An apparatus for use in heterogeneous catalytic reactions comprising a column reactor comprising a plurality of trays mounted one above another, each adapted to hold a predetermined liquid volume and a charge of particles of a solid catalyst thereon; means for introducing a liquid phase reactant above the uppermost tray; means for introducing a vapor phase reactant below the lowermost tray; means for removing a liquid phase post-reaction stream from below the lowermost tray; means for removing a vapor phase post-reaction stream from above the uppermost tray; vapor upcomer means associated with each tray adapted to allow vapor to enter that tray from below; undertow means associated with each tray adapted to remove liquid from that tray and the column reactor before being introduced into the column reactor at a lower tray; means for temporarily directing said liquid removed from a tray to bypass at least one lower tray and be reintroduced to the column reactor at a tray located below said at least one bypassed tray; means for removing the liquid and catalyst from said at least one bypassed tray: and means for replacing a liquid and catalyst inventory on said at least one bypassed tray.
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
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 8/20 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
C07C 67/00 - Preparation of carboxylic acid esters
C07C 67/08 - Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
C07C 67/48 - SeparationPurificationStabilisationUse of additives
C07C 67/52 - SeparationPurificationStabilisationUse of additives by change in the physical state, e.g. crystallisation
C07C 67/54 - SeparationPurificationStabilisationUse of additives by change in the physical state, e.g. crystallisation by distillation
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
2.
Process for improving the hydrogen content of a synthesis gas
A process for improving the hydrogen content of a synthesis gas stream to a synthesis loop, comprising the steps of: (a) removing a purge stream comprising hydrogen and hydrocarbons from a synthesis loop; (b) separating hydrogen from the purge stream; (c) passing the purge stream to a reformer and reacting with steam and oxygen to produce a stream comprising hydrogen and carbon monoxide; (d) subjecting the reformed reaction product stream to a shift reaction to produce a stream comprising carbon dioxide and hydrogen; (e) subjecting the product stream from the shift reaction to separation to separate hydrogen from carbon dioxide; (f) supplying the separated hydrogen to the synthesis loop; and (g) removing the carbon dioxide.
C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10K 1/32 - Purifying combustible gases containing carbon monoxide with selectively absorptive solids, e.g. active carbon
C10K 3/04 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content
An apparatus for use in heterogeneous catalytic reactions comprising a column reactor comprising a plurality of trays mounted one above another, each adapted to hold a predetermined liquid volume and a charge of particles of a solid catalyst thereon; means for introducing a liquid phase reactant above the uppermost tray; means for introducing a vapour phase reactant below the lowermost tray; means for removing a liquid phase post-reaction stream from below the lowermost tray; means for removing a vapour phase post-reaction stream from above the uppermost tray; vapour upcomer means associated with each tray adapted to allow vapour to enter that tray from below; underflow means associated with each tray adapted to remove liquid from that tray and the column reactor before being introduced into the column reactor at a lower tray; means for temporarily directing said liquid removed from a tray to bypass at least one lower tray and be reintroduced to the column reactor at a tray located below said at least one bypassed tray; means for removing the liquid and catalyst from said at least one bypassed tray: and means for replacing a liquid and catalyst inventory on said at least one bypassed tray.
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
C07C 67/08 - Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
B01D 3/16 - Fractionating columns in which vapour bubbles through liquid
A process for the conversion of synthesis gas to higher hydrocarbons by contacting a gaseous stream comprising synthesis gas with a particulate Fischer-Tropsch catalyst, said process being carried out in a tubular reactor having an inlet and an outlet, said outlet being located downstream of the inlet, said reactor comprising one or more tubes having located therein one or more carriers for said particulate catalyst and cooling medium in contact with said tubes; wherein said catalyst carrier comprises: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt; said process comprising: (a) introducing the gaseous reactants through the inlet; (b) passing said reactants downwardly through said at least one tube to the upper surface of the, or the first catalyst carrier where they pass into the passage defined by the inner perforated wall of the container before passing radially through the catalyst bed towards the perforated outer wall; (c) allowing reaction to occur as the synthesis gas contacts the catalyst; (d) passing unreacted reactant and product out of the container though the perforated outer wall and then upwardly between the inner surface of the skirt and the outer wall of the annular container until they reach the seal where they are directed over the end of the skirt and caused to flow downwardly between the outer surface of the skirt and the inner surface of the reactor tube where heat transfer takes place; (e) repeating steps (b) to (d) at any subsequent catalyst carrier; and (f) removing product from the outlet.
