A process for upgrading a biomass feed stream comprises liquefaction and deoxygenation in one step. The process comprises reacting the biomass feed stream over a catalyst in the presence of hydrogen in a reactor to produce a reactor effluent stream. The reactor effluent stream is separated to provide a liquid effluent stream comprising bio-oil. An oil stream is added to the reactor in an oil to biomass weight ratio of less than about 2:1. A bio-oil stream is taken from the liquid effluent stream. The bio-oil stream may be processed to produce one or more fuel streams.
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
A process for upgrading a biomass feed stream comprises liquefaction and deoxygenation in one step. The process comprises reacting the biomass feed stream over a catalyst in the presence of hydrogen in a reactor to produce a reactor effluent stream. The reactor effluent stream is separated to provide a liquid effluent stream comprising bio-oil. An oil stream is added to the reactor in an oil to biomass weight ratio of less than 2:1. A bio-oil stream is taken from the liquid effluent stream. The bio-oil stream may be processed to produce one or more fuel streams.
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
Electric heating elements are described. The electric heating elements can be electrical resistance heated elements or electrical impedance heated elements. The electric heating elements have a heat transfer enhancement structure on the surface and/or may be at least partially made from a porous metal. Electric heaters incorporating the electric heating elements and methods of heating a fluid process streams are also described.
Electric heating elements are described. The electric heating elements can be electrical resistance heated elements or electrical impedance heated elements. The electric heating elements have a heat transfer enhancement structure on the surface and/or may be at least partially made from a porous metal. Electric heaters incorporating the electric heating elements and methods of heating a fluid process streams are also described.
H05B 3/12 - Éléments chauffants caractérisés par la composition ou la nature des matériaux ou par la disposition du conducteur caractérisés par la composition ou la nature du matériau conducteur
5.
PROCESS FOR UTILIZING CARBON OXIDES IN A FLUE GAS STREAM
A process of separating carbon oxides from a flue gas stream is disclosed. The process comprises separating a flue gas stream into a first flue gas stream and a second flue gas stream. The first flue gas stream is combusted with an oxygen stream in a boiler to provide a carbon dioxide rich flue gas stream. A carbon dioxide recycle stream is taken from the carbon dioxide rich flue gas stream. The second flue gas stream is recycled to an oxygenate production unit. The carbon dioxide recycle stream is recycled to the boiler or to a regenerator or both.
A process of separating carbon oxides from a flue gas stream is disclosed. The process comprises separating a flue gas stream into a first flue gas stream and a second flue gas stream. The first flue gas stream is combusted with an oxygen stream in a boiler to provide a carbon dioxide rich flue gas stream. A carbon dioxide recycle stream is taken from the carbon dioxide rich flue gas stream. The second flue gas stream is recycled to an oxygenate production unit. The carbon dioxide recycle stream is recycled to the boiler or to a regenerator or both.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
Methods for a pre-treating process that removes organic chlorides from pyrolysis oils, vegetable oils, fats, or combinations thereof before they are sent to a processing unit are described, as well as an apparatus for the pre-treatment process. The pre-treatment process involves the catalytic hydrodechlorination of the pyrolysis oils, vegetable oils, fats, or combinations thereof. The pre-treatment process may include saturating dienes.
C10G 67/06 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène uniquement par plusieurs étapes en série comprenant un procédé d'absorption ou d'adsorption comme étape de raffinage en l'absence d'hydrogène
C10G 67/10 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène uniquement par plusieurs étapes en série comprenant un traitement alcalin comme étape de raffinage en l'absence d'hydrogène
C10G 45/02 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage
C10G 25/00 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, au moyen d'absorbants ou d'adsorbants solides
C10G 19/02 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, par un traitement alcalin avec des solutions aqueuses alcalines
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
Methods for a pre-treating process that removes organic chlorides from pyrolysis oils, vegetable oils, fats, or combinations thereof before they are sent to a processing unit are described, as well as an apparatus for the pre-treatment process. The pre-treatment process involves the catalytic hydrodechlorination of the pyrolysis oils, vegetable oils, fats, or combinations thereof. The pre-treatment process may include saturating dienes.
Processes for converting Fischer-Tropsch products into aromatics are described. The processes involve processing a selected portion of the Fischer-Tropsch effluent or Fischer-Tropsch plus hydrocracking effluent in a separate, low pressure reforming reaction zone. The feed comprises the portion of the Fischer-Tropsch or Fischer-Tropsch/hydrocracking products boiling around the heavy naphtha and kerosene/light distillate range with a molecular composition of approximately C6 to C16 paraffins and iso-paraffins which would form alkylated mono or bicyclic compounds boiling in the naphtha-jet range.
A process for catalytically cracking hydrocarbons is disclosed. The process comprises contacting a hydrocarbon feed stream with a catalyst to catalytically crack the hydrocarbon feed stream to provide a cracked stream and spent catalyst. The spent catalyst is disengaged from the cracked stream in a reactor vessel. Hydrocarbons are stripped from the spent catalyst. The cracked stream is fractionated in a main fractionation column into products comprising a slurry oil stream from a bottom of the main fractionation column. The slurry oil stream is filtered in a filter vessel through a filter to provide a filtered slurry oil stream. Thereafter, the filter is backflushed with a hydrocarbon stream to produce a backflushed hydrocarbon stream comprising catalyst fines. The backflushed hydrocarbon stream is recycled to the reactor vessel. An apparatus for catalytically cracking hydrocarbons is also disclosed.
C10G 11/18 - Craquage catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures avec catalyseurs solides mobiles préchauffés selon la technique du "lit fluidisé"
C10G 31/09 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, par des méthodes non prévues ailleurs par filtration
12.
POLYELECTROLYTE MULTILAYER COATED PROTON EXCHANGE MEMBRANE FOR ELECTROLYSIS AND FUEL CELL APPLICATIONS
A method for preparing a new polyelectrolyte multilayer coated proton-exchange membrane has been developed for electrolysis and fuel cell applications. The method comprises: applying a polyelectrolyte multilayer coating to a surface of a cation exchange membrane, the polyelectrolyte multilayer coating comprising alternating layers of a polycation polymer and a polyanion polymer to form the polyelectrolyte multilayer coated proton-exchange membrane and optionally treating the polyelectrolyte multilayer coated proton-exchange membrane in an acidic solution. The polycation polymer layer is in contact with the cation exchange membrane.
H01M 8/1032 - Matériaux d’électrolyte polymère caractérisés par la structure chimique de la chaîne principale du polymère conducteur ionique comprenant du soufre, p. ex. des polyéthersulfones sulfonés [S-PES]
H01M 8/1025 - Matériaux d’électrolyte polymère caractérisés par la structure chimique de la chaîne principale du polymère conducteur ionique comprenant uniquement du carbone et de l’oxygène, p. ex. des polyéthers, des polyétheréthercétones sulfonés [S-PEEK], des polysaccharides sulfonés, des celluloses sulfonés ou des polyesters sulfonés
H01M 8/1027 - Matériaux d’électrolyte polymère caractérisés par la structure chimique de la chaîne principale du polymère conducteur ionique comprenant du carbone, de l’oxygène et d’autres atomes, p. ex. des polyéthersulfones sulfonés [S- PES]
H01M 8/103 - Matériaux d’électrolyte polymère caractérisés par la structure chimique de la chaîne principale du polymère conducteur ionique comprenant de l’azote, p. ex. des polybenzimidazoles sulfonés [S-PBI], des polybenzimidazoles comprenant de l’acide phosphorique, des polyamides sulfonés [S-PA] ou des polyphosphazènes sulfonés
H01M 8/1039 - Matériaux d’électrolyte polymère halogénés, p. ex. des fluorures de polyvinylidène sulfonés
H01M 8/1053 - Composites ou mélanges à électrolyte polymère constitués de couches de polymères dont au moins une couche est conductrice ionique
H01M 8/1081 - Matériaux d’électrolyte polymère caractérisés par le procédé de fabrication à partir de solutions, de dispersions ou de suspensions de polymères uniquement
H01M 8/1088 - Modification chimique, p. ex. sulfonation
13.
