The present invention relates to a process for the hydroconversion of a plastic feedstock comprising: (a1) a step of non-catalytic hydroconversion of said feedstock in the presence of hydrogen, in contact with a source of radicals, said source comprising sulfur and being introduced in such a way that the sulfur content is between 3% and 20% by weight of the feedstock, to produce first conversion products; (a2) a step of catalytic hydroconversion of the first conversion products in the presence of hydrogen, in contact with at least one hydroconversion catalyst, said hydroconversion catalyst comprising at least one hydro-dehydrogenating element selected from the group formed by the non-noble elements of Group VIB and Group VIII of the periodic table, taken alone or as a mixture, and a porous support comprising a porous mineral matrix and at least one zeolite, said steps (a1) and (a2) being carried out at an absolute pressure of between 1 MPa and 38 MPa, at a temperature of greater than or equal to 200°C and less than 400°C, at an hourly space velocity relative to each hydroconversion reactor of between 0.05 h‐1 and 10 h‐1, and with an amount of hydrogen of between 50 Nm3/m3and 5000 Nm3/m3.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/06 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
C10G 49/18 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or in the presence of hydrogen-generating compounds, e.g. ammonia, water, hydrogen sulfide
C08J 11/16 - Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with inorganic material
C10B 53/07 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of synthetic polymeric materials, e.g. tyres
C10G 47/22 - Non-catalytic cracking in the presence of hydrogen
C10G 47/24 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles
The present invention relates to a solid material mainly composed of BHET having a crystal form with a particular X-ray diffraction diagram, a method for the preparation thereof, a composition comprising said material, and the use of said composition for preparing a polyester.
The present invention relates to a catalytic composition for the selective oligomerization of ethylene, in particular for the trimerization and/or tetramerization of ethylene respectively into 1-hexene and/or 1-octene, which catalytic composition comprises: - at least one chromium- or titanium-based metal precursor; - at least one support in the form of solid methylaluminoxane (MAO); - at least one additive in the form of an aluminium-based compound. The invention further relates to an oligomerization method, preferably for the selective trimerization and/or tetramerization of ethylene respectively into 1-hexene and/or 1-octene, which method uses the catalytic composition according to the invention.
B01J 31/02 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
B01J 31/14 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides of aluminium or boron
The invention relates to an aromatic compound conversion unit (5), comprising: - a section (1) for the pre-fractionation of at least one stream comprising A9+ compounds into at least two effluents: a first effluent (3) enriched in aromatic compounds only substituted by methyls, and a second effluent (4) depleted in aromatic compounds only substituted by methyls; - a section (11) for the isomerisation of the A9+ of the second effluent, producing an isomerization effluent (7) enriched in aromatic compounds substituted in at least two methyl groups; - a section (8) for the post-fractionation of the isomerisation effluent originating from the A9+ isomerization section into at least two effluents: an effluent (10) enriched in aromatic 9-carbon-containing compounds and an effluent (9) depleted in aromatic 9-carbon-containing compounds; - means for recycling the effluent enriched in aromatic 9-carbon-containing compounds to the pre-fractionation section (1).
C07C 5/27 - Rearrangement of carbon atoms in the hydrocarbon skeleton
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
C07C 7/04 - Purification, separation or stabilisation of hydrocarbons; Use of additives by distillation
The present invention relates to a method for the hydroconversion of a plastic feedstock, the method comprising: (a1) a step of non-catalytic hydroconversion of the feedstock in the presence of hydrogen, in contact with a source of radicals, the source comprising sulfur and being added in such a way that the sulfur content is between 3% and 20% by weight of the feedstock, to produce first conversion products; (a2) a step of catalytic hydroconversion of the first conversion products in the presence of hydrogen, in contact with at least one hydroconversion catalyst, the hydroconversion catalyst comprising at least one hydro-dehydrogenating element selected from the group formed by the non-noble group VIB and group VIII elements of the periodic table, taken alone or as a mixture, with the exception of iron, and a non-zeolitic porous support comprising at least one amorphous silica-alumina, steps (a1) and (a2) being implemented at an absolute pressure of between 1 MPa and 38 MPa, at a temperature of between 200°C and 550°C, at an hourly space velocity relative to the volume of each hydroconversion reactor of between 0.05 h-1 and 10 h-1, and with an amount of hydrogen of between 50 Nm3/m3and 5000 Nm3/m3.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/06 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
C10G 49/18 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or in the presence of hydrogen-generating compounds, e.g. ammonia, water, hydrogen sulfide
C10G 47/22 - Non-catalytic cracking in the presence of hydrogen
C10G 47/24 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles
C10B 53/07 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of synthetic polymeric materials, e.g. tyres
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
6.
MIXING CHAMBER FOR A GAS-SOLID CO-CURRENT DOWNFLOW FLUIDISED-BED REACTOR
The invention relates to a device and a process for gas-solid co-current downflow fluidised-bed catalytic cracking comprising/using: a pipeline (1) suitable for carrying a downflow (4) of catalyst particles; a mixing chamber (2) connected to and fed by the pipeline with catalyst particles and comprising an inner wall, at least one first injector (5) of hydrocarbon feed (6) and a central bulk part (12) defining an annular zone (13) through which the catalyst particles pass through the mixing chamber; and a gas-solid co-current downflow fluidised bed reactor (3) fed by the mixing chamber with a mixture comprising catalyst particles and hydrocarbon feed, wherein the central bulk part comprises at least one internal element (11) arranged under the at least one first injector and being suitable for distributing the mixture towards the wall of the mixing chamber.
B01J 4/00 - Feed devices; Feed or outlet control devices
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
B01J 8/34 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
7.
METHOD FOR PREDICTING A LOG DURING DRILLING OF A WELL
The invention relates to a method for predicting a log beyond the depth of the drill bit of a well. Based on at least one log training curve acquired in a training well of depth larger than that of the drill bit, which curve is fitted to a curve of the log acquired in the well, a model for predicting the log in the well is constructed by means of a supervised machine-learning method. For each training curve, a compound training curve formed by the segment of the training curve fitted to the curve of the well up to the drill bit, and by the segment of the training curve fitted to the other training curves beyond the drill bit, is constructed. The values of the well log are predicted beyond the drill bit depth by applying the model to the compound training curves.
The present invention relates to a method for converting lignocellulosic biomass by bringing, in the aqueous phase, pretreated lignocellulosic biomass into contact with at least one biocatalyst (3) in a first reactor (1) containing a reaction medium comprising the pretreated lignocellulosic biomass (2) in the aqueous phase and the biocatalyst, the method comprising: - (a) a first step of liquefaction by adding the pretreated lignocellulosic biomass and at least one biocatalyst to the reactor without removing any or all of the reaction medium from the reactor; - followed by (b) a second step of continuous liquefaction with the continuous removal of some of the reaction medium from the first reactor, the addition of at least one biocatalyst, and the continuous addition of pretreated lignocellulosic biomass.
The invention relates to a simulated moving bed, SMB, separation column/method comprising/using a shell (1) which comprises a plurality of adsorbent beds separated by a plurality of trays, each tray comprising a plurality of panels (6), referred to as self-supporting panels, each panel (6) comprising a multi-sided metal frame (7), wherein the metal frame (7) is supported on a first side (13) by the shell and is supported on a second side (14) by: a main beam (3) arranged diametrically in the shell (1); and/or the shell (1) or a central tower (5) arranged in the shell (1), wherein the metal frame (7) comprises at least one third side (15) connecting the first side (13) to the second side (14), and wherein the at least one third side (15) has a height (H) and a thickness that are suitable for ensuring the mechanical strength of the panel.
B01D 15/18 - Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
C07C 7/12 - Purification, separation or stabilisation of hydrocarbons; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
B01F 25/721 - Spray-mixers, e.g. for mixing intersecting sheets of material with nozzles for spraying a fluid on falling particles or on a liquid curtain
11.
GAS-SOLID CO-CURRENT DOWNFLOW FLUIDISED BED REACTOR WITH HOMOGENEOUS FLOW
The invention relates to a device and a process for gas-solid co-current downflow fluidised bed catalytic cracking comprising/using: a pipeline (1) suitable for carrying a downflow (4) of catalyst particles; a mixing chamber (2) connected to the pipeline (1) and suitable for being fed by the pipeline with a downflow, the mixing chamber comprising an inner wall and at least one first injector (5) of hydrocarbon feed (6); a gas-solid co-current downflow fluidised bed reactor (3) connected to the mixing chamber and suitable for being fed by the mixing chamber with a mixture comprising catalyst particles and hydrocarbon feed, the downflow gas-solid co-current fluidised bed reactor comprising an inner wall, wherein the inner wall of the mixing chamber and/or of the downflow gas-solid co-current fluidised bed reactor comprises one or more obstacles (9).
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
The invention relates to a method for treating a lignocellulosic biomass, the method comprising: - a) a step of impregnating the biomass with a liquor to obtain an impregnated biomass; - b) a step of cooking the impregnated biomass, optionally accompanied by a steam explosion, to obtain a pretreated biomass; - c) a step of enzyme hydrolysis of the pretreated biomass, to obtain a hydrolyzed biomass in the form of one or more sugars; - d) a step of solid/liquid separation of the hydrolyzed biomass in the form of one or more sugars or of the hydrolyzed biomass in the form of one or more sugars which is then treated in one or more other steps subsequent to enzyme hydrolysis step c), so as to obtain a separated juice and an unconverted solid residue; - e) a step of recirculating at least some of the unconverted solid residue back to impregnation step a) and/or to cooking step b).
