In a process for recovering styrene monomer from polystyrene, a feed comprising benzene, toluene, ethylbenzene, styrene monomer and C9+ aromatics produced by depolymerizing polystyrene is supplied to a first fractionation column and divided into a first bottoms fraction containing part of the C9+ aromatics in the feed and a first overhead fraction composed of the remainder of the feed. The first overhead fraction is supplied to a second fractionation column and divided into a second overhead fraction rich in benzene, toluene, and ethylbenzene compared to the first overhead fraction and a second bottoms fraction rich in styrene monomer and C9+ aromatics compared to the first overhead fraction. The second bottoms fraction is supplied to a third fractionation column and divided into a third overhead fraction rich in styrene monomer compared to the second bottoms fraction and a third bottoms fraction rich in C9+ aromatics compared to the second bottoms fraction.
C07C 4/22 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by depolymerisation to the original monomer, e.g. dicyclopentadiene to cyclopentadiene
A downer reactor assembly includes an outer disengager vessel, at least one downer reactor extending vertically from a top end to a lower end within the outer disengager vessel, and a mushroom-shaped distributor end cap positioned at the lower end of the at least one downer reactor. A process for cracking a hydrocarbon feedstock includes providing a catalyst feed to at least one downer reactor assembly. Discharging the catalyst feed at a lower end of at least one downer reactor underneath a mushroom-shaped distributor cap. The process includes separating hydrocarbon vapors from the catalyst feed under gravity and distributing upward flowing hydrocarbon vapors separated from the catalyst feed through nozzle holes in the mushroom-shaped distributor cap.
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 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
3.
STYRENE MONOMER FROM FEEDSTOCK INCLUDING PYROLYSIS OIL
A system can be used to generate styrene monomer product from feedstock originating from a pyrolysis operation and a dehydrogenation operation. The system can include a styrene processing subsystem and a distillation column. The styrene processing subsystem can be positioned to receive first feedstock and to generate the styrene monomer product. The styrene processing subsystem can include an initial distillation column. The distillation column can be coupled with the initial distillation column to provide at least a portion of the first feedstock. The distillation column can positioned to receive second feedstock that can include pyrolysis oil and to generate the portion of the first feedstock by separating styrene from the pyrolysis oil.
C07C 4/22 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by depolymerisation to the original monomer, e.g. dicyclopentadiene to cyclopentadiene
C07C 15/16 - Polycyclic non-condensed hydrocarbons containing at least two phenyl groups linked by one single acyclic carbon atom
A chemical manufacturing process may include an open loop that provides both feedstock delivery and refrigeration. For example, the process may include conveying a hydrocarbon feedstock (e.g., propane or propylene) in a liquid phase from a feedstock accumulator to a shell side of a heat exchanger and vaporizing the feedstock in the heat exchanger. Then, the method may include collecting the feedstock in a vapor phase from the heat exchanger in an economizer; compressing and condensing a first portion of the feedstock in the vapor phase from the economizer in a compressor; and recycling the feedstock in the liquid phase from the compressor to the feedstock accumulator, which closes the refrigeration loop. As the open part of the loop to provide feedstock to the reactor, the method may further include conveying a second portion of the feedstock in the vapor phase from the economizer to a reactor.
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 fluid catalytic cracking process includes regenerating a spent catalyst from a stripper vessel in a first regeneration stage to produce a partially regenerated catalyst, regenerating the partially regenerated catalyst in second regeneration stage to produce a fully regenerated catalyst, and providing a first portion of the fully regenerated catalyst to a riser reactor. The process includes generating the spent catalyst with the riser reactor and providing the spent catalyst to a stripper vessel and providing a second portion of the fully regenerated catalyst to the stripper vessel to mix with the spent catalyst for better stripping efficiency and prompting further reactions, resulting in overall reduced coke load, sulfur, and nitrogen to be burned, and providing necessary heat needed for the following coke gasification to produce synthesis gas in the first regeneration stage.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
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 8/26 - 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 two or more fluidised beds, e.g. reactor and regeneration installations
C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen
A fluid catalytic cracking process includes regenerating a spent catalyst from a stripper vessel in a first regeneration stage to produce a partially regenerated catalyst, regenerating the partially regenerated catalyst in second regeneration stage to produce a fully regenerated catalyst, and providing a first portion of the fully regenerated catalyst to a riser reactor. The process includes generating the spent catalyst with the riser reactor and providing the spent catalyst to a stripper vessel and providing a second portion of the fully regenerated catalyst to the stripper vessel to mix with the spent catalyst for better stripping efficiency and prompting further reactions, resulting in overall reduced coke load, sulfur, and nitrogen to be burned, and providing necessary heat needed for the following coke gasification to produce synthesis gas in the first regeneration stage.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01J 38/34 - Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed with plural distinct serial combustion stages
B01J 38/40 - Treating with free oxygen-containing gas and forming useful by-products
C10J 3/46 - Gasification of granular or pulverulent fuels in suspension
7.
