a complex of metal oxides wherein a heat-decomposable nitrogen containing compound is added during the process for the preparation of the catalyst.
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
Described herein is a method for removing coke deposits in radiant tubes of an olefin cracking furnace and removing accumulated spalled coke from one or more outlet elbows of the olefin cracking furnace without performing a cold shutdown of the furnace.
Described herein is a method for removing coke deposits in radiant tubes of an olefin cracking furnace and removing accumulated spalled coke from one or more outlet elbows of the olefin cracking furnace without performing a cold shutdown of the furnace.
The present invention relates to a low viscosity lubricant process, product, and composition characterized by low Noack volatility, low pour point, useful low temperature viscometrics, and high viscosity index and more particularly concerns a PAO composition having a kinetic viscosity at 100° C. in the range of about 4 cSt.
C10G 50/02 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation of hydrocarbon oils for lubricating purposes
C10M 107/10 - Hydrocarbon polymersHydrocarbon polymers modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
31.
IMPROVED CATALYST FOR n-BUTANE OXIDATION TO MALEIC ANHYDRIDE
A process for the preparation of a promoted VPO catalyst, wherein the catalyst comprises the mixed oxides of vanadium and phosphorus and wherein the catalyst is promoted with at least one of niobium, cobalt, iron, zinc, molybdenum or titanium, said process comprising the steps of (i) preparing a VPO catalyst comprising vanadyl pyrophosphate as the major component and containing less than 5 wt% of vanadyl phosphate, (ii) contacting the VPO catalyst with a solution comprising a metal source compound of at least one metal selected from the group consisting of niobium, cobalt, iron, zinc, molybdenum or titanium to form a metal impregnated VPO catalyst, and (iii) drying the metal impregnated VPO catalyst to form the promoted VPO catalyst. In one embodiment, a niobium promoted VPO catalyst is prepared.
B01J 27/199 - Vanadium with chromium, molybdenum, tungsten or polonium
B01J 37/02 - Impregnation, coating or precipitation
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
Catalytic compositions are provided that are effective for providing increased acrylonitrile product without a significant decrease in hydrogen cyanide and/or acetonitrile production and provide an overall increase in production of acrylonitrile, hydrogen cyanide and acetonitrile. The catalytic compositions include a complex of metal oxides and include at least about 15% monoclinic (m) scheelite phase plus tetragonal (t) scheelite phase by weight and have a weight ratio of m- phase to m-phase plus t-phase of 0.45 or greater.
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
The invention is an improved apparatus for continuously stirring polymer particles in reactive gas-filled polymerization reactors incorporating contiguous paddle stations on a coaxial drive shaft wherein the drive shaft is driven by a hydraulic motor.
B01J 8/38 - 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 with fluidised bed containing a rotatable device or being subject to rotation
34.
Operation of multi-reactor polyolefin manufacturing process
The invention relates to an improved process for manufacturing an olefin polymer composition, in particular polyethylene, that incorporates two or more reaction zones in an optimized configuration that ease product transitions and allows for improved reactor quality control.
The invention relates to a continuous process to make and isolate methylal by reacting formaldehyde and methanol with an acid catalyst under at least partial formation of methylal and water, to form a mixture M2 comprising formaldehyde, methanol, methylal, and water, separating the said mixture M2 in a distillation column B into three distinct product streams, one being a distillate taken from the column head BH which is rich in methylal, one taken from the column bottom stream BB being almost pure water, and one taken from the side of the column B below the reaction zone which stream is rich in methanol, characterised in that the ratio of the amount of substance of methanol to the amount of substance of formaldehyde in the mixture Ml is at least 3 mol/mol, and to an apparatus to be used with this process.
The present invention relates to a process for the preparation of an agglomerated rubber latex and the use thereof for the manufacture of ABS thermoplastic molding compositions or thermoplastic compositions of the ABS type and polymer compositions containing ABS thermoplastic compositions.
C08C 1/07 - Increasing the size of dispersed rubber particles characterised by the agglomerating agents used
C08F 279/02 - Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group on to polymers of conjugated dienes
C08L 51/04 - Compositions of graft polymers in which the grafted component is obtained by reactions only involving carbon-to-carbon unsaturated bondsCompositions of derivatives of such polymers grafted on to rubbers
An olefin polymerization process comprises gas-phase polymerization of at least one olefin monomer in more than one polymerization zones in one or more polymerization reactors using a high activity catalyst injected in the front end of the reactor to give solid polymer particles. According to the process of the invention, different hydrogen to olefin ratios are controlled and applied to the reactor leading to the production of very different molecular weights and therefore broadening the molecular weight distribution of the polymer produced.
The present disclosure is generally directed to process of gasification of carbonaceous materials to produce synthesis gas or syngas. The present disclosure provides improved methods of gasification comprising adding a molecular oxygen- containing gas and optionally adding water into said gasifier. This disclosure is also directed to process of production of one or more alcohols from said syngas via fermentation or digestion in the presence of at least one microorganism.
The present disclosure is generally directed to process of gasification of carbonaceous materials to produce synthesis gas or syngas. The present disclosure provides improved methods of gasification comprising: adding one or more carbonaceous materials, adding a molecular oxygen-containing gas, adding a methane-containing gas and optionally adding water or steam into said gasifier. This disclosure is also directed to process of production of one or more alcohols from said syngas via fermentation or digestion in the presence of at least one microorganism.
C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
40.
METHODS FOR GASIFICATION OF CARBONACEOUS MATERIALS
The present disclosure is generally directed to process of gasification of carbonaceous materials to produce synthesis gas or syngas. The present disclosure provides improved methods of gasification comprising: adding one or more carbonaceous materials, adding a molecular oxygen-containing gas, adding carbon dioxide gas and optionally adding water into said gasifier. This disclosure is also directed to process of production of one or more alcohols from said syngas via fermentation or digestion in the presence of at least one microorganism.
C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
A catalytic composition useful for the conversion of an olefin selected from the group consisting of propylene, isobutylene or mixtures thereof, to acrylonitrile, methaciylonitrile, and mixtures thereof. The catalytic composition comprises a complex of metal oxides comprising bismuth, molybdenum, iron, cerium and other promoters, wherein the ratio of cerium to iron in the composition is greater than or equal to 0.8 and less than or equal to 5.
