Abstract

A biofuel includes a mixture of a gasoil generated from hydropyrolysis and hydroconversion of a solid biomass containing lignocellulose. The gasoil has a cetane index less than 46. The biofuel also includes a hydroprocessed ester fatty acid (HEFA) generated from hydrotreating a renewable resource having fats and oils. A cetane index of the biofuel is greater than 46.

IPC Classes  ?

• C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10B 57/12 - Applying additives during coking
• C10G 1/06 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

A biofuel includes a mixture having a gasoil generated from hydropyrolysis and hydroconversion of a solid biomass containing lignocellulose and an isomerized hydroprocessed ester and fatty acid (HEFA) generated from hydrotreating a renewable resource having fats and oils. The gasoil has a cetane index less than 46 and at least 10 parts per million weight (ppmw) of a heteroatom and a cetane index of the biofuel is greater than 46.

IPC Classes  ?

• C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10B 57/12 - Applying additives during coking
• C10G 1/06 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Abstract

This invention provides an aviation fuel composition comprising: a cycloparaffinic kerosene generated from hydropyrolysis and hydroconversion of a solid biomass containing lignocellulose, wherein the cycloparaffinic kerosene comprises at least 90 vol% cycloparaffins and less than 1 vol% aromatics; a paraffinic-based kerosene comprising normal and iso-paraffins in an amount of greater than 95%; and optionally, a petroleum-derived kerosene.The aviation fuel composition of the present invention provides an environmentally-friendly fuel while providing improved lubricity and low temperature viscosity properties.

IPC Classes  ?

• C10B 57/12 - Applying additives during coking
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• 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 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
• C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons

Abstract

This invention provides direct air capture (DAC) systems and processes for operating such systems that can operate continuously to remove carbon dioxide from an atmosphere under power from a wide range of intermittent renewable energy sources, and which is supplemented with recycled or excess energy derived from a parallel industrial process.

IPC Classes  ?

• B01D 53/02 - 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 by adsorption, e.g. preparative gas chromatography
• B01D 53/04 - 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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
• B01D 53/14 - 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 by absorption

Abstract

This invention provides systems and processes for operating systems that can operate continuously to remove carbon dioxide from an atmosphere under power from a wide range of intermittent renewable energy sources.

IPC Classes  ?

• B01D 53/02 - 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 by adsorption, e.g. preparative gas chromatography
• B01D 53/04 - 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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
• B01D 53/14 - 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 by absorption

Abstract

The present disclosure relates to a method of sequestering carbon dioxide which comprises the steps of capturing carbon dioxide from an industrial gaseous waste stream and/or the atmosphere, converting a CO2 from the CO2 gas stream into a (COOH)2 and combining the (COOH)2, a mono-alcohol (X-OH), preferably CH3CH2OH, and a first acid catalyst comprising a H2SO4 at a temperature ranging from about 80 °C to about 100 °C and under atmospheric pressure to produce an ester comprising a (COOX)2 and preferably (COOEt)2;and the ester obtained is reacted with a polyol, preferably glycerine to form a polyester, preferably the polyester is a hydrogel.The present disclosure further relates to the use of a hydrogel which is obtainable by said method.

IPC Classes  ?

• C08G 63/06 - Polyesters derived from hydroxy carboxylic acids or from polycarboxylic acids and polyhydroxy compounds derived from hydroxy carboxylic acids
• A01G 18/00 - Cultivation of mushrooms
• A01G 24/35 - Growth substrates; Culture media; Apparatus or methods therefor based on or containing synthetic organic compounds containing water-absorbing polymers
• B01D 53/62 - Carbon oxides
• C07C 51/00 - Preparation of carboxylic acids or their salts, halides, or anhydrides
• C07C 51/15 - Preparation of carboxylic acids or their salts, halides, or anhydrides by reaction of organic compounds with carbon dioxide, e.g. Kolbe-Schmitt synthesis
• C07C 55/06 - Oxalic acid
• C07C 67/03 - Preparation of carboxylic acid esters by reacting an ester group with a hydroxy group
• C07C 67/08 - Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
• C08G 63/78 - Preparation processes
• C09K 17/00 - Soil-conditioning materials or soil-stabilising materials

Abstract

A process for improving yield of kerosene from a renewable feedstock involves directing a hydroprocessed liquid stream to a lead stripper to separate a lead stripper bottoms stream and a lead stripper overhead stream comprising naphtha, lower and higher boiling point range hydrocarbons and water. Bulk water is removed from the lead stripper overhead stream resulting in an unstabilized hydrocarbon stream, which is passed to a stabilization column to separate a stabilized naphtha-containing stream from the lower boiling point range hydrocarbons. The stabilized naphtha-containing stream is passed to a rectification column to separate a rectification bottoms stream and a naphtha product stream. Kerosene and diesel boiling range product streams are separated from the lead stripper bottoms stream in a vacuum fractionator.

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 7/00 - Distillation of hydrocarbon oils
• C10G 7/02 - Stabilising gasoline by removing gases by fractioning
• C10G 49/22 - Separation of effluents

Abstract

The present invention relates to a method for producing syngas using a catalytic reverse water gas shift (RWGS) reaction, the method at least comprising the steps of: a) providing a feed stream (10) comprising at least hydrogen (Hz) and carbon dioxide (CO2); b) heating the feed stream (10) provided in step a) in a first heat exchanger (3) thereby obtaining a first heated feed stream (20); c) introducing the first heated feed stream (20) into a first RWGS reactor (2) and subjecting it to a first catalytic RWGS reaction, thereby obtaining a first syngas containing stream (30); d) cooling the first syngas containing stream (30) obtained in step c) in the first heat exchanger (3) against the feed stream (10) provided in step a), thereby obtaining a first cooled syngas stream (40); e) separating the first cooled syngas stream (40) obtained in step d) in a first gas/liquid separator (6) thereby obtaining a first water-enriched stream (60) and a first water-depleted syngas stream (50); f) heating the first water-depleted syngas stream (50) obtained in step e) in a second heat exchanger (13) thereby obtaining a heated first water-depleted syngas stream (70); g) introducing the heated first water-depleted syngas stream (70) obtained in step f) into a second RWGS reactor (12) and subjecting it to a second catalytic RWGS reaction, thereby obtaining a second syngas containing stream (80); h) cooling the second syngas containing stream (80) obtained in step g) in the second heat exchanger (13) against the first water-depleted syngas (50) stream obtained in step e), thereby obtaining a second cooled syngas stream (90); i) separating the second cooled syngas stream (90) obtained in step h) in a second gas/liquid separator (16) thereby obtaining a second water-enriched stream (110) and a second water-depleted syngas stream (100); j ) separating the second water-depleted syngas stream (100) obtained in step i) in a CO2 removal unit (8) thereby obtaining a CO2-enriched stream (120) and a CO2- depleted syngas stream (130); k) combining the CO2-enriched stream (120) obtained in step j) with the feed stream (10) provided in step a) and/or the first water-depleted syngas stream (50) obtained in step e); wherein the temperature of the first syngas containing stream (30) obtained in step c) and the second syngas containing stream (80) obtained in step g) is kept below 600°C, preferably below 550°C; and wherein the first and the second RWGS reactors (2,3) each comprise a multi-tubular reactor heated by molten salt circulating around the tubes of the multi-tubular reactor.

IPC Classes  ?

• C01B 3/16 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts

Abstract

A process for producing kerosene involves reacting a renewable feedstock in a hydroprocessing section under hydroprocessing conditions sufficient to cause a hydroprocessing reaction to produce a hydroprocessed effluent. The hydroprocessed effluent is separated to produce a hydroprocessed liquid stream and a separation system offgas stream. The hydroprocessed liquid stream is directed to a work-up section where gases are stripped to produce a stripped liquid product stream and a stripper offgas stream. A gas stream comprising the separation system offgas stream and/or the stripper offgas stream are directed to a gas-handling section to obtain a pressurized gas stream and a hydrocarbon fraction that is liquid at a pressure in a range from 0 - 1.5 MPaG and a temperature in a range from 0 to 50C. The hydrocarbon fraction is recycled to the work-up section. A kerosene stream separated in the product recovery unit has a higher yield compared to conventional processes.

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 7/00 - Distillation of hydrocarbon oils
• C10G 49/22 - Separation of effluents

Abstract

A process for improving yield of kerosene from a renewable feedstock involves directing a to a lead stripper to separate a lead stripper bottoms stream comprising naphtha and higher boiling point range hydrocarbons and a lead stripper overhead stream. The lead stripper bottoms stream is passed to a naphtha recovery column to separate a vapor stream comprising naphtha and water in an overhead stream from a heavy hydrocarbon product stream. The vapor stream is condensed and water is removed to produce a product naphtha stream. Kerosene and diesel boiling point range product streams are separated from the heavy hydrocarbon product stream in a vacuum fractionator.

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 7/00 - Distillation of hydrocarbon oils
• C10G 49/22 - Separation of effluents

Abstract

This invention provides a thermal energy storage device (100) comprising a powder bed (110), at least two electrodes (301, 302, 303), and at least one heat transfer tube (200). The powder bed (110) has an electrical resistivity in a range of 500-50,000 Qm. The at least two electrodes (301, 302, 303) are embedded in the powder bed (110) and arranged to heat the powder bed (110) by providing a voltage between the electrodes (301, 302, 303). The at least one heat transfer tube (200) is arranged to contain a heat transfer fluid and has an inlet (210) and an outlet (220) connectable to a thermal energy consumer (30). The heat transfer tube (200) and the powder bed (110) are thermally coupled via an electrically insulating material.

IPC Classes  ?

• F28D 20/00 - Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups or

Abstract

The present invention relates to a method of subjecting a biomass feedstock to hydropyrolysis, the method at least comprising the steps of : a ) supplying a biomass feedstock and a fluidizing gas comprising hydrogen to a bulk reactor zone of a fluidized bed reactor containing a deoxygenating catalyst; b) subjecting the biomass feedstock in the bulk reactor zone of the fluidized bed reactor to a hydropyrolysis reaction by contacting the biomass feedstock with the deoxygenating catalyst in the presence of the fluidizing gas, thereby obtaining a hydropyrolysis reactor output comprising at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char; wherein the bulk reactor zone is cooled by means of a cooling fluid flowing through a plurality of tubes running through the bulk reactor zone, the plurality of tubes having inlets into and outlets from the bulk reactor zone; and wherein the cooling fluid flowing in the tubes at the point ( 'A' ) where the biomass feedstock enters the bulk reactor zone has a temperature of at least 320° C, preferably at least 340° C, more preferably at least 350° C, even more preferably at least 370°C, yet even more preferably at least 380°C.

IPC Classes  ?