ELECTRIC FURNACE FOR CRACKING HYDROCARBON FEEDSTOCK WITH HEAT RECOVERY
An electric cracking furnace system for converting a hydrocarbon feedstock into cracked gas includes a mixing device for mixing hydrocarbon feedstock with slightly superheated and/or saturated steam. The system includes a steam drum, an electric furnace, a primary transfer line exchanger (PTLE), a secondary transfer line exchanger (STLE), and a tertiary transfer line exchanger (TTLE). The electric furnace includes a feed inlet for a hydrocarbon feedstock-saturated steam mixture and an outlet for a cracked gas. The steam drum includes a saturated steam outlet connected to the mixing device, and a water outlet and a steam inlet both connected to the STLE. The PTLE is configured to preheat the hydrocarbon feedstock-saturated steam mixture before entry into the electric furnace and to cool the cracked gas provided by the electric furnace. The STLE is configured to generate steam and to cool the cracked gas provided by the PTLE.
The disclosure generally provides a modification of a calcination process of lime bearing sludge in such a way that the flue gas generated by the calcination process contains primarily carbon dioxide and water vapor along with only minor amounts of other gaseous species. Such a flue gas can be treated by standard industrial gas scrubbing and purification processes to remove residual particulate solids, to condense and remove the water vapor as liquid water, and further treatment to produce essentially pure carbon dioxide. The resulting product may be used for purposes that do not involve a net emission of carbon dioxide to the atmosphere, thereby reducing environmental harm. Such purified carbon dioxide may be used in industry for enhanced oil recovery (EOR) processes, synthetic fuels production, carbonated beverage production, pharmaceutical production, or other beneficial uses.
A process for controlling catalyst temperature in a fluidized catalytic cracking ("FCC") system includes regenerating a spent catalyst feed in a regenerator at a first temperature to produce a regenerated catalyst feed, withdrawing at least a portion of the regenerated catalyst feed to a reactor, and cooling the portion of the regenerated catalyst between an outlet of the regenerator and an inlet of the reactor. A fluidized catalytic cracking ("FCC") system includes a catalyst regenerator configured and adapted to regenerate a spent catalyst feed at a first temperature to produce a regenerated catalyst, a reactor downstream from an outlet of the catalyst regenerator, a catalyst cooler between the outlet of the catalyst regenerator and an inlet of the reactor. The catalyst cooler is configured and adapted to cool at least a portion of a regenerated catalyst from the catalyst regenerator. In embodiments, the FCC system is a downer FCC system including at least one downer reactor and a spent catalyst riser regenerator.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
B01J 38/30 - Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
B01J 38/32 - Indirectly heating or cooling material within regeneration zone or prior to entry into regeneration zone
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
10.
SYSTEMS AND PROCESSES FOR RESIDENCE TIME CONTROL IN DOWNER REACTORS
A downer reactor assembly includes an outer disengager vessel, at least one downer reactor extending vertically from a top end to a lower end within the outer disengager vessel, and a mushroom-shaped distributor end cap positioned at the lower end of the at least one downer reactor. A process for cracking a hydrocarbon feedstock includes providing a catalyst feed to at least one downer reactor assembly. Discharging the catalyst feed at a lower end of at least one downer reactor underneath a mushroom- shaped distributor cap. The process includes separating hydrocarbon vapors from the catalyst feed under gravity and distributing upward flowing hydrocarbon vapors separated from the catalyst feed through nozzle holes in the mushroom-shaped distributor cap.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
11.