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
A process for the preparation of a catalyst wherein the relative ratios of the elements in said catalyst are represented by the following formula: Moi2 Bia Feb Ac Dd Ee Ff Gg Cej, Ox wherein: A is at least one element selected from the group consisting of sodium, potassium, rubidium and cesium; and D is at least one element selected from the group consisting of nickel, cobalt, manganese, zinc, magnesium, calcium, strontium, cadmium and barium; E is at least one element selected from the group consisting of chromium, tungsten, boron, aluminum, gallium, indium, phosphorus, arsenic, antimony, vanadium and tellurium; F is at least one element selected from the group consisting of a rare earth element, titanium, zirconium, hafnium, niobium, tantalum, aluminum, gallium, indium, thallium, silicon, germanium, and lead; G is at least one element selected from the group consisting of silver, gold, ruthenium, rhodium, palladium, osmium, iridium, platinum and mercury; and a, b, c, d, e, f, g, h and n are, respectively, the atomic ratios of bismuth (Bi), iron (Fe), A, D, E, F, cerium (Ce) and oxygen (O), relative to 12 atoms of molybdenum (Mo), wherein a is from 0.05 to 7, b is from 0.1 to 7, c is from 0.01 to 5, d is from 0.1 to 12, e is from 0 to 5, f is from 0 to 5, g is from 0 to 0.2, h is from 0.01 to 5, and n is the number of oxygen atoms required to satisfy the valence requirements of the other component elements present; and wherein the elements in said catalyst are combined together in an aqueous catalyst precursor slurry, the aqueous precursor slurry so obtained is dried to form a catalyst precursor, and the catalyst precursor is calcined to form said catalyst, the process comprising: (i) combining, in an aqueous solution, source compounds of Bi and Ce, and optionally one or more of Na, K, Rb, Cs, Ca, a rare earth element, Pb, W and Y, to form a mixture, (ii) adding a source compound of molybdenum to the mixture to react with the mixture and form a precipitate slurry, and (iii) combining the precipitate slurry with source compounds of the remaining elements and of the remaining molybdenum in the catalyst to form the aqueous catalyst precursor slurry.
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
A catalytic composition useful for the conversion of an olefin selected from the group consisting of propylene, isobutylene or mixtures thereof, to acrylonitrile, methacrylonitrile, and mixtures thereof. The catalytic composition comprising a complex of metal oxides comprising bismuth, molybdenum, iron, cerium and other promoter elements, wherein the X-ray diffraction pattern of the catalytic composition has X-ray diffraction peaks at 2θ angle 28 ± 0.3 degrees and 2θ angle 26.5 ± 0.3 degrees, and wherein the ratio of the intensity of the most intense x-ray diffraction peak within 2θ angle 28 ± 0.3 degrees to the intensity of most intense x-ray diffraction peak within 2θ angle 26.5 ± 0.3 degrees is defined as X/Y, and wherein X/Y is greater than or equal to 0.7.
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
44.
HIGH EFFICIENCY AMMOXIDATION PROCESS AND MIXED METAL OXIDE CATALYSTS
A process and novel catalyst for the production of acrylonitrile, acetonitrile and hydrogen cyanide characterized by the relative yields of acrylonitrile, acetonitrile and hydrogen cyanide produced in the process and by the catalyst, which are defined by the following: α = [(%AN + (3 * %HCN) + (1.5 * %ACN)) ÷ %PC] * 100 wherein: %AN is the Acrylonitrile Yield and %AN ≥ 81, %HCN is the Hydrogen Cyanide Yield, %ACN is the Acetonitrile Yield, %PC is the Propylene Conversion, and α is greater than 100.
B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
B01J 23/887 - Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
The invention relates to an improved process for the manufacture of an olefin polymer composition in which corrosive trace cocatalyst and catalyst residues are removed from the hydrocarbon gas recycle stream prior to compression and re-use in the polymerization zone(s).
The present invention relates to the control of flow of a particulate feed to a reactor, and in particular provides a process for providing a slurry of particulate matter to a reactor, comprising providing a slurry comprising said particulate matter and diluent, and passing said slurry to the inlet of a reactor feed pump from where it is then pumped to the reactor, characterized in that a stream of additional diluent is also passed to the inlet of the reactor feed pump, the reactor feed pump is operated at an essentially constant volumetric flow rate, and the amount of particulate matter in slurry passed into the reactor is adjusted by adjusting the flow.
Process for producing an olefin polymer in a slurry polymerisation process is disclosed, in which the process is operating at a temperature of 90°C to 107°C and utilising a chromium catalyst having an activity of at least 1,000 g polymer / g catalyst/hour on a support having a pore volume of at least 1.3 cm3/g, comprising adding to the polymerisation mixture from 0.1 to l00ppm by weight of an anti-static agent, wherein the resulting polymer has a particle size distribution such that less than 8vol%, preferably less than 5Vol% of the polymer particles have an average diameter of 125μm or less.
The present invention relates to a low viscosity lubricant process, product, and composition characterized by low Noack volatility, low pour point, useful low temperature viscometrics, and high viscosity index and more particularly concerns a PAO composition having a kinetic viscosity at 100° C. in the range of about 4 cSt.
This invention relates to drilling fluids and processes for making drilling fluids, such as for use in environmentally sensitive areas. The environmentally friendly drilling fluid includes a first fluid component having between about 5 weight percent to about 95 weight percent of olefins with a chain length in a range of between about C12 and about C48. The first fluid component includes at least about 50 weight percent trisubstituted olefin functionality. The environmentally friendly drilling fluid includes a second fluid component.
An olefin polymerization process comprises gas-phase polymerization of at least one olefin monomer in more than one polymerization zones in one or more polymerization reactors using a high activity catalyst injected in the front end of the reactor to give solid polymer particles. According to the process of the invention, different hydrogen to olefin ratios are applied to the reactor leading to the production of very different molecular weights and therefore broadening the molecular weight distribution of the polymer produced.
