Processes for producing mono-methyl alkylbenzenes from natural oils are described. The processes includes a linear selective cracking process to crack C14+ chains into C9 to C14 chains which are useful for making linear alkylbenzene for use in detergents and a hydroisomerization step to produce paraffins with mono-methyl branching which can be reacted with benzene to form the mono-methyl alkyl benzenes.
C07C 2/64 - Addition sur un atome de carbone d'un cycle aromatique à six chaînons
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
2.
TWO-STAGE CATALYTIC AMINATION-CYCLIZATION PROCESS FOR THE PRODUCTION OF PIPERAZINE AND SUBSTITUTED PIPERAZINE
Processes for the production of piperazine and alkylated piperazine (2-MethylPiperazine) are described. The processes involve forming selective aminated intermediates in situ using a two-stage reactor system. The amination reaction zone is designed to form a fully or partially aminated product, while the cyclization reactor is tailored for the inter/intramolecular cyclization of the previously formed aminated intermediate.
C07D 211/12 - Composés hétérocycliques contenant des cycles pyridiques hydrogénés, non condensés avec d'autres cycles avec uniquement des atomes d'hydrogène et de carbone liés directement à l'atome d'azote du cycle ne comportant pas de liaison double entre chaînons cycliques ou entre chaînons cycliques et chaînons non cycliques avec des radicaux hydrocarbonés ou des radicaux hydrocarbonés substitués, liés directement aux atomes de carbone du cycle avec des radicaux ne contenant que des atomes de carbone et d'hydrogène liés aux atomes de carbone du cycle avec uniquement des atomes d'hydrogène liés à l'atome d'azote du cycle
3.
A PROCESS OF REFORMING A RENEWABLE NAPHTHA AND COMPOSITION
A process of reforming a renewable naphtha is disclosed. The process comprises hydrotreating a renewable naphtha stream with a hydrotreating hydrogen stream in the presence of a hydrotreating catalyst in a hydrotreating reactor to produce a hydrotreated naphtha stream. The hydrotreated naphtha stream is reformed with a hydrogen stream in the presence of a reforming catalyst in a reforming reactor at reforming conditions comprising an average inlet temperature of no more than about 550°C to produce a reformed naphtha stream comprising greater than about 50 wt% aromatics. A reformed naphtha composition is also disclosed. The reformed naphtha composition comprises greater than about 50 wt% aromatics and a Research Octane Number of greater than about 80.
A renewable naphtha composition is disclosed. The renewable naphtha composition comprises less than about 0.1 wt% oxygen. More than about 50 wt% hydrocarbons with 6 to 10 carbon atoms of the renewable naphtha composition are cyclic. The renewable naphtha composition has a T90 of no more than about 420°F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
Rotary valves for pressure swing adsorption units are described. The rotary valve includes the use of a floating seal sheet which is not rigidly attached to any other component of the valve. The seal sheet rests on a flat plate and has another flat plate on top of it. The seal sheet has holes that have bearing surfaces which prevent it from rotating.
F16K 11/10 - Soupapes ou clapets à voies multiples, p. ex. clapets mélangeursRaccords de tuyauteries comportant de tels clapets ou soupapesAménagement d'obturateurs et de voies d'écoulement spécialement conçu pour mélanger les fluides dont plusieurs éléments de fermeture ne se déplacent pas comme un tout
F16K 31/04 - Moyens de fonctionnementDispositifs de retour à la position de repos électriquesMoyens de fonctionnementDispositifs de retour à la position de repos magnétiques utilisant un moteur
F16K 25/00 - Détails constitutifs relatifs au contact entre corps de soupapes ou de clapets et leurs sièges
Rotary valves for pressure swing adsorption units are described. The rotary valve top head, bottom head and body are all fabricated from standard piping blind flanges. The rotary valve includes a rotor plate which rotates to connect and seal various fluid passages. Fluid communication passages are machined directly into the rotor plate and connect to the inlets and/or outlets of associated vessels. By designing the passages into the rotor plate, the device can use multiple openings (orifices) of differing sizes to connect two or more vessels while also adjusting the fluid flow rate by the opening size. Once machined these passages can be closed via welding a cover over them.
F16K 11/10 - Soupapes ou clapets à voies multiples, p. ex. clapets mélangeursRaccords de tuyauteries comportant de tels clapets ou soupapesAménagement d'obturateurs et de voies d'écoulement spécialement conçu pour mélanger les fluides dont plusieurs éléments de fermeture ne se déplacent pas comme un tout
F16K 31/04 - Moyens de fonctionnementDispositifs de retour à la position de repos électriquesMoyens de fonctionnementDispositifs de retour à la position de repos magnétiques utilisant un moteur
Processes for the production of piperazine and alkylated piperazine (2-MethylPiperazine) are described. The processes involve forming selective aminated intermediates in situ using a two-stage reactor system. The amination reaction zone is designed to form a fully or partially aminated product, while the cyclization reactor is tailored for the inter/intramolecular cyclization of the previously formed aminated intermediate.
C07D 295/00 - Composés hétérocycliques contenant des cycles polyméthylène imine d'au moins cinq chaînons, des cycles aza-3 bicyclo [3.2.2] nonane, piperazine, morpholine ou thiomorpholine, ne comportant que des atomes d'hydrogène liés directement aux atomes de carbone du cycle
A process for dimerizing and oligomerizing olefins to distillate fuels which subjects oligomerized product to hydrocracking and hydroisomerization in a single reactor to convert heavier oligomers to jet fuel range oligomers. A jet fuel product stream may be taken from a side of a stripping column which produces a heavy drag stream from a bottom of the stripping column to ensure an end point boiling specification is achieved.
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
9.
INTEGRATION OF ON-PURPOSE PIPERAZINE AND METHYL-SUBSTITUTED PIPERAZINE PROCESS WITH MONOETHANOLAMINE (MEA)/REDUCTIVE AMINATION (RA) PROCESS
Integrated processes for producing piperazine are described. The processes combine commercial processes for producing highly selective aminated compounds with cyclization of the aminated compounds. A stream from the commercial amination process containing the desired aminated compounds is sent to the cyclization reactor. Commercially available processes for ethyleneamine manufacturing include, but are not limited to, reductive amination of monoethanolamine (RA/MEA) and amination of ethylene dichloride (EDC). The aminated compounds from the commercial process are cyclized to produce piperazine and optionally alkylated piperazine.
A sustainable kerosene composition is disclosed. The sustainable kerosene composition comprises greater than about 80 wt% cyclic compounds. The sustainable kerosene composition has a T10 of at least about 110°C and a final boiling point of no more than about 300°C. The sustainable kerosene composition can be characterized by a flash point of at least about 38°C. The sustainable kerosene composition comprises no more than about 12 wt% hydrogen. The sustainable kerosene composition can be used to produce low viscosity and low freeze point blendstock.