SYSTEMS AND PROCESSES FOR TEMPERATURE CONTROL IN FLUIDIZED CATALYTIC CRACKING
A fluidized catalytic cracking ("FCC") system includes a catalyst regenerator configured and adapted to regenerate a spent catalyst feed to produce a regenerated catalyst. The system includes a reactor downstream from an outlet of the catalyst regenerator to receive regenerated catalyst therefrom. The system includes a spent catalyst riser between an outlet of the reactor and an inlet of the regenerator. The spent catalyst riser includes a torch oil injection nozzle configured and adapted to provide heat to the catalyst regenerator. A process for controlling catalyst temperature in an FCC system includes regenerating a spent catalyst feed in a catalyst regenerator to produce a regenerated catalyst feed, withdrawing at least a portion of the regenerated catalyst feed to a to a reactor, receiving a spent catalyst from the reactor in a spent catalyst riser, and heating the spent catalyst in the spent catalyst riser with a torch oil injection nozzle. In embodiments, the reactor is a downer.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
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
12.
SYSTEMS AND METHODS FOR ENHANCING THE RECOVERY OF STYRENE
A method for enhancing the recovery of styrene includes feeding a hot liquid residue stream to a stripping vessel from a styrene monomer purification finishing system. The hot liquid residue stream includes styrene and compounds less volatile than styrene. The method includes introducing a gas to the stripping vessel to strip a portion of the styrene as vapor, generating a vaporized styrene portion, returning the vaporized styrene portion and the gas to the styrene monomer purification finishing system, recovering at least a portion of the vaporized styrene portion into a styrene monomer product, and producing a final liquid residue stream from a bottom of the stripping vessel with a lower concentration of styrene than the hot liquid residue stream feeding the stripping vessel.
C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
C07C 4/22 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by depolymerisation to the original monomer, e.g. dicyclopentadiene to cyclopentadiene
PROCESSES FOR MAKING ETHYLENE GLYCOL AND/OR PROPYLENE GLYCOL FROM ALDOSE- AND/OR KETOSE-YIELDING CARBOHYDRATES WITH INTEGRATED TUNGSTEN CATALYST RECOVERY
Integrated processes are disclosed for the catalytic conversion of carbohydrate to ethylene glycol and/or propylene glycol using a homogeneous, tungsten-containing retro-aldol catalyst. In these processes, the carbohydrate is subjected to retro-aldol conversion and hydrogenation to provide a reaction product containing ethylene glycol and/or propylene glycol, other reaction process including organic acids, itols and tungsten species. Ethylene glycol and propylene glycol are separated from the reaction product for purification, and at least a portion of the remaining fraction is subjected to ion exclusion chromatography to provide an eluant containing tungsten species and a subsequent eluant containing organic acids and a substantially reduced concentration of tungsten species. At least a portion of the eluant containing tungsten species can be recycled for reuse directly or with intervening unit operations to enhance the catalytic activity of the tungsten species. The organic-containing fraction can be subjected to one or more unit operations to provide salable products or subjected to selective hydrogenolysis to lower glycols.
C07C 29/09 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
C07C 29/74 - SeparationPurificationStabilisationUse of additives
C07C 29/153 - 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 catalyst used
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
An apparatus includes a riser reactor within the reaction vessel. The riser reactor defines a longitudinal axis and including a riser reactor inlet at one end and at least one riser reactor outlet at an opposite end. The apparatus includes a separation vessel including at least one separation chamber and at least one collection chamber distributed in an alternating manner about the longitudinal axis. Each separation chamber comprises two vertical lateral walls which also comprise a wall of an adjacent one of the at least one collection chamber. A lateral separation chamber outlet is defined in at least one of the vertical lateral walls to provide fluid and particle communication from the lateral separation chamber to the adjacent one of the at least one collection chamber. The separation vessel includes at least one collection chamber deflector positioned in the at least one collection chamber.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01D 45/06 - Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by reversal of direction of flow
B01D 45/08 - Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
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 system for stabilizing a hydrocarbon feedstock includes a High Pressure Separation (HPS) unit in fluid communication with a feedstock inlet. The HPS unit includes an oil outlet. The system includes a heated Low Pressure (LP) separator unit downstream from and in fluid communication with the oil outlet of the HPS unit. The heated LP separator unit includes an oil outlet. The system includes a heat exchanger positioned between the HPS unit and the heated LP separator unit.
C10G 31/06 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
A cracking furnace for cracking a hydrocarbon feed, the furnace including a firebox having a single radiant zone including, a first plurality of cracking coils each having a first shape arranged within the firebox. The radiant zone includes a second plurality of cracking coils each having a second shape arranged within the radiant zone. A burner section positioned below the first plurality cracking coils and below the second plurality of cracking coils. A convection section is positioned on top of the firebox configured to recover residual heat from the firebox.
F28F 1/10 - Tubular elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
18.