C08L 23/00 - Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bondCompositions of derivatives of such polymers
Copolymers of ethylene and α-olefins having C7 - C12 carbon atoms having : (a) a density (D) in the range 0.900 - 0.940 g/cm3, (b) a melt index MI2 (2.16 kg, 19O°C) in the range of 0.01 - 50 g/10 min, (c) a melt elastic modulus G' (G"= 500 Pa) in the range 20 to 150 Pa, and (d) a tear strength (MD) of ≥ 220 g, a tear strength (TD) of ≥ 470 g, and a Dart Drop Impact (DDI) of ≥1800 g of a blown film having a thickness of 25 μm produced from the copolymer; where MD is referred to the machine direction and TD is the transverse direction of the blown film are suitably prepared in the gas phase by use of a supported metallocene catalyst system. Particularly suitable are copolymers of ethylene and 1-octene and the resultant blown films show improved processsability and exhibit an improved balance of film properties of dart impact and tear strength.
The present invention relates to a process for polymerisation in a gas-phase fluidised bed, and in particular to a process for the introduction of a polymerisation catalyst in solid form into a gas-phase fluidised bed, which process comprises using an injection device having an inner tube of internal cross-sectional area of 10 to 100 mm and an outer tube forming an annulus around said inner tube with a cross-sectional area of 1 to 10 times the internal cross-sectional area of the inner tube, and passing said polymerisation catalyst and a carrier gas through the inner tube and into the gas-phase fluidised bed at a linear velocity of said carrier gas of 4 to 14 m/s and at a mass flow rate of earner gas in the range 10-35 kg/li, and passing a shielding gas through the outer tube and into the gas-phase fluidised bed at a linear velocity of said shielding gas of 1 to 10 times the linear velocity of the carrier gas through the inner tube and at a mass flow rate of the shielding gas in the range 100-500 kg/h, wherein no cooled recycle process gas is provided to the injection device.
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
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 19/26 - Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
The present invention relates to methods useful for the production of polymer powder, and in particular to a method for transitioning from a first process for production of a first polymer to a second process for the production of a second polymer during a polymerisation campaign in a polymerisation apparatus, said polymerisation apparatus comprising a reaction vessel and a degassing vessel, in which the respective first and second processes each comprise: (a) bringing a principal olefin and a comonomer into contact with a catalyst under gas phase polymerisation conditions in the reaction vessel to form the respective first or second polymer, wherein said first and second process utilise the same principal olefin but differ in at least one of (i) the comonomer used and (ii) the reaction temperature at which the polymer is produced, and (b) subsequently contacting the respective first or second polymer with a purge gas in the degassing vessel to remove unreacted monomers, characterised in that the method for transitioning comprises changing the flow rate of purge gas in the degassing vessel from a first rate, X1, used for degassing of the first polymer to a second rate, X2, used for degassing of the second polymer, the second rate being defined relative to the flow rate, Xi, and temperature, Ti, used for an earlier polymer produced during the campaign using the same comonomer as the second process, and the reaction temperature, T2 in the second process, and that a. where T2 is increased relative to Ti, X2 is at least 1% lower than Xi for each 1 °C increase in T2 compared to Ti, b. where T2 is decreased relative to Ti, X2 is at least 1% higher than X1 for each I °C decrease in T2 compared to Ti, and c. where T2 is equal to Ti, X2 is at least equal to X1, preferably equal to Xi.
C08F 10/00 - Homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
C08F 297/08 - Macromolecular compounds obtained by successively polymerising different monomer systems using a catalyst of the ionic or coordination type without deactivating the intermediate polymer using a catalyst of the coordination type polymerising mono-olefins
54.
PROCESS FOR START-UP OF A POLYMERISATION REACTION FLUIDISED BED
The present invention relates to a process for polymerisation, and, in particular, to a process for start-up of a gas phase fluidised bed polymerisation reaction, said reaction comprising polymerisation of one or more monomers using a catalyst in a reactor, and said process comprising:a) providing a start-up bed of particles in the reactor in the presence of the one or more monomers but in the absence of the catalyst, b) introducing catalyst to the reactor to initiate reaction and start-up polymer production, said introduction being designated as time T0, c) at a time Ti, Ti being between 1 and 6 hours after T0, the value of Xi is less than a threshold value, wherein: X1 = Gumulative production in the-time period Tn to T1 (Cumulative catalyst injection the time period T0 to Ti * PiC2=), PiC2= being the ethylene partial pressure in the reactor at the time Ti, d) subsequently stopping the injection of catalyst, e) talcing a corrective action to address the low value of Xi.
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
55.
METHOD FOR CONTROLLING A PROCESS FOR POLYMERISATION OF AN OLEFIN
The present invention relates to a method for controlling a process for polymerisation of an olefin, and in particular to a method for controlling a process for polymerising at least one olefin in a reaction zone, said process comprising in the reaction zone a reaction mixture and polymer particles, the reaction mixture comprising a principal olefin and at least one further reagent, and wherein the process is controlled using the ratio of at least one further reagent to principal olefin in the polymer particles in the reaction zone or in the amorphous phase of said polymer particles.
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
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
56.
APPARATUS AND PROCESS FOR GAS PHASE FLUIDISED BED POLYMERISATION REACTION
The present invention relates to an apparatus and a process for polymerisation, and, in particular, provides an apparatus for gas phase fluidised bed polymerisation of olefins, which apparatus comprises: A) a first section which is an upright cylindrical section having a diameter, D1, and cross- sectional area, A1, and B) a second section, provided vertically above the first section and centred about a common vertical axis to the upright cylindrical first section, the base of the second section having a cylindrical cross-section of diameter D1 and being joined to the top of the first section, and the horizontal cross-sectional area of the second section above its base being greater than the cross-sectional area of the first section, characterised in that: i) D1 is greater than 4.5 metres, and ii) the second section has a maximum horizontal cross- sectional area, A2, which is between 3.2 and 6 times the cross-sectional area, A1, of the first section.