PROCESS AND APPARATUS FOR CATALYTICALLY CRACKING HYDROCARBONS WITH RECYCLED SLURRY FILTER BACKFLUSH
A process for catalytically cracking hydrocarbons is disclosed. The process comprises contacting a hydrocarbon feed stream with a catalyst to catalytically crack the hydrocarbon feed stream to provide a cracked stream and spent catalyst. The spent catalyst is disengaged from the cracked stream in a reactor vessel. Hydrocarbons are stripped from the spent catalyst. The cracked stream is fractionated in a main fractionation column into products comprising a slurry oil stream from a bottom of the main fractionation column. The slurry oil stream is filtered in a filter vessel through a filter to provide a filtered slurry oil stream. Thereafter, the filter is backflushed with a hydrocarbon stream to produce a backflushed hydrocarbon stream comprising catalyst fines. The backflushed hydrocarbon stream is recycled to the reactor vessel. An apparatus for catalytically cracking hydrocarbons is also disclosed.
C10G 11/18 - Craquage catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures avec catalyseurs solides mobiles préchauffés selon la technique du "lit fluidisé"
A process for separating paraffins is disclosed. The process comprises separating a feed stream into a first vapor stream and a first liquid stream. The first vapor stream is fed to a first distillation column at a first inlet. A liquid side stream is taken from the first distillation column. The liquid side stream is separated into a second vapor stream and a second liquid stream. The second vapor stream and said first liquid stream are fractionated in the first distillation column. The liquid side stream is taken from an outlet located above an inlet for passing the first liquid stream in the first distillation column.
A method of increasing aromatic yield, or hydrogen yield, or reformate octane, or combinations thereof for a selected set of operating conditions in a reforming process is described. The process uses a centerpipe having a top connection section, a bottom connection section, and an intermediate connection section in which the diameter of the intermediate section is less than a diameter of the top connection section, or the bottom connection section, or both. This arrangement can be present in one or more of the reforming reactors in the reforming reaction zone. A method of optimizing the diameter of the intermediate section is also described.
B01J 8/04 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes le fluide passant successivement à travers plusieurs lits
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
A process of hydrocracking a feed stream is provided. The hydrocracking process comprises hydrocracking a feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open at least (95) vol% of all rings present in the feed stream to produce a hydrocracked effluent stream that is aliphatic. The feed stream to the hydrocracking process may comprise more than one feedstock. The feed stream to the hydrocracking process may comprise a petroleum origin feed or a biobased feed or a combination of both.
C10G 45/46 - Hydrogénation des hydrocarbures aromatiques caractérisée par le catalyseur utilisé
C10G 65/08 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série ne comprenant que des étapes de raffinage au moins une étape étant une hydrogénation des hydrocarbures aromatiques
A method of increasing aromatic yield, or hydrogen yield, or reformate octane, or combinations thereof for a selected set of operating conditions in a reforming process is described. The process uses a centerpipe having a top connection section, a bottom connection section, and an intermediate connection section in which the diameter of the intermediate section is less than a diameter of the top connection section, or the bottom connection section, or both. This arrangement can be present in one or more of the reforming reactors in the reforming reaction zone. A method of optimizing the diameter of the intermediate section is also described.
C10G 59/02 - Traitement d'essence "naphta" uniquement par plusieurs procédés de réformage, ou par au moins un procédé de réformage et au moins un procédé ne modifiant pas substantiellement le point d'ébullition de l'essence "naphta" uniquement par plusieurs étapes en série
A process of hydrocracking a feed stream is provided. The hydrocracking process comprises hydrocracking a feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open at least 95 vol % of all rings present in the feed stream to produce a hydrocracked effluent stream that is aliphatic. The feed stream to the hydrocracking process may comprise more than one feedstock. The feed stream to the hydrocracking process may comprise a petroleum origin feed or a bio-based feed or a combination of both.
C10G 67/02 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène uniquement par plusieurs étapes en série
A process for separating paraffins is disclosed. The process comprises separating a feed stream into a first vapor stream and a first liquid stream. The first vapor stream is fed to a first distillation column at a first inlet. A liquid side stream is taken from the first distillation column. The liquid side stream is separated into a second vapor stream and a second liquid stream. The second vapor stream and said first liquid stream are fractionated in the first distillation column. The liquid side stream is taken from an outlet located above an inlet for passing the first liquid stream in the first distillation column.
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactor to produce a paraffinic stream. The ethane present in the paraffinic stream is converted into ethylene in a steam cracking unit. An ethylene stream is separated from a C3+ hydrocarbon stream and the C3+ hydrocarbon stream is recycled to the reactor.
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
21.
PROCESS FOR CONVERTING NAPHTHA WITH CRACKED RECYCLE
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactor to produce a paraffinic stream. The ethane present in the paraffinic stream is converted into ethylene in a steam cracking unit. An ethylene stream is separated from a C3+ hydrocarbon stream and the C3+ hydrocarbon stream is recycled to the reactor.
C10G 45/60 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour changer la structure du squelette de certains hydrocarbures sans craquer les autres hydrocarbures présents, p. ex. pour abaisser le point d'écoulementHydrocraquage sélectif des paraffines normales caractérisé par le catalyseur utilisé
C10G 69/06 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique en l'absence d'hydrogène
A process for separating paraffins is disclosed. The process comprises separating a paraffinic stream to provide a first stream comprising C3− hydrocarbons and a second stream comprising C3+ hydrocarbons. The first stream is compressed to provide a first compressed stream. The first compressed stream is fractionated in a fractionation column to provide an overhead stream and a bottom stream comprising C2+ hydrocarbons.
A process for dehydration of an ethanol feed stream comprising sending said ethanol feed stream and steam to a radial flow reactor to contact a catalyst under reaction conditions and produce an effluent comprising ethylene. The use of a radial flow reactor eliminates concerns about pressure drops that may occur with conventional fixed bed downflow reactors.
C07C 1/24 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir de composés organiques ne renfermant que des atomes d'oxygène en tant qu'hétéro-atomes par élimination d'eau
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
A process for separating paraffins is disclosed. The process comprises separating a paraffinic stream to provide a first stream comprising C3- hydrocarbons and a second stream comprising C3+ hydrocarbons. The first stream is compressed to provide a first compressed stream. The first compressed stream is fractionated in a fractionation column to provide an overhead stream and a bottom stream comprising C2+ hydrocarbons.
Processes for recovery of carbon dioxide from a flue gas stream and removal of NOx compounds from the recovered carbon dioxide are described. The processes can recover gaseous, liquid, or supercritical carbon dioxide. The processes incorporate a NOx stripping column after the CO2 fractionation column to remove NOx compounds formed in the CO2 fractionation column.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
F25J 3/02 - Procédés ou appareils pour séparer les constituants des mélanges gazeux impliquant l'emploi d'une liquéfaction ou d'une solidification par rectification, c.-à-d. par échange continuel de chaleur et de matière entre un courant de vapeur et un courant de liquide
A process of producing toluene is disclosed. The process comprises contacting a hydrocarbonaceous feed stream with a dehydrogenation catalyst to produce a dehydrogenated effluent stream. The dehydrogenated effluent stream is separated into a vapor stream comprising hydrogen and a liquid stream. The liquid stream is fractionated to provide a fractionator overhead stream comprising C7-hydrocarbons and a fractionator bottoms stream comprising toluene. The fractionator overhead stream is passed to a stabilizer column to provide an offgas stream.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C07C 5/367 - Formation d'un cycle aromatique à six chaînons à partir d'un cycle à six chaînons existant, p. ex. déshydrogénation de l'éthylcyclohexane en éthylbenzène
C07C 7/09 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par condensation fractionnée
A process of producing toluene is disclosed. The process comprises contacting a hydrocarbonaceous feed stream with a dehydrogenation catalyst to produce a dehydrogenated effluent stream. The dehydrogenated effluent stream is separated into a vapor stream comprising hydrogen and a liquid stream. The liquid stream is fractionated to provide a fractionator overhead stream comprising C7- hydrocarbons and a fractionator bottoms stream comprising toluene. The fractionator overhead stream is passed to a stabilizer column to provide an offgas stream.
C07C 5/367 - Formation d'un cycle aromatique à six chaînons à partir d'un cycle à six chaînons existant, p. ex. déshydrogénation de l'éthylcyclohexane en éthylbenzène
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
A process for production of a liquid fuel is disclosed. The process comprises producing a ethylene stream in a dehydration unit. A C3 olefin stream is produced in a MTO unit. The C3 olefin stream and the ethylene stream are oligomerized with an oligomerization catalyst to produce an oligomerized olefin stream comprising a fuel stream.