• 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
• B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
• 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

Abstract

This invention provides a heat integration process across two or more industrial processes, said heat integration process comprising : in a first process in a fluidised catalyst reactor in which a hydrocarbon feed is contacted with a regenerated catalyst in the upstream section of a reactor riser, passing the hydrocarbon feed and the catalyst admixed therewith through the reactor, thereby converting the hydrocarbon feed and deactivating the catalyst by deposition of carbonaceous deposits thereon, separating the deactivated catalyst from the converted hydrocarbon feed, passing the deactivated catalyst to a regenerator vessel wherein deposits are removed from the deactivated catalyst under exothermic process conditions by means of a regenerating medium introduced into the regenerator vessel, thereby regenerating and heating the catalyst, and passing the regenerated hot catalyst to the upstream section of the reactor, wherein a chemical feedstock for a second process is passed through a heat exchange system in direct contact with the regenerator vessel in order to provide heat to said chemical feedstock and second process.

IPC Classes  ?

• C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
• C07C 5/333 - Catalytic processes
• C07C 11/06 - Propene
• C07C 11/09 - Isobutene

Abstract

A system for the treatment of a liquid plastic-derived oil having a pretreating section that includes a pretreating system having one or more reactors that may receive the liquid plastic-derived oil having one or more contaminants and a first contamination level. The one or more reactors includes a sorbent material having a faujasite (FAU) crystal framework type zeolitic molecular sieve and that may remove a first portion of the one or more contaminants from the liquid plastic-derived oil and generate a treated liquid plastic-derived oil having a second contamination level that is less than the first contamination level. The liquid plastic-derived oil is derived from a solid plastic waste (SPW), and the first portion of the one or more contaminants includes a halogen.

IPC Classes  ?

• 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 25/05 - Removal of non-hydrocarbon compounds, e.g. sulfur compounds
• 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 67/06 - 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 including a sorption process as the refining step in the absence of hydrogen
• 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 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 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

Abstract

The present invention relates to a method for producing syngas using a catalytic reverse water gas shift (RWGS) reaction, the method at least comprising the steps of: a) providing a feed stream (10) comprising at least hydrogen (H2) and carbon dioxide (CO2); b) heating the feed stream (10) provided in step a) in a first heat exchanger (3) thereby obtaining a first heated feed stream (20); c) introducing the first heated feed stream (20) into a RWGS reactor (2) and subjecting it to a catalytic RWGS reaction, thereby obtaining a syngas containing stream (30); d) cooling the syngas containing stream (30) obtained in step c) in the first heat exchanger (3) against the feed stream (10) provided in step a), thereby obtaining a first cooled syngas stream (40); e) cooling the first cooled syngas stream (40) obtained in step d) in a second heat exchanger (5) thereby obtaining a second cooled syngas stream (50); f) separating the second cooled syngas stream (50) obtained in step e) in a gas/liquid separator (6) thereby obtaining a water-enriched stream (110) and a water-depleted syngas stream (100); g) separating the water-depleted syngas stream (100) obtained in step f) in a CO2 removal unit (8) thereby obtaining a CO2-enriched stream (120) and a CO2-depleted syngas stream (130); and - 31 h) combining the CO2-enriched stream (120) obtained in step g) with the feed stream (10) provided in step a).

IPC Classes  ?

• C01B 3/12 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
• C01B 3/16 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
• C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification

Abstract

Methods and systems for steam production are provided. Methods include providing feedwater having an electrical conductivity of less than 200 µS/cm to an electrode boiler, andconverting the feedwater to saturated steam by the electrode boiler. The saturated steam is provided as a first fluid to a heat exchange component. Water having an electrical conductivity of more than 200 µS/cm is provided to the heat exchange component as a second fluid, where the second fluid is heated through indirect thermal transfer with the saturated steam to generate wet steam. The saturated steam is at least partially condensed in the heat exchange componentthrough the indirect thermal transfer with the second fluid. At least a portion of the thus obtained condensed fluid is fed back to the electrode boiler for use as part of the low-conductivity water to generate said saturated steam.

IPC Classes  ?

• F22B 1/30 - Electrode boilers
• E21B 43/24 - Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection

Abstract

The present invention relates to a method for removing carbon dioxide (CO2) from a CO2-containing stream, the method at least comprising the steps of: a) providing a CO2-containing stream (10), preferably air wherein the CO2-containing stream (10) has a CO2 content in the range of from 10 to 1000 ppmv, preferably from 100 to 1000 ppmv; b) removing CO2 from the CO2-containing stream (10) provided in step a) in a first CO2removal unit (2), thereby obtaining a first CO2-enriched stream (30) and a first CO2-depleted stream (20); c) liquefying the first CO2-enriched stream (30) obtained in step b) in a liquefaction unit (3); d) removing from the liquefaction unit (3) at least a liquefied CO2 stream (40) and a gaseous stream (15) containing at least nitrogen [N2(g) ], oxygen [O2 (g) ] and CO2 (g).

IPC Classes  ?

• 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
• B01D 53/62 - Carbon oxides

Abstract

The present invention relates to a hydraulic fracturing fluid composition comprising a homogeneous non-aqueous organic phase mixture which mixture comprises a base fluid and one or more surfactants.

IPC Classes  ?

• C09K 8/68 - Compositions based on water or polar solvents containing organic compounds
• E21B 43/26 - Methods for stimulating production by forming crevices or fractures

Abstract

A reactor that may contact a gas stream with a catalyst composition includes a catalyst bed module having a first grouping including a first plurality of foam catalyst blocks each bounded by a first front face having a first surface area with an opposing first back face, a first top side with an opposing first bottom side, and a first side face with an opposing first alternate side face and a second grouping adjacent to the first grouping and having a second plurality of foam catalyst blocks each bounded by a second front face having a second surface area with an opposing second back face, a second top side with an opposing second bottom side, and a second side face with an opposing second alternate side face. The first back face of the first plurality of foam catalyst blocks and the second back face of the second plurality of foam catalyst face each face the other in a spaced relationship. The reactor also includes a sealing frame disposed between the first and second groupings and that may maintain the spaced relationship and form a sealed volume between the first plurality of foam catalyst blocks and the second plurality of foam catalyst blocks and a support frame having a support surface and an opening and that may support the first grouping and the second grouping. The first grouping and the second grouping are secured to the support surface such that the opening is positioned between the first grouping and the second grouping and adjacent to the sealed volume, and the sealed volume and the opening provide a passage for gas flow.

IPC Classes  ?

• B01D 53/86 - Catalytic processes

Abstract

A process for hydroprocessing a renewable feedstock in a fixed-bed reactor system having at least one catalytic bed involves directing a downward flow of the renewable feedstock to a filtering zone having top-open interstitial portions to receive the downward flow and top-covered annular portions that are in fluid communication with a headspace between the filtering zone and a catalytic zone. The feedstock flows from the interstitial portions to the annular portions through a filtering material disposed between the interstitial portions and the annular portions, resulting in a filtered feedstock, which then flows to the catalytic zone. In the catalytic zone, filtered feedstock is reacted under hydroprocessing conditions sufficient to cause a reaction selected from the group consisting of hydrogenation, hydrodeoxygenation, hydrodenitrogenation, hydrodesulphurization, hydrodemetalation, hydrocracking, hydroisomerization, and combinations thereof.

IPC Classes  ?

• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01D 24/10 - Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof with the filter bed stationary during the filtration the filtering material being held in a closed container
• B01D 24/20 - Filters comprising loose filtering material, i.e. filtering material without any binder between the individual particles or fibres thereof with the filter bed stationary during the filtration the filtering material being provided in an open container
• B01D 29/15 - Supported filter elements arranged for inward flow filtration
• B01D 29/54 - Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups ;   Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition in parallel connection arranged concentrically or coaxially
• B01D 39/20 - Other self-supporting filtering material of inorganic material, e.g. asbestos paper or metallic filtering material of non-woven wires
• B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
• 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 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
• C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions

Abstract

Bottom hole pressure (BHP) actuals and bottom hole temperature (BHT) actuals in a hydrocarbon production well are recorded as a function of time, during production of hydrocarbon fluids. Selective statistical measures of both the BHP actuals and the BHT actuals are determined as a function of time. These selective statistical measures suitably represent estimates of expected normal BHP actuals and BHT actuals in case there is no imminent sand failure, supplemented with an uncertainty measure of the estimates of expected normal BHP and BHT. The BHP actuals and the BHT actuals are compared with respective BHP and BHT anomaly thresholds based on the selective statistical measures. An anomaly alert is automatically issued upon meeting a condition wherein both the BHP actuals and the BHT actuals exceed their respective anomaly threshold. The anomaly alert is an indication of a predicted imminent sand failure of the hydrocarbon production well in operation.

IPC Classes  ?

• E21B 43/00 - Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
• E21B 47/06 - Measuring temperature or pressure

Abstract

Novel modular reactor configurations utilizing resistance heating elements are provided. The resistance heating elements pass through the reaction zone of reactor modules and conduct electricity thereby providing resistance heating in the reaction zone to facilitate the conversion of the reactants to products when reactants are present in the reaction zone. The resistance heating elements may be configured as plurality of wires, a plurality of plates, wiremesh, gauze, and/or a metallic monolith.

IPC Classes  ?

• B01J 19/00 - Chemical, physical or physico-chemical processes in general; Their relevant apparatus

Abstract

The present invention provides an electrically heated apparatus (1), at least comprising: - an electrically heated furnace (2) having a roof (2A) and walls defining a space (3); - at least one tube (10) running through the space (3), wherein the at least one tube (10) has an inlet (11) and an outlet (12) outside of the space (3); - electrical radiative heating elements (20) located in the space (3), which heating elements (20) can heat the at least one tube (10); wherein the heating elements (20) suspend from the roof (2A) of the space (3); and wherein the roof (2A) of the space (3) has a shape configured to have heating elements (20) suspending at different heights.

IPC Classes  ?

• B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
• B01J 19/24 - Stationary reactors without moving elements inside

Abstract

A method for maximizing the selectivity (S) of an epoxidation catalyst in an ethylene oxide reactor system, comprising: receiving a measured reactor selectivity (Smeas), a measured reactor temperature (Tmeas), and one or more operational parameters from an ethylene oxide production system configured to convert, in the ethylene oxide reactor system, a feed gas comprising ethylene and oxygen into ethylene oxide in the presence of the epoxidation catalyst and a chloride-containing catalyst moderator. The epoxidation catalyst comprises silver and a promoting amount of rhenium (Re), and the measured reactor selectivity (Smeas), the measured reactor temperature (Tmeas), and the one or more operational parameters comprise real-time and historical operating data points over time generated by the ethylene oxide production system. The method also includes using a processor to (a) calculate, using a model, for each time point, a model-estimated selectivity (Sest) and a model-estimated temperature (Test) of the epoxidation catalyst at an optimum moderator level (Mopt). The model-estimated selectivity (Sest) and the model-estimated temperature (Test) are determined based on at least one operational parameter of the one or more operational parameters at said time points, the at least one operational parameter does not include a moderator level, and the model is based, at least in part, on empirical historical data associated with the epoxidation catalyst, the ethylene oxide production system, or both. The method also includes using the processor to (b) determine a difference (?S) between the measured reactor selectivity (Smeas) and the model-estimated selectivity (Sest) and a difference (?T) between the measured reactor temperature (Tmeas) and the model-estimated temperature(Test) for each of the time points, (c) fit a curve to the delta selectivity (?S) data points as a function of the corresponding delta temperature (?T) data points to obtain a fitted curve, (d) determine a real-time relative effective moderator level (RCleffreal-time) based on the fitted curve and real-time values of ?S (?Sreal-time) and ?T (?Treal-time) and (e) output an actionable recommendation based on the real-time RCleff. The method further includes using the processor to (f) display the actionable recommendation on a display.