The invention relates to a method for constructing a wind farm in a predetermined space, in which at least the following successive steps are carried out: a) forming different grids (GR) in the predetermined space; b) for each grid, determining the average annual energy production of a mini-farm (AEP-mf) composed of wind turbines on the points of intersection of a mesh; c) selecting (Ch) a few grids that make it possible to maximize the energy production; d) for each grid c in step c), determining (Alg1) a first arrangement of the predefined number of wind turbines on the grid; e) modifying (Alg2) the position of the wind turbines on the grid; f) determining a definitive arrangement (Disp_F) of the wind turbines in the predetermined space, and constructing (Const) the wind farm.
The present invention relates to a crosslinkable electrolyte formulation comprising at least: - a hydrocarbon molecule comprising three to six, preferably four, thiol functions; - a bifunctional chain extender in the form of a hydrocarbon chain having two C=C double bonds ; - a monofunctional single-ion chain terminator comprising a C=C double bond and mobile lithium; - a monofunctional polyethylene-glycol-type chain terminator; - a nucleophilic-base-type catalyst, in which the molar ratio [C=C double bonds]/[thiols] is 1. The invention also relates to the preparation and use of a crosslinked solid electrolyte.
The present invention relates to a method for preparing a catalyst comprising at least one compound of a phosphate salt, of the M1HxPOy type, x being a fractional number between [0-2] and y being a fractional number between [3-4], with M selected from the group formed by the metals of group I and group II of the periodic table, taken alone or as a mixture, and a substrate comprising porous silicon carbide SiC, said method comprising at least a step of adding said phosphate salt to the substrate comprising the silicon carbide.
B01J 27/18 - Phosphorus; Compounds thereof containing oxygen with metals
B01J 27/228 - Silicon carbide with phosphorus, arsenic, antimony or bismuth
C07C 51/377 - Preparation of carboxylic acids or their salts, halides, or anhydrides by reactions not involving formation of carboxyl groups by hydrogenolysis of functional groups
B01J 37/02 - Impregnation, coating or precipitation
B01J 35/10 - Solids characterised by their surface properties or porosity
16.
SYSTEMS AND PROCESSES FOR TEMPERATURE CONTROL IN FLUIDIZED CATALYTIC CRACKING
A process for controlling catalyst temperature in a fluidized catalytic cracking ("FCC") system includes regenerating a spent catalyst feed in a regenerator at a first temperature to produce a regenerated catalyst feed, withdrawing at least a portion of the regenerated catalyst feed to a reactor, and cooling the portion of the regenerated catalyst between an outlet of the regenerator and an inlet of the reactor. A fluidized catalytic cracking ("FCC") system includes a catalyst regenerator configured and adapted to regenerate a spent catalyst feed at a first temperature to produce a regenerated catalyst, a reactor downstream from an outlet of the catalyst regenerator, a catalyst cooler between the outlet of the catalyst regenerator and an inlet of the reactor. The catalyst cooler is configured and adapted to cool at least a portion of a regenerated catalyst from the catalyst regenerator. In embodiments, the FCC system is a downer FCC system including at least one downer reactor and a spent catalyst riser regenerator.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
B01J 38/30 - Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
B01J 38/32 - Indirectly heating or cooling material within regeneration zone or prior to entry into regeneration zone
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
17.
SYSTEMS AND PROCESSES FOR TEMPERATURE CONTROL IN FLUIDIZED CATALYTIC CRACKING
A fluidized catalytic cracking ("FCC") system includes a catalyst regenerator configured and adapted to regenerate a spent catalyst feed to produce a regenerated catalyst. The system includes a reactor downstream from an outlet of the catalyst regenerator to receive regenerated catalyst therefrom. The system includes a spent catalyst riser between an outlet of the reactor and an inlet of the regenerator. The spent catalyst riser includes a torch oil injection nozzle configured and adapted to provide heat to the catalyst regenerator. A process for controlling catalyst temperature in an FCC system includes regenerating a spent catalyst feed in a catalyst regenerator to produce a regenerated catalyst feed, withdrawing at least a portion of the regenerated catalyst feed to a to a reactor, receiving a spent catalyst from the reactor in a spent catalyst riser, and heating the spent catalyst in the spent catalyst riser with a torch oil injection nozzle. In embodiments, the reactor is a downer.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
B01J 8/24 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
18.
METHOD FOR DEHYDRATING A FEEDSTOCK COMPRISING AN ALCOHOL FOR THE PRODUCTION OF ALKENES
2n2n+12n+1 where n is an integer between 3 and 20, the method comprising an isomerization dehydration step carried out in the gas phase, at a weighted mean temperature of between 200 and 300°C, at a pressure of between 0.1 and 1 MPa, at a weight hourly space velocity (PPH) of between 1 and 25 h-1, in the presence of a catalyst comprising at least one zeolite, wherein the zeolite has at least one series of channels, the pore opening of which is defined by a ring of eight oxygen atoms (8MR) and has a mesopore volume of 0.10 ml/g or greater.
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
The invention relates to a process for the hydrotreatment of a hydrocarbon feedstock, of which at least 50% by weight of the compounds have an initial boiling point of greater than 300°C and a final boiling point of lower than 650°C, so as to obtain a hydrotreated effluent. Said process comprises the following steps: a) said hydrocarbon feedstock is brought into contact, in the presence of hydrogen, with at least one first catalyst comprising an alumina support and an active phase consisting of nickel and molybdenum; b) the effluent obtained in step a) is brought into contact, in the presence of hydrogen, with at least one second catalyst comprising a silica-alumina support and an active phase consisting of nickel and tungsten, phosphorus and an organic compound.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 45/50 - Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metal, or compounds thereof
C10G 45/54 - Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
C10G 65/08 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a hydrogenation of the aromatic hydrocarbons
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
20.
PROCESS FOR PREPARING A CATALYST COMPRISING A GROUP VIII METAL AND A SUPPORT IN THE FORM OF A MONOLITH OR A FOAM COATED WITH ALPHA ALUMINA
Process for preparing a selective hydrogenation catalyst comprising an active phase based on at least one group VIII metal, deposited on an alpha alumina, and a support in the form of a ceramic or metal foam or monolith, which process comprises at least the following steps: - supplying a gamma alumina powder comprising a specific surface area of between 100 and 500 m²/g; - bringing into contact, by coating, the gamma alumina powder and a support in the form of a ceramic or metal foam or monolith; - calcining at a temperature of between 900°C and 1300°C; - bringing the calcined catalyst precursor into contact with a solution comprising a precursor of the active phase comprising a group VIII metal; - drying and then calcining the material.
C10G 45/40 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof
21.
IMPROVED METHOD FOR CONVERTING A FEEDSTOCK CONTAINING A BIOMASS FRACTION FOR THE PRODUCTION OF HYDROCARBONS BY MEANS OF FISCHER-TROPSCH SYNTHESIS
COMMISSARIAT A L'ENERGIE ATOMIQUE ET AUX ENERGIES ALTERNATIVES (France)
Inventor
Heraud, Jean-Philippe
Kalaydjian, François
Pires Da Cruz, Antonio
Hequet, Michael
Abstract
The present invention relates to a method for converting a feedstock comprising at least one biomass fraction into hydrocarbons, the method comprising a step a) of pretreating the feedstock; a water electrolysis step b) for obtaining a stream of hydrogen and a stream of oxygen, wherein the water is at least partially produced by means of Fischer-Tropsch synthesis carried out in step e); a step c) of gasifying the feedstock pretreated in step a) in the presence of all or some of the stream of oxygen from the water electrolysis step b) so as to obtain a gaseous effluent comprising a synthesis gas; an optional step d) of conditioning the gaseous effluent comprising a synthesis gas from step c); and a step e) of synthesising, by means of Fischer-Tropsch synthesis, the gaseous effluent from step c) or, optionally, from step d) in the presence of all or some of the hydrogen from the water electrolysis step b) so as to produce a stream comprising synthesis liquid hydrocarbons and at least one gaseous effluent.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
C10K 1/34 - Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
C10K 1/10 - Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
B01D 53/00 - Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
22.
METHOD FOR REJUVENATING A CATALYST FROM A HYDROPROCESSING AND/OR HYDROCRACKING PROCESS
The invention relates to a method for rejuvenating a catalyst comprising a group VIII metal, a group VIB metal and an oxide support not containing zeolite, comprising the following steps of: a) regenerating the catalyst at a temperature of greater than 360°C and less than 420°C so as to obtain a regenerated catalyst having a certain carbon and sulfur content and a proportion of crystalline phase determined by X-ray diffraction and characterised by a ratio of less than 0.6, b) placing the regenerated catalyst in contact with an aqueous solution consisting of water, phosphoric acid and an organic acid, each having an acidity constant pKa greater than 1.5, c) drying at a temperature of less than 200°C.