C10G 69/12 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de polymérisation ou d'alkylation
A fuel composition comprises at least 85 wt% iso-paraffins, a freezing point of no more than -47C, a final boiling point of no more than 300°C, a density at 15°C of 730 to 772 kg/m3 and at least 3 wt% C17+ hydrocarbons. A blended fuel composition is also disclosed in which the synthetic fuel composition is blended with a natural fuel composition to provide Jet A-1 with a lower freeze point. A process for blending is also disclosed.
Processes and apparatuses for separating carbon monoxide from ethylene. The ethylene may be produced from biobased alcohol. The separation utilizes a fractionation column which produces a carbon monoxide depleted ethylene steam and an overhead steam comprising carbon monoxide and ethylene. The ethylene from the overhead steam may be recovered in an absorption zone with an absorbing liquid. A oxygenate fractionation zone may be utilized to remove oxygenates from the carbon monoxide depleted ethylene stream.
C07C 7/09 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par condensation fractionnée
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
micromicro /totmesotot)micrototmesotot tot represent the non-micropore surface area and total surface area, respectively. The hierarchical metallophosphates of the invention are of use in hydrocarbon conversion processes such as hydroisomerization or dewaxing.
This invention relates to a novel family of hierarchical metallophosphates which are represented by the empirical formula:
This invention relates to a novel family of hierarchical metallophosphates which are represented by the empirical formula:
R
r
+
M
m
2
+
E
P
x
Si
y
O
z
This invention relates to a novel family of hierarchical metallophosphates which are represented by the empirical formula:
R
r
+
M
m
2
+
E
P
x
Si
y
O
z
where M is a divalent framework metal such as magnesium or zinc, R is an organoammonium cation, E is a trivalent framework element such as aluminum or gallium, and in which the hierarchical metallophosphates possess a pore structure having at least 75% of its total surface area being micropore surface area and a hierarchy factor of at least 0.09, said hierarchy factor defined as [(Vmicro/Vtot)*(Smeso/Stot)], where Vmicro and Vtot represent the micropore volume and total pore volume below 450 Å, respectively, and Smeso and Stot represent the non-micropore surface area and total surface area, respectively. The hierarchical metallophosphates of the invention are of use in hydrocarbon conversion processes such as hydroisomerization or dewaxing.
A zeolitic catalyst and a process for its use is provided where the metal, preferably platinum, on the catalyst is not well dispersed as shown by low levels of H2 chemisorption, and low chemisorption hydrogen to platinum ratios. In a process for converting naphtha to light olefins that comprises contacting a naphtha stream with a zeolitic catalyst to produce a light paraffin stream at conditions which dehydrogenate the naphtha to olefins, interconvert the olefins to lighter olefins and hydrogenate the lighter olefins to produce a light paraffin stream comprising ethane and propane, this catalyst produces a higher proportion of ethane.
C07C 5/03 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de liaisons doubles carbone-carbone non aromatiques
C07C 5/32 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par déshydrogénation avec formation d'hydrogène libre
35.
PROCESS FOR INCREASING LIQUID FUEL YIELD FROM CARBON OXIDES
A process for supplementing production of liquid fuel from carbon oxides is disclosed. The process comprises contacting a hydrocarbon feed stream with a catalyst in a reactor to produce a reactor effluent stream. The reactor effluent stream is separated to provide a dry gas stream. The dry gas further separated into a CO2 rich stream and a CO2 lean stream. The CO2 lean stream is used to produce methanol. The methanol is contacted with an MTO catalyst to produce an olefin stream. The olefin stream is oligomerized by contacting it with an oligomerization catalyst in an oligomerization reactor to produce an oligomerized olefin stream which is further hydrogenated. A sustainable aviation fuel is taken from the hydrogenated oligomerized stream.
C10G 69/12 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de polymérisation ou d'alkylation
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
A process of producing jet fuel is disclosed. The process comprises separating lignin from a lignocellulosic biomass to provide a lignin stream. The lignin stream is pyrolyzed and/or hydrotreated to produce an aromatic rich bio-oil stream. The aromatics in the aromatic rich bio-oil stream are alkylated with an alkylating agent to produce an alkylated aromatic product stream. The alkylating agent can be taken from the lignocellulosic biomass. The process produces a green jet fuel.
A process for supplementing production of liquid fuel from carbon oxides is disclosed. The process comprises contacting a hydrocarbon feed stream with a catalyst in a reactor to produce a reactor effluent stream. The reactor effluent stream is separated to provide a dry gas stream. The dry gas further separated into a CO2 rich stream and a CO2 lean stream. The CO2 lean stream is used to produce methanol. The methanol is contacted with an MTO catalyst to produce an olefin stream. The olefin stream is oligomerized by contacting it with an oligomerization catalyst in an oligomerization reactor to produce an oligomerized olefin stream which is further hydrogenated. A sustainable aviation fuel is taken from the hydrogenated oligomerized stream.
C10G 69/12 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de polymérisation ou d'alkylation
A process of producing jet fuel is disclosed. The process comprises separating lignin from a lignocellulosic biomass to provide a lignin stream. The lignin stream is pyrolyzed and/or hydrotreated to produce an aromatic rich bio-oil stream. The aromatics in the aromatic rich bio-oil stream are alkylated with an alkylating agent to produce an alkylated aromatic product stream. The alkylating agent can be taken from the lignocellulosic biomass. The process produces a green jet fuel.
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
39.
CATALYSTS AND PROCESS FOR CATALYTICALLY CONVERTING NAPHTHA TO LIGHT OLEFINS
A zeolitic catalyst and a process for its use is provided where the metal, preferably platinum, on the catalyst is not well dispersed as shown by low levels of H2 chemisorption, and low chemisorption hydrogen to platinum ratios. In a process for converting naphtha to light olefins that comprises contacting a naphtha stream with a zeolitic catalyst to produce a light paraffin stream at conditions which dehydrogenate the naphtha to olefins, interconvert the olefins to lighter olefins and hydrogenate the lighter olefins to produce a light paraffin stream comprising ethane and propane, this catalyst produces a higher proportion of ethane.
C07C 7/13 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par adsorption, c.-à-d. purification ou séparation d'hydrocarbures à l'aide de solides, p. ex. à l'aide d'échangeurs d'ions par la technique du tamis moléculaire
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C07C 7/20 - Emploi d'additifs, p. ex. pour la stabilisation
A hydrocarbon conversion process is disclosed. The process introduces a feed stream comprising hydrocarbons into a vessel having a refractory lining. The refractory lining comprises a refractory material and reinforcement metallic fibers. The reinforcement metallic fibers comprise about 0.5 wt % to about 8 wt % aluminum, 10 wt % to about 35 wt % chromium, and no less than about 50 wt % iron. The hydrocarbons are converted in the vessel at conversion conditions with or without a catalyst to yield a product stream.
C10G 75/04 - Inhibition de la corrosion ou des salissures dans des appareils de traitement ou de conversion des huiles d'hydrocarbures, en général par addition d'agents antisalissures
B01J 19/02 - Appareils caractérisés par le fait qu'ils sont construits avec des matériaux choisis pour leurs propriétés de résistance aux agents chimiques
C04B 35/76 - Fibres, filaments, "whiskers", paillettes ou analogues
41.
PROCESS FOR PRODUCING 5-HYDROXYMETHYLFURFURAL USING METAL PHOSPHATES
Processes for synthesizing 5-hydroxymethylfurfural are described. The processes comprise contacting a feed comprising biomass-derived cellulose, or a sugar monomer or oligomer, or a mixture thereof with a catalyst comprising a metal phosphate. The metal phosphate may comprise hafnium phosphate, or zirconium phosphate, or combinations thereof. The catalyst has a ratio of Bronsted acid sites to Lewis acid sites greater than or equal to 0.27 and a total acid density less than or equal to 0.4.
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactant passage of a reactor to produce a light paraffinic stream. The reactant passage is cooled by indirect heat exchange with a heat transferred media in a cooling passage adjacent to the reactant passage. The light paraffinic stream is separated into an ethane stream and a propane stream.
C10G 47/30 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur avec des particules solides en mouvement selon la technique du "lit fluidisé"
43.