IPC Classes  ?

• G16C 20/10 - Analysis or design of chemical reactions, syntheses or processes
• C07D 301/10 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase with catalysts containing silver or gold
• G16C 20/70 - Machine learning, data mining or chemometrics

Abstract

An unleaded aviation fuel composition having a MON of at least 99.6, sulfur content of less than 0.05 wt%,CHN content of at least 97.2 wt%, less than 2.8 wt% of oxygen content, a T10 of at most 75ºC, T40 of at least 75º C, a T50 of at most 105º C, a T90 of at most 135ºC, a final boiling point of less than 190°C, an adjusted heat of combustion of at least 43.5 MJ/kg, a vapor pressure in the range of 38 to 49 kPa, comprising from 20 vol.% to 35 vol.% of toluene having a MON of at least 107; from 2 vol.% to 10 vol.% of aniline; from above 30 vol% to 55 vol% of at least one alkylate oralkyate blend having an initial boiling range of from 32°C to 60°C and a final boiling range of from 105°C to140°C, having T40 of less than 99°C, T50 of less than 100°C, T90 of less than 110°C, the alkylate or alkylate blend comprising isoparaffins from 4 to 9 carbon atoms, 3-20 vol% of C5 isoparaffins, 3-15 vol% of C7 isoparaffins, and 60-90 vol% of C8 isoparaffins, based on the alkylate or alkylate blend, and less than 1 vol% of C10+, based on the alkylate or alkylate blend; at least 8 vol% of isopentane in an amount sufficient to reach a vapor pressure in the range of 38 to 49 kPa; from 0.1 vol% to 10 vol%, preferably from 1 vol% to 8 vol%, of a straight chain alkyl acetate having a straight chain alkyl group having 4 to 8 carbon atoms; and from 0.1 vol% to 10 vol%, preferably from 2 vol% to 8 vol%, of a branched chain alcohol having from 4 to 8 carbon atoms, provided that the branched chain does not contain any t-butyl groups; wherein the volume ratio of straight chain alkyl actetate to branched chain alcohol is in the range of 3:1 to 1:3; and wherein the fuel composition contains less than 15 vol% of C8 aromatics. As well as meeting the requirements of the ASTM D910 specification, the unleaded aviation fuel compositions ofthe present invention have improved octane properties.

IPC Classes  ?

• C10L 1/06 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
• C10L 1/10 - Liquid carbonaceous fuels containing additives
• C10L 1/14 - Organic compounds
• C10L 1/16 - Hydrocarbons
• C10L 1/18 - Organic compounds containing oxygen
• C10L 1/182 - Organic compounds containing oxygen containing hydroxy groups; Salts thereof
• C10L 1/223 - Organic compounds containing nitrogen containing at least one carbon-to-nitrogen single bond having at least one amino group bound to an aromatic carbon atom

Abstract

The present invention provides an electrically heated apparatus (1) at least comprising: - an electrically heated furnace (2) having walls (2A, 2B) defining a space (3); - a first row (4) of tubes (10) running through the space (3), wherein the tubes (10) have an inlet (11) and outlet (12) outside of the space (3); - a second row (14) of tubes (10) running through the space (3), wherein the tubes (10) have an inlet (11) and outlet (12) outside of the space (3); - a first set (5) of electrical radiative heating elements (20) located in the space (3), wherein the first set (5) comprises electrical radiative heating elements (20) located between the first (4) and second rows (14) of tubes (10).

IPC Classes  ?

• F27D 11/02 - Ohmic resistance heating
• F27D 99/00 - Subject matter not provided for in other groups of this subclass
• B01J 6/00 - Calcining; Fusing
• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
• F27B 5/14 - Arrangements of heating devices

Abstract

The present invention provides a catalytic cracking reactor comprising a conduit, configured to allow the passage of a flow of catalyst particles, and an injection zone comprising a ring of feed injectors extending inwardly from the wall of reactor and angled to inject feed into the flow of catalyst particles, characterised in that the reactor also comprises a contacting device protruding into the reactor from the inner wall of said reactor upstream of the injection zone. The present invention also provides a method of mixing a fluidised stream of catalyst particles with a hydrocarbon feed, said method comprising the steps of: a) creating a stream of fluidised catalyst particles in a reactor; b) passing said stream of fluidised catalyst particles past a contacting device protruding into the reactor from the inner wall of said reactor; c) subsequently passing the stream of fluidised catalyst particles through an injection zone comprising a ring of feed injectors extending inwardly from the wall of the reactor and contacting said stream of fluidised catalyst particles with hydrocarbon feed provided through said feed injectors; d) passing the stream of fluidised catalyst particles contacted with hydrocarbon feed to a downstream section of the reactor to convert the hydrocarbon feed to a converted product in the presence of the catalyst particles.

IPC Classes  ?

• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01F 23/50 - Mixing liquids with solids
• 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 8/20 - 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
• B01J 8/38 - 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 fluidised bed containing a rotatable device or being subject to rotation
• C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique

Abstract

The invention provides a gas distribution system comprising a plurality of flow passages in fluid communication with a gas source, each flow passage having disposed therein a number of nozzles, wherein at least a portion of said nozzles are fitted with a sintered metal filter.

IPC Classes  ?

• 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
• B05B 1/00 - Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means
• C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique

Abstract

A process for the epoxidation of ethylene comprising:contacting an inlet feed gas comprising ethylene, oxygen and one or more reaction modifiers consisting of organic chlorides with an epoxidation catalyst comprising a carrier, and having silver, a rhenium promoter, and oneor more alkali metal promoters deposited thereon;wherein the inlet feed gas has an overall catalystchloriding effectiveness value (Cleff) represented by the formula (I): wherein [MC], [EC], [EDC], and [VC] are the concentrations in ppmv of methyl chloride (MC), ethylchloride (EC), ethylene dichloride (EDC), and vinylchloride (VC), respectively, and [CH4], [C2H6] and [C2H4] are the concentrations in mole percent of methane, ethane, and ethylene, respectively, in the inlet feedgas; wherein at a cumulative ethylene oxide production cumEO1 of at least 0.2 kton ethylene oxide/m3 catalyst, said process is operating at a reaction temperature having a value T1 and with the inlet feed gas having an optimum overall catalyst chloriding effectiveness value of Cleff1 to produce ethylene oxide with an ethylene oxide production parameter at a value EO1; and characterised in that the carrier is a fluoride-mineralized alpha-alumina carrier and said process is subsequently operated such that at a cumulative ethylene oxide production cumEOx,wherein cumEOx is at least 0.6 kton ethylene oxide/m3 catalyst greater than cumEO1, the reaction temperature5has an increased value Tx to maintain said ethylene oxide production parameter at a value EO1 whilst the optimum overall catalyst chloriding effectiveness value of theinlet feed gas Cleffx is controlled such that the ratioof Cleffx/Cleff1 is in the range of from 0.8 to 1.2.

IPC Classes  ?

• C07D 301/10 - Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase with catalysts containing silver or gold

Abstract

A process for producing alpha-olefins comprising contacting an ethylene feed with an oligomerization catalyst system in an oligomerization reaction zone under oligomerization reaction conditions to produce a product stream comprising alpha-olefins wherein the catalyst system comprises an iron-ligand complex and a co-catalyst and the residence time in the reaction zone is in the range of from 2 to 40 minutes.

IPC Classes  ?

• C07C 2/32 - Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
• C07C 2/34 - Metal-hydrocarbon complexes
• C07C 11/02 - Alkenes
• C07C 11/08 - Alkenes with four carbon atoms
• C07C 11/107 - Alkenes with six carbon atoms

Abstract

A process for producing alpha-olefins comprising contacting an ethylene feed with an oligomerization catalyst system in an oligomerization reaction zone under oligomerization reaction conditions to produce a product stream comprising alpha-olefins wherein the catalyst system comprises a metal-ligand complex and a co-catalyst and the oligomerization reaction conditions comprise a reaction temperature of at least 115 °C.

IPC Classes  ?

• C07C 2/32 - Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
• C07C 2/34 - Metal-hydrocarbon complexes
• C07C 11/02 - Alkenes
• C07C 11/08 - Alkenes with four carbon atoms
• C07C 11/107 - Alkenes with six carbon atoms

Abstract

The invention relates to pre-treating an oil derived from a renewable feedstock to remove at least a portion of one or more contaminants by filtering the oil with a nanofiltration membrane. The resulting permeate oil has a reduced concentration of the contaminant relative to the feed stream to the nanofiltration membrane.

IPC Classes  ?

• B01D 61/02 - Reverse osmosis; Hyperfiltration
• B01D 17/00 - Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
• B01D 65/08 - Prevention of membrane fouling or of concentration polarisation
• C10G 31/11 - Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by dialysis

Abstract

The present invention relates to a method and an apparatus for producing syngas using catalytic reverse water gas shift (RWGS) reaction comprising heat exchangers and two RWGS reactors.

IPC Classes  ?

• C01B 3/16 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
• B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
• B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes
• C10K 3/02 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment

Abstract

Systems and method for production of furfural comprising combining a xylose-containing solution with an extraction solution comprising water-insoluble boronic acid to provide a first combined solution comprising an aqueous phase and a non-aqueous phase, said non-aqueous phase comprising xylose-diboronate ester (BA2X); combining at least a portion of the non-aqueous phase with an ionic conversion solution having a pH of less than or equal to 4 and comprising one or more salts to form a second combined solution, wherein the ionic conversion solution has a calculated molar ionic strength of at least 1, heating the second combined solution to convert at least a portion of the xylose-diboronate ester into furfural; separating the second combined solution into a second aqueous phase comprising from a second non-aqueous phase and recovering furfural from the second non-aqueous phase.

IPC Classes  ?