B01J 19/24 - Stationary reactors without moving elements inside
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
A process for the conversion of synthesis gas to methanol by contacting a gaseous stream comprising synthesis gas with a particulate catalyst, said process being carried out in a tubular reactor having an inlet and an outlet, said outlet being located downstream of the inlet, said reactor comprising one or more tubes having located therein one or more carriers for said particulate catalyst and cooling medium in contact with said tubes; wherein said catalyst carrier comprises: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wail, a top surface closing the annular- container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wall of the annular container from a position at or near- the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt; said process comprising: (a) introducing the gaseous reactants through the inlet; (b) passing said reactants downwardly through said at least one tube to the upper surface of the, or the first catalyst carrier where they pass into the passage defined by the inner perforated wall of the container before passing radially through the catalyst bed towards the perforated outer wall; (c) allowing reaction to occur as the synthesis gas contacts the catalyst; (d) passing unreacted reactant and product out of the container though the perforated outer wail and then upwardly between the inner surface of the skirt and the outer wall of the annular container until they reach the seal where they are directed over the end of the skirt and caused to flow downwardly between the outer surface of the skirt and the inner surface of the reactor tube where heat transfer takes place; (e) repeating steps (b) to (d) at any subsequent catalyst carrier; and (f) removing product from the outlet.
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
B01J 19/24 - Stationary reactors without moving elements inside
C07C 29/152 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
A process for the production of anhydrides by contacting a gaseous feed stream with a particulate catalyst, said process being carried out in a tubular reactor having an inlet and an outlet, said outlet being located downstream of the inlet, said reactor comprising one or more tubes having located therein one or more carriers for said particulate catalyst and cooling medium in contact with said tubes; wherein said catalyst carrier comprises: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wail of the annular container from a position at or near the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt; said process comprising: (a) introducing the gaseous reactants through the inlet; (b) passing said reactants downwardly through said at least one tube to the upper surface of the, or the first catalyst carrier where they pass into the passage defined by the inner perforated wall of the container before passing radially through the catalyst bed towards the perforated outer wall; (c) allowing reaction to occur as the gas contacts the catalyst; (d) passing unreacted reactant and product out of the container though the perforated outer wall and then upwardly between the inner surface of the skirt and the outer wall of the annular container until they reach the seal where they are directed over the end of the skirt and caused to flow downwardly between the outer surface of the skirt and the inner surface of the reactor tube where heat transfer takes place; (e) repeating steps (b) to (d) at any subsequent catalyst carrier; and (f) removing product from the outlet.
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
B01J 19/24 - Stationary reactors without moving elements inside
C07C 51/31 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation of cyclic compounds with ring-splitting
A monolith catalyst carrier for insertion in a tube of a tubular reactor comprising: a container for holding a monolith catalyst in use, said container having a bottom surface closing the container and a skirt extending upwardly from the bottom surface of said container to a position below the location of a seal and spaced therefrom, said skirt being positioned such that there a space between an outer surface of the monolith catalyst and the skirt; and a seal located at or near a top surface of the monolith catalyst and extending from the monolith catalyst by a distance which extends beyond an outer surface of the skirt.
A liquid/gas reactor comprising: (a) a bulk catalyst bed and means for supplying fresh feed and recycled at least partially converted liquid product stream to said bulk catalyst bed; (b) means for collecting an at least partially converted liquid product stream from said bulk catalyst bed and recyling at least a portion thereof to step (a); (c) a minor catalyst bed extending substantially vertically through the bulk catalyst bed and means for supplying recycled at least partially converted product stream only to said minor catalyst bed; and (d) a separating wall between said bulk and said minor catalyst bed.
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
C10G 45/32 - Selective hydrogenation of the diolefin or acetylene compounds
C10G 49/00 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or
C07C 7/167 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
9.