A process of fractionating a stream is disclosed. The process comprises fractionating a reactor effluent stream in a fractionation column. A reboiling stream is taken from a reboil outlet in a side of the fractionation column. The reboiling stream is combined with a stripping vapor stream to provide a mixed reboiling stream. The mixed reboiling stream is heated in a reboiler to vaporize less than 70 vol% of the mixed reboiling stream to produce a reboiled stream. The reboiled stream is charged to the fractionation column through a reboiled inlet in a side of the fractionation column. A stripping vapor stream may be fed to the fractionation column near a bottom stage. An overhead product stream and a bottom product stream is taken from the fractionation column.
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
12.
ROTARY VALVE WITH SEAL SHEET FOR HIGH PURITY APPLICATIONS
Rotary valves for pressure swing adsorption units are described. The rotary valve includes the use of a floating seal sheet which is not rigidly attached to any other component of the valve. The seal sheet rests on a flat plate and has another flat plate on top of it. The seal sheet has holes that have bearing surfaces which prevent it from rotating.
F16K 11/074 - Soupapes ou clapets à voies multiples, p. ex. clapets mélangeursRaccords de tuyauteries comportant de tels clapets ou soupapesAménagement d'obturateurs et de voies d'écoulement spécialement conçu pour mélanger les fluides dont toutes les faces d'obturation se déplacent comme un tout comportant uniquement des tiroirs à éléments de fermeture articulés à pivot à faces d'obturation planes
Rotary valves for pressure swing adsorption units are described. The rotary valve top head, bottom head and body are all fabricated from standard piping blind flanges. The rotary valve includes a rotor plate which rotates to connect and seal various fluid passages. Fluid communication passages are machined directly into the rotor plate and connect to the inlets and/or outlets of associated vessels. By designing the passages into the rotor plate, the device can use multiple openings (orifices) of differing sizes to connect two or more vessels while also adjusting the fluid flow rate by the opening size. Once machined these passages can be closed via welding a cover over them.
F16K 11/074 - Soupapes ou clapets à voies multiples, p. ex. clapets mélangeursRaccords de tuyauteries comportant de tels clapets ou soupapesAménagement d'obturateurs et de voies d'écoulement spécialement conçu pour mélanger les fluides dont toutes les faces d'obturation se déplacent comme un tout comportant uniquement des tiroirs à éléments de fermeture articulés à pivot à faces d'obturation planes
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
A sustainable kerosene composition is disclosed. The sustainable kerosene composition comprises greater than about 80 wt % cyclic compounds. The sustainable kerosene composition has a T10 of at least about 110° C. and a final boiling point of no more than about 300° C. The sustainable kerosene composition can be characterized by a flash point of at least about 38° C. The sustainable kerosene composition comprises no more than about 12 wt % hydrogen. The sustainable kerosene composition can be used to produce low viscosity and low freeze point blendstock.
A process of reforming a renewable naphtha is disclosed. The process comprises hydrotreating a renewable naphtha stream with a hydrotreating hydrogen stream in the presence of a hydrotreating catalyst in a hydrotreating reactor to produce a hydrotreated naphtha stream. The hydrotreated naphtha stream is reformed with a hydrogen stream in the presence of a reforming catalyst in a reforming reactor at reforming conditions comprising an average inlet temperature of no more than about 550° C. to produce a reformed naphtha stream comprising greater than about 50 wt % aromatics. A reformed naphtha composition is also disclosed. The reformed naphtha composition comprises greater than about 50 wt % aromatics and a Research Octane Number of greater than about 80.
C10G 63/02 - Traitement d'essence "naphta" par au moins un procédé de réformage et au moins un procédé de conversion uniquement par plusieurs étapes en série
A process of fractionating a stream is disclosed. The process comprises fractionating a reactor effluent stream in a fractionation column. A reboiling stream is taken from a reboil outlet in a side of the fractionation column. The reboiling stream is combined with a stripping vapor stream to provide a mixed reboiling stream. The mixed reboiling stream is heated in a reboiler to vaporize less than 70 vol % of the mixed reboiling stream to produce a reboiled stream. The reboiled stream is charged to the fractionation column through a reboiled inlet in a side of the fractionation column. A stripping vapor stream may be fed to the fractionation column near a bottom stage. An overhead product stream and a bottom product stream is taken from the fractionation column.
B01D 3/34 - Distillation ou procédés d'échange apparentés dans lesquels des liquides sont en contact avec des milieux gazeux, p. ex. extraction avec une ou plusieurs substances auxiliaires
B01D 3/32 - Autres caractéristiques de colonnes de fractionnement
C10G 7/00 - Distillation des huiles d'hydrocarbures
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 renewable naphtha composition is disclosed. The renewable naphtha composition comprises less than about 0.1 wt % oxygen. More than about 50 wt % hydrocarbons with 6 to 10 carbon atoms of the renewable naphtha composition are cyclic. The renewable naphtha composition has a T90 of no more than about 420° F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
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
19.
ELECTRIC HEATER FOR HEATING A PROCESS FLUID WITH A WORKING FLUID
An electric heater, systems comprising an electric heater, and methods of heating a process fluid using an electric heater. The electric heater has an electric heating element inside of a housing. A working fluid is passed into the housing and is heated by the electric heating element. The heated working fluid flows within the housing and transfer heat to process fluid contained in conduits extending within the housing of the heater.
Processes and apparatuses for heating a process fluid with an electric heater by controlling one or more process conditions based on information about the process. The electric heater uses a working fluid to transfer heat from an electrical heating element to the process fluid. The working fluid is recirculated in a loop. A controller is configured to receive the information and adjust a condition based on the received information.
F24H 1/18 - Appareils de chauffage à accumulation d'eau
F24H 9/1818 - Disposition ou montage des éléments chauffants électriques
C10G 9/24 - Craquage thermique non catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures par chauffage électrique
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
H05B 3/40 - Éléments chauffants ayant la forme de tiges ou de tubes
21.
PROCESSES AND APPARATUSES FOR HEATING A PROCESS FLUID
Processes and apparatuses for heating a process fluid with an electric heater by controlling one or more process conditions based on information about the process. The electric heater uses a working fluid to transfer heat from an electrical heating element to the process fluid. The working fluid is recirculated in a loop. A controller is configured to receive the information and adjust a condition based on the received information.
An electric heater, systems comprising an electric heater, and methods of heating a process fluid using an electric heater. The electric heater has an electric heating element inside of a housing. A working fluid is passed into the housing and is heated by the electric heating element. The heated working fluid flows within the housing and transfer heat to process fluid contained in conduits extending within the housing of the heater.
F24H 1/12 - Chauffe-eau instantanés, c.-à-d. dans lesquels il n'y a production de chaleur que lorsque l'eau s'écoule, p. ex. avec contact direct de l'eau avec l'agent chauffant dans lesquels l'eau est maintenue séparée de l'agent chauffant
23.