PROCESS FOR CONVERTING NAPHTHA TO PARAFFINS WITH HYDROCRACKED CHARGE STREAMS
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream with a catalyst and hydrogen to produce a light paraffinic stream. The light paraffinic stream is separated into an ethane stream and a propane stream. The ethane stream is thermally cracked to produce ethylene and a pyrolysis gasoline by-product stream. The pyrolysis gasoline stream is hydrocracked to provide a cracked naphtha stream. The cracked naphtha stream may be contacted with a catalyst and hydrogen with the naphtha stream.
C10G 63/04 - Traitement d'essence "naphta" par au moins un procédé de réformage et au moins un procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage
44.
HYDROTREATING CATALYST FOR REMOVAL OF CONTAMINANTS FROM HYDROPROCESSING FEEDS
A hydroprocessing catalyst is provided that is made with an organic acid, such as tartaric acid, that provides for an improved capacity for removal of silicon from hydrocarbon feeds. The silicon acts as a poison to the catalyst when not removed. The catalyst has more available hydroxyl sites than catalysts made using other impregnation liquids besides tartaric acid.
C10G 45/08 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage caractérisé par le catalyseur utilisé contenant du nickel ou du cobalt, ou leurs composés en combinaison avec du chrome, du molybdène ou du tungstène, ou leurs composés
45.
PROCESS FOR CONVERTING NAPHTHA WITH PROPANE RECYCLE
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactor to produce a light paraffinic stream. The light paraffinic stream is separated into an ethane stream and a propane stream. A propane recycle stream taken from the propane stream is recycled to the reactor.
An apparatus for supporting conduits in a radial flow reactor. A support plate rests on an internal surface of the reactor below a cylindrical wall of the reactor. Lugs are connected to the support plate and a support ring is supported by the lugs. The conduits are supported by the support ring. Stabilizing plates may be utilized. Also a process of installing such a supporting apparatus in a reactor.
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
B01J 8/04 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes le fluide passant successivement à travers plusieurs lits
B01J 8/06 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes dans des réacteurs tubulairesProcédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes les particules solides étant disposées dans des tubes
B01J 19/30 - Éléments de remplissage non agglomérés ou en forme, p. ex. anneaux de Raschig ou éléments de Berl en forme de selle, destinés à être versés dans l'appareil de transfert de chaleur ou de matière
47.
PROCESSES AND APPARATUSES FOR REDUCING MOLECULAR WEIGHT FLUCTUATION IN A TAIL GAS STREAM FROM A PRESSURE SWING ADSORPTION PROCESS
Processes and apparatuses for reducing molecular weight fluctuation in a tail gas stream from a pressure swing adsorption process. The steps of the vessels in the PSA separation zone are synchronized such that when one of the vessels is generating a low molecular weight tail gas, there is another vessel generating a high molecular weight tail gas. Additionally, the steps may be split into sub-steps that utilize gas streams with different pressures/flow rates.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
Processes and apparatuses for reducing molecular weight fluctuation in a tail gas stream from a pressure swing adsorption process. Multiple PSA separation zone are synchronized such that when one of the PSA units is generating a low molecular weight tail gas, there is another PSA unit generating a high molecular weight tail gas.
A process for converting naphtha to ethane and propane is disclosed. The process comprises separating a naphtha stream into a plurality of naphtha streams. Each of the plurality of naphtha streams and a hydrogen stream are contacted with a catalyst in a dedicated one of a plurality of reactors to produce a plurality of contacted streams. One of the contacted streams can be separated into an ethane stream and a propane stream.
A process for converting naphtha to ethane and propane is disclosed. The process comprises contacting a naphtha stream with a catalyst in a reactor to produce a converted stream. The converted stream is separated into a light paraffin stream and an aromatic stream. The aromatic stream is recycled to the reactor. The light paraffin stream is separated into an ethane stream and a propane stream.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C07C 5/03 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de liaisons doubles carbone-carbone non aromatiques
C10G 47/02 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur caractérisé par le catalyseur utilisé
51.
PROCESS FOR PRODUCING 5-HYDROXYMETHYLFURFURAL USING METAL PHOSPHATES
Processes for synthesizing 5 -hydroxymethylfurfural are described. The processes comprise contacting a feed comprising biomass-derived cellulose, or a sugar monomer or oligomer, or a mixture thereof with a catalyst comprising a metal phosphate. The metal phosphate may comprise hafnium phosphate, or zirconium phosphate, or combinations thereof. The catalyst has a ratio of Bronsted acid sites to Lewis acid sites greater than or equal to 0.27 and a total acid density less than or equal to 0.4.
A process for catalytic production of olefins comprises of passing a n-paraffin rich stream to an isomerization unit to provide a first hydrocarbon stream rich in iso-paraffins and contacting a first hydrocarbon stream with a first stream of fluid catalyst in a first reactor riser to produce a first mixture of spent catalyst and product gases. The process comprises separating, in a first disengagement vessel, the first mixture of spent catalyst and product gases into a first cracked product stream and a first stream of cool catalyst. The process comprises contacting a second hydrocarbon stream with a second stream of fluid catalyst in a second reactor riser to produce a second mixture of spent catalyst and product gases. Separating, in a second disengagement vessel, the second mixture of spent catalyst and product gases to provide a second cracked product stream and a second stream of cool catalyst. The first cracked product stream and the second cracked product stream are passed upwardly through a gas recovery conduit, and further separating from catalyst in a series of cyclones to produce a hot product stream.
C10G 57/02 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de craquage ou de raffinage et au moins un autre procédé de conversion avec polymérisation
C10G 11/18 - Craquage catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures avec catalyseurs solides mobiles préchauffés selon la technique du "lit fluidisé"
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
53.
PROCESS FOR CONVERTING NAPHTHA TO PARAFFINS WITH HYDROCRACKED CHARGE STREAMS
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream with a catalyst and hydrogen to produce a light paraffinic stream. The light paraffinic stream is separated into an ethane stream and a propane stream. The ethane stream is thermally cracked to produce ethylene and a pyrolysis gasoline by-product stream. The pyrolysis gasoline stream is hydrocracked to provide a cracked naphtha stream. The cracked naphtha stream may be contacted with a catalyst and hydrogen with the naphtha stream.
C10G 69/06 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique en l'absence d'hydrogène
C10G 69/08 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de réformage d'essence "naphta"
C10G 65/12 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série comprenant des étapes de craquage et d'autres étapes d'hydrotraitement
C10G 47/00 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur
A process is provided to produce increased amounts of cycloparaffin compounds in a methanol to jet fuel process by modifying the olefin oligomerization step that after hydrogenation provides the increased quantities of cycloparaffins for jet fuel. A two stage oligomerization process is employed in which an acidic catalyst such as a zeolite is in one reactor and a metal, such as nickel, on alumina catalyst is in a second reactor. The two stages may be in either order in the process. A small amount of aromatic compounds may be added to the feed to achieve the desired level of cycloparaffins in the product. Adjustments to other aspects of the process may also help to provide a product with higher cycloparaffin content.
C07C 1/24 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir de composés organiques ne renfermant que des atomes d'oxygène en tant qu'hétéro-atomes par élimination d'eau
C07C 5/03 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de liaisons doubles carbone-carbone non aromatiques
55.
PROCESS FOR PRODUCING HYDROGEN FROM HYDROGEN-CONTAINING GAS
Processes for producing hydrogen from hydrogen-containing gas streams, such as coke oven gas (COG), steam cracker off gas, delayed coker off gas, and syngas from low-temperature gasification processes, are described. A hydrogen membrane separation unit separates a hydrogen-containing stream into a hydrogen-rich permeate stream and a hydrogen-lean residue stream. The hydrogen-lean residue stream is sent to a methane reforming zone for conversion of the methane and other light hydrocarbons to hydrogen. The hydrogen is then recovered in a hydrogen recovery zone. The hydrogen-containing stream can be pretreated to remove contaminants, if desired.
C01B 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
56.
PROCESSES AND APPARATUSES FOR SUPPORTING CONDUITS IN A RADIAL FLOW REACTOR
An apparatus for supporting conduits in a radial flow reactor. A support plate rests on an internal surface of the reactor below a cylindrical wall of the reactor. Lugs are connected to the support plate and a support ring is supported by the lugs. The conduits are supported by the support ring. Stabilizing plates may be utilized. Also a process of installing such a supporting apparatus in a reactor.