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
C08F 10/00 - Homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
The present invention provides a process for the production of a degassed polymer powder, which process comprises a) feeding i) a principal monomer, and ii) one or more comonomers fed in an amount of at least 5000ppmw relative to the principal monomer feed rate, and iii) optionally one or more added alkanes having 2 to 10 carbon atoms, fed in an amount of at least lOOOppmw relative to the principal monomer feed rate; into a polymerisation reactor wherein the monomer and comonomers react to foπn a polymer comprising residual hydrocarbons comprising one or more hydrocarbons having 3 to 10 carbon atoms, and b) passing the polymer to a degassing step wherein it is contacted with a purge gas to remove at least some of the residual hydrocarbons, characterised in that: 1) the G/P ratio in the degassing step is higher than a minimum G/P ratio, G being the purge gas mass flow rate in the degassing step and P being the polymer throughput of the degassing step, and 2) the purge gas has a concentration of critical hydrocarbon component which is lower than a maximum concentration of said critical hydrocarbon component in the purge gas, the critical hydrocarbon component being the heaviest hydrocarbon component selected from (i), (ii) and (iii) fed in step (a), which minimum G/P ratio and maximum concentration of said critical hydrocarbon component in the purge gas have been calculated based on the absorption coefficient, Kh, for the polymer powder to be degassed.
The present invention comprises a method for preparing a mixed oxide catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutane by ammoxidation in a gaseous phase via methods of contacting any one of the antimony compound, the molybdenum compound, and the vanadium compound with hydrogen peroxide prior to combining with source compounds for the remaining elements in 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 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
59.
METHODS FOR SEQUESTRING CARBON DIOXIDE INTO ALCOHOLS VIA GASIFICATION AND FERMENTATION
The present invention is directed to improvements in gasification for use with synthesis gas fermentation. Further, the present invention is directed to improvements in gasification for the production of alcohols from a gaseous substrate containing at least one reducing gas containing at least one microorganism.
The present invention relates to an extruder for a polymer, and a process for extruding a polymer using said extruder. In particular, the present invention provides an extruder comprising: (i) two or more barrel sections (1a, 1b, 1c) arranged sequentially from: (a) an upstream feed barrel section (1a) to which polymer feedstock to be extruded is fed, the upstream feed barrel section containing two or more screws each having a diameter of X; to (b) a downstream barrel section (1c) from which melted polymer is passed to a die and extruded; and (ii) one or more feed ports for feeding polymer feedstock to be extruded into the extruder at its upstream end, characterised in that the total area of the one or more feed ports through which polymer feedstock is introduced is greater than 4*X, and a process for extrusion of polymer comprising feeding a polymer feedstock to the feed port of such an extruder.
The present invention relates to a polymerisation process and in particular to a process for the copolymerisation of ethylene and an α-olefϊn comonomer having 7 to 10 carbon atoms in a fluidised bed gas phase reactor in the presence of a multi-site Ziegler-Natta polymerisation catalyst characterised in that (i) said process is operated in condensed mode, (ii) the amount of said α-olefin is maintained below that at which substantial condensation in the reactor occurs and (iii) at least one of the following apply: a) the catalyst has an uptake rate of 1-octene of at least 700; b) the polymerisation is performed in the presence of an activity promoter.
The present invention relates to methods for sustaining microorganism culture in a syngas fermentation reactor in decreased concentration or absence of various substrates comprising: adding carbon dioxide and optionally alcohol; maintaining free acetic acid concentrations; and performing the above mentioned steps within specified time.
C12N 1/00 - Microorganisms, e.g. protozoaCompositions thereofProcesses of propagating, maintaining or preserving microorganisms or compositions thereofProcesses of preparing or isolating a composition containing a microorganismCulture media therefor
A process for the ammoxidation of a saturated or unsaturated hydrocarbon to form an unsaturated nitrile, the process including the steps of contacting the hydrocarbon with ammonia, an oxygen-containing gas, and steam, in the presence of a mixed oxide catalyst.
The present invention relates to a low viscosity lubricant process, product, and composition characterized by low Noack volatility, low pour point, useful low temperature viscometrics, and high viscosity index and more particularly concerns a PAO composition having a kinetic viscosity at 100°C in the range of about 4 cSt.
C10M 107/10 - Hydrocarbon polymersHydrocarbon polymers modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
C10M 143/08 - Lubricating composition characterised by the additive being a macromolecular hydrocarbon or such hydrocarbon modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
C10G 50/02 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation of hydrocarbon oils for lubricating purposes
The present invention relates to a low viscosity lubricant process, product, and composition characterized by low Noack volatility, low pour point, useful low temperature viscometrics, and high viscosity index and more particularly concerns a PAO composition having a kinetic viscosity at 100.degree.C in the range of about 4 cSt.
C10G 50/02 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation of hydrocarbon oils for lubricating purposes
C10M 107/10 - Hydrocarbon polymersHydrocarbon polymers modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
C10M 143/08 - Lubricating composition characterised by the additive being a macromolecular hydrocarbon or such hydrocarbon modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
66.
METHOD OF MAKING MIXED METAL OXIDE CATALYSTS FOR AMMOXIDATION AND/OR OXIDATION OF LOWER ALKANE HYDROCARBONS
The present invention comprises a method for preparing a mixed oxide catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutene by ammoxidation in a gaseous phase via methods of heating or calcining precursor solid mixture to obtain mixed metal oxide catalyst compositions that exhibit catalytic activity.
The present invention relates to a process for polymerisation of ethylene, in particular a process which comprises using a catalyst system comprising comprising a catalyst system comprising: i) a solid catalyst comprising Ti, Mg and halogen, ii) a first activator which is at least one trialkyl aluminium compound of the formula AlR3, where each R is independently a C2 to C20 alkyl radical, and iii) a second activator which is at least one alkylaluminium chloride of the formula AlR'2C1, where each R' is independently a C2 to C20 alkyl radical, characterised in that the second activator is introduced directly in the polymerisation reactor, without precontact with the solid catalyst, continuously or semi-continuously and at a maximum rate of introduction at any time corresponding to less than 10 ppm by weight of chlorine relative to the rate of polyethylene production.