CRYSTALLINE ALUMINOBORATES, THEIR METHOD OF PREPARATION AND USE
An aluminoborate composition comprising an empirical formula:
An aluminoborate composition comprising an empirical formula:
An aluminoborate composition comprising an empirical formula:
where M is a trivalent framework element, B is boron, O is oxygen, N is nitrogen and H is hydrogen, x is 3-8, y is 1-5, z is 16-25, a is 1 and b is 10-15. This composition is effective in removing per- and polyfluoroalkyl substances from water.
B01J 20/02 - Compositions absorbantes ou adsorbantes solides ou compositions facilitant la filtrationAbsorbants ou adsorbants pour la chromatographieProcédés pour leur préparation, régénération ou réactivation contenant une substance inorganique
B01J 20/30 - Procédés de préparation, de régénération ou de réactivation
C01B 21/092 - Composés contenant de l'azote et des non-métaux contenant un ou plusieurs atomes d'hydrogène contenant en outre un ou plusieurs atomes de métaux
C02F 1/28 - Traitement de l'eau, des eaux résiduaires ou des eaux d'égout par absorption ou adsorption
C02F 101/34 - Composés organiques contenant de l'oxygène
C02F 101/36 - Composés organiques contenant des atomes d'halogène
24.
PROCESS FOR CONTROLLING HEAT TRANSFER AND GENERATING POWER
A process for controlling heat transfer in a hydrogenation process is provided. A hydrocarbon feed stream is hydrogenated in a hydrogenation reactor in the presence of hydrogen and a hydrogenation catalyst to produce a hydrogenated effluent. In an embodiment, the hydrogen is green hydrogen. A first feed stream is taken from the hydrogenated effluent and said first feed stream is sent to a steam generator to produce a steam stream. A pressure of the steam stream produced in the steam generator is adjusted to control the temperature of the first feed stream and the first feed stream is then charged to a second reactor.
C07C 5/10 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de cycles aromatiques à six chaînons
F01K 7/16 - Ensembles fonctionnels de machines à vapeur caractérisés par l'emploi de types particuliers de machines motricesEnsembles fonctionnels ou machines motrices caractérisés par un circuit de vapeur, un cycle de fonctionnement ou des phases particuliersDispositifs de commande spécialement adaptés à ces systèmes, cycles ou phasesUtilisation de la vapeur soutirée ou de la vapeur d'évacuation pour le réchauffage de l'eau d'alimentation les machines motrices étant uniquement du type turbine
F22B 1/16 - Méthodes de production de vapeur caractérisées par le genre de chauffage par exploitation de l'énergie thermique contenue dans une source chaude la source chaude étant un liquide chaud ou une vapeur chaude, p. ex. un liquide résiduel, une vapeur résiduelle
F22G 1/00 - Surchauffe de la vapeur caractérisée par la méthode de chauffage
25.
PROCESSES FOR REMOVING PERFLUOROALKYL SUBSTANCES AND REGENERATING AN ADSORBENT USED WITH SAME
Processes and apparatuses for degrading PFAS into calcium fluoride, carbon dioxide, and water. PFAS are heated and introduced to a calcium base which will degrade the PFAS. The PFAS may be in a stream that is a PFAS enriched stream formed by desorbing the PFAS from an adsorbent which removed the PFAS from a contaminant stream. The PFAS may be desorbed in the presence of the calcium base. The calcium base may be calcium hydroxide, calcium oxide, calcium carbonate, or combinations thereof.
A62D 3/36 - Détoxification au moyen de réactifs acides ou alcalins
B01D 15/20 - Adsorption sélective, p. ex. chromatographie caractérisée par des caractéristiques de structure ou de fonctionnement relatives au conditionnement de la matière adsorbante ou absorbante
B01J 20/20 - Compositions absorbantes ou adsorbantes solides ou compositions facilitant la filtrationAbsorbants ou adsorbants pour la chromatographieProcédés pour leur préparation, régénération ou réactivation contenant une substance inorganique contenant du carbone libreCompositions absorbantes ou adsorbantes solides ou compositions facilitant la filtrationAbsorbants ou adsorbants pour la chromatographieProcédés pour leur préparation, régénération ou réactivation contenant une substance inorganique contenant du carbone obtenu par des procédés de carbonisation
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern to a pressure swing adsorption unit and then to an electrochemical compression unit to produce hydrogen having a purity of above 99.5 mol% to close to 100 mol%.
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 3/50 - Séparation de l'hydrogène ou des gaz contenant de l'hydrogène à partir de mélanges gazeux, p. ex. purification
B01D 53/32 - 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 effets électriques autres que ceux prévus au groupe
27.
APPARATUS AND PROCESS FOR PRODUCING A SUPERHEATED STEAM
An apparatus and a process for producing a superheated steam is disclosed. The apparatus comprises a primary heater comprising a radiant section and a convection section. The primary heater comprises a convective heat transfer conduit in communication with a source of water and passing through the convection section to provide a steam stream. The apparatus further comprises a secondary heater. The secondary heater comprises a radiant section and a secondary heat transfer conduit in communication with the convective heat transfer conduit of the primary heater. The secondary heat transfer conduit passes through the radiant section of the secondary heater to provide a superheated steam stream. Further, a process for producing a superheated steam is disclosed.
A hydroprocessing catalyst is provided that is supported hydrotreating catalyst, where the shaped support of 0.36-0.46 void fraction is comprised of a single source of gamma alumina with a medium pore diameter of 10 nm and at least 0.95 cc/g pore volume but not more than 1.10 cc/g, and includes a single, Group IIIb metal dispersed by mulling or mixing in a forming step, and a surface area by nitrogen BET between 230 m2/g and 260 m2/g, and where the finished catalyst can be described in terms of molar ratios relative to aluminum, where the aluminum concentration may vary from 26 to 30 wt%, Al:Group VIb 4.8-5.6, Al:Group VIII 14.9-19.0, Al:Group Va 9.6-12.7, and Al:Group IIIb 112.5-228.2.
A process for converting a feed in a series of reactors is disclosed. The process comprises taking at least two hydrocarbon streams, a first hydrocarbon feed stream and a second hydrocarbon feed stream. The first hydrocarbon feed stream and the second hydrocarbon feed stream are heat exchanged in a heat exchanger with a second product stream from a second reactor. A heat exchanged first hydrocarbon feed stream is charged into a first catalyst bed in a first reactor to produce a first product stream and a heat exchanged second hydrocarbon feed stream is charged into a second catalyst bed in the second reactor to produce the second product stream. The second product stream is at a higher temperature than the first hydrocarbon feed stream and the second hydrocarbon feed stream.
C10G 11/00 - Craquage catalytique, en l'absence d'hydrogène, des huiles d'hydrocarbures
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
30.
IMPROVING YIELD OF HYDROXYMETHYLFURFURAL THROUGH PURIFICATION OF SUGAR FEED
Hydroxymethylfurfural (HMF) is derived from C6 sugars and is a versatile platform chemical with the potential to replace a range of conventional building blocks. It has been found that the remove of certain components such as oxygenated contaminants from C6 sugars can significantly improve the yields of HMF. The oxygenated contaminants may be removed by ion exchange resins, adsorbents, solvent extraction and pH adjustment via addition of base.