B01J 8/02 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés avec des particules immobiles, p. ex. dans des lits fixes
57.
PROCESS FOR CRACKING TO LIGHT OLEFINS WITH ISOMERIZATION
We have discovered a process for catalytic production of olefins comprising passing a feed stream to an isomerization unit to provide a first hydrocarbon stream rich in iso-paraffins. The first hydrocarbon stream is contacted with a first stream of fluid catalyst in a first reactor riser to produce a first mixture of spent catalyst and product gases. The first mixture of spent catalyst and product gases is separated into a first cracked product stream and a first stream of cool catalyst. A dilute ethylene stream is separated from the first cracked product stream which is oligomerized to produce a second hydrocarbon stream comprising C4+ oligomers. The second hydrocarbon stream is contacted with a second stream of fluid catalyst in a second reactor riser to produce a second mixture of spent catalyst and product gases.
C10G 57/02 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de craquage ou de raffinage et au moins un autre procédé de conversion avec polymérisation
58.
PROCESS FOR CONVERTING NAPHTHA TO LIGHT PARAFFINS WITH RECYCLE
A process for converting naphtha to ethane and propane is disclosed. The process comprises contacting a naphtha stream with a catalyst in a reactor to produce a converted stream. The converted stream is separated into a light paraffin stream and an aromatic stream. The aromatic stream is recycled to the reactor. The light paraffin stream is separated into an ethane stream and a propane stream.
A process for converting naphtha to ethane and propane is disclosed. The process comprises separating a naphtha stream into a plurality of naphtha streams. Each of the plurality of naphtha streams and a hydrogen stream are contacted with a catalyst in a dedicated one of a plurality of reactors to produce a plurality of contacted streams. One of the contacted streams can be separated into an ethane stream and a propane stream.
C10G 47/00 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur
C10G 55/06 - Traitement des huiles d'hydrocarbures, en l'absence d'hydrogène, par au moins un procédé de raffinage et par au moins un procédé de craquage uniquement par plusieurs étapes en série comprenant au moins une étape de craquage catalytique
60.
HYDROTREATING CATALYST FOR REMOVAL OF CONTAMINANTS FROM HYDROPROCESSING FEEDS
A hydroprocessing catalyst is provided that is made with an organic acid, such as tartaric acid, that provides for an improved capacity for removal of silicon from hydrocarbon feeds. The catalyst has more available hydroxyl sites than catalysts made using other impregnation liquids besides tartaric acid.
B01J 31/02 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant des composés organiques ou des hydrures métalliques
C10G 45/04 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage caractérisé par le catalyseur utilisé
Aromatic transalkylation processes are described which reduce the hydrogen makeup gas requirement to the aromatic transalkylation unit and improve the energy efficiency of the aromatics complex. The processes may utilize a hot separator, optionally one or more flash drums, and optionally a stripper column. The aromatic transalkylation separator bottom liquid may be preheated and flashed to a low-pressure drum to separate light hydrocarbons, such Ci to Cs, as a vapor stream from the aromatics rich liquid hydrocarbons stream. A portion of flash drum liquid may recycled back to a product condenser inlet as a sponge liquid to absorb the light hydrocarbons from the reactor effluent stream and thereby improve the hydrogen purity of the recycle gas (RG) without purging RG.
C07C 6/12 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un nombre différent d'atomes de carbone par des réactions de redistribution par conversion d'une liaison carbone-carbone saturée exclusivement dans les hydrocarbures contenant un cycle aromatique à six chaînons
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C07C 7/144 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par emploi de membranes, p. ex. par perméation sélective
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
62.
PROCESSES AND APPARATUSES FOR REMOVING CARBON MONOXIDE FROM AN ETHYLENE STREAM
Processes and apparatuses for separating carbon monoxide from ethylene. The ethylene may be produced from biobased alcohol. The separation utilizes a fractionation column which produces a carbon monoxide depleted ethylene steam and an overhead steam comprising carbon monoxide and ethylene. The ethylene from the overhead steam may be recovered in an absorption zone with an absorbing liquid. A oxygenate fractionation zone may be utilized to remove oxygenates from the carbon monoxide depleted ethylene stream.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C07C 7/10 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par extraction, c.-à-d. purification ou séparation d'hydrocarbures liquides à l'aide de liquides
A process is provided to produce increased amounts of cycloparaffin compounds in a methanol to jet fuel process by modifying the olefin oligomerization step that after hydrogenation provides the increased quantities of cycloparaffins for jet fuel. A two stage oligomerization process is employed in which an acidic catalyst such as a zeolite is in one reactor and a metal, such as nickel, on alumina catalyst is in a second reactor. The two stages may be in either order in the process. A small amount of aromatic compounds may be added to the feed to achieve the desired level of cycloparaffins in the product. Adjustments to other aspects of the process may also help to provide a product with higher cycloparaffin content.
C10G 69/12 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de polymérisation ou d'alkylation
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
64.
ISOTHERMAL PROCESS FOR CONVERTING NAPHTHA TO LIGHT PARAFFINS
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactant passage of a reactor to produce a light paraffinic stream. The reactant passage is cooled by indirect heat exchange with a heat transferred media in a cooling passage adjacent to the reactant passage. The light paraffinic stream is separated into an ethane stream and a propane stream.
C07C 5/03 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de liaisons doubles carbone-carbone non aromatiques
C10G 47/02 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur caractérisé par le catalyseur utilisé
65.
PROCESS FOR CONVERTING NAPHTHA WITH PROPANE RECYCLE
A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactor to produce a light paraffinic stream. The light paraffinic stream is separated into an ethane stream and a propane stream. A propane recycle stream taken from the propane stream is recycled to the reactor.
C10G 47/02 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur caractérisé par le catalyseur utilisé
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
C10G 69/06 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de craquage thermique en l'absence d'hydrogène
66.
AN INTEGRATED PROCESS TO PRODUCE PHENOL FROM COAL DERIVED LIQUID
Process for producing phenol, cresol and xylenes from a coal-derived feed are described. The processes combine dealkylation of alkylphenols from coal derived liquids followed by benzene and/or toluene transalkylation to reduce the production of non-ideal alkylbenzenes and reduce the usage of benzene/toluene. Alkylphenols from the coal derived liquids are converted in a dealkylation reaction zone comprising a dealkylation reactor to make phenol. The unconverted alkylphenols and an aromatic compound, such as benzene or toluene, are fed to a transalkylation reaction zone comprising a transalkylation reactor to make more phenol. Cresols and xylenes can also be produced.
C07C 37/50 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone d'un cycle aromatique à six chaînons par des réactions diminuant le nombre d'atomes de carbone
C07C 6/12 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un nombre différent d'atomes de carbone par des réactions de redistribution par conversion d'une liaison carbone-carbone saturée exclusivement dans les hydrocarbures contenant un cycle aromatique à six chaînons
C07C 37/48 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone d'un cycle aromatique à six chaînons par échange de groupes hydrocarbonés, éventuellement substitués, avec d'autres composés, p. ex. par transalkylation
Processes and apparatuses for reducing molecular weight fluctuation in a tail gas stream from a pressure swing adsorption process. Multiple PSA separation zone are synchronized such that when one of the PSA units is generating a low molecular weight tail gas, there is another PSA unit generating a high molecular weight tail gas.
Processes and apparatuses for separating carbon monoxide from ethylene. The ethylene may be produced from biobased alcohol. The separation utilizes a fractionation column which produces a carbon monoxide depleted ethylene stream and an overhead stream comprising carbon monoxide and ethylene. The ethylene from the overhead stream may be recovered in an absorption zone with an absorbing liquid. A oxygenate fractionation zone may be utilized to remove oxygenates from the carbon monoxide depleted ethylene stream.