CONTINUOUS PROCESSES FOR THE SELECTIVE CONVERSION OF ALDOHEXOSE-YIELDING CARBOHYDRATE TO ETHYLENE GLYCOL USING LOW CONCENTRATIONS OF RETRO-ALDOL CATALYST
Retro-aldol processes are disclosed that use very low concentrations of retro-aldol catalyst in combination with hydrogenation catalyst of certain activities, sizes and spatial dispersions to obtain the high selectivities to ethylene glycol.
C07C 29/09 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
C07C 29/10 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes
C07C 29/12 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of esters of mineral acids
19.
Continuous processes for the selective conversion of aldohexose-yielding carbohydrate to ethylene glycol using low concentrations of retro-aldol catalyst
T.EN STONE & WEBSTER PROCESS TECHNOLOGY, INC. (USA)
T.EN PROCESS TECHNOLOGY, INC. (USA)
Inventor
Schreck, David James
Nunley, Mark
Bunning, Donald
Albin, Brooke
Kapicak, Louis A.
Bradford, Michael
Abstract
Retro-aldol processes are disclosed that use very low concentrations of retro-aldol catalyst in combination with hydrogenation catalyst of certain activities, sizes and spatial dispersions to obtain the high selectivities to ethylene glycol.
C07C 29/136 - 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
C07C 29/74 - SeparationPurificationStabilisationUse of additives
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 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
A process for converting lignocellulosic feedstock includes providing a lignocellulosic feedstock into a first inlet of a first reactor at a first end, and providing a hot feedstock into a second inlet of the first reactor at a second end of the first reactor. The process includes heating and reacting the lignocellulosic feedstock with the hot feedstock and outputting a first product stream from a first product outlet of the first reactor. The first product stream is an alkane rich product stream. A reactor system includes a first reactor having a first inlet at a first end, a second inlet at a second end and at least one product outlet. The first reactor is configured to receive a lignocellulosic feedstock at the first inlet and a hot feedstock at the second inlet. The system includes a second reactor having a first inlet downstream from the at least one product outlet.
C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
C10B 47/00 - Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
C10B 49/02 - Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
C10B 51/00 - Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
21.
METHODS FOR OPERATING CONTINUOUS, UNMODULATED, MULTIPLE CATALYTIC STEP PROCESSES
Control methods are disclosed for continuous, unmodulated, multiple catalytic conversion step processes using at least two catalysts, a first catalyst and a second catalyst, that accommodate changes in the performance of each catalyst and the relative performances of the catalysts. In the methods, certain process parameters are used in a manner that is indicative of changes in catalyst performance, and the control methods provide for adjustment of at least one of: the absolute amount of catalytically active species and relative amounts of each of the first catalyst and second catalyst and at least one of the rate of feed or concentration of the raw material to the reaction zone.
A packing system includes a first packing element layer including a plurality of blades and a second packing element layer including a plurality of blades. The packing system includes intra-layer variation and/or inter-layer variation. Intra-layer variation includes (i) varying spacing between blades within the first and/or the second packing element layer, (ii) varying sizes of the blades within the first and/or the second packing element layer, and/or (iii) varying angle of inclination of the blades within the first and/or second packing element layer. Inter-layer variation includes the blades of the first packing layer having a first spacing, a first size and a first angle of inclination, and the blades of the second packing layer having a second spacing, a second size, and a second angle of inclination. The second spacing, size, and/or angle of inclination is different from the first spacing, size, and/or angle of inclination.
B01J 8/34 - 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 stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
B01J 19/32 - Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
23.
CONTINUOUS, CARBOHYDRATE TO ETHYLENE GLYCOL PROCESSES
By this invention processes are provided for the conversion of carbohydrate to ethylene glycol by retro-aldol catalysis and sequential hydrogenation using control methods having at least one of acetol (hydroxyacetone) and a tracer as inputs.
C07C 29/132 - 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
T.EN STONE & WEBSTER PROCESS TECHNOLOGY, INC. (USA)
T.EN PROCESS TECHNOLOGY, INC. (USA)
Inventor
Schreck, David James
Chrisman, Ray
Bunning, Donald
Kapicak, Lou
Albin, Brooke
Nunley, Mark
Bradford, Michael
Abstract
Processes are disclosed for the catalytic conversion of carbohydrate feed to one or both of ethylene glycol and propylene glycol. In the disclosed processes, a portion of the aqueous medium in the reaction zone of the catalytic process is withdrawn and recycled and the recycle is integrated to enhance the overall process.
C07C 29/17 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
25.