A process for the ammoxidation or oxidation of a saturated or unsaturated or mixture of saturated and unsaturated hydrocarbon, the process including the steps of combining a performance modifier, a fresh mixed oxide catalyst, or a used mixed oxide catalyst and a fresh and used mixed oxide catalyst to form a catalyst mixture, and contacting the hydrocarbon with an oxygen-containing gas, or an oxygen-containing gas and ammonia, in the presence of the catalyst mixture. The performance modifier may include a compound selected from the group consisting of aluminum compounds, antimony compounds, arsenic compounds, boron compounds, cerium compounds, germanium compounds, lithium compounds, molybdenum compounds, neodymium compounds, niobium compounds, phosphorus compounds, selenium compounds, tantalum compounds, tellurium compounds, titanium compounds, tungsten compounds, vanadium compounds, zirconium compounds and mixtures thereof.
C07C 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
Disclosed is an apparatus for mixing of a first gas and a second gas, comprising: i) a linear first tube (1) for supply of the first gas, said first tube comprising an inlet (2) for the first gas at an upstream end and tapering to form a nozzle (3) at a downstream end, and ii) a linear second tube (4) for supply of the second gas, said second tube comprising an inlet (5) for the second gas at an upstream end, a first portion (6) which forms an annulus around the outer surface of the first tube upstream of the nozzle, and a second portion (7) which forms a sheath around the nozzle (3) of the first tube (1) and which forms an area of expanded cross-section (8) compared to the annulus.
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
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 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
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01F 5/00 - Flow mixers; Mixers for falling materials, e.g. solid particles
The present invention relates to a process for the production of one or more C2+ alcohols. In particular, the present invention relates to a process for the production of C2+ alcohols from a methane-containing feedstock, which process comprises: a. Passing said methane- containing feedstock and carbon dioxide to a non- oxidative reforming process to produce a first product stream comprising CO, H2 and CO2, optionally in the presence of steam, but with the proviso that where steam is present in the feed to the reforming process the steam and CO2 are present in a molar ratio of less than 5: 1, b. Passing the first product stream comprising CO, H2 and CO2 to a bacterial fermentation step wherein it is converted to produce a second product stream comprising one or more C2+ alcohols in the liquid phase and a gaseous third product stream comprising CO, H2 and CO2, the fermentation step being operated to provide a conversion of CO of at least 60%, wherein CO, H2 and CO2 are recycled from the gaseous third product stream to the reforming process of step (a).
A catalyst composition comprising molybdenum, vanadium, and antimony, and at least one other element selected from the group consisting of praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, and lutetium. Such catalyst compositions are effective for the gas-phase conversion of propane to acrylonitrile and isobutane to methacrylonitrile (via ammoxidation).
B01J 37/10 - Heat treatment in the presence of water, e.g. steam
C07C 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
72.
PROCESS FOR DEVOLATILIZATION OF A POLYMER OF AN AROMATIC ALKYLENE
The present invention relates to a process for devolatilization of a polymer of an aromatic alkylene, such as styrene, and in particular, to an improved process using water as a stripping agent (i) in which the total amount of water to be disposed of can be reduced, (ii) which allows at least a portion of the water to be recycled as stripping agent, reducing make-up requirements for the stripping agent, and (iii) which allows at least a portion of the aromatic alkylene monomer in the water to be recycled to the polymerisation process (via the devolatilization steps) rather than disposed of.
The present invention relates to a process for the dehydration of one or more alcohols, which process comprises contacting one or more alcohols in the presence of one or more ethers with a supported heteropolyacid catalyst, characterised in that: (i) the heteropolyacid is tungstosilicic acid in the form of the free acid and supported on a silica support, (ii) said supported heteropolyacid catalyst has a heteropolyacid loading of from 0.5 to 0.9 mg/m2 of catalyst support surface area, and (iii) that said process comprises passing the one or more alcohols and one or more ethers in the vapour phase over a bed of the supported heteropolyacid catalyst at a temperature between 200°C and 280°C.
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
Catalytic compositions and processes are disclosed for economical conversions of lower alkane hydrocarbons. Broadly, the present invention discloses solid promoter treated compositions containing mixed metal oxides that exhibit catalytic activity for ammoxidation of lower alkane hydrocarbons to produce an unsaturated nitrile in high yield. Generally, these solid oxide compositions comprise, as component elements, molybdenum (Mo), vanadium (V) niobium (Nb) and at least one active element selected from the group consisting of the elements having the ability to form positive ions. Mixed metal oxide catalytic compositions advantageously are formed process steps comprising impregnation of a base catalyst with an aqueous medium comprising sources of one or more promoter element drying the resulting material; and thereafter subjecting the dried material to heat treatment, under a gaseous atmosphere that is substantially free of dioxygen, at elevated temperatures of at least 400° C. Also described are methods for forming the improved catalysts having the desired crystalline structure and ammoxidation processes for conversion of lower alkanes.
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
C07C 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
75.
MIXED METAL OXIDE CATALYSTS AND CATALYTIC CONVERSIONS OF LOWER ALKANE HYDROCARBONS
Catalytic compositions and processes are disclosed for economical conversions of lower alkane hydrocarbons. Broadly, the present invention discloses solid compositions containing mixed metal oxides that exhibit catalytic activity for ammoxidation of lower alkane hydrocarbons to produce an unsaturated nitrile in high yield. Generally, these solid oxide compositions comprise, as component elements, molybdenum (Mo), vanadium (V) niobium (Nb) and at least one active element selected from the group consisting of the elements having the ability to form positive ions. Mixed metal oxide catalytic compositions advantageously comprise one or more crystalline phases at least one of which phases has pre-determined unit cell volume and aspect ratio. Also described are methods for forming the improved catalysts having the desired crystalline structure and ammoxidation processes for conversion of lower alkanes.
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
C07C 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
An olefin polymerization process comprises gas-phase polymerization of at least one olefin monomer in more than one polymerization zones using a high activity Ziegler-Natta catalyst system comprising a solid, magnesium- supported, titanium-containing component and an aluminum alkyl component comprising introducing the titanium-containing component and an aluminum alkyl component into the first polymerization zone and then introducing additional aluminum alkyl component into a subsequent polymerization zone without added titanium-containing component.