C07C 7/04 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par distillation
C07C 1/24 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir de composés organiques ne renfermant que des atomes d'oxygène en tant qu'hétéro-atomes par élimination d'eau
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C07C 7/09 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par condensation fractionnée
C07C 7/11 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par absorption, c.-à-d. purification ou séparation d'hydrocarbures gazeux à l'aide de liquides
A process for upgrading a bio-oil stream is disclosed. The process comprises reacting a bio-oil stream with hydrogen in the presence of a catalyst in a reactor to produce an upgraded bio-oil stream. The upgraded bio-oil stream is charged to an FCC unit, a hydroprocessing unit, or a reforming unit to produce an intermediate blend or a fuel stream. A fuel oil stream can be taken from the upgraded bio-oil stream. The catalyst may be separated and recycled to the reactor. The upgraded bio-oil stream can be used directly to produce an intermediate blend or fuel. A fuel oil stream may be taken from the upgraded bio-oil stream.
A process for upgrading a bio-oil stream is disclosed. The process comprises reacting a bio-oil stream with hydrogen in the presence of a catalyst in a reactor to produce an upgraded bio-oil stream. A recycle oil stream is taken from the upgraded bio-oil stream. The recycle oil stream is recycled to the reactor to provide the upgraded bio-oil stream. Concentration of functional groups such as an oxygenate group in the recycle oil stream is measured. Based on the measurement of the concentration of the oxygenate in the recycle oil stream, the recycle rate of the recycle oil stream can be adjusted.
Aromatic transalkylation processes are described which reduce the hydrogen makeup gas requirement to the aromatic transalkylation unit and improve the energy efficiency of the aromatics complex. The processes may utilize a hot separator, optionally one or more flash drums, and optionally a stripper column. The aromatic transalkylation separator bottom liquid may be preheated and flashed to a low-pressure drum to separate light hydrocarbons, such C1 to C5, as a vapor stream from the aromatics rich liquid hydrocarbons stream. A portion of flash drum liquid may recycled back to a product condenser inlet as a sponge liquid to absorb the light hydrocarbons from the reactor effluent stream and thereby improve the hydrogen purity of the recycle gas (RG) without purging RG.
C07C 7/09 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par condensation fractionnée
C07C 7/00 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs
C07C 7/10 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par extraction, c.-à-d. purification ou séparation d'hydrocarbures liquides à l'aide de liquides
C07C 7/144 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par emploi de membranes, p. ex. par perméation sélective
72.
INTEGRATED HYDROGEN PRODUCTION AND CARBON DIOXIDE RECOVERY PROCESS
Integrated processes for hydrogen production and carbon dioxide recovery are described. The processes use a chilling stream in a cryogenic carbon dioxide recovery unit. The chilling stream chills a working fluid which chills the hydrogen- depleted tail gas stream from a hydrogen pressure swing adsorption (PSA) unit to form a carbon dioxide product stream.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01D 53/34 - Épuration chimique ou biologique des gaz résiduaires
C01B 3/48 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants suivie par une réaction de la vapeur d'eau avec l'oxyde de carbone
C01B 3/56 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés
A process for upgrading a bio-oil stream is disclosed. The process comprises reacting a bio-oil stream with hydrogen in the presence of a catalyst and a stable oil in a reactor to produce an upgraded bio-oil stream. A recycle oil stream is taken from the upgraded bio-oil stream. The recycle oil stream is recycled to the reactor to provide the stable oil. The content of the reactor can be measured using various techniques and characterized based on the concentration of one or more functional groups for example oxygenates. Further, a fuel oil stream can be taken from the upgraded bio-oil stream.
Integrated processes for hydrogen production and carbon dioxide recovery are described. The processes use a chilling stream in a cryogenic carbon dioxide recovery unit. The chilling stream chills a working fluid which chills the hydrogen-depleted tail gas stream from a hydrogen pressure swing adsorption (PSA) unit to form a carbon dioxide product stream.
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
Anion exchange polymers with both anion exchange functional groups and amine functional groups have been developed for use in AEMs. The polymer comprises a plurality of repeating units of formula (I). Anion exchange membranes and membrane electrode assemblies incorporating the anion exchange polymers are also described. Membranes made using the anion exchange polymer have low gas or electrolyte crossover, high mechanical strength, low swelling, high performance, and high long term stability.
C08G 10/00 - Polymères de condensation obtenus uniquement à partir d'aldéhydes ou de cétones avec des hydrocarbures aromatiques ou avec leurs dérivés halogénés
C08G 61/12 - Composés macromoléculaires contenant d'autres atomes que le carbone dans la chaîne principale de la macromolécule
B01J 41/13 - Composés macromoléculaires obtenus autrement que par des réactions ne faisant intervenir que des liaisons carbone-carbone non saturées
C25B 13/08 - DiaphragmesÉléments d'espacement caractérisés par le matériau à base de matériaux organiques
H01M 8/103 - Matériaux d’électrolyte polymère caractérisés par la structure chimique de la chaîne principale du polymère conducteur ionique comprenant de l’azote, p. ex. des polybenzimidazoles sulfonés [S-PBI], des polybenzimidazoles comprenant de l’acide phosphorique, des polyamides sulfonés [S-PA] ou des polyphosphazènes sulfonés
76.
ANION EXCHANGE POLYMERS AND MEMBRANES FOR ELECTROLYSIS
Anion exchange polymers with both anion exchange functional groups and amine functional groups have been developed for use in AEMs. The polymer comprises a plurality of repeating units of formula (I)
Anion exchange polymers with both anion exchange functional groups and amine functional groups have been developed for use in AEMs. The polymer comprises a plurality of repeating units of formula (I)
Anion exchange polymers with both anion exchange functional groups and amine functional groups have been developed for use in AEMs. The polymer comprises a plurality of repeating units of formula (I)
Anion exchange membranes and membrane electrode assemblies incorporating the anion exchange polymers are also described. Membranes made using the anion exchange polymer have low gas or electrolyte crossover, high mechanical strength, low swelling, high performance, and high long term stability.
Hydrodeoxygenating a biorenewable feed that is concentrated in free fatty acids with 12 and 14 carbon atoms at a moderate hydrodeoxygenation ratio that is less than the ratio of hydrodeoxygenation utilized for traditional biorenewable feeds such as vegetable oil or even mineral feedstocks, normal paraffins in the range desired by the detergents industry can be produced. Either hydroisomerization or an iso-normal separation can be performed to provide green fuel streams. Two reactors are proposed, one for hydrodeoxygenation of the biorenewable feed that is concentrated in free fatty acids with 12 and 14 carbon atoms and the other for a traditional biorenewable feed or even a mineral feed operated at a higher deoxygenation ratio.
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C07C 2/64 - Addition sur un atome de carbone d'un cycle aromatique à six chaînons
C07C 2/76 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un plus petit nombre d'atomes de carbone par condensation d'hydrocarbures avec élimination partielle d'hydrogène
C07C 15/107 - Hydrocarbures monocycliques comportant une chaîne latérale saturée contenant au moins six atomes de carbone, p. ex. dérivés alkylés pour détergents
C10G 45/02 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage
C10G 45/58 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour changer la structure du squelette de certains hydrocarbures sans craquer les autres hydrocarbures présents, p. ex. pour abaisser le point d'écoulementHydrocraquage sélectif des paraffines normales
78.
METHOD OF MAKING A CATALYST INK AND CONTINUOUS CATALYST INK MIXING SYSTEM
Methods of continuously dispersing catalyst inks for use in coating processes are described. The catalyst ink is continuously mixed in a high shear mixing unit, and the mixed ink is sonicated in a sonication unit. Part of the sonicated catalyst ink is returned to the high shear mixing unit. The method provides continuous mixing and sonicating of the catalyst ink. The mixed and sonicated ink can then be applied to a substrate in a defined pattern.
Cu/M2+M3+oxide or CuO/M2+M3+oxide catalysts have been developed for use in producing isobutanol in propanol-methanol, ethanol-methanol and propanol/ethanol mixture-methanol Guerbet reactions. The catal sts can also be used in makin n-butanol in ethanol-ethanol reactions. The Cu/M2+M3+oxide or CuO/M2M3oxide catalyst has an average Cu or CuO particle size greater than or equal to 20 nm. M2+may comprise divalent magnesium, calcium, strontium, barium, zinc, or combinations thereof. M3+ may comprise trivalent aluminum, gallium, chromium, or combinations thereof. Catalysts, methods of making the catalysts, and methods of using the catalysts are described.