• C07D 307/50 - Preparation from natural products
• C08B 37/14 - Hemicellulose; Derivatives thereof

Abstract

A process for producing alpha-olefins comprising: a) contacting an ethylene feed with an oligomerization catalyst system in an oligomerization reaction zone under oligomerization reaction conditions to produce a product stream comprising alpha-olefins; and b) cooling at least a portion of the reaction zone using a heat exchange medium having an inlet temperature and an outlet temperature wherein the catalyst system comprises a metal-ligand complex and a co-catalyst; the oligomerization reaction conditions comprise a reaction temperature of greater than 70 °C; and the difference between the reaction zone temperature and the inlet temperature of the heat exchange medium is from 0.5 to 15 °C.

IPC Classes  ?

• C07C 2/32 - Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
• C07C 2/34 - Metal-hydrocarbon complexes
• C07C 11/02 - Alkenes
• C07C 11/08 - Alkenes with four carbon atoms
• C07C 11/107 - Alkenes with six carbon atoms

Abstract

The invention provides a process for producing alpha-olefins comprising: a) contacting an ethylene feed with an oligomerization catalyst system, the catalyst system comprising a metal-ligand catalyst and a co-catalyst, in an oligomerization reaction zone under oligomerization conditions to produce a product stream comprising alpha-olefins; b) withdrawing the product stream from the oligomerization reaction zone wherein the product stream further comprises oligomerization catalyst system; c) contacting the product stream with a catalyst deactivating agent to form a deactivated product stream that contains deactivated catalyst components; and d) heating the deactivated product stream to separate one or more components from the deactivated product stream.

IPC Classes  ?

• C07C 2/32 - Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
• B01J 31/00 - Catalysts comprising hydrides, coordination complexes or organic compounds
• C07C 2/34 - Metal-hydrocarbon complexes

Abstract

A process for producing alpha-olefins comprising contacting an ethylene feed with an oligomerization catalyst system in an oligomerization reaction zone under oligomerization reaction conditions to produce a product stream comprising alpha-olefins wherein the catalyst system comprises an iron-ligand complex and a co-catalyst and the molar ratio of oxygen to iron being fed to the oligomerization reaction zone is of from 1:1 to 200:1. Alternatively, the molar ratio of oxygen to aluminum in MMAO being fed to the oligomerization reaction zone is less than 1:5.

IPC Classes  ?

• C07C 2/32 - Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
• C07C 2/34 - Metal-hydrocarbon complexes
• C07C 11/02 - Alkenes

Abstract

A method for treating an offgas produced in the processing of a renewable feedstock, includes hydrotreating a renewable feedstock to produce an effluent having a hydrotreated liquid and a vapour phase. The effluent vapour phase contains hydrogen,carbon dioxide, hydrogen sulphide and carbon monoxide. The effluent is separated into a liquid stream and an offgas streams. The offgas stream, containing carbon dioxide and hydrogen sulphide is directed to a biological desulfurization unit where a majority of the hydrogen sulphide is converted to elemental sulphur and a CO2-rich gas stream is produced.

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• B01D 53/52 - Hydrogen sulfide
• B01D 53/84 - Biological processes
• C10K 1/00 - Purifying combustible gases containing carbon monoxide
• C10K 1/12 - Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting

Abstract

Systems and method for production of furfural comprising combining a xylose-containing solution with an extraction solution comprising water-insoluble boronic acid to provide a first combined solution comprising an aqueous phase and a non-aqueous phase, said non-aqueous phase comprising xylose-diboronate ester (BA2X); combining at least a portion of the non-aqueous phase with a conversion solution to form a second combined solution, heating the second combined solution to convert at least a portion of the xylose-diboronate ester into furfural to a temperature at or above which the second combined solution consists essentially of a homogeneous liquid phase, cooling down the heated second combined solution to a temperature wherein the cooled second combined solution comprises an aqueous phase comprising water and furfural and (ii) a non-aqueous phase comprising water-insoluble boronic acid and furfural.

IPC Classes  ?

• C08H 7/00 - Lignin; Modified lignin; High-molecular-weight products derived therefrom
• C07D 307/50 - Preparation from natural products

Abstract

A process includes a.) supplying a biomass feedstock, a fluidizing gas having hydrogen, and a catalyst recirculation stream having deoxygenating catalyst to a mixing zone of a fluidized bed reactor; b.) allowing the biomass feedstock, the fluidizing gas and the deoxygenating catalyst to move upwards through the fluidized bed reactor from the mixing zone to a bulk reactor zone; c.) allowing the biomass feedstock to contact the deoxygenating catalyst in the presence of the fluidizing gas in the bulk reactor zone of the fluidized bed reactor to produce a hydropyrolysis reactor output including at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char; and d.) withdrawing at least a portion of the deoxygenating catalyst from the bulk reactor zone to form the catalyst recirculation stream that is supplied to the mixing zone in step a).

IPC Classes  ?

• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• 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 1/08 - 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 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

Abstract

Use of a paraffinic gasoil in a fuel composition for reducing microbial growth, The present invention is relevant for a wide range of fuel compositions including diesel fuels, heating oils, aviation fuels, marine fuels, and the like.

IPC Classes  ?

• C10L 10/04 - Use of additives to fuels or fires for particular purposes for minimising corrosion or incrustation
• C10G 29/20 - Organic compounds not containing metal atoms
• C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons

Abstract

Use of a detergent additive in a fuel composition for reducing microbial growth, The present invention is relevant for a wide range of fuel compositions including diesel fuels, heating oils, aviation fuels, marine fuels, and the like.

IPC Classes  ?

• C10L 1/22 - Organic compounds containing nitrogen
• C10L 1/198 - Macromolecular compounds obtained otherwise than by reactions involving only carbon-to-carbon unsaturated bonds
• C10L 1/238 - Macromolecular compounds obtained otherwise than by reactions involving only carbon-to-carbon unsaturated bonds
• C10L 10/04 - Use of additives to fuels or fires for particular purposes for minimising corrosion or incrustation
• C10L 10/18 - Use of additives to fuels or fires for particular purposes use of detergents or dispersants for purposes not provided for in groups
• C10L 1/222 - Organic compounds containing nitrogen containing at least one carbon-to-nitrogen single bond
• C10L 1/2383 - Polyamines or polyimines, or derivatives thereof

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) contacting said liquid stream with a washing solvent thereby removing heteroatom containing organic compounds; b) liquid-liquid extraction of the washed stream with an extraction solvent; wherein during step a) and/or between multiple steps a) and/or between steps a) and b) and/or after step b), heteroatom containing organic compounds, optional aromatic hydrocarbons and optional other contaminants are removed from said liquid stream and/or from a washed stream resulting from step a) and/or from a raffinate stream resulting from step b), respectively, by contacting the latter stream(s) with a sorption agent. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 53/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
• C10G 53/08 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

The present disclosure relates to a method for replacing a catalyst of a reactor train of an operating hydroprocessing system comprising a plurality of reactor trains comprising a catalyst and each configured to receive a feed fluid and combine a portion of the feed fluid with a hydrogen stream over the catalyst to generate a hydrotreated fluid, the method comprising activating a valving system of the operating hydroprocessing system to disrupt operation of a select reactor train comprising a spent catalyst to form a disrupted reactor train while maintaining operation of at least one other reactor train; activating the gas processing system to form a decontaminated catalyst, removing the decontaminated catalyst from the disrupted reactor train to form a catalyst free reactor train; loading the catalyst free reactor train with a fresh catalyst to produce a charged reactor train; and restoring operation of the catalyst charged reactor train.

IPC Classes  ?

• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
• B01J 19/18 - Stationary reactors having moving elements inside
• B01J 19/24 - Stationary reactors without moving elements inside
• B01J 38/00 - Regeneration or reactivation of catalysts, in general
• B01J 38/04 - Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
• C10G 69/14 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural parallel stages only

Abstract

The present invention provides a process for hydro-demetallizing of residual hydro-carbonaceous feedstock, the process comprising:passing the feedstock to a vertically-disposed reaction zone comprising at least one moving bed reactor, wherein the at least one moving bed reactor comprises at least one catalyst bed of hydro-demetallization catalyst and is configured for catalyst addition and removal;subjecting the hydrodemetallization catalyst to in-line fresh catalyst deairing, pressurizing, and hydrocarbon soaking via a catalyst sluicing system before entering the moving bed reactor;further subjecting the hydrodemetallization catalyst to sulphidic activation before entering the moving bed reactor at a top portion of the moving bed reactor, wherein the hydrodemetallization catalyst is added to the moving bed reactor through gravity; removing any spent hydrodemetallization catalyst from a bottom portion of the moving bed reactor during processing of the feedstock; and subjecting the removed spent hydrodemetallization catalyst to in-line spent catalyst hydrocarbon removal, depressurizing, inerting, and airing; and wherein reactor internals located within the reaction zone provide balance and controlled catalyst movement during catalyst addition and removal from the moving bed reactor.

IPC Classes  ?

• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01J 8/12 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
• B01J 23/882 - Molybdenum and cobalt
• B01J 23/883 - Molybdenum and nickel
• B01J 27/19 - Molybdenum
• B01J 37/20 - Sulfiding
• C10G 45/04 - 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
• 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

Abstract

The present invention provides a process for hydro-demetallizing of residual hydro-carbonaceous feedstock, the process comprising:passing the feedstock to a vertically-disposed reaction zone comprising at least one moving bed reactor to produce an effluent, wherein the at least one moving bed reactor comprises at least one catalyst bed of hydro-demetallization catalyst and is configured for catalyst addition and removal;subjecting the hydrodemetallization catalyst to in-line fresh catalyst deairing, pressurizing, and hydrocarbon soaking via a catalyst sluicing system before entering the moving bed reactor;further subjecting the hydrodemetallization catalyst to sulphidic activation before entering the moving bed reactor at a top portion of the moving bed reactor, wherein the hydrodemetallization catalyst is added to the moving bed reactor through gravity; removing any spent hydrodemetallization catalyst from a bottom portion of the moving bed reactor during processing of the feedstock; and subjecting the removed spent hydrodemetallization catalyst to in-line spent catalyst hydrocarbon removal, depressurizing, inerting, and airing; passing the effluent to at least one fixed bed reactor for further processing; and wherein reactor internals located within the reaction zone provide balance and controlled catalyst movement during catalyst addition and removal from the moving bed reactor.

IPC Classes  ?

• B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
• B01J 8/12 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
• B01J 23/883 - Molybdenum and nickel
• B01J 37/20 - Sulfiding
• B01J 37/28 - Phosphorising
• C10G 45/04 - 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
• 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 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
• 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

Abstract

A facility for the production of liquefied natural gas comprising a liquefaction train. The train comprises a plurality of modules to perform the process steps associated with liquefied natural gas production. The train further comprises a primary cooling loop to cool at least a process stream from each module and a first and a second mixed refrigerants against a first coolant comprising clean water. The primary cooling loop is a closed clean water loop, and the cooling is against an ambient temperature. The train further comprises a first plurality of heat exchangers through which the primary cooling loop extends. The cooling is via heat exchange in at least the first plurality of heat exchangers with respect to the first coolant. More than 50% of the first plurality of heat exchangers are printed circuit heat exchangers, which are adapted to provide at least 80% of the cooling against the ambient temperature.