A slurry hydrocracking process is disclosed. The process comprises charging a catalyst, a bio-oil stream, a recycle stream, and a hydrogen stream to a slurry hydrocracking reactor. The bio-oil stream, and the recycle stream are hydrocracked in the presence of the catalyst and the hydrogen stream to produce a slurry hydrocracked effluent stream. A recycle stream is taken from the hydrocracked effluent stream. The bio-oil stream is added to the recycle stream which is charged into the slurry hydrocracking 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
32.
OLEFINS TO FUEL IN A SINGLE-STAGE OLIGOMERIZATION PROCESS
This disclosure describes a process for producing a sustainable aviation fuel including oligomerizing a charge olefin stream over a single oligomerization catalyst to produce an oligomerized stream with greater than about 50% and less than about 99.5% olefins conversion per pass in the charge stream.
A process of producing a fuel stream comprising renewable carbon is disclosed. The process comprises producing an olefinic stream or an alcohol stream from a renewable feedstock. An aromatic stream and an alkylating agent comprising the olefinic stream or the alcohol stream is charged to an alkylation reactor to alkylate the aromatic stream with the alkylating agent to produce an alkylated aromatic product stream. The alkylated aromatic product stream comprises about 0.1 wt % to about 67 wt % renewable carbon.
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
34.
IMPROVING YIELD OF HYDROXYMETHYLFURFURAL THROUGH PURIFICATION OF SUGAR FEED
Hydroxymethylfurfural (HMF) is derived from C6 sugars and is a versatile platform chemical with the potential to replace a range of conventional building blocks. It has been found that the remove of certain components such as oxygenated contaminants from C6 sugars can significantly improve the yields of HMF. The oxygenated contaminants may be removed by ion exchange resins, adsorbents, solvent extraction and pH adjustment via addition of base.
A sustainable aviation fuel composition is disclosed. The sustainable aviation fuel composition comprises a T10 of more than about 110° C. and a final boiling point of no more than about 300° C., about 5 to about 25 wt % aromatics, no more than about 15 wt % hydrogen, no more than about 1 wt % oxygen, and has a flash point of at least about 38° C. Further, a process of producing sustainable aviation fuel is disclosed. The sustainable aviation fuel can be used as fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Combustibles carbonés liquides à base essentielle de mélanges d'hydrocarbures
C10G 45/16 - 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 avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
C10G 45/44 - Hydrogénation des hydrocarbures aromatiques
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
36.
PURIFICATION OF HYDROGEN REMOVED FROM UNDERGROUND STORAGE
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern to a pressure swing adsorption unit and then to an electrochemical compression unit to produce hydrogen having a purity of above 99.5 mol % to close to 100 mol %.
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
B01D 53/32 - 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 effets électriques autres que ceux prévus au groupe
A slurry hydrocracking process is disclosed. The process comprises charging a catalyst, a bio-oil stream, a recycle stream, and a hydrogen stream to a slurry hydrocracking reactor. The bio-oil stream, and the recycle stream are hydrocracked in the presence of the catalyst and the hydrogen stream to produce a slurry hydrocracked effluent stream. A recycle stream is taken from the hydrocracked effluent stream. The bio-oil stream is added to the recycle stream which is charged into the slurry hydrocracking reactor.
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C10G 45/04 - 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
38.
OLEFINS TO FUEL IN A SINGLE-STAGE OLIGOMERIZATION PROCESS
This disclosure describes a process for producing a sustainable aviation fuel including oligomerizing a charge olefin stream over a single oligomerization catalyst to produce an oligomerized stream with greater than 50% and less than 99.5% olefins conversion per pass in the charge stream.
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
A renewable naphtha composition is disclosed. The renewable naphtha composition comprises 0.1 wt% to 15 wt% oxygen, and C4 to C8 hydrocarbons comprising more than 50 wt% cyclic hydrocarbons in the renewable naphtha composition. The renewable naphtha composition has a final boiling point of no more than 420°F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Combustibles carbonés liquides à base essentielle de mélanges d'hydrocarbures
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
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
40.
PROCESS AND APPARATUS FOR PRODUCING ULTRA PURE CO2 IN A CARBON CAPTURE PROCESS
Processes for producing two CO2 streams having different purities, including one stream comprising ultra high purity CO2. The processes incorporate a second fractionation column in a CO2 fractionation process. The bottoms stream from the first cryogenic fractionation column is sent to the second CO2 fractionation column. The second CO2 fractionation column can produce ultra high purity CO2. The bottoms stream from the first column can be divided and a portion of the bottoms stream can be recovered as a second CO2 product stream having a lower purity than the purity of the product stream.
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 hydroprocessing catalyst is provided that is supported hydrotreating catalyst, where the shaped support of 0.36-0.46 void fraction is comprised of a single source of gamma alumina with a medium pore diameter of 10 nm and at least 0.95 cc/g pore volume but not more than 1.10 cc/g, and includes a single, Group IIIb metal dispersed by mulling or mixing in a forming step, and a surface area by nitrogen BET between about 230 m2/g and 260 m2/g, and where the finished catalyst can be described in terms of molar ratios relative to aluminum, where the aluminum concentration may vary from 26 to 30 wt %, Al: Group VIb 4.8-5.6, Al: Group VIII 14.9-19.0, Al: Group Va 9.6-12.7, and Al: Group IIIb 112.5-228.2.
A process for converting a feed in a series of reactors is disclosed. The process comprises taking at least two hydrocarbon streams, a first hydrocarbon feed stream and a second hydrocarbon feed stream. The first hydrocarbon feed stream and the second hydrocarbon feed stream are heat exchanged in a heat exchanger with a second product stream from a second reactor. A heat exchanged first hydrocarbon feed stream is charged into a first catalyst bed in a first reactor to produce a first product stream and a heat exchanged second hydrocarbon feed stream is charged into a second catalyst bed in the second reactor to produce the second product stream. The second product stream is at a higher temperature than the first hydrocarbon feed stream and the second hydrocarbon feed stream.
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 8/26 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées selon la technique du "lit fluidisé" comportant au moins deux lits fluidisés, p. ex. installations de réaction et de régénération
C07C 4/00 - Préparations d'hydrocarbures à partir d'hydrocarbures contenant un plus grand nombre d'atomes de carbone
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
A renewable naphtha composition is disclosed. The renewable naphtha composition comprises about 0.1 wt % to about 15 wt % oxygen, and C4 to about C8 hydrocarbons comprising more than about 50 wt % cyclic hydrocarbons in the renewable naphtha composition. The renewable naphtha composition has a final boiling point of no more than about 420° F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/02 - Combustibles carbonés liquides à base essentielle de composants formés uniquement de carbone, d'hydrogène et d'oxygène
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
44.