B01J 35/30 - Catalyseurs caractérisés par leur forme ou leurs propriétés physiques, en général caractérisés par leurs propriétés physiques
B01J 23/78 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe du cuivre ou des métaux du groupe du fer en combinaison avec des métaux, oxydes ou hydroxydes prévus dans les groupes avec des métaux alcalins ou alcalino-terreux ou du béryllium
B01J 23/825 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe du cuivre ou des métaux du groupe du fer en combinaison avec des métaux, oxydes ou hydroxydes prévus dans les groupes avec du gallium, de l'indium ou du thallium
B01J 23/80 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe du cuivre ou des métaux du groupe du fer en combinaison avec des métaux, oxydes ou hydroxydes prévus dans les groupes avec du zinc, du cadmium ou du mercure
C07C 29/34 - Préparation de composés comportant des groupes hydroxyle ou O-métal liés à un atome de carbone ne faisant pas partie d'un cycle aromatique à six chaînons par des réactions augmentant le nombre d'atomes de carbone sans formation de groupes hydroxyle par condensation impliquant des groupes hydroxyle, ou leurs esters d'acides minéraux, p. ex. réaction de Guerbet
B01J 37/02 - Imprégnation, revêtement ou précipitation
A process for oligomerizing and oligomerizing olefins to distillate fuels which regenerates a first stage oligomerization catalyst bed and/or a second oligomerization catalyst bed in situ by contact with an oxygen gas at elevated temperature. Purge and pressurization of the oligomerization catalyst bed before regeneration and pressure maintenance after regeneration can be achieved with an inert gas provided by carbon dioxide generated from fermenting starches and sugars from biomass to make alcohol or from carbon burn in the regeneration process. The alcohol can also be dehydrated to olefins to provide the olefin charge stream for oligomerization. The oligomerization catalyst can be restored to full activity. A regeneration process can enable continuous operation.
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
B01J 38/12 - Traitement avec un gaz contenant de l'oxygène libre
C12P 1/00 - Préparation de composés ou de compositions, non prévue dans les groupes , utilisant des micro-organismes ou des enzymesProcédés généraux de préparation de composés ou de compositions utilisant des micro-organismes ou des enzymes
C12P 7/02 - Préparation de composés organiques contenant de l'oxygène contenant un groupe hydroxyle
81.
INTEGRATED STEAM CRACKING AND HYDROGEN PRODUCTION PROCESS
Integrated steam cracking processes and hydrogen production processes are described. The steam cracker off gas stream and the synthesis gas stream are sent to the separation zone of the hydrogen production process and separated into a hydrogen stream, a carbon dioxide stream, and a second off gas stream in a separation zone. The second off gas stream comprises methane from the synthesis gas and methane from the steam cracker off gas stream, as well as carbon monoxide from the synthesis gas stream. All or a portion of the hydrogen product stream is sent to the steam cracking zone as fuel for the steam cracker reactor. The remainder (if any) of the hydrogen product stream can be recovered. The second off gas stream is sent to the hydrogen production zone as feed for the synthesis gas reactor. The carbon dioxide can be recovered.
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
C01B 3/56 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés
C01B 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
C10G 9/36 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par contact direct avec des fluides inertes préchauffés, p. ex. avec des métaux ou sels fondus avec des gaz ou vapeurs chauds
Methods of continuously dispersing catalyst inks for use in coating processes are described. The catalyst ink is continuously mixed in a high shear mixing unit, and the mixed ink is sonicated in a sonication unit. Part of the sonicated catalyst ink is returned to the high shear mixing unit. The method provides continuous mixing and sonicating of the catalyst ink. The mixed and sonicated ink can then be applied to a substrate in a defined pattern.
C25B 9/23 - Cellules comprenant des électrodes fixes de dimensions stablesAssemblages de leurs éléments de structure avec des diaphragmes comprenant des membranes échangeuses d'ions dans ou sur lesquelles est incrusté du matériau pour électrode
C25B 11/051 - Électrodes comportant des électro-catalyseurs sur un substrat ou un support
84.
PROCESS FOR REGENERATING OLIGOMERIZATION CATALYST WITH PURGE
A process for oligomerizing and oligomerizing olefins to distillate fuels which regenerates a first stage oligomerization catalyst bed and/or a second oligomerization catalyst bed in situ by contact with an oxygen gas at elevated temperature. Purge and pressurization of the oligomerization catalyst bed before regeneration and pressure maintenance after regeneration can be achieved with an inert gas provided by carbon dioxide generated from fermenting starches and sugars from biomass to make alcohol or from carbon burn in the regeneration process. The alcohol can also be dehydrated to olefins to provide the olefin charge stream for oligomerization. The oligomerization catalyst can be restored to full activity. A regeneration process can enable continuous operation.
C10G 69/10 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de réformage d'essence "naphta" un hydrocraquage des fractions à haut point d'ébullition en essence "naphta" et un réformage de l'essence "naphta" obtenue
C10G 35/24 - Commande ou régulation des opérations de réformage
C10G 45/58 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour changer la structure du squelette de certains hydrocarbures sans craquer les autres hydrocarbures présents, p. ex. pour abaisser le point d'écoulementHydrocraquage sélectif des paraffines normales
86.
INTEGRATED STEAM CRACKING AND HYDROGEN PRODUCTION PROCESS
Integrated steam cracking processes and hydrogen production processes are described. The steam cracker off gas stream and the synthesis gas stream are sent to the separation zone of the hydrogen production process and separated into a hydrogen stream, a carbon dioxide stream, and a second off gas stream in a separation zone. The second off gas stream comprises methane from the synthesis gas and methane from the steam cracker off gas stream, as well as carbon monoxide from the synthesis gas stream. All or a portion of the hydrogen product stream is sent to the steam cracking zone as fuel for the steam cracker reactor. The remainder (if any) of the hydrogen product stream can be recovered. The second off gas stream is sent to the hydrogen production zone as feed for the synthesis gas reactor. The carbon dioxide can be recovered.
B01D 53/00 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols
B01D 53/22 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par diffusion
C01B 3/24 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par décomposition de composés organiques gazeux ou liquides d'hydrocarbures
C01B 3/36 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants avec l'oxygène ou des mélanges contenant de l'oxygène comme agents gazéifiants
C01B 3/48 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants suivie par une réaction de la vapeur d'eau avec l'oxyde de carbone
C01B 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
C01B 3/56 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés
Systems and processes for removing sulfur compounds from a hydrocarbon stream. Sulfur compounds are extracted from a hydrocarbon feed stream with a caustic stream to provide a treated hydrocarbon stream and a rich caustic stream. The sulfur compounds in the rich caustic stream are oxidized in the presence of a catalyst to provide a lean caustic stream. The lean caustic stream is returned to extract sulfur from the hydrocarbon stream. Data such as a concentration of sulfurs species and degree of caustic saturation with the sulfur species in the rich caustic stream may be provided by a sensor, compared against other real-time or historical data and used to provide a recommended adjustment to process conditions associated with an extraction unit, or an oxidation unit, or both.
A catalyst regenerator vessel and a process for combusting carbonaceous deposits from catalyst is disclosed. The catalyst regenerator vessel comprises a combustion gas distributor in fluid communication with a combustion gas line for introducing a combustion gas to the vessel, a catalyst pipe, and a catalyst distributor in fluid communication with the catalyst pipe. The catalyst distributor comprises a header and a nozzle, the header and the nozzle are in fluid communication with the catalyst pipe for distributing coked catalyst to the vessel. The header comprises a header and a plurality of nozzles including an angular nozzle projecting at an angle to a longitudinal axis of the header. The process comprises delivering coked catalyst from a catalyst pipe to the catalyst distributor wherein the catalyst distributor discharges the coked catalyst from at least two sides of the catalyst pipe into the regenerator vessel.
B01J 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
B01J 8/18 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées
B01J 38/04 - Traitement avec un gaz ou une vapeurTraitement avec des liquides vaporisables au contact du catalyseur épuisé
C10G 11/18 - Craquage catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures avec catalyseurs solides mobiles préchauffés selon la technique du "lit fluidisé"
89.
SYSTEMS AND PROCESS FOR CALIBRATING A SENSOR USED IN A SULFUR EXTRACTION PROCESS
Systems and processes for removing sulfur compounds from a hydrocarbon stream. Sulfur compounds are extracted from a hydrocarbon feed stream with a caustic stream to provide a treated hydrocarbon stream and a rich caustic stream. The sulfur compounds in the rich caustic stream are oxidized in the presence of a catalyst to provide a lean caustic stream. The lean caustic stream is returned to extract sulfur from the hydrocarbon stream. Data such as a concentration of sulfurs species and degree of caustic saturation with the sulfur species in the rich caustic stream may be provided by a sensor, compared against other real-time or historical data and used to provide a recommended adjustment to process conditions associated with an extraction unit, or an oxidation unit, or both.