IPC Classes  ?

• F25J 1/00 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures

Abstract

An unleaded aviation fuel composition having a MON of at least 99.6, sulfur content of less than 0.05wt%, CHN content of at least 98wt%, less than 2 wt% of oxygen content, an adjusted heat of combustion of at least 43.5 MJ/kg, a vapor pressure in the range of 38 to 49 kPa, comprising a blend comprising: from 5 vol.% to 25 vol.% of toluene having a MON of at least 107; from 0.5 vol.% to 4 vol.% of aniline;from 30 vol% to 70 vol% of at least one alkylate or alkyate blend having an initial boiling range of from 32°C to 60°C and a final boiling range of from 105°C to 140°C, having T40 of less than 99°C, T50 of less than 100°C, T90 of less than 110°C, the alkylate or alkylate blend comprising isoparaffins from 4 to 9 carbon atoms, 3-20vol% of C5 isoparaffins, 3-15vol% of C7 isoparaffins, and 60-90 vol% of C8 isoparaffins, based on the alkylate or alkylate blend, and less than 1 vol% of C10+, based on the alkylate or alkylate blend; from 0.1 vol.% to 10 vol.% of branched alkyl acetate; at least 8 vol% of isopentane, isobutane, or mixture thereof in an amount sufficient to reach a vapor pressure in the range of 38 to 49 kPa; from 2 vol.% to 10 vol.% of mesitylene; wherein the fuel composition contains less than 1 vol% of C8 aromatics. As well as meeting the requirements of the ASTM D910 specification, the unleaded aviation fuel compositions of the present invention exhibit reduced bladder delamination, improved materials compatibility such as reduced elastomer swelling and reduced paint staining, and improved engine endurance.

IPC Classes  ?

• C10L 1/06 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
• C10L 1/14 - Organic compounds
• C10L 1/16 - Hydrocarbons
• C10L 1/19 - Esters
• C10L 1/222 - Organic compounds containing nitrogen containing at least one carbon-to-nitrogen single bond
• C10L 1/223 - Organic compounds containing nitrogen containing at least one carbon-to-nitrogen single bond having at least one amino group bound to an aromatic carbon atom
• C10L 10/10 - Use of additives to fuels or fires for particular purposes for improving the octane number

Abstract

Use of a diesel fuel composition comprising (5) vol% or greater of biodiesel for reducing the build-up of deposits in an Exhaust Gas Recirculation (EGR) system of a compression ignition internal combustion engine.

IPC Classes  ?

• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
• C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
• C10L 1/19 - Esters
• C10L 10/04 - Use of additives to fuels or fires for particular purposes for minimising corrosion or incrustation

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving (i) contacting said liquid stream with a washing solvent thereby removing heteroatom containing organic compounds; a) liquid- liquid extraction of the washed stream with an extraction solvent thereby recovering part of the aliphatic hydrocarbons; b1) mixing the extract stream, comprising extraction solvent, aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to recover additional aliphatic hydrocarbons; b2) mixing the remaining stream with additional demixing solvent to remove heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 21/28 - Recovery of used solvent
• C10G 53/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving (i) contacting said liquid stream with a washing solvent thereby removing heteroatom containing organic compounds; a) liquid-liquid extraction of the washed stream with an extraction solvent; b) mixing the extract stream, comprising extraction solvent, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to remove additional heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 21/06 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
• C10G 21/28 - Recovery of used solvent
• C10G 53/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) liquid-liquid extraction of said liquid stream with an extraction solvent, wherein before and/or after step a)heteroatom containing organic compounds, optional aromatic hydrocarbons and optional other contaminants are removed from said liquid stream and/or from a raffinate stream resulting from step a), respectively, by contacting the latter stream(s) with a sorption agent. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 21/28 - Recovery of used solvent
• C10G 53/00 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
• C10G 53/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
• C10G 53/08 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) liquid-liquid extraction of said liquid stream with an extraction solvent; b) mixing the extract stream, comprising extraction solvent, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to remove part of the heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream, wherein before and/or after step c) additional heteroatom containing organic compounds and optional aromatic hydrocarbons are removed from that remaining stream and/or from a stream resulting from step c), respectively, by contacting the latter stream (s) with a sorption agent. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 53/00 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
• C10G 53/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
• C10G 53/08 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
• C10G 55/00 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

The present disclosure relates to a process for generating a stripped fluid having reduced chloride content, the process comprising stripping chloride from a hydroprocessing effluent using a hot high pressure stripper to generate the stripped fluid and a vapour, wherein the stripped fluid comprises a lower chloride content than the hydroprocessing effluent, and wherein the vapour comprises chloride.

IPC Classes  ?

• C10G 45/02 - 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

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) liquid-liquid extraction of said liquid stream with an extraction solvent thereby recovering part of the aliphatic hydrocarbons; b1) mixing the extract stream, comprising extraction solvent, aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to recover additional aliphatic hydrocarbons; b2) mixing the remaining stream with additional demixing solvent to remove heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

IPC Classes  ?

• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 21/12 - Organic compounds only
• C10G 21/28 - Recovery of used solvent
• C10G 53/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step including only extraction steps, e.g. deasphalting by solvent treatment followed by extraction of aromatics
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

An isolation joint is provided with a downhole tubular that has an expandable section which, in axial direction, is sandwiched between a first separator section and a second separator section of the downhole tubular. The expandable section has a circumferential band of increased wall thickness compared to the wall thicknesses of the first and second separator sections. Furthermore, the downhole tubular is provided with a mating support at a predetermined axial location relative to said at least expandable section, adapted for mating with the local expander device within said downhole tubular. This mating support ensures transversal alignment with of a local expander device with the downhole tubular such that the local expansion exclusively is activated within the expandable section.

IPC Classes  ?

• E21B 23/04 - Apparatus for displacing, setting, locking, releasing or removing tools, packers or the like in boreholes or wells operated by fluid means, e.g. actuated by explosion
• E21B 23/06 - Apparatus for displacing, setting, locking, releasing or removing tools, packers or the like in boreholes or wells for setting packers
• E21B 43/10 - Setting of casings, screens or liners in wells

Abstract

A reactor system, which is active in pyrolyzing methane at effective conditions, comprising a molten salt medium and a reaction vessel, the molten salt being contained within the reaction vessel using various methods of catalyst distribution within the vessel such that when methane passes through the vessel, it comes into contact with said catalyst causing a pyrolysis reaction thereby producing molecular hydrogen with reduced carbon dioxide emissions. The catalyst may be placed within the reaction vessel either as suspended particles or in a structured packed form.

IPC Classes  ?

• B01J 19/24 - Stationary reactors without moving elements inside
• C01B 32/05 - Preparation or purification of carbon not covered by groups , , ,
• C01B 3/26 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts

Abstract

The specification discloses a highly macroporous catalyst for hydroprocessing and hydroconversion of heavy hydrocarbon feedstocks. The high macroporosity catalyst incudes an inorganic oxide, molybdenum, and nickel components. It has a pore structure such that at least 18 % of its total pore volume is in pores of a diameter greater than 5,000 angstroms and at least 25 % of its total pore volume is in pores of a diameter greater than 1,000 angstroms. Preferably, the pore structure is bimodal. The catalyst is made by co-mulling the catalytic components with a high molecular weight polyacrylamide followed by forming the co-mulled mixture into a particle or an extrudate. The particle or extrudate is dried and calcined under controlled calcination temperature conditions to yield a calcined particle or extrudate of the high macroporosity catalyst composition.

IPC Classes  ?

• B01J 23/883 - Molybdenum and nickel

Abstract

A process for hydroprocessing a renewable feedstock involves introducing the renewable feedstock and hydrogen in a downward flow into a top portion of a fixed-bed reactor and distributing the downward flow to a top surface of a first catalyst bed in a manner such that the top surface is uniformly wetted across the reactor cross section. The feedstock then flows downwardly through the first catalyst bed, where it is reacted under hydroprocessing conditions sufficient to cause a reaction selected from the group consisting of hydrogenation, hydrodeoxygenation, hydrodenitrogenation, hydrodesulphurization, hydrodemetallization, hydrocracking, hydroisomerization, and combinations thereof. A hydrocarbon liquid separated from the reaction effluent is recycled to the renewable feedstock in a ratio of 0.4:1 to 1.8:1, based on the volume of the renewable feedstock.

IPC Classes  ?

• B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
• B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
• 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
• C10G 49/00 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or
• C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
• 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 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps

Abstract

The invention relates to a process for the production of ethylene in an integrated configuration comprising (i) a steam cracker configuration which comprises a steam cracker unit, a water condensation unit and a carbon dioxide removal unit and (ii) an oxidative dehydrogenation (ODH) configuration which comprises an ODH unit and a water condensation unit, wherein an effluent coming from the ODH configuration, which effluent comprises unconverted ethane and ethylene, is fed to the steam cracker configuration at a position which is downstream of the steam cracker unit, and wherein unconverted oxygen, carbon monoxide and acetylene are removed from at least a portion of the stream coming from the ODH unit by oxidation of carbon monoxide and acetylene into carbon dioxide in an oxidation unit which is located at a position (a) which is downstream of the ODH unit, and (b) which is downstream of the steam cracker unit and upstream of the carbon dioxide removal unit of the steam cracker configuration.

IPC Classes  ?

• C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• C07C 7/148 - Purification, separation or stabilisation of hydrocarbons; Use of additives by treatment giving rise to a chemical modification of at least one compound
• C07C 11/04 - Ethene

Abstract

A gasoline fuel composition for a spark ignition internal combustion engine comprising (a) gasoline blending components, (b) renewable naphtha at a level of 10 to 30% v/v and (c) oxygenated hydrocarbon at a level of 20% v/v or less, wherein the gasoline blending components comprise (a) 0- 30 % v/v alkylate, (b) from 0 to 15% v/v isomerate; (c) 0 to 20% v/v catalytic cracked tops naphtha; and (d) 20% to 40 % v/v of heavy reformate, wherein the total amount of alkylate, isomerate, catalytic cracked tops naphtha and heavy reformate is at least 50% v/v based on the total fuel composition, and wherein the gasoline fuel composition meets the EN228 specification. While the low octane number of renewable naphtha would normally severely restrict its blendability in gasoline to low levels, it has now been found that renewable naphtha can be included in, for example, ethanol-containing gasoline fuel compositions, in surprisingly and significantly high blend ratios of renewable naphtha to ethanol.

IPC Classes  ?