PROCESS AND ROTARY PRESSURE FILTRATION APPARATUS FOR SLURRY SEPARATION OF AROMATIC CARBOXYLIC ACIDS
A process for removing aromatic carboxylic acid from a slurry thereof in solvent comprising the steps of: (a) splitting the slurry into sub streams and supplying each of said sub streams to a respective rotary pressure filters such that said sub stream pass through the filters in parallel; and (b) passing gas through the rotary pressure filters in series in an open-loop arrangement.
C07C 51/47 - SeparationPurificationStabilisationUse of additives by solid-liquid treatmentSeparationPurificationStabilisationUse of additives by chemisorption
B01D 33/37 - Filters with filtering elements which move during the filtering operation with multiple filtering elements characterised by their mutual disposition in parallel connection
B01D 33/66 - Handling the filter cake in the filter for purposes other than for regenerating for drying by gases or by heating
10.
PROCESS FOR IMPROVING THE HYDROGEN CONTENT OF A SYNTHESIS GAS
A process for improving the hydrogen content of a synthesis gas stream to a synthesis loop, comprising the steps of: (a)removing a purge stream comprising hydrogen and hydrocarbons from a synthesis loop; (b)separating hydrogen from the purge stream; (c)passing the purge stream to a reformer and reacting with steam and oxygen to produce a stream comprising hydrogen and carbon monoxide; (d)subjecting the reformed reaction product stream to a shift reaction to produce a stream comprising carbon dioxide and hydrogen; (e)subjecting the product stream from the shift reaction to separation to separate hydrogen from carbon dioxide; (f)supplying the separated hydrogen to the synthesis loop; and (g)removing the carbon dioxide.
C01B 3/34 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
11.
PROCESS FOR THE PURIFICATION OF AROMATIC DICARBOXYLIC ACID
A process for the purification of aromatic dicarboxylic acid comprising the steps of: (a) slurrying crude aromatic dicarboxylic acid solids with water recycled from at least a filtration step in a feed preparation zone; (b) supplying flash steam in vapour phase to the feed preparation zone from at least one of a crystallisation step, a filtration step, and a drier step; (c) preheating the slurried aromatic dicarboxylic acid solids to form a solution; (d) subjecting the heated solution to hydrogenation; (e) pure aromatic dicarboxylic acid to crystallise; (f) filtering out the crystals of pure aromatic dicarboxylic acid and recovering water in a single stage filtration process; (g) supplying at least part of the recovered water to the feed preparation zone; and (h) drying the filtered crystals and recovering same, wherein the flash stream recovered from at least one of a crystallisation step, a filtration step or a drier step is recovered as a vapour phase stream having a pressure of from about atmospheric to 5 barg and is supplied to the feed preparation zone without phase change. Also described is a system for the purification of aromatic dicarboxylic acid and a feed preparation vessel therefor.
A process for the separation of acetic acid and water in the presence of dimethylbenzene and methyl acetate comprising: supplying a feed comprising acetic acid, water, dimethylbenzene, and methyl acetate to a distillation column; operating the distillation column to separate the acetic acid and water; removing a stream comprising acetic acid from the column as bottoms; removing a stream comprising the water, dimethylbenzene and methyl acetate from the column as gaseous overhead stream; passing the gaseous overhead stream through a condenser such that at least a portion is condensed; passing the condensed overhead stream to a reflux drum; withdrawing a portion of the condensed aqueous overhead stream from a lower section of the reflux drum and returning said aqueous stream to the distillation column as reflux; removing a portion of the condensed stream from the upper section of the reflux drum; allowing said removed portion of the condensed overhead stream to separate into an upper layer comprising dimethylbenzene and a lower layer comprising water and methyl acetate; decanting the upper layer comprising dimethylbenzene; and removing the lower layer comprising water and methyl acetate and wherein no condensed organic overhead stream is returned to the distillation column as reflux. Also disclosed is a reflux drum and apparatus for the separation of acetic acid and water in the presence of dimethylbenzene and methyl acetate.