B01J 38/12 - Treating with free oxygen-containing gas
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
23.
METHOD FOR REJUVENATING A CATALYST FROM A HYDROPROCESSING AND/OR HYDROCRACKING PROCESS
The invention relates to a method for rejuvenating a catalyst comprising a group VIII metal, a group VI B metal and an oxide support not containing zeolite, comprising the following steps of: a) regenerating the catalyst at a temperature of greater than 360°C and less than 420°C so as to obtain a regenerated catalyst having a certain carbon and sulphur content and a proportion of crystalline phase determined by X-ray diffraction and characterised by a ratio of less than 0.6, b) then placing the regenerated catalyst in contact with at least one acidic or basic, organic or inorganic compound, c) drying at a temperature of less than 200°C.
B01J 38/12 - Treating with free oxygen-containing gas
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
24.
REGENERATION METHOD COMPRISING A REGENERATION STEP, A REJUVENATION STEP AND A CALCINATION STEP OF A ZEOLITE-BASED HYDROCRACKING CATALYST, AND USE THEREOF IN A HYDROCRACKING PROCESS
The present invention relates to a method for regenerating an at least partially spent catalyst from a hydrocracking process, said at least partially spent catalyst originating from a fresh catalyst comprising at least one group VIIl metal, at least one group VIB metal and a support comprising at least one zeolite, said method comprising at least the following steps: a) a regeneration step in which the at least partially spent catalyst is subjected to a thermal and/or hydrothermal treatment in the presence of an oxygen-containing gas at a temperature between 350° C and 460° C so as to obtain a regenerated catalyst, b) a step of rejuvenating the regenerated catalyst obtained in step a) by bringing same in contact with an organic or inorganic, acidic or basic compound, c) a step of calcining the catalyst obtained in step b) at a temperature higher than 300° C, optionally in the presence of water, in order to obtain a calcined rejuvenated catalyst.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
The present invention relates to a process for regenerating an at least partially spent catalyst derived from a hydrocracking process, the at least partially spent catalyst being derived from a fresh catalyst comprising at least one group VIII metal, at least one group VIB metal, and a substrate comprising at least one zeolite, the process comprising at least the following two steps: a) a regeneration step in which the at least partially spent catalyst is subjected to a thermal and/or hydrothermal treatment in the presence of an oxygen-containing gas at a temperature of between 350°C and 460°C so as to obtain a regenerated catalyst; b) a step of rejuvenating the regenerated catalyst derived from step a) by bringing it into contact with an acidic or basic, organic or inorganic compound, the acidic or basic, organic or inorganic compound not comprising the element phosphorus, in order to obtain a rejuvenated catalyst.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 37/14 - Oxidising with gases containing free oxygen
B01J 38/12 - Treating with free oxygen-containing gas
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
26.
METHOD FOR REGENERATING A ZEOLITE-BASED HYDROCRACKING CATALYST, AND USE THEREOF IN A HYDROCRACKING PROCESS
The present invention relates to a method for regenerating an at least partially spent catalyst from a hydrocracking process, said at least partially spent catalyst originating from a fresh catalyst comprising at least one group VIIl metal, at least one group VIB metal and a support comprising at least one zeolite, said method comprising at least one regeneration step in which the at least partially spent catalyst is subjected to a thermal and/or hydrothermal treatment in the presence of an oxygen-containing gas at a temperature between 350° C and 460° C so as to obtain a regenerated catalyst, said method not comprising any subsequent rejuvenation step of bringing the regenerated catalyst in contact with at least one organic or inorganic, acid or basic compound.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 37/14 - Oxidising with gases containing free oxygen
B01J 38/12 - Treating with free oxygen-containing gas
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
27.
PROCESS FOR PREPARING A CATALYST COMPRISING A GROUP VIII METAL FROM AN ALPHA ALUMINA
Process for preparing a selective hydrogenation catalyst comprising an active phase based on at least one group VIII metal, deposited on an alpha alumina, and a support in the form of a ceramic or metal foam or monolith, which process comprises at least the following steps: - supplying an alpha alumina powder comprising a specific surface area of between 1 and 50 m²/g; - bringing the alumina powder into contact with a solution comprising a precursor of the active phase comprising a group VIII metal; - drying and then calcining the catalyst precursor; - bringing the calcined catalyst precursor into contact with a support in the form of a ceramic or metal foam or monolith ; - calcining.
C10G 45/40 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof
28.
METHOD FOR PREPARING A CATALYST CONTAINING AN ACTIVE NICKEL PHASE AND A NICKEL-COPPER ALLOY
The invention relates to a method for preparing a catalyst containing nickel and copper and a porous alumina support, comprising the following steps of : a) bringing the alumina support into contact with a solution containing a nickel precursor and a first organic compound having at least one carboxylic acid function; b) drying at a temperature below 250°C, then calcining at a temperature of between 250°C and 550°C; c) bringing the calcined catalyst precursor obtained at the end of step b) into contact with a solution containing a nickel precursor, a copper precursor and a second organic compound having at least one carboxylic acid function; d) drying at a temperature below 250°C.
B01J 37/18 - Reducing with gases containing free hydrogen
C10G 45/48 - Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
C10G 45/36 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
29.
CLOSTRIDIUM BACTERIA MODIFIED TO SIMULTANEOUSLY ASSIMILATE A PLURALITY OF SUGARS, AND PREPARATION AND USES THEREOF
ClostridiumClostridium. The invention further relates to methods, tools and kits for deleting or modifying one or more coding sequences, or controlling the transcription of one or more coding sequences, the XylR and/or AraR transcriptional repressors, the genetically modified bacteria obtained and the uses thereof, in particular to simultaneously ferment at least one hexose and pentose, or the carbon-containing elements of a substrate comprising at least two carbon-containing elements chosen from among glucose, arabinose, xylose, mannose and galactose.
The present invention relates to a method for treating a catalyst comprising at least one aluminosilicate zeolite of the ZSM-5 family and a binder comprising silicon oxide, such that said treatment comprises a steam treatment of the catalyst, said steam treatment being carried out - on the catalyst in the form of a catalyst bed of catalyst particles - said bed being positioned in a reactor for catalytic conversion of hydrocarbons, - with a stream of steam treatment gas passing through said bed and comprising steam, - at a temperature of at least 150°C, - and a pressure of at most 3x106 Pa.
12344 being independently chosen from among linear, branched or cyclic alkyl groups, having 1 to 10 carbon atoms, and X- being the hydroxide ion OH-; - in at least one solvent, bringing the dehydration catalyst into contact with the feedstock comprising a hexose at a temperature of between 30 and 160°C and a pressure of between 0.0001 and 8.0 MPa.
B01J 29/70 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups
32.
SYSTEM FOR LOCKING AND UNLOCKING AN ELONGATED ELEMENT WITH A SHEATH AND AN ATTACHMENT ELEMENT AT EITHER END OF THE SHEATH
The invention relates to a system for locking/unlocking a cable 14 to/from a support, which system comprises: - a sheath with an opening at each end for the cable 14 to pass therethrough 11; - a first attachment element 12 attached to the sheath 11 at a first end; - a second attachment element attached to the sheath 11 at a second end; - a spacer means for increasing the distance between the first and second attachment elements in order to exert a tension on the sheath 11. The second attachment element comprises at least two movable bodies 15 and 16 that are movable relative to one another and a drive means 25 for driving a first movement of one of the bodies 15 or 16 relative to the other, the first movement causing the sheath 11 to tighten on the elongated element 14 at the second end.
F16G 11/04 - Means for fastening cables or ropes to one another or to other objects; Caps or sleeves for fixing on cables or ropes with wedging action, e.g. friction clamps of grommet-thimble type
The invention relates to a method for compressing carbon dioxide comprising at least the following steps: a) compressing (Comp) the fluid to a pressure (P1) greater than 8 bar and strictly lower than 50 bar; b) cooling (Ref1) the compressed fluid to a temperature (T1') between -50°C and 15°C so as to partially liquefy the fluid, the gas fraction of the fluid being between 1% and 99% by volume; c) compressing (PP), by means of multi-stage compression, the compressed and cooled fluid to a pressure (P3) strictly lower than the critical pressure of the fluid; d) preferably cooling (Ref2) the fluid produced by the multi-stage compression step (PP) in order to completely liquefy at least the carbon dioxide; e) compressing (PSP) the fluid so that the pressure (P4) of the fluid exceeds the critical point of the fluid. The invention also relates to a transport and storage method, as well as to a system for compressing carbon dioxide.
The invention relates to a system for obtaining water from at least one underwater spring, which system comprises a separation means (1) for separating the spring water from the seawater, an overflow tank (5) comprising an opening for receiving the water and a collection device (4) for collecting the spring water spring, the overflow tank (5) comprising an overflow wall configured such that the spring water travels over the overflow wall in order to enter, under gravitational force, into the collection device (4). Moreover, the overflow cross-section of the overflow tank (5) is strictly greater than the flow cross-section of the opening and the overflow cross-section of the overflow tank (5) is located above sea level (8). Figure 1 to be published.