• C10L 1/06 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition

Abstract

Presented is a catalyst composition having exceptional properties for converting sulfur, sulfur compounds, and carbon monoxide contained in gas streams by catalyzed hydrolysis, hydrogenation and water-gas shift reactions. The catalyst comprises underbedded molybdenum and cobalt with an overlayer of molybdenum and cobalt. These metals are present in the catalyst within certain concentration ranges and relative weight ratios. The underbedded metals are present in the catalyst within a specified range relative to the overlayer and total metals. The underbedded metals are formed by co-mulling an inorganic oxide with the catalytically active metals of molybdenum and cobalt. The co-mulled mixture is calcined and then impregnated with overlaid molybdenum and cobalt.

IPC Classes  ?

• B01J 23/882 - Molybdenum and cobalt
• B01J 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/04 - Mixing
• C10G 45/00 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds

Abstract

The invention relates to a process for the production of ethylene by oxidative dehydrogenation (ODH) of ethane, comprising: a) supplying ethane and oxygen to a first ODH zone which is formed by multiple reactor tubes containing a mixed metal oxide ODH catalyst bed; b) contacting the ethane and oxygen with the catalyst resulting in multiple effluent streams, wherein the multiple reactor tubes are cooled by a coolant; c) mixing at least a portion of the multiple effluent streams from step b) resulting in a mixture comprising ethylene, unconverted ethane and unconverted oxygen; d) supplying at least a portion of the mixture from step c) to a second ODH zone containing a mixed metal oxide ODH catalyst bed; e) contacting at least a portion of the mixture from step c) with the catalyst in the second ODH zone resulting in a stream comprising ethylene and unconverted ethane.

IPC Classes  ?

• B01J 23/28 - Molybdenum
• C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• C07C 11/04 - Ethene

Abstract

The present invention relates to a method for the production of hydrogen. Hydrogen is used in many different chemical and industrial processes. Hydrogen is also an important fuel for future transportation and other uses as it does not generate any carbon dioxide emissions when used. The invention provides for a process for producing hydrogen comprising the steps of partially oxidizing a hydrocarbon to obtain a synthesis gas, providing the synthesis gas to a reactor in which carbon monoxide is converted to carbon dioxide, removing the carbon dioxide to obtain hydrogen. The carbon dioxide is used in a chemical process and/or stored in a geological reservoir.

IPC Classes  ?

• B01D 53/047 - Pressure swing adsorption
• C01B 32/50 - Carbon dioxide
• B01D 53/14 - 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 by absorption
• C01B 3/36 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
• C01B 3/48 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
• C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids

Abstract

The present invention relates to a process for converting feed streams selected from (1) a gas stream comprising carbon dioxide and a hydrogen rich gas stream; (2) a methane rich gas stream; and (3) a combination of feed streams (1) and (2) into a product stream comprising carbon monoxide, water and hydrogen, the process comprising introducing feed streams selected from (1), (2) or (3) and oxygen into a reaction vessel, wherein the process comprises in switching mode performing a reverse water gas shift reaction introducing feed stream (1) and oxygen (method I) or a partial oxidation reaction introducing feed stream (2) and oxygen (method II) in the reaction vessel wherein no catalyst is present. The reaction vessel is provided with a burner located at the top of the reaction vessel, the burner comprising coaxial channels for the separate introduction of the different gas streams. During the switching mode from method I to method II or vice verse, the feed streams are gradually changed to the relevant feed streams, so that feed stream (3) is present in an intermediate phase, while also changing the temperature of the reactor to the desired temperature for the relevant method.

IPC Classes  ?

• C01B 3/12 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
• C01B 3/36 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
• C10K 3/02 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment

Abstract

The present invention relates to a process for converting carbon dioxide and hydrogen by performing a reverse water gas shift reaction at elevated temperature, the process comprising introducing carbon dioxide, hydrogen and oxygen into a reaction vessel having an inlet and an outlet, and, wherein the reverse water gas shift reaction takes place in two different zones of the reaction vessel, being a top zone (z1) adjacent to a bottom zone (z2), wherein (a) no catalyst is present in the top zone (z1) of the reaction vessel, and (b) at least a gas stream comprising carbon dioxide, a hydrogen rich gas stream and an oxygen rich gas stream are introduced into the inlet at the top zone (z1) of the reaction vessel in separate feed streams, wherein the hydrogen rich gas stream is introduced into the reaction vessel at a temperature between 15 and 450°C, (c) the hydrogen rich gas stream and oxygen rich gas stream being introduced in close vicinity of each other, wherein at least the hydrogen rich gas stream and the oxygen rich gas stream are introduced into the reaction vessel via a burner comprising coaxial channels for the separate introduction of the different gas streams, the burner being located at the top of the reaction vessel,wherein the hydrogen and oxygen in the hydrogen rich gas stream and oxygen rich gas stream undergo a combustion reaction upon entering the reaction vessel, thereby providing the heating energy required for the reverse water-gas shift reaction; and(d) the temperature in the top zone (z1) of the reaction vessel is maintained in the range of 700 to 1200°C by varying the flow of any of the gas streams which are introduced into the reaction vessel; and (e) the bottom zone (z2) of the reaction vessel is provided with a catalyst bed comprising a reverse water gas shift catalyst, the top of the catalyst bed being placed at a distance from the burner in the top zone (z1) sufficient to prevent damage from flame impingement on the catalyst bed; (f) wherein in the bottom zone (z2) of the reaction vessel a catalytic reverse water gas shift reaction takes place at elevated temperatures, thereby converting unconverted carbon dioxide and hydrogen;to produce a product stream comprising mainly carbon monoxide, hydrogen and water. The process is useful in reducing the carbon footprint of certain industrial technologies, and in addition, the process is useful in the production of synthesis gas.

IPC Classes  ?

• C01B 3/16 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
• C10K 3/02 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment

Abstract

A device for filtering and settling entrained particles from a gas feed stream, the device comprising a cylindrical v-wire filter element to filter the entrained particles, a cap located above the v-wire filter element comprising an outer surface, an under surface, and a downward rim attached to a perimeter of the under surface, and an open annulus area located between and in fluid communication with an open top portion of the v-wire filter element and the under surface of the cap.

IPC Classes  ?

• B01D 46/00 - Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
• B01D 46/10 - Particle separators, e.g. dust precipitators, using filter plates, sheets or pads having plane surfaces
• B01D 46/24 - Particle separators, e.g. dust precipitators, using rigid hollow filter bodies

Abstract

A method for operating an adsorption-based system for removing water and potentially other components from a feed stream. The system includes at least two dehydration units each comprising an adsorption bed. The method includes the steps of: i) obtaining process data from one or more sensors at a predetermined time resolution, the sensors at least comprising at least one moisture sensor at a specified location in each of the dehydration units; ii) dehydrating the feed stream by operating the adsorption-based system in regenerative mode, wherein at least one active unit of the at least two dehydration units is in an adsorption cycle, and wherein at least another one of the at least two dehydration units is being regenerated; iii) estimating an adsorption bed water adsorption capacity during every adsorption cycle; and iv) using the process data to update the estimated adsorption bed water adsorption capacity.

IPC Classes  ?

• B01D 53/04 - 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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
• C10L 3/10 - Working-up natural gas or synthetic natural gas
• G05B 19/414 - Structure of the control system, e.g. common controller or multiprocessor systems, interface to servo, programmable interface controller

Abstract

The present invention provides a method of preparing a supported catalyst, preferably a hydrocracking catalyst, the method at least comprising the steps of: a) providing a zeolite Y having a bulk silica to alumina ratio (SAR) of at least 10; b) mixing the zeolite Y provided in step a) with a base, water and a surfactant, thereby obtaining a slurry of the zeolite Y; c) reducing the water content of the slurry obtained in step b) thereby obtaining solids with reduced water content, wherein the reducing of the water content in step c) involves the addition of a binder; d) shaping the solids with reduced water content obtained in step c) thereby obtaining a shaped catalyst carrier; e) calcining the shaped catalyst carrier obtained in step d) at a temperature above 300°C in the presence of the surfactant of step b), thereby obtaining a calcined catalyst carrier; f) impregnating the catalyst carrier calcined in step e) with a hydrogenation component thereby obtaining a supported catalyst; wherein no heat treatment at a temperature of above 500°C takes place between the mixing of step b) and the shaping of step d).

IPC Classes  ?

• B01J 29/08 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
• 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 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
• B01J 37/08 - Heat treatment
• C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/20 - Sulfiding

Abstract

The disclosure provides a method and system for optimizing production of a natural gas liquefaction process, the method comprising the steps of: selecting at least one manipulated variable (MV) for controlling the liquefaction process; selecting at least one control variable (CV), the at least one control variable at least comprising liquefied natural gas (LNG) throughput; providing at least one model, each model providing a dependency of the at least one control variable (CV) on the at least one manipulated variable (MV); using the at least one model to estimate LNG throughput for at least one of the manipulated variables (MV);obtaining process data from the liquefaction process, the process data at least including observed values of LNG throughput; for combinations of the at least one manipulated variable and the at least one control variable, testing the interdependency thereof; creating a gain matrix based on said interdependencies; and using the gain matrix to optimize a process control system of the liquefaction process.

IPC Classes  ?

• F25J 1/00 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
• F25J 1/02 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen
• G05B 13/04 - Adaptive control systems, i.e. systems automatically adjusting themselves to have a performance which is optimum according to some preassigned criterion electric involving the use of models or simulators
• G05B 17/00 - Systems involving the use of models or simulators of said systems
• G05B 23/00 - Testing or monitoring of control systems or parts thereof

Abstract

The present invention provides a method of preparing acetylene (C2H2), the method at least comprising the steps of: a) providing a methane-containing stream; b) subjecting the methane-containing stream provided in step a) to non-catalytic pyrolysis, thereby obtaining carbon and hydrogen; c) reacting the carbon obtained in step b) with CaO, thereby obtaining CaC2 and CO; d) reacting the CaC2 obtained in step c) with H2O, thereby obtaining acetylene (C2H2) and Ca(OH)2; e) decomposing the Ca(OH)2 obtained in step d), thereby obtaining CaO and H2O; f) using the CaO as obtained in step e) in the reaction of step c).

IPC Classes  ?

• C10H 1/00 - Acetylene gas generators with dropwise, gravity, non-automatic water feed
• C07C 1/00 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon

Abstract

Use of a paraffinic gasoil in a diesel fuel composition for reducing the amount of SCR reagent required by an SCR system fitted to a compression ignition internal combustion engine. The present invention has the advantage that the number of SCR reagent vehicle fills per year is reduced, hence minimising the user's exposure to a corrosive liquid.

IPC Classes  ?