APPARATUS AND PROCESS FOR PRODUCING A SUPERHEATED STEAM
An apparatus and a process for producing a superheated steam is disclosed. The apparatus comprises a primary heater comprising a radiant section and a convection section. The primary heater comprises a convective heat transfer conduit in communication with a source of water and passing through the convection section to provide a steam stream. The apparatus further comprises a secondary heater. The secondary heater comprises a radiant section and a secondary heat transfer conduit in communication with the convective heat transfer conduit of the primary heater. The secondary heat transfer conduit passes through the radiant section of the secondary heater to provide a superheated steam stream. Further, a process for producing a superheated steam is disclosed.
F22G 3/00 - Surchauffeurs de vapeur caractérisés par des particularités structuralesDétails ou parties constitutives de ces appareils
F22G 1/02 - Surchauffe de la vapeur caractérisée par la méthode de chauffage la chaleur étant fournie par les fumées chaudes provenant du foyer de la chaudière
F22G 1/16 - Surchauffe de la vapeur caractérisée par la méthode de chauffage en employant une source de chaleur séparée, indépendante de la chaleur fournie à la chaudière, p. ex. par électricité, combustion auxiliaire de mazout
45.
PROCESS OF PRODUCING A FUEL STREAM COMPRISING RENEWABLE CARBON
A process of producing a fuel stream comprising renewable carbon is disclosed. The process comprises producing an olefinic stream or an alcohol stream from a renewable feedstock. An aromatic stream and an alkylating agent comprising the olefinic stream or the alcohol stream is charged to an alkylation reactor to alkylate the aromatic stream with the alkylating agent to produce an alkylated aromatic product stream. The alkylated aromatic product stream comprises 0.1 wt% to 67 wt% renewable carbon.
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 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
A process for dehydrating ethanol to ethylene. The steps include: (a) reacting an ethanol feed stream over a dehydration catalyst to produce ethylene in a dehydration product stream; (b) separating said dehydration product stream into a product liquid stream comprising water and dissolved oxygenates and a product vapor stream of ethylene; (c) taking a bypass stream from said product liquid stream; and, (d) sending the bypass stream to the dehydration reactor bypassing a wastewater stripping column.
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 7/04 - 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
A process for controlling heat transfer in a hydrogenation process is provided. A hydrocarbon feed stream is hydrogenated in a hydrogenation reactor in the presence of hydrogen and a hydrogenation catalyst to produce a hydrogenated effluent. In an embodiment, the hydrogen is green hydrogen. A first feed stream is taken from the hydrogenated effluent and said first feed stream is sent to a steam generator to produce a steam stream. A pressure of the steam stream produced in the steam generator is adjusted to control the temperature of the first feed stream and the first feed stream is then charged to a second reactor.
C07C 5/10 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant le même nombre d'atomes de carbone par hydrogénation de cycles aromatiques à six chaînons
C07C 13/18 - Hydrocarbures monocycliques ou leurs dérivés hydrocarbonés acycliques à cycle hexagonal à cycle du cyclohexane
A sustainable aviation fuel composition is disclosed. The sustainable aviation fuel composition comprises a T10 of more than about 110°C and a final boiling point of no more than about 300°C, about 5 to about 25 wt% aromatics, no more than about 15 wt% hydrogen, no more than about 1 wt% oxygen, and has a flash point of at least about 38°C. Further, a process of producing sustainable aviation fuel is disclosed. The sustainable aviation fuel can be used as fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Combustibles carbonés liquides à base essentielle de mélanges d'hydrocarbures
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
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
49.
PROCESS AND APPARATUS FOR PRODUCING ULTRA PURE CO2 IN A CARBON CAPTURE PROCESS
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
50.
PROCESS FOR THE PRODUCTION OF A CO-MIXTURE OF PIPERAZINE AND METHYL-SUBSTITUTED PIPERAZINE
Catalytic processes to manufacture piperazine and 2-methyl piperazine simultaneously through co-feeding a linear alkanolamine, or a diol, or an ethyleneamine with an analog of the alkanolamine, or the diol, or the ethyleneamine in the presence of anhydrous ammonia to produce a reaction mixture comprising the piperazine and the methyl-substituted piperazine are described. The catalyst comprises a 10 membered ring zeolite.
B01J 29/40 - Zéolites aluminosilicates cristallinesLeurs composés isomorphes du type pentasil, p. ex. types ZSM-5, ZSM-8 ou ZSM-11
C07D 241/04 - Composés hétérocycliques contenant des cycles diazine-1,4 ou diazine-1,4 hydrogéné non condensés avec d'autres cycles ne comportant pas de liaisons doubles entre chaînons cycliques ou entre chaînons cycliques et chaînons non cycliques
C07D 295/027 - Composés hétérocycliques contenant des cycles polyméthylène imine d'au moins cinq chaînons, des cycles aza-3 bicyclo [3.2.2] nonane, piperazine, morpholine ou thiomorpholine, ne comportant que des atomes d'hydrogène liés directement aux atomes de carbone du cycle contenant uniquement des atomes d'hydrogène et de carbone en plus des hétéro-éléments du cycle ne contenant qu'un hétérocycle
51.
CATALYTIC METHOD FOR SELECTIVE CYCLO-AMINATION OF ALKANOLAMINE AND DIOL TO PRODUCE ON-PURPOSE CYCLIC ETHYLENEAMINES OF PIPERAZINE AND DERIVATIVES
Catalytic processes to produce on purpose piperazine are described. The processes are based on the use of a 10-member ring zeolite, preferably with MFI topology, with tunned morphology and acidity to promote intermolecular or intramolecular cyclization of alkanolamines, ethyleneamines, or diols to cyclic piperazine. The unavoidable byproducts due to thermodynamics can be tuned to favor piperazine upon recycling. The processes can be used to manufacture piperazine which can be used as solvent for post-combustion CO2 capture.
B01J 29/70 - Zéolites aluminosilicates cristallinesLeurs composés isomorphes de types caractérisés par leur structure spécifique non prévus dans les groupes
C07D 295/027 - Composés hétérocycliques contenant des cycles polyméthylène imine d'au moins cinq chaînons, des cycles aza-3 bicyclo [3.2.2] nonane, piperazine, morpholine ou thiomorpholine, ne comportant que des atomes d'hydrogène liés directement aux atomes de carbone du cycle contenant uniquement des atomes d'hydrogène et de carbone en plus des hétéro-éléments du cycle ne contenant qu'un hétérocycle
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
A semi-permeable cover for a radial flow reactor that is located on top of a bed of catalyst in the reactor. The cover allows for a small portion of process gas to flow therethrough. The semi-permeable cover may be a self-deploying blank with a biasing element or have a spiral seam. The cover may be made from separate pieces. A shroud may be provided to cover an upper end of the center pipe in the reactor.
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
54.