The invention relates to a method for processing lignocellulosic biomass, the method using at least one reactor (9; 14) for processing the biomass, the reactor (9; 14) being provided with a feed device (6; 11) equipped with a biomass inlet and a biomass outlet, the biomass outlet being in fluid communication with an inlet of the reactor, such that - a residue (8; 13) is extracted from the biomass, as it passes through the feed device (6; 11) to the reactor (9; 14), via an extraction outlet provided in the device, the residue being a solid and liquid mixture; - the residue is separated into a solid residue (32; 42) and a liquid residue (31; 41); - at least some of the solid residue (32; 42) is added back into the feed device or into one of the feed devices.
The present invention relates to a process for hydrocracking hydrocarbon feedstocks, comprising at least the steps of a) hydrotreatment of said feedstocks; b) a first step of hydrocracking of at least a portion of the effluent leaving step a); c) the gas/liquid separation of the effluent resulting from step b) to produce a liquid effluent and a gaseous effluent; d) the separation of the liquid effluent resulting from step c) into at least one "converted" effluent comprising hydrocarbon compounds having boiling points of less than a temperature T1 of between 340°C and 385°C and an unconverted liquid fraction comprising hydrocarbon compounds having a boiling point of greater than the temperature T1; e) the fractionation of the "converted" liquid effluent resulting from step d) and comprising hydrocarbon compounds having boiling points of less than the temperature T1, to obtain at least one first fraction comprising hydrocarbon compounds having a boiling point of less than a temperature T2 of between 150°C and 220°C and at least one second fraction comprising hydrocarbon compounds having a boiling point of greater than the temperature T2 but less than the temperature T1; f) a second step of hydrocracking of at least a portion of the second liquid fraction resulting from step e) and comprising hydrocarbon compounds having a boiling point of greater than the temperature T2, but less than the temperature T1.
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
C10G 65/10 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
37.
PROCESS FOR RECYCLING USED PLASTICS BASED ON POLYETHYLENE USING A LIGHT HYDROCARBON SOLVENT
Process for purifying a plastic feedstock comprising polyethylene, which comprises: a) dissolving the plastic feedstock in a dissolution solvent comprising a hydrocarbon compound having a boiling point of between -15°C and 100°C, at a dissolution temperature of between 120°C and 220°C and a dissolution pressure of between 1.0 and 25.0 MPa absolute, to obtain a crude polymer solution; b) purifying the crude polymer solution, comprising: b1) separation of the insoluble matter; and/or b2) washing, with a dense solution; and/or b3) extraction, by an extraction solvent; and/or b4) adsorption of the impurities; then c) solvent-polymer separation, using a supercritical separation section, at a temperature of between 160 and 300°C and a pressure of between 2.7 and 10.0 MPa absolute, followed by at least one solvent recovery section, to obtain purified polyethylene.
Process for purifying a plastic feedstock, comprising: a) a dissolution step comprising placing the plastic feedstock in contact with a dissolution solvent comprising a hydrocarbon compound having a boiling point of between -15 and 100°C, at a dissolution temperature of between 120°C and 250°C and a dissolution pressure of between 1.0 and 25.0 MPa, to obtain a crude polymer solution; b) a step of purifying the crude polymer solution to obtain a purified polymer solution, comprising: b1) separation of the insoluble matter; and/or b2) washing, by contact with a dense solution; and/or b3) extraction, by contact with an extraction solvent; and/or b4) adsorption of the impurities; then c) a solvent-polymer separation step, using a supercritical separation section, operated at between 160 and 300°C and at a pressure of between 2.7 and 10.0 MPa, followed by at least one solvent recovery section, to obtain purified thermoplastics.
The invention relates to a method for purifying a plastics feedstock comprising polypropylene, said method comprising the steps of: a) dissolving the plastics feedstock in a dissolution solvent comprising a hydrocarbon compound having a boiling point of between -15°C and 100°C, at a dissolution temperature of between 150°C and 250°C and a dissolution pressure of between 1.0 and 18.0 MPa absolute, in order to obtain a crude polymer solution; b) purifying the crude polymer solution, comprising: b1) separating the insoluble substances; and/or b2) washing, using a dense solution; and/or b3) extraction, using an extraction solvent; and/or b4) adsorbing impurities; then c) solvent-polymer separation, using a supercritical separation section, at a temperature of between 160 and 300°C and a pressure of between 2.7 and 10.0 MPa absolute, followed by at least one solvent recovery section, in order to obtain purified polypropylene.
C01B 39/48 - Other types characterised by their X-ray diffraction pattern and their defined composition using at least one organic template directing agent
SYNTHESIS OF LEVULINIC ACID BY HYDRATION OF FURFURYL ALCOHOL IN THE PRESENCE OF A HOMOGENEOUS ACID CATALYST AND OF A SOLVENT BASED ON ETHER AND/OR ACETALS
The present invention relates to a method for synthesising levulinic acid by hydration of furfuryl alcohol at a temperature of between 25 and 140°C in the presence of a homogeneous acid catalyst and of a solvent based on ether and/or acetal. The use of such a solvent makes it possible to obtain an equivalent, or better, yield than the yields obtained with known solvents, while having high stability properties.
The present invention relates to a method for separating levulinic acid from a composition comprising levulinic acid and humins, in which said composition is subjected to a step of thermal separation in the presence of a flux having a boiling point above that of levulinic acid so as to obtain a light fraction containing levulinic acid and a heavy fraction containing the humins and said flux. The presence of a flux makes it possible to reduce the viscosity of the humins and to increase the degree of levulinic acid recovery.
The present invention relates to a vehicle comprising a powertrain (2) equipped with a cooling system (1). The cooling system (1) comprises a radiator (3) on the front face of the vehicle, this radiator being equipped with an electric motor-fan device (5), which is powered by a dedicated electric circuit. Said dedicated electric circuit comprises a power generation device (7) independent of the powertrain, and a rechargeable electric battery (6).
hhh) during a predetermined period. The forecast model is a combination of a calibrated transfer function (FT CS) and a power variation model (MOD VAR) constructed by way of machine learning, the combination (MOD PRO) being corrected (COR) on the basis of the produced power. A produced power forecast is then determined in real time by applying the produced power forecast model (MOD COR).
The present invention relates to a column for the liquid-liquid extraction of a feedstock by an extraction solvent, comprising perforated trays (Pi) for the passage of a dispersed phase (B), the perforated trays being spaced apart by an inter-tray space (8), and comprising spillways (6), a spillway being a hole allowing the passage of a continuous phase (A) through a perforated tray, the extraction column (1) alternately comprising perforated trays of type I having two peripheral spillways, and perforated trays of type II having a single central spillway, wherein: the cross-section S2 of the central spillways is larger than the cross-section S1 of the peripheral spillways, cross-section S1 corresponding to the sum of the cross-sections of the two peripheral spillways. The present invention also relates to a liquid-liquid extraction method using said liquid-liquid extraction column.
B01D 11/04 - Solvent extraction of solutions which are liquid
C07C 7/10 - Purification, separation or stabilisation of hydrocarbons; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
The present invention relates to a column for the liquid-liquid extraction of a feedstock by an extraction solvent, comprising perforated trays (Pi) for the passage of a dispersed phase (B), the perforated trays being spaced apart by an inter-tray space (8), and comprising spillways (6), a spillway being a hole allowing the passage of a continuous phase (A) through a perforated tray, the extraction column (1) alternately comprising perforated trays of type I having two peripheral spillways, and perforated trays of type II having a single central spillway, wherein: the height H1 of the inter-tray spaces located directly downstream of the trays of type I, in the direction of flow of the continuous phase, is greater than the height H2 of the inter-tray spaces located directly downstream of the trays of type II. The present invention also relates to a liquid-liquid extraction method using said liquid-liquid extraction column.
B01D 11/04 - Solvent extraction of solutions which are liquid
C07C 7/10 - Purification, separation or stabilisation of hydrocarbons; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
2223322S coming from the method, to decrease the consumption of the sulphurising agent to maintain the catalysts in sulphide form in feedstocks having low sulphur content.
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10B 53/07 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of synthetic polymeric materials, e.g. tyres
48.
VEHICLE WITH A COOLING SYSTEM COMPRISING A COLD PLATE
The present invention relates to a vehicle comprising a cooling system that is intended to cool at least one heat-producing vehicle member (5). The cooling system comprises a closed circuit (5) for the circulation of thermal fluid which comprises a radiator (7), a means for exchanging heat with the heat-producing member (5), a pump (6) and a cold plate device (1). The cold plate (1) is incorporated into a part of the bodywork of the vehicle.
The present invention relates to a method and to a device for separating aromatic compounds from a feedstock (1) comprising a mixture of aromatic and non-aromatic compounds, in which aromatics are extracted from the feedstock in a liquid-liquid extractor (T1) fed with a solvent stream (2) in order to produce at least an extract (4) concentrated in aromatic compounds, with respect to the feedstock, and a raffinate (3) concentrated in non-aromatic compounds, with respect to the composition of the feedstock; and in which an upper part (Z1) and a lower part (Z2) of the liquid-liquid extractor (T1) are fed respectively with a first fraction (51) and a second fraction (52) of extract recycle stream (5), the upper part and the lower part being defined with respect to the position of the feed point of the feedstock in the liquid-liquid extractor.