• C10L 10/02 - Use of additives to fuels or fires for particular purposes for reducing smoke development
• C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
• C10L 1/16 - Hydrocarbons
• F01N 3/20 - Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operation; Control specially adapted for catalytic conversion

Abstract

The present disclosure relates to a solid adsorbent for capturing carbon dioxide (CO2) from a gas stream comprising CO2, the solid adsorbent comprising an amine covalently bonded to a polymer resin (e.g., a polystyrene resin), wherein the solid adsorbent has a CO2 uptake capacity of greater than about 7 wt. % at a temperature of about 40 °C, and wherein the solid adsorbent has a CO2 uptake capacity of less than about 1.5 wt. % at a temperature of about 100 °C, as measured when the gas stream further comprises a concentration of the CO2 of about 4 vol. %, by volume of the gas stream.

IPC Classes  ?

• B01J 20/26 - Synthetic macromolecular compounds
• B01D 53/02 - 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 by adsorption, e.g. preparative gas chromatography
• B01D 53/62 - Carbon oxides
• 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 20/32 - Impregnating or coating
• B01J 20/34 - Regenerating or reactivating

Abstract

The present invention relates to an electrically heated reactor having an outer surface area, an inlet and an outlet, wherein (a) the reactor is a tube surrounded by electrical heating means at a certain distance; (b) the electrical heating means comprises radiative sheeting placed coaxially with regard to the reactor tube, the surface area of the sheeting facing the outer surface area of the reactor tube defining an inner surface area of the electrical heating means; (c) the inner surface area of the heating means covers at least 60% of the reactor tube outer surface area;and (d) the distance between the reactor tube and the heating means is selected such that the ratio between the inner surface area of the electrical heating means to the reactor tube outer surface area is in the range of 0.7 to 3Ø Electrically heated processes demand managing a heat-flux and temperature profile. In many applications the heat-flux is larger where the process flow enters the reactor whilst having a lower temperature. Towards the exit of the reactor tube the heat-flux is lower whilst the process flow having higher temperature. The present invention can accommodate this requirement. The reactor is useful in many industrial scale high temperature gas conversion and heating technologies.

IPC Classes  ?

• B01J 8/06 - Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the solid particles being arranged in tubes

Abstract

A process for the production of a high purity first diol from a product stream comprising two or more C2 to C7 diols, said process comprising the steps of: (i) providing the product stream to a first distillation column; (ii) providing an extractant selected from the group of C3 to C6 sugar alcohols and mixtures thereof to the first distillation column; (iii) operating the first distillation column to obtain a first bottoms stream comprising at least a first diol and the extractant; (iv) providing the first bottoms stream to a second distillation column operating to obtain a second top stream comprising the first diol and diols with atmospheric boiling points at least 10 °C higher than the first diol, and (v) providing the second top stream to a third distillation column to obtain a third top stream comprising the first diol; wherein the product stream comprises 0.1 to 10 wt% of diols with atmospheric boiling points at least 10 °C higher than the first diol, calculated upon the total weight of C2 to C7 diols in the product stream.

IPC Classes  ?

• C07C 29/84 - Separation; Purification; Stabilisation; Use of additives by physical treatment by distillation by extractive distillation
• C07C 31/20 - Dihydroxylic alcohols

Abstract

Implementations of the disclosed subject matter provide a process for upgrading refinery residue feedstock. Step a) may include introducing the refinery residue feedstock into a fluidized bed reactor as a solid. In step b), the refinery residue feedstock may be heated to a devolatilizing and thermal cracking temperature in the fluidized bed reactor to produce a product stream comprising gaseous hydrocarbons and solid coke. The gaseous hydrocarbons may be subjected to catalytic hydroprocessing, in step c), in the presence of molecular hydrogen to increase the hydrogen to carbon ratio and lower the average molecular weight of the gaseous hydrocarbons. In step d), the gaseous hydrocarbons may be separated from the solid coke. In step e), the gaseous hydrocarbons from step d) may be subjected to further processing to produce at least one of: C1-C3 hydrocarbons, liquefied petroleum gas, naphtha range hydrocarbons, and middle distillate range hydrocarbons.

IPC Classes  ?

• C10G 70/02 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by hydrogenation
• C10B 49/22 - Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique

Abstract

The present application relates to a method for estimating the temperature rise rate of a battery under pulsed heating. By establishing an equivalent circuit model of the battery, parameters in the equivalent circuit model of the battery are identified to obtain the effective entropy potential of the battery and the relationship between the open circuit voltage and the pulsed heating current of the battery. The amplitude and period of the pulsed heating current are pulsed parameters. Then according to the effective entropy potential and the relationship between the open circuit voltage and the pulsed heating current of the battery, a heat generation model is established. By using the heat generation model and the heat transfer power of the battery, an energy formulation of the battery in the process of pulsed heating is obtained, so as to obtain the temperature rise rate of the battery under pulsed heating. By establishing an equivalent circuit model of the battery and using the heat generation model of the battery and the heat transfer power model of the battery, the foregoing method can obtain the relationship between the temperature rise rate of the battery under pulsed heating and the pulsed heating current, providing a convenient and comprehensive estimation method for determining the heating effect of pulsed heating in practical applications.

IPC Classes  ?

• H01M 10/48 - Accumulators combined with arrangements for measuring, testing or indicating the condition of cells, e.g. the level or density of the electrolyte
• H02J 7/00 - Circuit arrangements for charging or depolarising batteries or for supplying loads from batteries
• H01M 10/633 - Control systems - characterised by algorithms, flow charts, software details or the like
• H01M 10/44 - Methods for charging or discharging

Abstract

The present application relates to a method and system for determining parameters of battery pulsed heating. The reference potential of the anode of the lithium-ion battery is obtained in real time in the positive and negative pulsed heating process under various heating parameters. The reference potential of the anode is the voltage difference between the anode of the lithium-ion battery and the reference electrode. By judging the relationship between the reference potential of the anode and the threshold potential, it is judged whether Li plating has occurred to the lithium-ion battery. Li plating may lead to a decrease in the available capacity of the battery, and puncture of the membrane by dendrite, which causes a short circuit in the battery and induces thermal runaway of the battery, bringing about many hazards such as performance reduction and safety risks. Therefore, when the reference potential of the anode is smaller than the threshold potential, the first heating parameters need to be adjusted to avoid the occurrence of Li plating and improve the life of the battery. By recording the heating parameters when the reference potential of the anode is greater than the threshold potential, it can be ensured that the pulsed heating parameters have no significant impact on the life of the battery.

IPC Classes  ?

• H01M 10/633 - Control systems - characterised by algorithms, flow charts, software details or the like
• B60L 58/25 - Methods or circuit arrangements for monitoring or controlling batteries or fuel cells, specially adapted for electric vehicles for monitoring or controlling batteries for controlling the temperature of batteries by controlling the electric load
• B60L 58/27 - Methods or circuit arrangements for monitoring or controlling batteries or fuel cells, specially adapted for electric vehicles for monitoring or controlling batteries for controlling the temperature of batteries by heating
• H01M 10/48 - Accumulators combined with arrangements for measuring, testing or indicating the condition of cells, e.g. the level or density of the electrolyte
• H01M 10/0525 - Rocking-chair batteries, i.e. batteries with lithium insertion or intercalation in both electrodes; Lithium-ion batteries
• H01M 10/44 - Methods for charging or discharging

Abstract

The present application relates to a durability test method and system and a data table generation method for battery pulsed heating. The battery to be tested is put into a temperature chamber, and the temperature of the temperature chamber is set at a first temperature value. The lithium-ion battery is subjected to pulsed heating under first pulse parameters until the pulsed heating time reaches the preset pulse duration. The temperature of the temperature chamber is adjusted to a second temperature value and a capacity degradation value of the battery to be tested is obtained at the second temperature value, so as to obtain durability of the battery to be tested. Before testing of the capacity degradation value of the battery to be tested, continuous pulsed heating is conducted. After the battery is heated for a period of time, the temperature elevation and heat dissipation of the battery will reach stable values and the temperature will no longer rise. Such pulsed heating does not require a long period of standing at low temperature. Therefore, a large amount of test time can be saved, the test period is shortened, and the influence of battery temperature on battery durability can be verified through a large number of experiments.

IPC Classes  ?

• G01R 31/392 - Determining battery ageing or deterioration, e.g. state of health
• H01M 10/48 - Accumulators combined with arrangements for measuring, testing or indicating the condition of cells, e.g. the level or density of the electrolyte
• H01M 10/633 - Control systems - characterised by algorithms, flow charts, software details or the like
• H01M 10/44 - Methods for charging or discharging

Abstract

A sulfur-resistant, high activity methane oxidation catalyst for use in removing methane from gas streams having a concentration of methane by oxidizing the methane. The methane oxidation catalyst is especially useful in processing gas streams that also have a concentration of a sulfur compound. The sulfur-resistant methane oxidation catalyst includes a unique multi-crystalline zirconia as a support for a platinum component and a ruthenium component. The multi-crystalline zirconia contributes to the excellent properties of the catalyst. The platinum and ruthenium components can be included in the methane oxidation catalyst in a specific weight ratio that also contributes to the enhanced properties of the catalyst. The sulfur-resistant methane oxidation catalyst may also include a chloride component that contributes to enhanced properties of the catalyst.

IPC Classes  ?

• B01J 23/46 - Ruthenium, rhodium, osmium or iridium
• B01D 53/86 - Catalytic processes
• B01J 23/42 - Platinum
• B01J 29/06 - Crystalline aluminosilicate zeolites; Isomorphous compounds thereof

Abstract

A fuel composition wherein the fuel composition comprises (a) a major amount of liquefied methane based gas in cryogenic state having a temperature in the range from -182°C to -100°C and, preferably, a pressure in the range of 1 bar to 15 bar, and (b) a minor amount of an 5 ignition improving additive, wherein the ignition improving additive has a melting point of less than -105°C, a boiling point of less than 60°C and an autoignition temperature of lower than 480°C and wherein the ignition improving additive is selected from alkanes, alkenes, alcohols, ethers, alkynes, aldehydes, ketones, amides, nitroalkanes, nitosoalkanes, nitrates, nitrites, cycloalkanes, cycloalkenes, dienes, peroxides, triatomic oxygen, trimethylamine, ethylene oxide, propylene oxide, and mixtures thereof.

IPC Classes  ?

• C10L 3/06 - Natural gas; Synthetic natural gas obtained by processes not covered by , or
• C10L 10/00 - Use of additives to fuels or fires for particular purposes

Abstract

The present disclosure provides a heat exchanger system and a method of using the heat exchanger system for heating, cooling or condensing a gaseous multiple component process stream comprising at least one hydrocarbon. The heat exchanger system comprises: - a shell having at least one first inlet and at least one first outlet defining a flow path for a first process fluid, and at least one second inlet and at least one second outlet defining a flow path for a second process fluid; - a number of parallel tubes arranged in the shell between the first inlet and the first outlet, each tube having an outer surface being provided with a multitude of plate fins extending radially outward from the outer surface; the first flow path extending along the outer surface of the tubes, and the second flow path extending through the tubes. The multiple component process stream may comprise two or more components selected from the group of methane, ethane, propane, and nitrogen. The heat exchanger may be used to cool or condense a mixed refrigerant, comprising one or more hydrocarbons, in a process for the liquefaction of natural gas.