PROCESS FOR MAKING ETHYLENE GLYCOL AND/OR PROPYLENE GLYCOL FROM ALDOSE- AND/OR KETOSE-YIELDING CARBOHYDRATES WITH EX SITU HYDROGENOLYSIS OR HYDROGENATION CATALYST TREATMENT
T.EN STONE & WEBSTER PROCESS TECHNOLOGY, INC. (USA)
T.EN PROCESS TECHNOLOGY, INC. (USA)
Inventor
Schreck, David James
Bunning, Donald
Kapicak, Lou
Albin, Brooke
Nunley, Mark
Bradford, Michael
Abstract
Processes are disclosed for the catalytic conversion using a heterogeneous hydrogenolysis or hydrogenation catalyst of carbohydrate feed to one or both of ethylene glycol and propylene glycol. In the disclosed processes, a portion of the heterogeneous catalyst in the reaction zone of the catalytic process is withdrawn and recycled and the recycle is integrated to enhance the overall process.
C07C 29/17 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
B01J 38/68 - Liquid treating or treating in liquid phase, e.g. dissolved or suspended including substantial dissolution or chemical precipitation of a catalyst component in the ultimate reconstitution of the catalyst
26.
Methods for operating continuous, unmodulated, multiple catalytic step processes
Control methods are disclosed for continuous, unmodulated, multiple catalytic conversion step processes using at least two catalysts, a first catalyst and a second catalyst, that accommodate changes in the performance of each catalyst and the relative performances of the catalysts. In the methods, certain process parameters are used in a manner that is indicative of changes in catalyst performance, and the control methods provide for adjustment of at least one of: the absolute amount of catalytically active species and relative amounts of each of the first catalyst and second catalyst and at least one of the rate of feed or concentration of the raw material to the reaction zone.
C07C 29/132 - 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
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/24 - Stationary reactors without moving elements inside
C07C 29/17 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
A system for stabilizing a hydrocarbon feedstock includes a High Pressure Separation (HPS) unit in fluid communication with a feedstock inlet. The HPS unit includes an oil outlet. A Heated Low Pressure (LP) Separator unit is downstream from the oil outlet of the HPS unit. The Heated LP Separator unit includes an oil outlet.
C10G 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
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
B01J 35/10 - Solids characterised by their surface properties or porosity
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
C07C 29/132 - 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
B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
B01J 23/46 - Ruthenium, rhodium, osmium or iridium
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 31/10 - Monohydroxylic acyclic alcohols containing three carbon atoms
C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
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
B01J 35/10 - Solids characterised by their surface properties or porosity
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
C07C 29/132 - 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
B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
B01J 23/46 - Ruthenium, rhodium, osmium or iridium
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 31/10 - Monohydroxylic acyclic alcohols containing three carbon atoms
C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
B01J 23/76 - 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
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
B01J 35/10 - Solids characterised by their surface properties or porosity
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 29/132 - 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
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
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
31.
CONTINUOUS PROCESSES FOR THE HIGHLY SELECTIVE CONVERSION OF ALDOHEXOSE-YIELDING CARBOHYDRATE TO ETHYLENE GLYCOL
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
32.
Continuous processes for the highly selective conversion of aldohexose-yielding carbohydrate to ethylene glycol
B01J 23/46 - Ruthenium, rhodium, osmium or iridium
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
B01J 35/10 - Solids characterised by their surface properties or porosity
C07C 29/00 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
C07C 31/10 - Monohydroxylic acyclic alcohols containing three carbon atoms
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
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
C07C 31/125 - Monohydroxylic acyclic alcohols containing five to twenty-two carbon atoms
33.
Process for the continuous production of ethylene glycol from carbohydrates
T.EN STONE & WEBSTER PROCESS TECHNOLOGY, INC. (USA)
T.EN PROCESS TECHNOLOGY, INC. (USA)
Inventor
Schreck, David James
Chrisman, Ray
Albin, Brooke
Clinton, Nye Atwood
Bradford, Marion Mckinley
Abstract
A continuous process for converting carbohydrates to ethylene and propylene glycol. The carbohydrates are mixed with water and passed through a reactor at a temperature that hydrolyzes the carbohydrate mixture at least partially to monosaccharides. The reactor has a first zone comprising a retro-aldol catalyst and a second zone comprising a reducing catalyst. The aldose is converted in the first zone into glycolaldehyde by the retro-aldol catalyst and the glycolaldehyde, in the presence of hydrogen, is converted to ethylene glycol in the second zone of the reactor. The reaction products are removed from the reactor and the ethylene glycol is recovered. The selectivity to propylene glycol can be enhanced via feeding ketose as the carbohydrate.