B01D 11/04 - Solvent extraction of solutions which are liquid
C07C 7/10 - Purification, separation or stabilisation of hydrocarbons; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
C10G 1/04 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
51.
CATALYST BASED ON PALLADIUM AND ZINC ON AN ALUMINA SUPPORT
Catalyst consisting of an active phase of palladium and zinc, and a porous alumina support, the palladium content being between 0.01% and 2% by weight of palladium element relative to the total weight of the catalyst, the zinc content being between 5% and 30% by weight of zinc element relative to the total weight of the catalyst, said catalyst not comprising any alloy based on palladium and zinc, the metallic dispersion D of the palladium being between 10% and 30%.
B01J 23/60 - Platinum group metals with zinc, cadmium or mercury
B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
B01J 37/02 - Impregnation, coating or precipitation
C10G 45/40 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof
C07C 7/167 - Purification, separation or stabilisation of hydrocarbons; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
C07C 5/03 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
52.
PROCESS FOR PRODUCING CELLULOLYTIC AND/OR HEMICELLULOLYTIC ENZYMES
The present invention concerns a process for producing cellulolytic and/or hemicellulolytic enzymes by a cellulolytic and/or hemicellulolytic microorganism, said process comprising at least - a) a phase of growth of the microorganism in the presence of at least one carbonaceous substrate, then - b) a phase of production of the enzymes in the presence of at least one inductive substrate, and also: - c) a phase of preparation of a carbonaceous substrate comprising glucose and/or fructose, said carbonaceous substrate being used in one and/or the other of the phases a) of growth and b) of production, said phase of preparation comprising a step c1) of hydrolysis of sucrose in acidic aqueous medium to give glucose and fructose.
The present invention relates to a process for hydroconversion of a feedstock comprising a fraction of less than 50% by weight of plastic pyrolysis oil and/or CSR (102) and a heavy hydrocarbon fraction (101) containing a part of at least 50% by weight having a boiling point of at least 300 °C, and containing sulfur and nitrogen. The hydroconversion uses one or more ebullated-bed or hybrid ebullated-bed reactors (20), and preferably two successive hydroconversion steps. The process according to the invention makes it possible to produce higher quality materials with a lower boiling point, for example for the production of fuels or chemical compounds for petrochemistry, with an improved yield of certain cuts while allowing for facilitated treatment of the hydroconverted products in downstream steps as fixed bed hydrotreatment and maintaining good stability of the unconverted fraction.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 65/02 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10B 53/00 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
C10G 49/04 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 49/10 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or with moving solid particles
C10G 69/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
C10B 53/07 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of synthetic polymeric materials, e.g. tyres
54.
CATALYTIC MATERIAL BASED ON A GROUP VIB ELEMENT AND A GROUP IVB ELEMENT FOR THE PRODUCTION OF HYDROGEN BY ELECTROLYSIS OF WATER
CENTRE NATIONAL DE LA RECHERCHE SCIENTIFIQUE (CNRS) (France)
UNIVERSITE CLAUDE BERNARD (LYON 1) (France)
GRENOBLE INP (INSTITUT POLYTECHNIQUE DE GRENOBLE) (France)
UNIVERSITE SAVOIE MONT BLANC (France)
UNIVERSITE GRENOBLE ALPES (France)
Inventor
Bonduelle, Audrey
Obadia, Mona Marie
Cacciuttolo, Quentin
Steinmann, Stephan
Abidi, Nawras
Dubau, Laetitia
Sibert, Eric
Abstract
The invention relates to a catalytic material comprising at least one group VIB metal at least partially in sulphurated form, at least one group IVB metal at least partially in sulphurated form, and an electrically conductive support, wherein said group VIB metal is selected from molybdenum and/or tungsten, and said group IVB metal is selected from titanium, zirconium and/or hafnium.
The invention relates to a hydrocracking catalyst which is selective towards the naphtha cut and to the hydrocracking process utilizing said catalyst, said catalyst comprising at least one hydro-dehydrogenating element selected from the group consisting of group VIB elements and non-noble group VIII elements, individually or as a mixture from the periodic table, and a support comprising at least one porous mineral matrix, a first zeolite Y having an initial crystal parameter a0 of the elementary mesh greater than 24.42 Å and a second zeolite Y having an initial crystal parameter a0 of the elementary mesh strictly less than 24.40 Å, a BET specific surface area of between 700 and 1000 m2/g, a microporous volume determined by nitrogen adsorption of greater than 0.28 ml/g and a Brønsted acidity of greater than 300 micromoles/g.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 29/70 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups
B01J 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
B01J 37/02 - Impregnation, coating or precipitation
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
The present invention relates to a method for the hydroconversion of a feedstock comprising a vegetable and/or animal oil fraction (102), in particular used oil and a heavy hydrocarbon fraction (101) containing a portion of at least 50% by weight that has a boiling point of at least 300°C and containing sulphur and nitrogen, the sum of the vegetable and/or animal oil fraction (102) and of the heavy hydrocarbon fraction (101) forming 100% of the feedstock by weight. The hydroconversion implements one or more ebullated bed or hybrid ebullated-entrained bed reactors (20), and preferably two successive hydroconversion steps, with a view to producing materials having a higher quality, with a lower boiling point, for example for producing fuels or chemical products, while being designed to be used with said vegetable and/or animal oil fraction.
C10G 47/30 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised bed" technique
C10G 47/28 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "moving bed" technique
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 45/18 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles according to the "moving bed" technique
C10G 45/20 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles according to the "fluidised bed" technique
C10G 45/16 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles suspended in the oil, e.g. slurries
C10G 47/26 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
C10G 65/02 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 49/10 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or with moving solid particles
57.
METHOD FOR MONITORING THE CONCENTRATION OVER TIME OF A CHEMICAL COMPOUND IN A FLUID, BY MEANS OF AN OPTICAL MEASUREMENT SYSTEM
The invention relates to a method for determining a change over time of a concentration of a chemical compound in a fluid, by means of an optical measurement system. A model of the change in absorbance (A) as a function of the concentration is constructed: a plurality of absorption spectra (S1, S9) of the chemical compound are measured, each corresponding to a concentration of the chemical compound, a curve (DI) is defined which intersects each of the absorption spectra (S1, S9) at a single point such that the curve is a bijective function of the absorbance (A) and of the wavelength (L), and the model of the change in absorbance (A) as a function of the concentration is constructed on the basis of the absorbance values at the intersection points and the relative concentration at each absorption spectrum (S1, S9). A change over time of a concentration of the chemical compound is then determined by means of the model thus determined.
G01N 21/31 - Investigating relative effect of material at wavelengths characteristic of specific elements or molecules, e.g. atomic absorption spectrometry
G01N 21/33 - Investigating relative effect of material at wavelengths characteristic of specific elements or molecules, e.g. atomic absorption spectrometry using ultraviolet light
G01N 21/77 - Systems in which material is subjected to a chemical reaction, the progress or the result of the reaction being investigated by observing the effect on a chemical indicator
The invention relates to a method for producing an aqueous 5-hydroxymethylfurfural (5-HMF) solution, comprising: - a step a) of bringing a feed containing 5-HMF and dimethyl sulfoxide (DMSO) into contact with an intermediate aqueous back-extract from step c) in order to obtain an aqueous mixture, - a step b) of liquid-liquid extraction of the aqueous mixture by a stream of extraction solvent in order to produce an aqueous raffinate and an intermediate organic extract, - a step c) of backwashing the intermediate organic extract with an aqueous solvent in order to produce the intermediate aqueous back-extract and an organic raffinate, and - a step d) of liquid-liquid back-extraction of the organic raffinate obtained at the end of step c) by an aqueous stream in order to produce an organic effluent and an aqueous back-extract of 5-HMF.
2222S and C4-hydrocarbon compounds and, at the bottom, a stabilised petrol; (e) at least partially recycling the gaseous fraction obtained on completion of step (c) to at least one of steps (a) and/or (b).
C10G 45/06 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 45/38 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metals, or compounds thereof
The invention relates to a method for producing a light petrol fraction comprising a sulphur content of less than 10 ppm by weight relative to the total weight of the light petrol fraction from a petrol comprising sulphur compounds, olefins and diolefins, the method comprising: a) a selective hydrogenation step to hydrogenate the diolefins and to perform a reaction for increasing the weight of a portion of the sulphur compounds; b) a step of separating the effluent obtained from step a) into a gaseous fraction, a light petrol fraction and a heavy petrol fraction, step b) being performed in a fractionating column comprising n plates, n being an integer greater than or equal to 20, the first plate being the reboiler and the "nth" plate being the condenser, it being understood that the light petrol fraction is drawn off the fractionating column at the "n-ith" plate, wherein i is between 1 and 10.
C10G 45/38 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metals, or compounds thereof
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 45/06 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
The present invention relates to a method for regenerating a trapping mass for trapping heavy metals, which trapping mass is loaded with heavy metals, wherein the trapping mass is placed in contact with a sulphiding stream; a regenerated trapping mass having a heavy metal content of between 0.1% by weight and 45% by weight relative to the total weight of the regenerated trapping mass; and a method for trapping heavy metals from a gaseous or liquid feedstock, comprising placing the feedstock in contact with the regenerated trapping mass.