A process for the ammoxidation of a saturated or unsaturated or mixture of saturated and unsaturated hydrocarbon to produce an unsaturated nitrile, said process comprising contacting the saturated or unsaturated or mixture of saturated and unsaturated hydrocarbon with ammonia and an oxygen-containing gas in the presence of a catalyst composition comprising molybdenum, vanadium, antimony, niobium, tellurium, optionally at least one element select from the group consisting of titanium, tin, germanium, zirconium, hafnium, and optionally at least one lanthanide selected from the group consisting of lanthanum, cerium, praseodymium, neodymium, samarium, europium, gadolinium, dysprosium, holmium, erbium, thulium, ytterbium and lutetium. Such catalysts are characterized by very low levels of tellurium in the composition. Such catalyst compositions are effective for the gas-phase conversion of propane to acrylonitrile and isobutane to methacrylonitrile (via ammoxidation).
B01J 27/057 - Selenium or telluriumCompounds thereof
C07C 253/24 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
C07C 253/26 - Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
Novel copolymers of ethylene and alpha-olefins are provided having (a) a density in the range 0.900 - 0.940 g/cm3, (b) a melt index MI2 (2.16 kg, 190°C) in the range of 0.01 - 50 g/10 min, (c) a molecular weight distribution (Mw/Mn) in the range 3.5 to 4.5, (d) a melt elastic modulus G' (G'= 500 Pa) in the range 40 to 150 Pa, and (e) a melt index MI2 (2.16 kg, 190°C), Dow Rheology Index (DRI) and melt elastic modulus G' (G'= 500 Pa) satisfying the equations of [DRI/MI2] ᡶ 0 and [DRI/MI2] ឬ 0.0225G' - 0.745 The novel copolymers have improved processability and are particularly suitable for the preparation of films having improved mechanical and optical properties. The novel copolymers are suitably prepared in the gas phase in the presence of a supported raetallocene catalyst system.
A method for the preparation of copolymers of ethylene and α-olefins having a fraction (%) of the molecular weight component of ᡶ 1,000,000 of less than 6 % comprises polymerising ethylene and an α-olefin in the presence of a supported polymerisation catalyst system comprising (a) a transition metal compound (b) a porous support material, and (c) an activator characterized in that the support material has been (i) dried at a temperature in the range 0°C to 195°C in an inert atmosphere, and (ii) treated with an organometallic compound. The resultant supported catalyst systems show improved productivity and allow for control of the resultant polymer properties. Particularly preferred supported catalyst systems are those comprising metallocene complexes.
The present invention relates to a process for producing a polystyrene, in particular a process for producing a high impact polystyrene, which process comprises: 1) introducing into a pre-inversion reactor a styrene monomer, a rubber polymer and a grafting promoter, and polymerising the styrene monomer to form a polystyrene, said polymerisation being performed to a conversion of between 70 and 100% of the phase inversion start point of the styrene/polystyrene/rubber polymer mixture formed, 2) splitting the formed styrene/polystyrene/rubber polymer mixture to produce a first stream comprising 70 to 95% by weight of the formed mixture and a second stream comprising the balance of the formed mixture, 3) introducing the first stream into a second reactor wherein further styrene polymerisation is performed to cause phase inversion the first stream, 4) mixing the phase inverted first stream from step (3) with the second stream from step (2) at a shear rate of 5 to 30 s -1 in a static in-line mixer to cause a second phase inversion and produce a high impact polystyrene with a bimodal distribution of rubber particles.
C08F 279/02 - Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group on to polymers of conjugated dienes
Compositions comprising at least one C4-Q30 olefin or oxidation product thereof and kerosene or an aromatic solvent are particularly effective for use in removing asphaltene and asph.altene-containing organic deposits and in preventing or reducing the precipitation and deposition of asphaltenes from hydrocarbon fluids. When added to heavy oils comprising asphaltenes, alone or in combination with dispersants and further inhibitors, the invented compositions lower viscosity and pour point, and aid in preventing asphaltene precipitation during transport and in combustion...
E21B 37/06 - Methods or apparatus for cleaning boreholes or wells using chemical means for preventing or limiting the deposition of paraffins or like substances
E21B 37/00 - Methods or apparatus for cleaning boreholes or wells
82.
APPARATUS AND PROCESS FOR THE PRODUCTION OF OLEFINS
The present invention relates to an apparatus for reacting a first gaseous reactant stream with a second gaseous reactant stream to form a gaseous product stream, wherein the apparatus comprises at least one first supply means for the first gaseous reactant stream, at least one second supply means for the second gaseous reactant stream, a catalyst zone, a product quench zone and a waste heat boiler, wherein the product quench zone is positioned downstream of the catalyst zone and comprises a plurality of quench tubes, and wherein the waste heat boiler is positioned downstream of the exits of the quench tubes and comprises a plurality of boiler tubes, the waste heat boiler having a surface on which gas exiting the exits of the quench tubes impinges.
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
C10G 11/22 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours produced by partial combustion of the material to be cracked
F28F 27/02 - Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
83.
METHOD FOR STARTING OFAN AUTOTHERMAL CRACKING REACTION
The present invention provides a method for starting an autothermal cracking reaction for the production of one or more olefins, said autothermal cracking reaction comprising contacting a paraffinic hydrocarbon and oxygen with a catalyst at an elevated pressure, P1, which start-up method comprises: a) establishing a flow of a purge gas immediately downstream of the catalyst, b) contacting a pre-heated feed mixture comprising hydrogen, oxygen and a diluent with the catalyst at an elevated pressure, P2, which is less than P1, wherein the hydrogen to oxygen molar ratio is at least 0.5:1 and wherein the total feed mixture comprises less than 25wt% oxygen and at least 50wt% diluent, c) increasing the oxygen concentration in the feed mixture until a catalyst exit temperature of at least 7000C is reached, and d) increasing the pressure to the desired reaction pressure P1.
C07C 4/02 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
A supported catalyst for olefin polymerization comprises a selected ionic activator, a selected organometallic catalyst and a support material. The selected activator must contain an active hydrogen moeity. The organometallic catalyst is characterized by having a phosphinimine ligand and a substituted cyclopentadienyl ligand (which contains from 7 to 30 carbon atoms). The supported catalyst exhibits excellent activity in gas phase olefin polymerizations and may be used under substantially 'non-fouling' polymerization conditions.