A process for the separation of carboxylic acid from a slurry in a solvent is described comprising the steps of: supplying the slurry comprising crystals of carboxylic acid to a filter operating at pressure and at a temperature above the atmospheric boiling point of the solvent; mixing inert gas with solvent; supplying said inert gas and solvent mix to the filter; and removing a cake of separated crystals; wherein the inert gas removed from the filter is not recycled. Also described is a system for the separation of carboxylic acid crystals from a slurry in a solvent comprising: a pressure filter device having a slurry inlet, and an outlet for a cake of carboxylic acid crystals; means for mixing inert gas and solvent; means for supplying said inert gas and solvent mixture to the pressure filter; wherein said pressure filter device is configured to operate at pressure and at a temperature above the atmospheric boiling point of the solvent; and wherein said system does not include means for recycling the inert gas removed from the filter.
A process for the separation of solid carboxylic acid fines from mother liquor comprising said fines, wherein said process comprises the steps of: feeding the mother liquor containing fines to a settlement drum at above atmospheric pressure; and removing mother liquor having a lower concentration of carboxylic fines than that fed to the settlement drum; wherein said mother liquor removal occurs at a point above the point at which the mother liquor containing fines is fed to the settlement drum. Also described is a system for the separation of solid carboxylic acid fines from mother liquor, said system comprising: a settlement drum having an inlet for mother liquor comprising carboxylic acid fines and an outlet for mother liquor having a lower concentration of carboxylic acid fines content then that of the mother liquor introduced via the inlet; wherein said settlement drum is configured to operate at above atmospheric pressure and said outlet is located at a point in the settlement drum above said inlet.
C07C 51/47 - SeparationPurificationStabilisationUse of additives by solid-liquid treatmentSeparationPurificationStabilisationUse of additives by chemisorption
15.
PROCESS FOR THE PRODUCTION OF SUBSTITUTE NATURAL GAS
A process for the production of substitute natural gas comprising: providing a feed gas to a first and/or second and/or subsequent bulk methanator; subjecting that feed gas to methanation in the presence of a suitable catalyst; removing an at least partially reacted stream from the first bulk methanator and supplying it to the second and/or subsequent bulk methanator where it is subjected to further methanation; passing a product stream from the final bulk methanator to a trim methanator train where it is subjected to further methanation; removing a recycle stream downstream of the first, second or subsequent bulk methanator, and, in any order, passing it through a compressor, subjecting it to cooling and then supplying to a trim and/or recycle methanator for further methanation before being recycled to the first and/or second and/or subsequent methanator.
A process for the separation and drying of crude carboxylic acid crystals from a slurry in a solvent is described. The process comprises the steps of: supplying the slurry comprising crystals of carboxylic acid to a filter operating at pressure and at a temperature above the atmospheric boiling point of the solvent; removing a cake of separated crystals from said filter; and passing said cake to a thermal dryer. Also described is a system for the separation and drying of crude carboxylic acid from a slurry in a solvent comprising: a pressure filter device comprising a slurry inlet and an outlet for a cake of carboxylic acid crystals; and a thermal dryer and means for transporting the cake of carboxylic acid crystals from the pressure filter device to the dryer; wherein said pressure filter device is configured to operate at a pressure and temperature above the atmospheric boiling point of the solvent.
C07C 51/43 - SeparationPurificationStabilisationUse of additives by change of the physical state, e.g. crystallisation
C07C 51/47 - SeparationPurificationStabilisationUse of additives by solid-liquid treatmentSeparationPurificationStabilisationUse of additives by chemisorption
A catalyst carrier for insertion in a radial tube reactor, said catalyst carrier comprising: an annular container for holding catalyst in use, said container having a perforated inner wall defining a tube, a perforated outer wall, a top surface closing the annular container and a bottom surface closing the annular container; a surface closing the bottom of said tube formed by the inner wall of the annular container; a skirt extending upwardly from the perforated outer wall of the annular container from a position at or near the bottom surface of said container to a position below the location of a seal; and a seal located at or near the top surface and extending from the container by a distance which extends beyond an outer surface of the skirt.
B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds in tube reactorsChemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
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
18.