B01D 53/96 - Regeneration, reactivation or recycling of reactants
B01J 20/02 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/28 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
B01J 20/30 - Processes for preparing, regenerating or reactivating
The invention relates to a catalytic composition in the form of a Pickering emulsion, said composition having a first non-aqueous liquid phase L1 containing hydrocarbon compounds, in which drops of a second liquid phase L2 are stabilized by solid particles, said second liquid phase L2 containing at least one ionic liquid of formula Q+A-, where Q+is an organic cation and A- is an anion, and in which a Brønsted HB acid is dissolved.
The invention relates to a method and device for extraction by lithium adsorption in a simulated moving bed, wherein at least one column (Ci) is fed with a feedstock (F) comprising lithium and a desorbent (D), and an extract (E) and a raffinate (R) are drawn from the column (Ci), said column (Ci) comprising an adsorbent solid (Ai) comprising a lithiated aluminium oxyhydroxide and/or a lithiated aluminium hydroxide which are interconnected in a closed loop, the feeding and drawing points of the column (Ci) being shifted over time by a value corresponding to a predetermined amount of adsorbent solid with a permutation period and determining a plurality of operating zones of the column (Ci), and in particular the following main zones: a lithium desorption zone I; a desorption zone II for compounds other than lithium; and a lithium adsorption zone III.
B01D 15/18 - Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
B01J 20/08 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
C01D 3/16 - Purification by precipitation or adsorption
66.
METHOD AND SYSTEM FOR CONTROLLING AN ELECTRIC MACHINE DRIVEN BY AN INVERTER PROVIDED WITH A PLURALITY OF SWITCHING ARMS
The present invention relates to a method and a system for controlling an inverter (OND) of an electric machine (MEL), which implement a control model (MOD) that calculates the optimal current setpoints as a function of the torque setpoint (Cem*) or the speed setpoint and other operating variables (VAF), including a corrected operating variable (VARcorr). The correction of this operating variable is implemented by means of a feedback loop controlling the control voltage of the electric machine.
The invention relates to a method for producing an aqueous solution of 5-hydroxymethylfurfural (5-HMF), involving the following steps in succession: a) bringing a feed containing 5-HMF and dimethyl sulfoxide (DMSO) into contact with an intermediate aqueous counter-extract from a backwashing step c), b) a liquid-liquid extraction with an organic solvent followed by a backwashing step c) with an aqueous solvent to obtain an organic raffinate rich in 5-HMF and solvent. The raffinate then undergoes a concentration step d) and then a hydrodistillation step e) in order to obtain an aqueous solution of 5-HMF.
The invention describes a catalyst comprising at least one hydro/dehydrogenating element chosen from the group formed by the elements from group VIB and from group VIII of the periodic table, alone or as a mixture, and a support comprising at least one zeolite and one amorphous silica-alumina, wherein the zeolite has an acid site distribution index (ASDI) of greater than 0.15 and a density of acid sites (determined by H/D exchange) of between 0.05 and 1mmol/g, and wherein the support has a pore volume, measured by nitrogen porosimetry, developed within the pores with a diameter of between 6 nm and 11 nm, of less than 0.5 ml/g, a grain density, measured by mercury displacement under a pressure of 0.003 MPa, of greater than 0.93 g/ml, and a tapped packing density (TPD) of greater than 0.5 g/ml and less than 0.65 g/ml. A further subject of the present invention relates to the process for preparing said catalyst, comprising at least one step of preparing a silica-alumina gel by mixing a silica precursor with a specific alumina precursor, and to a process for hydrocracking a hydrocarbon feedstock in the presence of said catalyst.
B01J 29/08 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
B01J 29/78 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
69.
GAS-LIQUID SEPARATION DEVICE WITH A ZONE FOR GUIDING THE LIQUID AT THE OUTLET END, IN PARTICULAR FOR A THREE-PHASE FLUIDISED BED REACTOR
The invention relates to a gas-liquid separation device, in particular for use in the recirculation zone of three-phase fluidised bed reactors. The gas-liquid separation device comprises a plurality of separation elements, each having an inlet duct (70) and a succession of at least two bends (71, 72), a first bend (71) located in the plane (zy), the axis of the first bend (71) forming an orientation angle a relative to the vertical axis z of between 45° and 315°, and a second bend (72) forming a second orientation angle p with the first bend (71) of between 1° and 135°. The two first successive bends (71, 72) are separated by a distance D1 of between D/2 and 4D, D being the diameter of the inlet duct (70). Each separation element comprises a liquid guidance device (73) which is positioned at the outlet end of the second bend (72), and which has an open section.
C10G 49/12 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or with moving solid particles suspended in the oil, e.g. slurries
B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
Disclosed is a method for treating a petrol containing sulphur compounds, olefins and diolefins, the method comprising the following steps: (a) bringing the petrol into contact with hydrogen and a hydrodesulphurisation catalyst so as to obtain a partially desulphurised effluent; (b) bringing the partially desulphurised effluent obtained on completion of step (a) into contact, directly and without any separation, with a gaseous or liquid feedstock as a diluent, under normal conditions of temperature and pressure, so as to obtain a diluted and partially desulphurised effluent; (c) bringing the diluted and partially desulphurised effluent obtained on completion of step (b) into contact with hydrogen and a catalyst so as to obtain a desulphurised effluent.
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
C10G 69/04 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
C10G 45/38 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metals, or compounds thereof
C10G 11/00 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
C10G 45/32 - Selective hydrogenation of the diolefin or acetylene compounds
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
71.
LIQUID-LIQUID EXTRACTION COLUMN WITH VARIABLE INTER-TRAY SPACE
The present invention relates to a catalytic composition in the form of a capsule, having walls of solid material which define a closed volume containing a liquid phase that contains at least one ionic liquid of formula Q+A-, where Q+is an organic cation and A- is an anion, and in which a Brönsted HB acid is dissolved. It is provided that said liquid phase is in the form of a Pickering emulsion.
The invention relates to a production and separation device and method wherein: a reforming effluent (40) is produced and fractionated in a separation unit (1) and a fractionation train (5-6-7) for extracting benzene (22), toluene (23), xylenes (24) and C9-10 aromatics; aromatics are extracted from a feedstock (41) in a liquid-liquid extraction unit (14) to produce a first raffinate (43) and a first extract (42), the first extract (42) being sent to a benzene-toluene fractionation device (5); the xylenes are separated in a xylene separation unit (10) to produce a second extract (31) containing para-xylene, and a second raffinate (32) containing ortho-xylene and meta-xylene; and the second raffinate is isomerised in an isomerisation unit (11) so as to produce an isomerate (34) enriched in para-xylene sent to a fractionation train (5-6-7).
C10G 61/02 - Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
C10G 61/10 - Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen processes also including other conversion steps
C07C 7/00 - Purification, separation or stabilisation of hydrocarbons; Use of additives
C07C 5/22 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
C07C 6/04 - Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond
C07C 7/10 - Purification, separation or stabilisation of hydrocarbons; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
C07C 7/04 - Purification, separation or stabilisation of hydrocarbons; Use of additives by distillation
C10G 57/00 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
C10G 63/08 - Treatment of naphtha by at least one reforming process and at least one other conversion process plural parallel stages only including at least one cracking step
74.
HYDROCONVERSION IN A BUBBLING OR HYBRID BUBBLING/ENTRAINED BED OF A FEEDSTOCK COMPRISING A PLASTIC FRACTION
The present invention relates to a method for hydroconversion of a feedstock comprising a plastic fraction (102), in particular resulting from plastic waste, and a heavy hydrocarbon fraction (101), in particular a heavy hydrocarbon fraction containing a portion of at least 50% by weight, preferably at least 80% by weight, having a boiling temperature of at least 300°C. The hydroconversion uses one or more bubbling-bed or hybrid bubbling/entrained-bed reactors (20), and preferably two consecutive hydroconversion stages, with a view to producing higher quality materials with a lower boiling point, for example for fuel production purposes, while at the same time enabling the upcycling of plastic waste.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/08 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation with moving catalysts
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 49/12 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or with moving solid particles suspended in the oil, e.g. slurries
C10G 65/02 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
75.
DEVICE FOR SEPARATING A MIXTURE OF FLUIDS BY MICROFLUIDIC DISTILLATION
CENTRE NATIONAL DE LA RECHERCHE SCIENTIFIQUE (France)
INSTITUT POLYTECHNIQUE DE BORDEAUX (France)
UNIVERSITÉ DE BORDEAUX (France)
IFP ENERGIES NOUVELLES (France)
Inventor
Marre, Samuel
Nguyen, Olivier
Aymonier, Cyril
El Masri, Farah
Bonnin, Charles
Bergeot, Ghislain
Brunet-Errard, Lena
Abstract
The invention relates to a device (20) for separating a mixture of fluids by capillary action, of the type comprising: a separation duct (26); a first (64) and a second (66) fluid outlet, which are formed at the ends of the duct; and a fluid inlet (68); the duct comprising: a first channel (40) for guiding a flow of liquid by capillary action; a second channel (42) for guiding a flow of gas, the first and second channels being delimited by an interface (60) permitting exchanges of material between the flows. The first channel comprises a bottom surface (46) and a plurality of projecting studs (44); and each stud comprises an end (48), the ends of the studs forming a surface continuous with the interface (60).