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 10/00 - Homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
The use of high activity 'Single Site' polymerization catalysts often causes the fouling of polymerization reactors. The problem is particularly acute with gas phase polymerizations. While not wishing to be bound by theory it is believed that the fouling is initiated by the buildup of static charges in the reactor. The use of anti-static agents mitigates this problem, but typical antistatic agents contain polar species, which can deactivate the polymerization catalyst. We have now discovered that the use of a porous metal oxide support allows large levels of a selected antistatic agent to be used in a manner that reduces static/fouling problems in highly active polymerization catalysts.
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
The present invention relates to a process for the treatment of a product stream, more specifically of a product stream from an autothermal cracking process, said product stream comprising one or more olefins, hydrogen, carbon monoxide, carbon dioxide and one or more oxygenates, said process comprising contacting the product stream with at least one compound selected from those represented by formulas: (1) H2N-OR1, and (2) H2N-NR2R3, where: R1, R2 and R3 may each be independently selected from H and carbon containing substituents.
C10G 70/04 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes
C10G 11/22 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours produced by partial combustion of the material to be cracked
C10G 27/04 - Refining of hydrocarbon oils, in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
C07C 275/64 - Derivatives of urea, i.e. compounds containing any of the groups the nitrogen atoms not being part of nitro or nitroso groups having nitrogen atoms of urea groups singly-bound to oxygen atoms
C07C 281/06 - Compounds containing any of the groups e.g. semicarbazides
B01D 53/02 - 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 adsorption, e.g. preparative gas chromatography
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 53/72 - Organic compounds not provided for in groups , e.g. hydrocarbons
The present invention relates to a continuous method for treating a crude phenol stream comprising methylbenzofuran and hydroxyacetone by passing the crude phenol stream through at least two reactors connected in series the reactors containing an acidic ion exchange resin, whereby the temperature in successive reactors decreases in flow direction of the phenol stream so that the temperature in the first reactor in flow direction of the phenol stream is between 100° C. and 200° C. and the temperature in the last reactor in flow direction of the phenol stream is between 50° C. and 90° C. without a thermal separation step between any of two successive reactors and to the use of this method in a process for making phenol.
A method for the preparation of a polymer film containing 300 - 600 gels/m2 of size in the range 100 - 2000 騜m as measured by an optical control system (OCS) as hereinbefore described, said film being derived from an ethylene -&agr;-olefm copolymer is characterised in that said copolymer is prepared in a particle forming polymerisation process in the presence of a single site catalyst system. The preferred single site catalyst system comprises a metallocene and the preferred polymerisation process is a gas phase process. The invention is particularly directed to blown films.
Transition metal catalysts comprise (a) a source of a Group 3 to 10 transition metal, (b) a ligand having the formula: R1R2X-Y-XR3R4 wherein X is phosphorus, arsenic or antimony, Y is a bridging group having the formula: Z-(A)-D-Rm wherein Z is the moiety linking the X groups, A is a linear or cyclic hydrocarbyl, substituted hydrocarbyl, heterohydrocarbyl or substituted heterohydrocarbyl linking group wherein the number of atoms directly linking Z to D is 1, 2 or 3, D is N, P, As, O, S or Se, R is hydrogen, alkyl, hydrocarbyl, substituted hydrocarbyl, heteroalkyl, heterohydrocarbyl or substituted heterohydrocarbyl, and m is 1 or 2, R1,R2,R3, and R4 are the same or different and represent hydrocarbyl or functionalized hydrocarbyl moieties with the proviso that if D is nitrogen, R is not a cyclic ether, and optionally an activator. The transition metal catalysts are suitable for the selective trimerisation or tetramerisation of olefins in particular ethylene.
The present invention relates to a quench tube, having a length ( L), a diameter (D) and at least one guenchant inlet per tube which inlet passes guenchant into the tube from the side of said tube, and wherein, D is between 0.04 and 0.10 m and L/D is at least 5. The present invention also relates to an apparatus with one or more of said quench tubes wherein said apparatus comprises a catalyst zone which may have a cross sectional area of at least 0, 01m2. In processes using said tubes and/or said apparatuses a first gaseous reactant stream and a second reactant stream are contacted with a catalyst to produce a product stream which is quenched on exiting the catalyst. A process for producing olefins by autothermal cracking is also claimed.
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 4/00 - Feed devicesFeed or outlet control devices
B01J 7/02 - Apparatus for generating gases by wet methods
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
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
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 9/14 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
91.
PROCESS FOR CONTACTING A HYDROCARBON AND AN OXYGEN- CONTAINING GAS WITH A CATALYST BED
The present invention relates to a process for contacting a hydrocarbon and an oxygen-containing gas with a catalyst bed in a reactor at a space velocity of at least 10,000 h-1, said process being characterised in that a) the reactor has a polygonal internal cross-section at least in the section where the catalyst bed is held, b) the catalyst bed is made up of 2 or more layers of catalyst in the form of tiles of polygonal shape, said tiles having at least 4 sides, c) each layer of catalyst comprises at least 4 tiles which tessellate together to form said layer, and d) the edges where 2 tiles meet in one layer do not align with the edges where 2 tiles meet in an adjacent layer.
A catalyst system suitable for the polymerisation of olefins, said system comprising (a) a transition metal compound or lanthanide metal compound (b) a cocatalyst and (c) at least one porous support material characterised in that the porous support material has been pretreated with a halogen- containing organometallic compound, in particularly with a fluorine-containing organometallic compound. The catalyst system is particularly suitable for the preparation of polymers having broad molecular weight distributions from the polymerisation of olefins in the presence of a single site catalyst.
Processes using multiple expansion turbines for efficient recovery of power from a plurality of very high pressure streams of superheated vapor are disclosed. Beneficially, processes of the invention use at least two classes of expansion turbines. Processes according to this invention are particularly useful for recovery of power from very high pressure streams of superheated steam in an olefins manufacturing process. Such streams are typically produced by thermal cracking of suitable petroleum derived feed stocks, and the olefins being produced and purified are typically ethylene and/or propylene.