PROCESS FOR THE CO-PRODUCTION OF A STREAM OF A FATTY ALCOHOL HAVING A FIRST CARBON CHAIN LENGTH AND A STREAM OF A FATTY ALCOHOL HAVING A SECOND CARBON LENGTH
A process for the co-production of a stream of a fatty alcohol having first carbon chain lengths and a stream of a fatty alcohol having a second carbon chain lengths, said second carbon chain lengths being longer than said first carbon chain lengths, said process comprising the steps of: (a) supplying a stream comprising lower alkyl esters of fatty acids having chain lengths comprising the first and second chain lengths to a first vaporisation zone and contacting said stream with an amount of hydrogen recycled from step (i) which is sufficient to vaporise the lower alkyl esters of the fatty acids having the first carbon chain lengths into the hydrogen; (b) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having the first carbon chain lengths to a first reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having first carbon chain lengths; (c) recovering from the first reaction zone an alcohol product stream having first carbon chain lengths and the hydrogen; (d) supplying the unvaporised lower alkyl esters of the fatty acids having second carbon chain lengths remaining from step (a) to a second vaporisation zone; (e) contacting the unvaporised lower alkyl esters having second carbon chain lengths in the second vaporisation zone with an amount of hydrogen sufficient to vaporise the lower alkyl esters having fatty acids of the second carbon chain lengths into the hydrogen; (f) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having second carbon chain lengths to a second reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having second carbon chain lengths; (g) recovering from the second reaction zone an alcohol product stream having second carbon chain lengths and hydrogen; (h) separating the stream of fatty acid alcohol having the second carbon chain length from hydrogen; and (i) recycling a portion of the hydrogen recovered in step (h) to the first vaporisation zone and a portion to the second vapourisation zone.
C07C 29/149 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen-containing functional group of C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
19.
PROCESS FOR THE PURIFICATION OF METHANOL BY DISTILLATION
A process for distillation, in a distillation column, of a crude stream of methanol produced from synthesis gas, said crude stream comprising fusel oil and alkali wherein said fusel oil is removed from the distillation column as a vapour side draw from a point in the distillation column below the feed and wherein said vapour side draw is substantially free of alkali, A process for the production of methanol utilising this distillation process is also described.
C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
C07C 29/151 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
The invention comprises a process for the chemical treatment of a feed stream containing at least one organic compound comprising the step of contacting said feed stream with a catalyst comprising nickel and ruthenium in amounts to provide a mole ratio of ruthenium to nickel in the range from 0.15 x10-3 to 0.06. We have found that such catalysts maintain activity even in the presence of acid components which normally promote deactivation of nickel catalysts.
B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
C07C 29/145 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen-containing functional group of C=O containing groups, e.g. —COOH of ketones with hydrogen or hydrogen-containing gases
BP Exploration Operating Company Limited (United Kingdom)
Davy Process Technology Limited (United Kingdom)
Inventor
Clarkson, Jay Simon
Gamlin, Timothy Douglas
Hardy, Lawrence Trevor
Abstract
Process for converting synthesis gas to hydrocarbons in a slurry reactor in the presence of a Fischer-Tropsch catalyst comprising cobalt and zinc oxide. The process is carried out by a) activating the Fischer-Tropsch catalyst with a reducing gas consisting of hydrogen and an inert gas at a temperature between 330 and 400° C., and b) contacting the activated Fischer-Tropsch catalyst from step a) with synthesis gas in the slurry reactor in order to convert the synthesis gas into hydrocarbons.
A process for activating a reduced manganese copper catalyst comprising treating the catalyst at a temperature of more than 300°C to about 400°C with hydrogen.
A process for the removal of hydroxypropane from a crude product stream from the hydrogenation of glycerol, the crude product stream comprising 1,2-propanediol and hydroxypropanone as impurity, the process comprising: (a) where required condensing the crude product stream; and (b) contacting the crude product phase in the liquid phase with a stream of a hydrogen-containing gas in the presence of a heterogeneous catalyst at suitable temperatures and pressures such that hydroxypropanone present in the crude product stream is converted to the desired propanediol.