The present invention relates to a cyclone for gas-solid separation in a chemical looping combustion facility with a hydrocarbon feedstock using circulating fluidised bed reactors. The novel cyclone comprises a specific inlet duct with a lower wall and a sloped lateral wall and at least one auxiliary gas injection at the lower wall, which makes it possible to decrease the deposition of solids at the inlet of the cyclone, potentially carry out chemical reactions within the cyclone, and improve the efficiency of the cyclone. Figure 1 to be published.
The invention relates to a hydrocracking catalyst comprising at least one hydro-dehydrogenating element selected from the group formed of the non-noble elements from groups VIB and VIII of the periodic table taken alone or in a mixture, and a support comprising at least one porous inorganic matrix, an MPI-structure zeolite and a zeolite Y having an initial lattice constant a0 of the unit cell greater than 24.32 Å and a Bronsted acidity greater than 200 micromol/g.
C10G 47/18 - Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
B01J 29/10 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
B01J 29/42 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing iron group metals, noble metals or copper
B01J 29/48 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
78.
METHOD FOR CAPTURING MERCAPTANS USING A MACRO AND MESOPOROUS CAPTURE MASS
The invention relates to a method for capturing mercaptans in a sulphur-containing hydrocarbon feedstock, in the presence of a capture mass comprising an active phase based on at least one metal from group VIII, IB or IIB, and a mesoporous and macroporous support, said capture mass having a specific surface area of between 120 m 2/g and 350 m 2/g, and: - the volume of mesopores with a diameter greater than or equal to 2 nm and less than 50 nm represents between 40% and 70% by volume of the total pore volume of the capture mass; - and the volume of macropores with a diameter greater than or equal to 50 nm represents between 30% and 60% by volume of the total pore volume of the capture mass.
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 25/05 - Removal of non-hydrocarbon compounds, e.g. sulfur compounds
B01J 20/02 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/08 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/10 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
B01J 20/28 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
The present invention relates to a process for recovering mercaptans contained in a hydrocarbon-based feedstock containing sulfur, optionally partially desulfurised following a step of catalytic hydrodesulfurisation, at a temperature of between 170°C and 220°C, a pressure of between 0.2 MPa and 5 MPa, at an hourly space velocity, defined as the volumetric flow rate of the incoming feedstock over the volume of recovery mass, of between 0.1 h-1and 50 h-1, in the presence of a recovery mass comprising an active phase based on nickel with an Ni°/NiO ratio of between 0.25 and 4, and an inorganic support selected from the group consisting of alumina, silica, silica-alumina and clays.
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 25/05 - Removal of non-hydrocarbon compounds, e.g. sulfur compounds
B01J 20/02 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/08 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/10 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
B01J 20/28 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
The present invention relates to a process for scavenging mercaptans contained in a hydrocarbon-based feedstock containing sulfur, optionally partially desulfurised following a step of catalytic hydrodesulfurisation, at a temperature of between 40°C and 250°C, a pressure of between 0.2 MPa and 5 MPa, at an hourly space velocity, defined as the volumetric flow rate of the incoming feedstock over the volume of scavenger, of between 0.1 h-1and 50 h-1, in the presence of a scavenger comprising an active phase based on at least one metal from group VIII, IB or IIB, and an oxide or a porous oxide mixture, the active metal of which has been activated beforehand by reduction and then passivated with a view to the loading thereof by a carbon dioxide treatment.
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 25/05 - Removal of non-hydrocarbon compounds, e.g. sulfur compounds
B01J 20/02 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/08 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/10 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
B01J 20/28 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
The present invention relates to a crosslinkable electrolyte formulation comprising at least: ‐ a lithium salt or a mixture of lithium salts ‐ a hydrocarbon-based molecule comprising two thiol functions ‐ an unsaturated hydrocarbon-based molecule comprising two C=C double bonds ‐ a crosslinker, said crosslinker being a molecule bearing at least three C=C double bonds; wherein the [C=C double bond]/[thiols] molar ratio is between 1 and 1.1. The invention also relates to a method for preparing a crosslinked solid electrolyte using said formulation, and also to the use of said crosslinked solid electrolyte as solid electrolyte of an all-solid-state Li-ion battery or as component of the positive electrode (posolyte or catholyte) or negative electrode (negolyte or anolyte) of an electrochemical system.
The invention relates to a composition comprising mainly BHET and having a nitrogen content of less than or equal to 10 ppm by weight, the nitrogen content being determined according to a chemiluminescence method, with an ozone flow at 35 cm3/min, after oxidative combustion of a sample in liquid form, prepared by dilution of the composition in tetrahydrofuran, at a temperature of 1050-1100°C and in the presence of an oxidising mixture composed of oxygen and helium, and using a calibration curve formed using a diphenylamine standard diluted in toluene.
C08J 11/24 - Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with organic material by treatment with organic oxygen-containing compounds containing hydroxyl groups
83.
LOOP COMBUSTION PLANT AND METHOD COMPRISING A CYCLONE AIR REACTOR
The invention relates to a method for capturing mercaptans in a sulphur-containing hydrocarbon feedstock in the presence of a capture mass comprising an active phase based on at least one metal from group VIII, IB or IIB, and a mesoporous support having a bimodal mesopore distribution, said capture mass having a specific surface area of between 120 m 2/g and 350 m 2/g, and: - the volume of mesopores with a diameter greater than or equal to 2 nm and less than 20 nm represents between 35% and 70% by volume of the total pore volume of the capture mass; and - the volume of mesopores with a diameter greater than or equal to 20 nm and less than 50 nm represents between 25% and 60% by volume of the total pore volume of the capture mass.
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 25/05 - Removal of non-hydrocarbon compounds, e.g. sulfur compounds
B01J 20/02 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
B01J 20/08 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group comprising bauxite
B01J 20/10 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
B01J 20/28 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
The present invention relates to a method for determining the position of a source emitting at least one gaseous compound and/or particles in a geographical area, comprising at least one step of measuring the concentration of the gaseous compound, the direction and the speed of the wind for different consecutive geographical positions predefined so as to deviate by at most 45° with respect to an instantaneous or average wind direction. Then at least one pair of consecutive minimum and maximum values of the curve is determined and the position of the emitting source is determined from the positions of the mobile measuring system corresponding to the maximum values of the pairs, the time differences between the maximum and minimum values of the pairs and the average wind speeds and directions between the minimum and maximum values of the pairs.
G01M 3/20 - Investigating fluid tightness of structures by using fluid or vacuum by detecting the presence of fluid at the leakage point using special tracer materials, e.g. dye, fluorescent material, radioactive material
G01M 3/22 - Investigating fluid tightness of structures by using fluid or vacuum by detecting the presence of fluid at the leakage point using special tracer materials, e.g. dye, fluorescent material, radioactive material for valves
G01N 21/3504 - Investigating relative effect of material at wavelengths characteristic of specific elements or molecules, e.g. atomic absorption spectrometry using infrared light for analysing gases, e.g. multi-gas analysis
G01M 3/16 - Investigating fluid tightness of structures by using fluid or vacuum by detecting the presence of fluid at the leakage point using electric detection means
86.
PROCESS FOR PRODUCING A POLYESTER HAVING A REDUCED CRYSTALLISATION TEMPERATURE
The present invention relates to a process for producing a polyester, comprising: a) a step of esterification of a mixture comprising a monomer A of formula (1) and a monomer B of formula (2), or a monomer A of formula (1), a monomer B of formula (2) and isophthalic acid; wherein in formula (1) and formula (2) R122-CHR2)-, where R2 is selected from linear or branched alkyl groups comprising between 1 and 6 carbon atoms (C1 -C6) and a phenyl group, then b) a step of polycondensation.
C08L 67/02 - Polyesters derived from dicarboxylic acids and dihydroxy compounds
C08G 63/12 - Polyesters derived from hydroxy carboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from polycarboxylic acids and polyhydroxy compounds
The present invention relates to a process and a device for converting aromatic compounds, wherein aromatic compounds from a hydrocarbon-based feedstock (1) comprising aromatic compounds having 9 carbon atoms are isomerised in an isomerisation unit (A) in the presence of a bifunctional isomerisation catalyst having a hydrogenating/dehydrogenating function and a hydroisomerising function, in order to produce an isomerisation effluent (10) enriched in trimethylbenzenes. The present invention also relates to a process and a device for producing aromatic compounds comprising the process and the device for converting aromatic compounds.
1 (F/A)1 (F/A) of the initial furan compound content to the aminoxyl radical content is greater than or equal to 20; - said method is carried out in an electrolysis device that is compartmentalised into an anode compartment (3), in which the oxidation of the furan compound takes place and in which said furan compound, said solvent and said aminoxyl radical are contained, and a cathode compartment (8), said compartments being separated by an ion exchange membrane (2).