PROCESSES AND APPARATUSES FOR REDUCING INTERNAL DAMAGE IMPAIRMENT TO AN EQUIPMENT PIECE IN A CARBON CAPTURE UNIT
Processes and apparatuses for reducing internal damage impairment to an equipment piece in a carbon capture unit after shutdown of the carbon capture unit with a purge gas. Once a shutdown of the carbon capture unit has been detected purge gas is used to displace process fluid within spaces of the equipment piece. The carbon capture unit may be a cryogenic carbon capture unit, a solvent carbon capture unit, a membrane carbon capture unit, a solid adsorbent carbon capture unit, or any combination thereof.
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
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
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
B01D 53/30 - Commande par appareil d'analyse des gaz
55.
MODIFIED ALUMINOBORATE HAVING INCREASED SURFACE AREA AND METHODS OF MAKING
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al :B in the range of 5 to 8. It has an XRD diffraction pattern different from the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 50°C to 100°C and a solid: liquid ratio of 1 :20 to 1; 100 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
B01J 23/16 - Catalyseurs contenant des métaux, oxydes ou hydroxydes métalliques non prévus dans le groupe de l'arsenic, de l'antimoine, du bismuth, du vanadium, du niobium, du tantale, du polonium, du chrome, du molybdène, du tungstène, du manganèse, du technétium ou du rhénium
222 enriched stream and an evacuation gas stream; and introducing the evacuation gas stream to rotating equipment to displace any particulates in low flow and small clearance areas in the rotating equipment.
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 semi-permeable cover for a radial flow reactor that is located on top of a bed of catalyst in the reactor. The cover allows for a small portion of process gas to flow therethrough. The semi-permeable cover may be a self-deploying blank with a biasing element or have a spiral seam. The cover may be made from separate pieces. A shroud may be provided to cover an upper end of the center pipe in the 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 8/00 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés
58.
PROCESS FOR THE PRODUCTION OF A CO-MIXTURE OF PIPERAZINE AND METHYL-SUBSTITUTED PIPERAZINE
Catalytic processes to manufacture piperazine and 2- methyl piperazine simultaneously through co-feeding a linear alkanolamine, or a diol, or an ethyleneamine with an analog of the alkanolamine, or the diol, or the ethyleneamine in the presence of anhydrous ammonia to produce a reaction mixture comprising the piperazine and the methyl-substituted piperazine are described. The catalyst comprises a 10 membered ring zeolite.
C07D 241/04 - Composés hétérocycliques contenant des cycles diazine-1,4 ou diazine-1,4 hydrogéné non condensés avec d'autres cycles ne comportant pas de liaisons doubles entre chaînons cycliques ou entre chaînons cycliques et chaînons non cycliques
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including fats, oils and greases (FOGs) to fuel, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
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
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C10G 45/02 - 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
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including, hydroprocessing, and naphtha to ethane and propane to ethylene and propylene, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
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
C10G 67/16 - 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 parallèle
C10G 73/02 - Obtention des cires de pétrole à partir des huiles d'hydrocarburesDéparaffinage d'huiles d'hydrocarbures
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 2/00 - Production de mélanges liquides d'hydrocarbures de composition non définie à partir d'oxydes de carbone
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
Organic chlorides are removed from bio-oils, including vegetable oils and animal fats, that are to be coprocessed to meet sustainability goals. The organic chlorides are removed by using active materials such as silica-alumina containing adsorbents. The bio-oils that are targeted for treatment contain greater than 5 ppmw chlorides and are planned for more than 10% of the feedstream that is being processed.
xyzabb where M is a trivalent framework element, B is boron, O is oxygen, N is nitrogen and H is hydrogen, x is 3-8, y is 1-5, z is 16-25, a is 1 and b is 10-15. This composition is effective in removing per- and polyfluoroalkyl substances from water.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 1.5 to 2.5, and it has an XRD diffraction pattern substantially similar to the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 20° C. to 40° C. and a solid:liquid ratio of 1:20 to 1:100, or temperatures in the range of 50 to 100° C. and a solid:liquid ratio of 1:10 to 1:40 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 5 to 8. It has an XRD diffraction pattern different from the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 50° C. to 100° C. and a solid:liquid ratio of 1:20 to 1:100 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
Processes for displacing particulates from low flow and small clearance areas in rotating equipment associated with a carbon capture unit, the process comprising compressing, in a compressor, a flue gas stream to provide a compressed flue gas stream; processing, in a CO2 separation zone in a carbon capture unit, the compressed flue gas stream and providing a CO2 enriched stream and an evacuation gas stream; and introducing the evacuation gas stream to rotating equipment to displace any particulates in low flow and small clearance areas in the rotating equipment.
B08B 9/00 - Nettoyage d'objets creux par des procédés ou avec un appareillage spécialement adaptés à cet effet
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
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
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
66.
PROCESSES AND APPARATUSES FOR REDUCING INTERNAL DAMAGE IMPAIRMENT TO AN EQUIPMENT PIECE IN A CARBON CAPTURE UNIT
Processes and apparatuses for reducing internal damage impairment to an equipment piece in a carbon capture unit after shutdown of the carbon capture unit with a purge gas. Once a shutdown of the carbon capture unit has been detected purge gas is used to displace process fluid within spaces of the equipment piece. The carbon capture unit may be a cryogenic carbon capture unit, a solvent carbon capture unit, a membrane carbon capture unit, a solid adsorbent carbon capture unit, or any combination thereof.
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
67.
ENERGY EFFICIENT NON-FLAMMABLE REFRIGERATION FOR CO2-RICH PROCESS STREAMS
Processes for chilling CO2 rich streams are described. The processes combine the use of a refrigerant mixture comprising CO2 and a first refrigerant capable of depressing the freezing point of CO2 to less than or equal to −60° C. and a series of flash drums which reduce the temperature and pressure of the refrigerant mixture and concentrate the first refrigerant.
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 for dehydrating ethanol to ethylene. The steps include: (a) reacting an ethanol feed stream over a dehydration catalyst to produce ethylene in a dehydration product stream; (b) separating said dehydration product stream into a product liquid stream comprising water and dissolved oxygenates and a product vapor stream of ethylene; (c) taking a bypass stream from said product liquid stream; and, (d) sending the bypass stream to the dehydration reactor bypassing a wastewater stripping column.
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
69.
INTEGRATED FISCHER-TROPSCH AND LINEAR ALKYLBENZENE COMPLEX
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
Organic chlorides are removed from bio-oils, including vegetable oils and animal fats, that are to be coprocessed to meet sustainability goals. The organic chlorides are removed by using active materials such as silica-alumina containing adsorbents. The bio-oils that are targeted for treatment contain greater than 5 ppmw chlorides and are planned for more than 10% of the feedstream that is being processed.