C07C 29/60 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by elimination of hydroxy groups, e.g. by dehydration
C07C 29/90 - SeparationPurificationStabilisationUse of additives by treatment giving rise to a chemical modification of at least one compound using hydrogen only
A process for the co-production of a stream of a fatty alcohol having first carbon chain lengths and a stream of a fatty alcohol having a second carbon chain lengths, said second carbon chain lengths being longer than said first carbon chain lengths, said process comprising the steps of: (a) supplying a stream comprising lower alkyl esters of fatty acids having chain lengths comprising the first and second chain lengths to a first vaporisation zone and contacting said stream with an amount of hydrogen which is sufficient to vaporise the lower alkyl esters of the fatty acids having the first carbon chain lengths into the hydrogen; (b) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having the first carbon chain lengths to a first reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having first carbon chain lengths; (c) recovering from the first reaction zone an alcohol product stream having first carbon chain lengths and hydrogen; (d) separating the stream of fatty alcohol having the first carbon chain lengths from hydrogen; (e) supplying the unvaporised lower alkyl esters of the fatty acids having second carbon chain lengths remaining from step (a) to a second vaporisation zone; (f) contacting the unvaporised lower alkyl esters having second carbon chain lengths in the second vaporisation zone with hydrogen recovered in step (d) and an additional amount of hydrogen such that the total amount of hydrogen is sufficient to vaporise the lower alkyl esters having fatty acids of the second carbon chain lengths into the hydrogen; (g) supplying the hydrogen and the vaporised lower alkyl esters of fatty acids having second carbon chain lengths to a second reaction zone comprising catalyst and operating under reaction conditions to allow hydrogenation to the desired alcohol having second carbon chain lengths; and (h) recovering from the second reaction zone an alcohol product stream having second carbon chain lengths and hydrogen.
C07C 29/149 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen-containing functional group of C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
A process for use in equilibrium exothermic gas phase reactions comprising the steps of (a) providing a recycle stream with the addition of make-up gas, to form a feed gas stream; (b) heating the feed gas stream; (c) passing the heated feed gas stream to a first reactor containing a catalyst for the exothermic gas phase reactions at conditions suitable for the reaction; (d) removing a product stream comprising product and unreacted gases from the first reactor; (e) cooling and partially condensing the product stream to form a gas phase and a liquid phase; (f) separating the liquid phase containing the desired product from the product stream and removing said liquid phase; (g) separating the gas phase from the product stream to form a gas stream; (h) optionally mixing the gas stream from the product stream with additional make-up gas; (i) heating the gas stream; (j) passing the heated gas stream to a final reactor containing a catalyst for the exothermic gas phase reactions at conditions suitable for the reaction; (k) removing a final product stream comprising product and unreacted gases from the final reactor; (l) cooling and partially condensing the final product stream to form a final gas phase and a mal liquid phase; (m) separating the final liquid phase containing the desired product from the final product stream and removing said final liquid phase; and (n) separating the gas phase from the final product stream and recycling the gas to step (a); and in which the gas stream from step (g) is compressed prior to heating in step (i).
C07C 27/06 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds by reduction of oxygen-containing compounds by hydrogenation of oxides of carbon
BP EXPLORATION OPERATING COMPANY LIMITED (United Kingdom)
Inventor
Font Freide, Josephus Johannes Helena Maria
Hardy, Lawrence Trevor
Abstract
The present invention relates to a process for the conversion of synthesis gas to hydrocarbons in the presence of a modified supported Fischer-Tropsch catalyst composition, by addition of a silylating compound modifier, preferably an organosilicon compound such as bis (timethylsilyl) trif luoroacetamide.
B01J 23/06 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of zinc, cadmium or mercury
B01J 23/80 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with zinc, cadmium or mercury
B01J 31/02 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
B01J 33/00 - Protection of catalysts, e.g. by coating
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
27.
Electromechanical filter for Fischer-Tropsch synthesis
Electromechanical filtering unit having a conduit capable of conducting electricity, at least one first electrode connectable to a high voltage power supply (EHT) and at least one second electrode having a plurality of discrete openings which is earthed. The electrodes are positioned within the conduit and connected to the conduit such that electricity can pass between the electrodes via the conduit.
patents