F01K 7/02 - Steam engine plants characterised by the use of specific types of enginePlants or engines characterised by their use of special steam systems, cycles or processesControl means specially adapted for such systems, cycles or processesUse of withdrawn or exhaust steam for feed-water heating the engines being of multiple-expansion type
F01K 7/22 - Steam engine plants characterised by the use of specific types of enginePlants or engines characterised by their use of special steam systems, cycles or processesControl means specially adapted for such systems, cycles or processesUse of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type the turbines having inter-stage steam heating
F22B 31/04 - Heat supply by installation of two or more combustion apparatus, e.g. of separate combustion apparatus for the boiler and the superheater respectively
The present invention relates to a process for the treatment of the product stream from an autothermal cracking reaction, said product stream comprising one or more olefins, hydrogen, carbon monoxide, carbon dioxide, one or more aromatic compounds and one or more organic acid oxygenates, said process comprising reacting the organic acid oxygenates with an alkali at a temperature of at least 70°C.
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
B01D 53/72 - Organic compounds not provided for in groups , e.g. hydrocarbons
The present invention relates to a process for the removal of oxygenates from a gaseous stream also comprising carbon dioxide, said process comprising: a) providing a gaseous stream comprising one or more mono-olefᗚns, one or more oxygenates and carbon dioxide, b) treating the gaseous stream to reduce the oxygenate content thereof, wherein said treating comprises either : (i) contacting the gaseous stream with a bisulphite solution, to reduce the oxygenate content therein, and subsequently treating the gaseous stream to remove any sulphur dioxide in said stream and produce a gaseous product stream comprising one or more mono-olefms and carbon dioxide with a reduced oxygenate content, (ii) contacting the gaseous stream with a first aqueous stream to produce a gaseous product stream comprising one or more mono-olefms and carbon dioxide with a reduced oxygenate content, and a second aqueous stream with increased oxygenate content, and subsequently contacting the second aqueous stream with an aqueous bisulphite solution, or (iii) contacting the gaseous stream with a first aqueous stream to produce a gaseous product stream comprising one or more mono-olefᗚns and carbon dioxide with a reduced oxygenate content, and a second aqueous stream with increased oxygenate content, and subsequently contacting the second aqueous stream with an aqueous sulphite solution in the presence of an aqueous base, and c) subsequently treating the gaseous product stream comprising one or more mono- olefins and carbon dioxide with a reduced oxygenate content to remove the carbon dioxide therein.
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
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 53/72 - Organic compounds not provided for in groups , e.g. hydrocarbons
The present invention relates to a catalyst holder, and in particular to a catalyst holder for a catalyst for the reaction of a hydrocarbon with oxygen, wherein the catalyst holder comprises: (i) a first part which is adapted to provide a sealing engagement between the catalyst holder and a source of reactants, (ii) a second part, downstream of the first part as defined with respect to a flow of reactants, and (iii) a third part, downstream of the first and second parts as defined with respect to a flow of reactants and which is adapted to house the catalyst bed, the catalyst holder having a wall which defines the internal cross-sections of the first, second and third parts and extends from the first part to the third part, and wherein the wall of the second part has an average thickness narrower than the average wall thickness of the third part.
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
97.
PROCESS FOR THE REMOVAL OF OXYGENATES FROM A GASEOUS STREAM
The present invention relates to a process for the removal of oxygenates from a gaseous stream also comprising carbon dioxide, said process comprising: a) providing a first gaseous stream comprising one or more mono-olefin(s), at least 100ppm (by weight) of one or more oxygenates and at least 0.1 wt% carbon dioxide, and b) treating the first gaseous stream to produce a second gaseous stream comprising one or more mono-olefin(s) and at least 01 wt% carbon dioxide with reduced oxygenate content, wherein said treating comprises contacting the first gaseous stream with a first aqueous stream and with a first liquid hydrocarbon stream, and c) subsequently treating the second gaseous stream to remove the carbon dioxide therein.
C10G 70/06 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes by gas-liquid contact
B01D 53/72 - Organic compounds not provided for in groups , e.g. hydrocarbons
A complex compound comprising the skeletal unit (A), wherein the ring C(R1) -A1-A2-(A3)X-C(R2) -C- has delocalised unsaturation and is optionally substituted via one or more of A1, A2 and A3 by hydrogen, alkyl, aryl, halogen, or heterocyclic groups containing at least one N, S or O in a carbon ring; A1, A2 and A3 are carbon, nitrogen and, oxygen, R1 and R2 are hydrocarbyl, chlorine, bromine and iodine at least one of R1 and R2 being chlorine, bromine or iodine; x is zero or 1, 0 is oxygen, E is nitrogen, phosphorus or arsenic, Q is a divalent bridging group comprising one or more Group 14 atoms; X is a monovalent atom or group covalently or ionically bonded to M; L is a mono- or bidentate molecule datively bound to M, y satisfies the valency of M and z is from 0 to 5. The complex can be used to polymerise olefins optionally with organo-Al or - B compounds as activator.
The productivity of a catalyst in a gas phase polymerization of olefins (e.g. grams of polymer per gram of catalyst) may be increased by including in the gas phase from 1 to 20 weight % of an inert non-polymerizable hydrocarbon. The hydrocarbon may be in gaseous form but preferably is in liquid form.
C08F 4/22 - Metallic compounds other than hydrides and other than metallo-organic compoundsBoron halide or aluminium halide complexes with organic compounds containing oxygen of chromium, molybdenum, or tungsten
C08F 4/64 - Titanium, zirconium, hafnium, or compounds thereof
100.
RECOVERY OF CARBON MONOXIDE AND HYDROGEN FROM HYDROCARBON STREAMS
A process is described for the recovery of CO and optionally hydrogen from a stream containing CO, H2, methane, and hydrocarbons heavier than methane. The process is characterized by a two-stage removal (3, 6) of C2+hydrocarbons from the feed. In a first step the feed gas (1) is separated (3) into a first C2+depleted stream (5) and a first C2+enriched stream (4). The first C2-enriched stream (4) is rectified (6) to produce a second C2+depleted stream. The first and second C2+depleted streams (5, 9) are fed to a cryogenic system (10) for recovery of CO (12) and optionally hydrogen (11).
F25J 3/02 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