C07C 45/00 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds
C07C 29/00 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
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
C07C 45/67 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by reactions not involving the formation of C=O groups by isomerisationPreparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by reactions not involving the formation of C=O groups by change of size of the carbon skeleton
B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
B01J 21/06 - Silicon, titanium, zirconium or hafniumOxides or hydroxides thereof
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
34.
PROCESS FOR THE CONTINUOUS PRODUCTION OF ETHYLENE GLYCOL FROM CARBOHYDRATES
A continuous process for converting carbohydrates to ethylene and propylene glycol. The carbohydrates are mixed with water and passed through a reactor at a temperature that hydrolyzes the carbohydrate mixture at least partially to monosaccharides. The reactor has a first zone comprising a retro-aldol catalyst and a second zone comprising a reducing catalyst. The aldose is converted in the first zone into glycolaldehyde by the retro-aldol catalyst and the glycolaldehyde, in the presence of hydrogen, is converted to ethylene glycol in the second zone of the reactor. The reaction products are removed from the reactor and the ethylene glycol is recovered. The selectivity to propylene glycol can be enhanced via feeding ketose as the carbohydrate.
C07C 47/19 - Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen containing hydroxy groups
C10G 1/06 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
35.
Process for the continuous production of ethylene glycol from carbohydrates
T.EN STONE & WEBSTER PROCESS TECHNOLOGY, INC. (USA)
T.EN PROCESS TECHNOLOGY, INC. (USA)
Inventor
Schreck, David James
Chrisman, Ray
Albin, Brooke
Clinton, Nye Atwood
Bradford, Marion
Abstract
A continuous process for converting carbohydrates to ethylene and propylene glycol. The carbohydrates are mixed with water and passed through a reactor at a temperature that hydrolyzes the carbohydrate mixture at least partially to monosaccharides. The reactor has a first zone comprising a retro-aldol catalyst and a second zone comprising a reducing catalyst. The aldose is converted in the first zone into glycolaldehyde by the retro-aldol catalyst and the glycolaldehyde, in the presence of hydrogen, is converted to ethylene glycol in the second zone of the reactor. The reaction products are removed from the reactor and the ethylene glycol is recovered. The selectivity to propylene glycol can be enhanced via feeding ketose as the carbohydrate.
C07C 45/00 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds
C07C 29/00 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
C07C 29/141 - 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 a —CHO group with hydrogen or hydrogen-containing gases
C07C 45/67 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by reactions not involving the formation of C=O groups by isomerisationPreparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by reactions not involving the formation of C=O groups by change of size of the carbon skeleton
37 - Construction and mining; installation and repair services
42 - Scientific, technological and industrial services, research and design
Goods & Services
(1) Evaluation, namely, providing cost-effectiveness assessments and recommendations for industrial plants; design and engineering of industrial processes and plants engaged in the manufacturing and processing of chemicals, and initial operation of said processes and plants, namely, providing troubleshooting assessments and recommendations prior to and during start-up of said processes and plants; analysis, planning, and supervision of maintenance operations for process industries.
37 - Construction and mining; installation and repair services
42 - Scientific, technological and industrial services, research and design
Goods & Services
(1) Research, development, evaluation, consultation and technical services for others in connection with the process design, construction and operation of units for cracking of hydrocarbons, and the process designing, constructing and operating of such units for others.
37 - Construction and mining; installation and repair services
42 - Scientific, technological and industrial services, research and design
Goods & Services
(1) Research, development, evaluation, consultation and technical services for others in connection with the process design, construction and operation of units for cracking of hydrocarbons, and the process designing, constructing and operating of such units for others.
37 - Construction and mining; installation and repair services
42 - Scientific, technological and industrial services, research and design
Goods & Services
(1) Evaluation, design, and engineering of industrial processes and plants, particularly for manufacturing and/or processing of chemicals, and initial operation of said processes and plants; analysis, planning and supervision of maintenance operations for process industries; construction of industrial plants, such as chemical manufacturing and/or process plants, including the procurement of construction materials and construction of buildings, roads, etc. ancillary to said plants.
09 - Scientific and electric apparatus and instruments
11 - Environmental control apparatus
Goods & Services
(1) Bubble trays for use in fractionating, rectifying, absorbing, heat-exchanging and other towers, columns and devices for the distillation or other refining treatment of petroleum and other liquids.