B01J 20/28 - Compositions absorbantes ou adsorbantes solides ou compositions facilitant la filtrationAbsorbants ou adsorbants pour la chromatographieProcédés pour leur préparation, régénération ou réactivation caractérisées par leur forme ou leurs propriétés physiques
A process for producing light olefins is disclosed. The process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to produce a hydrocracked stream. A reforming charge stream is taken from the hydrocracked stream. The reforming charge stream is reformed over a reforming catalyst in a reforming reactor to convert naphthenes to aromatics and produce a reformed stream. The reformed stream is charged to an NEP reactor to convert the reformed stream over an NEP catalyst in the presence of NEP hydrogen to produce a light paraffinic stream. Ethylene and propylene can be produced from the light paraffinic stream.
A marine fuel oil composition is disclosed. The marine fuel oil composition comprises an acid number of less than about 2.5 mg KOH/g, a flash point temperature greater than about 140° F., and an oxygen concentration of at least about 2 wt %. Further, a process for producing marine fuel oil is disclosed.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 1.5 to 2.5, and it has an XRD diffraction pattern substantially similar to the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 20°C to 40°C and a solid: liquid ratio of 1:20 to 1:100, or temperatures in the range of 50 to 100 °C and a solid: liquid ratio of 1:10 to 1:40 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
2222 to less than or equal to -60°C and a series of flash drums which reduce the temperature and pressure of the refrigerant mixture and concentrate the first refrigerant.
F25J 1/00 - Procédés ou appareils de liquéfaction ou de solidification des gaz ou des mélanges gazeux
F25J 1/02 - Procédés ou appareils de liquéfaction ou de solidification des gaz ou des mélanges gazeux nécessitant l'emploi d'une réfrigération, p. ex. de l'hélium, de l'hydrogène
F25B 1/10 - Machines, installations ou systèmes à compression à cycle irréversible à compression multi-étagée
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
76.
PROCESS FOR PRODUCING A SINGLE PHASE IMMERSION COOLING FLUID FROM FISCHER-TROPSCH OIL
Processes for converting Fischer-Tropsch products into a single-phase immersion cooling fluid and optionally aviation fuel are described. Processes for converting Fischer-Tropsch products to sustainable aviation fuel can be modified and tailored to co-produce an immersion cooling base oil which can be used to generate a fluid with the required properties for single-phase immersion cooling.
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
C07C 15/107 - Hydrocarbures monocycliques comportant une chaîne latérale saturée contenant au moins six atomes de carbone, p. ex. dérivés alkylés pour détergents
C10G 2/00 - Production de mélanges liquides d'hydrocarbures de composition non définie à partir d'oxydes de carbone
C10G 57/00 - 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
A marine fuel oil composition is disclosed. The marine fuel oil composition comprises an acid number of less than about 2.5 mg KOH/g, a flash point temperature greater than about 140°F, and an oxygen concentration of at least about 2 wt%. Further, a process for producing marine fuel oil is disclosed.
Processes for converting Fischer-Tropsch products into a single-phase immersion cooling fluid and optionally aviation fuel are described. Processes for converting Fischer-Tropsch products to sustainable aviation fuel can be modified and tailored to co-produce an immersion cooling base oil which can be used to generate a fluid with the required properties for single-phase immersion cooling.
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern, a depleted gas field or a saline aquifer to a pressure swing adsorption unit and then to a membrane unit to produce hydrogen having a purity of above 99.5 mol %.
Integrated processes for producing p-xylene from biomass are described. The biomass is converted to sugars which are converted to 5-hydroxymethylfurfural (HMF) which is converted to dimethylfuran (DMF). The biomass derived DMF is reacted with internally generated de-watered, unpurified ethylene to form the p-xylene. The de-watered, unpurified ethylene is also derived from sugars made from the biomass.
C07C 2/86 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un plus petit nombre d'atomes de carbone par condensation d'un hydrocarbure et d'un non-hydrocarbure
C07D 307/36 - Composés hétérocycliques contenant des cycles à cinq chaînons comportant un atome d'oxygène comme unique hétéro-atome du cycle non condensés avec d'autres cycles comportant deux ou trois liaisons doubles entre chaînons cycliques ou entre chaînons cycliques et chaînons non cycliques avec uniquement des atomes d'hydrogène ou des radicaux ne contenant que des atomes d'hydrogène et de carbone, liés directement aux atomes de carbone du cycle
C07D 307/46 - Atomes d'oxygène liés par des liaisons doubles ou deux atomes d'oxygène liés par des liaisons simples au même atome de carbone
C10G 3/00 - Production de mélanges liquides d'hydrocarbures à partir de matières organiques contenant de l'oxygène, p. ex. huiles, acides gras
C12P 7/06 - Éthanol en tant que produit chimique et non en tant que boisson alcoolique
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
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including fats, oils and greases (FOGs) to fuel, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
C11C 3/12 - Graisses, huiles ou acides gras obtenus par transformation chimique des graisses, huiles ou acides gras, p. ex. ozonolyse par hydrogénation
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including, hydroprocessing, and naphtha to ethane and propane to ethylene and propylene, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
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
84.
HIGH SELECTIVITY AND HIGH CO2 PLASTICIZATION RESISTANT POLYMERIC MEMBRANES FOR GAS SEPARATIONS
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
Membranes made from the polymer and gas separation processes using the membranes made from the polymer are also described.
C08G 61/12 - Composés macromoléculaires contenant d'autres atomes que le carbone dans la chaîne principale de la macromolécule
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
B01D 71/62 - Polycondensats ayant des hétérocycles contenant de l'azote dans la chaîne principale
A process for converting plastics is disclosed. The process comprises pyrolyzing a plastic feed stream in a first pyrolysis reactor to produce a pyrolysis vapor stream. The pyrolysis vapor stream is pyrolyzed in a second pyrolysis reactor to produce a pyrolysis product stream. The first pyrolysis reactor may be operated at a higher temperature than the second pyrolysis reactor. The plastic feed stream may be separated from a mixed-plastic stream.
C08J 11/12 - Récupération ou traitement des résidus des polymères par coupure des chaînes moléculaires des polymères ou rupture des liaisons de réticulation par voie chimique, p. ex. dévulcanisation uniquement par traitement à la chaleur sèche
B29B 17/02 - Séparation de matières plastiques des autres matières
86.
PROCESS FOR CONVERTING OLEFINS TO DIESEL WITH BLENDING
We have formulated a process for oligomerizing an olefin stream to distillate fuel that meets appropriate distillate requirements. We have found that diesel produced by oligomerizing a charge olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream followed by saturation may have a viscosity that exceeds requirements. The process comprises blending jet fuel with diesel fuel to enable the diesel fuel to meet viscosity qualifications.
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
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern, a depleted gas field or a saline aquifer to a pressure swing adsorption unit and then to a membrane unit to produce hydrogen having a purity of above 99.5 mol%.