B01D 53/14 - Séparation de gaz ou de vapeursRécupération de vapeurs de solvants volatils dans les gazÉpuration chimique ou biologique des gaz résiduaires, p. ex. gaz d'échappement des moteurs à combustion, fumées, vapeurs, gaz de combustion ou aérosols par absorption
90.
HEAVY AROMATIC CONVERSION FOR INCREASED BTX PRODUCTION
The processes upgrade a low value heavy aromatics stream into a high value BTX precursor stream. It treats the naphthalenic molecules in the heavy aromatics stream comprising C9 to C12 aromatics prior to reaching the transalkylation reactor. The naphthalenic molecules are converted into BTX precursors by partially hydrogenating one of the aromatic rings and subsequently ring opening the saturated ring to form a monoaromatic prior to the transalkylation reactor. With naphthalene no longer present, the remaining C11 monoaromatics may be processed in the aromatics complex for an overall increased BTX production.
C07C 6/12 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un nombre différent d'atomes de carbone par des réactions de redistribution par conversion d'une liaison carbone-carbone saturée exclusivement dans les hydrocarbures contenant un cycle aromatique à six chaînons
91.
CONTROL PROCESS FOR LIQUID ORGANIC HYDROGEN CARRIER PROCESS
Processes for controlling liquid organic hydrogen carrier processes are described. The processes include flow control of hydrogen as the primary variable with toluene make- up based on reactor conditions. Make-up hydrogen gas is provided via a flow controller which can be adjusted by the operator. A pressure controller on the separator is used to adjust the temperature at the reactors with a temperature controller. The inlet temperature to the reactors is maintained by heat exchangers, such as steam generators. The reaction conditions are monitored by temperature measurement and the inlet and/or the outlet of the reactor. When hydrogen feed rates are adjusted, the unit operations must increase or reduce the toluene to balance this situation. A differential temperature controller is used to reset the toluene flowrate to the reactor to achieve the desired processing objective.
C01B 3/00 - HydrogèneMélanges gazeux contenant de l'hydrogèneSéparation de l'hydrogène à partir de mélanges en contenantPurification de l'hydrogène
C01B 3/34 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air par réaction d'hydrocarbures avec des agents gazéifiants
A catalyst regenerator vessel and a process for combusting carbonaceous deposits from catalyst is disclosed. The catalyst regenerator vessel comprises a combustion gas distributor in fluid communication with a combustion gas line for introducing a combustion gas to the vessel, a catalyst pipe, and a catalyst distributor in fluid communication with the catalyst pipe. The catalyst distributor comprises a header and a nozzle, the header and the nozzle are in fluid communication with the catalyst pipe for distributing coked catalyst to the vessel. The header comprises a header and a plurality of nozzles including an angular nozzle projecting at an angle to a longitudinal axis of the header. The process comprises delivering coked catalyst from a catalyst pipe to the catalyst distributor wherein the catalyst distributor discharges the coked catalyst from at least two sides of the catalyst pipe into the regenerator vessel.
Processes for controlling liquid organic hydrogen carrier processes are described. The processes include flow control of hydrogen as the primary variable with toluene make-up based on reactor conditions. Make-up hydrogen gas is provided via a flow controller which can be adjusted by the operator. A pressure controller on the separator is used to adjust the temperature at the reactors with a temperature controller. The inlet temperature to the reactors is maintained by heat exchangers, such as steam generators. The reaction conditions are monitored by temperature measurement and the inlet and/or the outlet of the reactor. When hydrogen feed rates are adjusted, the unit operations must increase or reduce the toluene to balance this situation. A differential temperature controller is used to reset the toluene flowrate to the reactor to achieve the desired processing objective.
Methods which utilize low-grade heat produced in the hydrogen production process to reduce the energy required by the compressor to compress the PSA tail gas stream. The low-grade heat is used to produce a low-pressure steam stream. The low pressure steam stream is introduced to a steam turbine to generate power. The power produced by the turbine reduces the amount of power required to operate the tail gas compressor, thus reducing the overall power requirement for the process.
C01B 3/56 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification par contact avec des solidesRégénération des solides usés
C01B 3/32 - Production d'hydrogène ou de mélanges gazeux contenant de l'hydrogène par réaction de composés organiques gazeux ou liquides avec des agents gazéifiants, p. ex. de l'eau, du gaz carbonique, de l'air
F25J 3/02 - Procédés ou appareils pour séparer les constituants des mélanges gazeux impliquant l'emploi d'une liquéfaction ou d'une solidification par rectification, c.-à-d. par échange continuel de chaleur et de matière entre un courant de vapeur et un courant de liquide
Processes integrating electric heaters or other heating sources for heating of liquid and two phase hydrocarbon streams resulting in reduced CO2 emissions are described. The processes shift a portion of the fired heater duty to an electric heater or other heat source. All or a portion of a vapor stream from a two phase separator is heated or superheated by an electric heater or other heat source to provide sufficient temperature that the heated/ superheated vapor stream acts as a heat source to a bottom or side draw stream from a column. The preheated bottom or side draw stream is sent to the fired heater.
A system comprises an image sensor having a field of view, a catalyst sample holder disposable in the field of view of the image sensor, an image collection platform that receives image data representing a captured image, and an image analysis platform that analyzes the image data to determine a predicted property for the solid catalyst sample.
Processes and apparatuses for hydrotreating a feed stream comprising a biorenewable feedstock. The process comprises hydrotreating the feed stream in the presence of hydrogen and a hydrotreating catalyst to provide a hydrotreated stream and isomerizing an isomerization feed stream in the presence of a hydrotreating catalyst to provide an isomerized stream. The isomerization feed stream includes at least a portion of the hydrotreated stream. Electric heaters are provided for one or both recycle vapor streams.
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C10G 69/02 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série
98.
METHOD AND SYSTEM FOR PREDICTING CATALYST PROPERTIES USING IMAGE ANALYSIS
A system comprises an image sensor having a field of view, a catalyst sample holder disposable in the field of view of the image sensor, an image collection platform that receives image data representing a captured image, and an image analysis platform that analyzes the image data to determine a predicted property for the solid catalyst sample.
A process and apparatus for producing biofuel from biorenewable feedstock is disclosed. The process comprises hydrotreating the biorenewable feed stream in a hydrotreating reactor to hydrodeoxygenate a biorenewable feed stream to provide a hydrotreated effluent stream. The hydrotreated effluent stream is separated in a hot separator into a hot separated vapor stream and a hot separated liquid stream. A hydroisomerization feed stream is taken from the hot separated liquid stream and hydroisomerized in a hydroisomerization reactor to provide a hydroisomerized stream. All or a portion of a return stream taken from the hot separated vapor stream is recycled to the hydroisomerization reactor. The disclosed process and apparatus minimize the carryover of the normal C16 to the biofuel and maximizes the hydroisomerization of n-paraffin hydrocarbons in the hydrotreated effluent stream to produce a biofuel which meets the biofuel specification without affecting or compromising the biofuel yield.
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C10G 45/58 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour changer la structure du squelette de certains hydrocarbures sans craquer les autres hydrocarbures présents, p. ex. pour abaisser le point d'écoulementHydrocraquage sélectif des paraffines normales
C10G 65/02 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série
100.
PROCESS AND APPARATUS FOR REDUCING PRESSURE IN A FLUE GAS STREAM
A process for reducing pressure of a flue gas stream comprising passing a pressurized flue gas stream from a catalyst regenerator to an orifice chamber through an inlet. The pressurized flue gas stream is longitudinally passed through orifices in a plurality of plates in the chamber to reduce the pressure of the flue gas stream and passed from the chamber at a lower pressure than at the inlet. The plurality of orifice plates in the chamber may be spaced apart along a height of the chamber in an apparatus embodiment. Each one of the orifice plates may comprise an array of orifice strips. The strips may be sized to be inserted and removed from the chamber through a manway for installation and replacement. The process and apparatus May enable rapid replacement of eroded plates.