The present invention relates to a method for treating a plastic pyrolysis oil, comprising: a) hydrogenating said feedstock in a mixture with at least part of the liquid effluent resulting from step c) and in the presence of hydrogen and a catalyst at a temperature between 140 and 340°C; b) hydrotreating said hydrogenated effluent in the presence of hydrogen and a catalyst; c) separating the hydrotreated effluent, said separation being carried out at high temperature and under high pressure in order to obtain a gaseous effluent and a liquid effluent, part of which is recycled upstream of step a); d) separating, carried out at low temperature and under high pressure and supplied with the gaseous effluent and the other part of the liquid effluent resulting from step c) and an aqueous solution, in order to obtain a hydrocarbon-based effluent.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
C10G 31/09 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by filtration
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 45/38 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum or tungsten metals, or compounds thereof
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 5/04 - Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
H02M 7/5388 - Conversion of dc power input into ac power output without possibility of reversal by static converters using discharge tubes with control electrode or semiconductor devices with control electrode using devices of a triode or transistor type requiring continuous application of a control signal using semiconductor devices only, e.g. single switched pulse inverters in a bridge configuration with asymmetrical configuration of switches
91.
HYDROCRACKING CATALYST COMPRISING A SPECIFIC Y ZEOLITE FOR NAPHTHA PRODUCTION
The invention describes a hydrocracking catalyst that is selective with regard to the naphtha cut, and further describes the hydrocracking process using said catalyst. The catalyst comprises at least one hydrogenating-dehydrogenating element selected from the group consisting of group VIB and non-noble group VIII elements of the periodic table, whether taken alone or as a mixture, and a carrier comprising at least one porous mineral matrix, a gamma zeolite having an initial crystal lattice constant a0 greater than 24.42 Å, and a beta zeolite, wherein the weight ratio of said gamma zeolite to said beta zeolite in the catalyst is strictly greater than 12.
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
92.
HYDROCRACKING CATALYST COMPRISING A ZEOLITE Y AND A ZEOLITE BETA IN A Y/BETA RATIO STRICTLY GREATER THAN 12 FOR NAPHTHA PRODUCTION
The invention describes a hydrocracking catalyst which is selective towards the naphtha cut, and the hydrocracking process utilizing said catalyst, said catalyst comprising at least one hydro-dehydrogenating element selected from the group consisting of group VIB and non-noble group VIII elements, individually or as a mixture, from the periodic table, and a support comprising at least one porous mineral matrix, a zeolite Y having an initial lattice parameter a0 of the unit cell of greater than 24.42 Å, and a zeolite beta, in which the weight ratio of said zeolite Y to said zeolite beta in the catalyst is strictly greater than 12.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 29/78 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
93.
HYDROCRACKING CATALYST FOR NAPHTHA PRODUCTION, COMPRISING A Y ZEOLITE HAVING A LATTICE CONSTANT STRICTLY GREATER THAN 24.50 ANGSTROMS AND A BETA ZEOLITE, WHEREIN THE Y/BETA RATIO IS BETWEEN 5 AND 12
00 strictly greater than 24.42 Å, and a beta zeolite, wherein the weight ratio of said gamma zeolite to said beta zeolite in the catalyst is between 5 and 12.
B01J 29/16 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J 29/78 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
94.
RENEWABLE JET PRODUCTION FROM CATALYTIC PYROLYSIS FEEDSTOCK
The present invention provides a process comprising preparing renewable jet fuel blendstock by: a. feeding biomass, catalyst, and optionally transport fluid to a catalytic pyrolysis process fluidized bed reactor maintained at reaction conditions to manufacture a raw fluid product stream containing renewable aromatics, b. feeding the raw fluid product stream of a) to a solids separation and stripping system to produce separated solids and a fluid product stream, c. feeding the fluid product stream of b) to a fractionation system in order to recover a fraction boiling at 180 °C to 300°C, d. hydrogenating at least a portion of the fraction generated in c) with hydrogen at hydrogenation conditions to produce a hydrogenated fraction containing naphthenes, suitable as jet fuel blendstock, e. optionally recovering the jet fuel blendstock comprising naphthenes from the hydrogenated fraction of d) in a product recovery system.
C10G 1/08 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation with moving catalysts
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 45/58 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
95.
MATERIAL COMPRISING A SILICA SHAPED BY EXTRUSION WITH A PHOSPHOPOTASSIUM OR CESIUM PHOSPHATE BINDER AND HAVING IMPROVED MECHANICAL PROPERTIES, AND PROCESS FOR THE PREPARATION THEREOF
The invention relates to a novel material based on potassium phosphate salt or cesium phosphate salt and silica comprising at least one source of silica shaped with at least one powder of potassium phosphate salt or cesium phosphate salt. The invention also relates to a process for preparing said material, comprising at least one step of mixing at least one powder of at least one silica source with at least one powder of at least one powder of potassium phosphate salt or cesium phosphate salt and at least one solvent, a step of shaping, preferably by extrusion, the mixture obtained at the end of the mixing step, and a step of preparing calcined extrudates, and optionally a final hydrothermal treatment step.
B01J 27/18 - Phosphorus; Compounds thereof containing oxygen with metals
B01J 35/10 - Solids characterised by their surface properties or porosity
B01J 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
96.
PROCESS FOR THE PREPARATION OF A SILICA SHAPED BY EXTRUSION WITH A PHOSPHOPOTASSIUM OR CESIUM PHOSPHATE BINDER AND HAVING IMPROVED MECHANICAL PROPERTIES, COMPRISING A PRE-MIXING STEP
The invention relates to a process for preparing a material based on a potassium phosphate salt or a cesium phosphate salt and silica, comprising at least one step of pre-mixing at least one colloidal silica sol with at least one powder of at least one potassium phosphate salt and/or cesium phosphate salt to obtain a suspension, followed by a step of adding a powder of at least one precipitated silica and at least one solvent to said suspension, and a step of shaping, preferably extruding, the paste obtained at the end of the mixing step. The obtained materials can advantageously be used as a support or as catalysts in catalytic processes.
B01J 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
B01J 27/182 - Phosphorus; Compounds thereof with silicon
C04B 35/14 - Shaped ceramic products characterised by their composition; Ceramic compositions; Processing powders of inorganic compounds preparatory to the manufacturing of ceramic products based on oxides based on silica
C04B 35/626 - Preparing or treating the powders individually or as batches
97.
RENEWABLE DIESEL PRODUCTION FROM CATALYTIC PYROLYSIS FEEDSTOCK
The present invention provides a catalytic pyrolysis process for the production of renewable diesel fuel. The present invention provides a process for preparing renewable diesel fuel, comprising preparing renewable diesel fuel by a) fractionating a mixture comprising renewable aromatics to produce a first fraction boiling at 180 °C to 350°C at atmospheric conditions, and a fraction boiling below the boiling point of the first fraction, blending at least a portion of the first fraction with at least one distillate cut having lower aromatic content than the first fraction, and b) hydrogenating a blend of the first fraction and distillate cut having lower aromatic content to produce a hydrogenated fraction comprising a renewable diesel fuel.
C10G 1/08 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation with moving catalysts
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 45/58 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
98.
METHOD FOR EXTRACTING A RESOURCE FROM AN UNDERGROUND FORMATION, BY MEANS OF A MULTI-CRITERIA DECISIONAL ANALYSIS
The present invention relates to a method for extracting a resource from an underground formation. Based on measurements, a meshed representation having values of properties of the formation in each mesh cell is constructed. To each mesh cell, a score representing the relevance of each property value to the extraction of the resource is attributed. Sets of mesh cells are defined depending on a spatially variable geological constraint and, for each set of mesh cells, weighting coefficients of the properties are determined by applying an analytic hierarchy process. For each mesh cell, a score representative of the extraction potential of the resource is determined by summing the scores attributed to each property weighted by the weighting coefficients of the properties in the mesh cell. Based on the scores representative of extraction potential, a scheme of extraction of the resource is determined and the resource is extracted according to the extraction scheme.
The invention relates to a method for processing a pyrolysis oil from plastics and/or solid recovered fuels, comprising: a) optional selective hydrogenation of the feedstock; b) hydroconversion in an ebullated bed, entrained bed and/or moving bed, in order to obtain a hydroconverted effluent; c) separation of the effluent from step b) in the presence of an aqueous stream to obtain a gaseous effluent, an aqueous effluent and a hydrocarbon liquid effluent; d) optional fractionation to obtain at least one gaseous stream and a fraction having a boiling point of less than or equal to 150°C and a fraction having a boiling point of greater than 150°C.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 65/10 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
C10G 45/36 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
C10G 31/08 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
C10G 25/00 - Refining of hydrocarbon oils, in the absence of hydrogen, with solid sorbents
C10G 49/10 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or with moving solid particles
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 69/06 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
The present invention relates to a process for producing alcohol(s), according to which a culture medium containing a sugary carbon-based substrate (2) is introduced into a reaction section (1) comprising a support (4) on which microorganisms are immobilised, in order to produce, by fermentation under the action of said microorganisms, a must (3) enriched in alcohol(s) and one or more fermentation gases, such that the process is carried out continuously in the liquid phase and such that, in order to control the production, the amount of living microorganisms immobilised on the support is monitored without intervention on said supports.
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