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 3/56 - 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 producing light olefins is disclosed. The process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to produce a hydrocracked stream. A reforming charge stream is taken from the hydrocracked stream. The reforming charge stream is reformed over a reforming catalyst in a reforming reactor to convert naphthenes to aromatics and produce a reformed stream. The reformed stream is charged to an NEP reactor to convert the reformed stream over an NEP catalyst in the presence of NEP hydrogen to produce a light paraffinic stream. Ethylene and propylene can be produced from the light paraffinic stream.
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"
A process for converting plastics is disclosed. The process comprises pyrolyzing a plastic feed stream in a first pyrolysis reactor to produce a pyrolysis vapor stream. The pyrolysis vapor stream is pyrolyzed in a second pyrolysis reactor to produce a pyrolysis product stream. The first pyrolysis reactor may be operated at a higher temperature than the second pyrolysis reactor. The plastic feed stream may be separated from a mixed-plastic stream.
C10G 1/02 - 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 par distillation
C10B 47/30 - Autres procédés dans des fours ou cornues tournants
C10B 53/07 - Distillation destructive spécialement conçue pour des matières premières solides particulières ou sous forme spéciale de matières polymères synthétiques, p. ex. pneumatiques
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
90.
INTEGRATED BIO-REFINERY FOR BIO-P-XYLENE WITH INTERNAL BIO-ETHYLENE PRODUCTION
Integrated processes for producing p-xylene from biomass are described. The biomass is converted to sugars which are converted to 5-hydroxymethylfurfural (HMF) which is converted to dimethylfuran (DMF). The biomass derived DMF is reacted with internally generated de-watered, unpurified ethylene to form the p-xylene. The de-watered, unpurified ethylene is also derived from sugars made from the biomass.
C07C 2/86 - Préparation d'hydrocarbures à partir d'hydrocarbures contenant un plus petit nombre d'atomes de carbone par condensation d'un hydrocarbure et d'un non-hydrocarbure
C12P 7/06 - Éthanol en tant que produit chimique et non en tant que boisson alcoolique
91.
PROCESS FOR UPGRADING FISCHER-TROPSCH OIL TO SYNTHETIC PARAFFINIC KEROSENE
Processes for converting Fischer-Tropsch products into synthetic paraffinic kerosene which can be used to make aviation. The process schemes provide the possibility of different degrees of isomerization of an unconverted oil recycle to maximize the distillate yields. Different process schemes can be employed depending on the type of Fischer-Tropsch feed, e.g., the distillate to wax ratio in the Fischer-Tropsch oil. The present invention provides routes to produce sustainable aviation fuel (SAF) from a Fischer-Tropsch complex with a lower level of isomerization leading to better SAF yields.
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 producing monomers is disclosed. The process comprises hydrocracking a pyrolysis oil stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open rings present in said pyrolysis oil stream to produce a hydrocracked effluent stream. The hydrocracked effluent stream is fractionating in a fractionation column to provide a naphtha stream. The naphtha stream is contacted with a NEP catalyst and hydrogen to produce a light paraffinic stream or with a reforming catalyst to produce an aromatics stream.
C10G 69/04 - 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 catalytique en l'absence d'hydrogène
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 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
C07C 5/327 - Formation de liaisons doubles carbone-carbone uniquement non aromatiques
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 7/09 - Purification, séparation ou stabilisation d'hydrocarburesEmploi d'additifs par condensation fractionnée
We have formulated a process for oligomerizing an olefin stream to distillate fuel that meets appropriate distillate requirements. We have found that diesel produced by oligomerizing a charge olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream followed by saturation may have a viscosity that exceeds requirements. The process comprises blending jet fuel with diesel fuel to enable the diesel fuel to meet viscosity qualifications.
C10G 50/00 - Production de mélanges d'hydrocarbures liquides à partir d'hydrocarbures à nombre inférieur d'atomes de carbone, p. ex. par oligomérisation
94.
PROCESS FOR UPGRADING FISCHER-TROPSCH OIL TO SYNTHETIC PARAFFINIC KEROSENE
Processes for converting Fischer-Tropsch products into synthetic paraffinic kerosene which can be used to make aviation. The process schemes provide the possibility of different degrees of isomerization of an unconverted oil recycle to maximize the distillate yields. Different process schemes can be employed depending on the type of Fischer-Tropsch feed, e.g., the distillate to wax ratio in the Fischer-Tropsch oil. The present invention provides routes to produce sustainable aviation fuel (SAF) from a Fischer-Tropsch complex with a lower level of isomerization leading to better SAF yields.
C10G 67/00 - 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
C10G 2/00 - Production de mélanges liquides d'hydrocarbures de composition non définie à partir d'oxydes de carbone
C10G 73/02 - Obtention des cires de pétrole à partir des huiles d'hydrocarburesDéparaffinage d'huiles d'hydrocarbures
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 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
A process for producing monomers is disclosed. The process comprises hydrocracking a pyrolysis oil stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open rings present in said pyrolysis oil stream to produce a hydrocracked effluent stream. The hydrocracked effluent stream is fractionating in a fractionation column to provide a naphtha stream. The naphtha stream is contacted with a NEP catalyst and hydrogen to produce a light paraffinic stream or with a reforming catalyst to produce an aromatics stream.
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
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 51/16 - Préparation d'acides carboxyliques, de leurs sels, halogénures ou anhydrides par oxydation
C07C 67/39 - Préparation d'esters d'acides carboxyliques par oxydation des groupes précurseurs de la partie acide de l'ester
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
A process for upgrading a bio-oil stream is disclosed. The process comprises discharging spent hydrotreating catalyst fines from a hydrotreating reactor. The hydrotreating catalyst fines comprise a metal from Group IVB, Group VB, Group VIB, Group VIIB, and Group VIII metals on an inorganic support. A bio-oil stream is reacted with hydrogen in the presence of the spent hydrotreating catalyst fines in a bio-oil reactor to produce an upgraded bio-oil stream. The spent hydrotreating catalyst fines can be characterized by a D90 particles size of 1000 microns.
B01D 53/04 - 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 adsorption, p. ex. chromatographie préparatoire en phase gazeuse avec adsorbants fixes
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
99.
METHODS FOR AUTONOMOUSLY MONITORING AND ANALYZING THE OPERATION OF A BATTERY ENERGY STORAGE SYSTEM
A method for monitoring and analyzing the operation of a battery energy storage system (BESS) comprises, entering data parameters from one or more subsystems of a field installed BESS into a correlation matrix and extracting target correlations from the correlation matrix. The target correlations along with independent data parameters are entered into a relational coefficient matrix to identify data features. The method further includes extracting the data features from the relational coefficient matrix to a generative and adversarial artificial intelligence network model, where the extracted data features are used to train the model with data from the field installed BESS solution.
Processes and apparatuses for treating NOx from a carbon dioxide stream. Prior to separating carbon dioxide and NOx, NOx is converted to nitrogen gas in an NOx conversion zone, which may include an SCR reactor and/or CO boiler. A carbon separation zone which may include one or more fractionation columns produces a CO2 stream and an NOx stream. The NOx is passed back to the NOx conversion zone.