IPC Classes  ?

• F25J 5/00 - Arrangements of cold-exchangers or cold-accumulators in separation or liquefaction plants
• F25J 1/02 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen
• F28B 1/00 - Condensers in which the steam or vapour is separated from the cooling medium by walls, e.g. surface condenser
• F28D 7/00 - Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
• F28F 1/24 - Tubular elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending transversely
• F28F 9/02 - Header boxes; End plates

Abstract

A reactor and a process for fluid catalytic cracking (FCC) a hydrocarbon feed in the riser-reactor, the process including injecting the hydrocarbon feed into an evaporation zone of the riser-reactor, injecting a first catalyst into the evaporation zone, wherein the first catalyst mixes with the hydrocarbon feed to generate a hydrocarbons stream in the evaporation zone, and wherein the temperature in the evaporation zone is less than 625°C, and passing the hydrocarbons stream from the evaporation zone into a cracking zone of the riser-reactor to generate a cracked product in the cracking zone.

IPC Classes  ?

• 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 8/38 - 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 fluidised bed containing a rotatable device or being subject to rotation

Abstract

A horseshoe lateral is drilled having two substantially parallel lateral sections connected with a horseshoe section.

IPC Classes  ?

• E21B 7/04 - Directional drilling
• E21B 43/30 - Specific pattern of wells, e.g. optimizing the spacing of wells

Abstract

A method for determining subsurface hydrocarbon fluid properties of reservoired hydrocarbons having a hydrocarbon seep involves locating a hydrocarbon seep at a seabed location where hydrocarbon is actively flowing out of the seabed. A sample of hydrocarbons is collected from the hydrocarbon seep. Physical, transport and/or thermodynamic fluid properties of reservoired hydrocarbons are determined from the sample of hydrocarbons.

IPC Classes  ?

• G01V 9/00 - Prospecting or detecting by methods not provided for in groups

Abstract

A method for determining a presence of reservoired hydrocarbons having a hydrocarbon seep involves locating a hydrocarbon seep at a seabed location where hydrocarbon is actively flowing out of the seabed. Temporally spaced isotopic compositions of the hydrocarbon seep are determined. When a temporal variance between the isotopic compositions falls within a predetermined temporal tolerance, the hydrocarbon seep is classified as being indicative of the presence of reservoired hydrocarbons. A unique identifier is assigned to the reservoired hydrocarbons.

IPC Classes  ?

• G01V 9/00 - Prospecting or detecting by methods not provided for in groups

Abstract

A method for determining a presence of reservoired hydrocarbons having a hydrocarbon seep involves locating a hydrocarbon seep at a seabed location where hydrocarbon is actively flowing out of the seabed. Temporally spaced molecular compositions of the hydrocarbon seep are determined. When a temporal variance between the molecular compositions falls within a predetermined temporal tolerance, the hydrocarbon seep is classified as being indicative of the presence of reservoired hydrocarbons. A unique identifier is assigned to the reservoired hydrocarbons.

IPC Classes  ?

• G01V 9/00 - Prospecting or detecting by methods not provided for in groups

Abstract

A process for the production of furfural from a biphasic composition including furfural, an organic solvent and soluble organic debris. The said process includes subjecting the biphasic composition to a liquid-liquid separation step to provide an organic phase and an aqueous phase. The organic phase includes the organic solvent, a first portion of the furfural and a first portion of soluble organic debris. The aqueous phase includes a remainder portion of the furfural and a remainder portion of soluble organic debris. The organic phase is subjected to a distillation step to provide a furfural stream and an organic solvent stream including the organic solvent and the first portion of the soluble organic debris. The organic solvent stream is conveyed to an adsorption unit to adsorb a second portion of the soluble organic debris, forming an organic debris-depleted recycle stream.

IPC Classes  ?

• C07D 307/48 - Furfural

Abstract

A downhole tool, which includes a tool housing having a longitudinal axis, is equipped with a sting for punching a hole in a casing wall and injecting a sealant though said hole. The tube has a fluid channel to establish fluid communication from within the tool housing to an exterior of the tool housing through the fluid channel. A press device acts on the sting to force the sting in a radially outward direction from the tool housing. A check valve is arranged in the fluid channel, which allows fluid communication in a direction from within the tool housing to an exterior of the tool housing and which blocks fluid flow in an opposite direction. In use, the sting can perforate a casing wall and the sealant can be injected into an annular space around the casing.

IPC Classes  ?

• E21B 33/13 - Methods or devices for cementing, for plugging holes, crevices, or the like
• E21B 43/112 - Perforators with extendable perforating members, e.g. actuated by fluid means

Abstract

The present disclosure provides a heat axchanger and heat exchange method for cooling a gaseous process stream. The heat exchanger unit (100, 200, 300) comprises: a heat exchanger vessel (2), the heat exchanger vessel (2) comprising a plurality of process stream conduits (12, 14) arranged to receive the gaseous process stream (10) and discharge a cooled process stream (18), and a plurality of refrigerant conduits (46, 48, 49) to receive at least part of a pre-cooled mixed refrigerant stream (58) and to discharge at least one cooled mixed refrigerant stream (72, 82); at least one expansion device (74, 84) arranged to receive at least part of the cooled mixed refrigerant stream (72, 82) and discharge a further cooled mixed refrigerant stream (76, 86), the further cooled mixed refrigerant stream (76, 86) being connected to at least one of a third refrigerant inlet (77) and a fourth refrigerant inlet (87) of the heat exchanger vessel (2) to provide cooling to the process stream conduits (12, 14) and the refrigerant conduits (46, 48, 49); a refrigerant bleed vessel (110) arranged to receive a first refrigerant split-off stream (112) from the cooled mixed refrigerant stream (72, 82) and to receive a second refrigerant split-off stream (114) from the pre-cooled mixed refrigerant stream; the refrigerant bleed vessel (110) comprising a bleed outlet (116) to discharge a bleed stream (118) and a recycle outlet (120) to discharge a recycle stream (122), the recycle outlet being fluidly connected to at least one of the third refrigerant inlet (77) and the fourth refrigerant inlet (87) of the heat exchanger vessel (2).

IPC Classes  ?

• F25J 1/00 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
• F25J 1/02 - Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen

Abstract

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid hydrocarbon feedstock stream, which comprises aliphatic hydrocarbons and additionally comprises aromatic hydrocarbons and/or polar components, said process comprising the steps of: feeding the liquid hydrocarbon feedstock stream to a first column; feeding a first solvent stream which comprises an organic solvent to the first column at a position which is higher than the position at which the liquid hydrocarbon feedstock stream is fed; contacting at least a portion of the liquid hydrocarbon feedstock stream with at least a portion of the first solvent stream; and recovering at least a portion of the aliphatic hydrocarbons by liquid-liquid extraction of aromatic hydrocarbons and/or polar components with organic solvent, resulting in a stream comprising recovered aliphatic hydrocarbons and optionally organic solvent and a bottom stream from the first column comprising organic solvent and aromatic hydrocarbons and/or polar components.

IPC Classes  ?

• C10G 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
• 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 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
• 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 21/02 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
• C10G 21/16 - Oxygen-containing compounds
• C10G 21/27 - Organic compounds not provided for in a single one of groups
• C10G 55/04 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Abstract

The present invention relates to metal-organic framework characterized in that it comprises a polymer coating; further the invention relates to a process for the preparation of said polymer-coated metal-organic framework and a process for recycling after degradation. The polymer coated MOFs of this invention find application in a broad range of technologies and therapeutic areas.

IPC Classes  ?

• B01J 20/22 - Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
• B01D 53/04 - 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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
• B01J 20/32 - Impregnating or coating
• B01J 20/34 - Regenerating or reactivating
• C02F 1/28 - Treatment of water, waste water, or sewage by sorption

Abstract

Presented is a selective hydrogenation catalyst and a method of making the catalyst. The catalyst comprises a carrier containing bi-metallic nanoparticles. The nanoparticles comprise a silver component and a palladium component. The catalyst is made by incorporating an aqueous dispersion of the bi-metallic nanoparticles onto a catalyst carrier followed by drying and calcining the carrier having incorporated therein the dispersion. The catalyst is used in the selective hydrogenation of highly unsaturated hydrocarbons contained olefin product streams.

IPC Classes  ?

• B01J 23/44 - Palladium
• B01J 23/50 - Silver
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/08 - Heat treatment
• B22F 9/24 - Making metallic powder or suspensions thereof; Apparatus or devices specially adapted therefor using chemical processes with reduction of metal compounds starting from liquid metal compounds, e.g. solutions
• C07C 5/05 - Partial hydrogenation
• C07C 5/09 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
• C10G 45/40 - Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof

Abstract

The invention relates to a process for preparing a shaped catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which comprises: a) preparing a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium; b) mixing the catalyst obtained in step a), a binder and optionally water, wherein the binder has a surface area greater than 100 m2/g and a water loss upon heating at a temperature of 485 °C which is greater than 1 wt.%; c) shaping the mixture obtained in step b) to form a shaped catalyst by means of tableting; and d) subjecting the shaped catalyst obtained in step c) to an elevated temperature. Further, the invention relates to a catalyst obtainable by said process and to a process of alkane oxidative dehydrogenation and/or alkene oxidation wherein said catalyst is used.

IPC Classes  ?

• B01J 23/28 - Molybdenum
• B01J 21/04 - Alumina
• B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
• B01J 27/057 - Selenium or tellurium; Compounds thereof
• B01J 37/00 - Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
• B01J 37/03 - Precipitation; Co-precipitation
• B01J 37/04 - Mixing
• B01J 37/08 - Heat treatment
• C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
• C07C 51/25 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring

Abstract

The present invention relates to a process for converting carbon dioxide and hydrogen into a product stream comprising carbon monoxide, water and hydrogen, the process comprising introducing carbon dioxide, hydrogen and oxygen into a reaction vessel, and performing a reverse water gas shift reaction at elevated temperature, wherein (a) no catalyst is present in the reaction vessel, and (b) at least a gas stream comprising carbon dioxide, a hydrogen rich gas stream and an oxygen rich gas stream are introduced into the reaction vessel in separate feed streams, wherein the hydrogen rich gas stream is introduced into the reaction vessel at a temperature between 15 and 450 °C, (c) the hydrogen rich gas stream and oxygen rich gas stream being introduced in close vicinity of each other, wherein at least the hydrogen rich gas stream and the oxygen rich gas stream are introduced into the reaction vessel via a burner comprising coaxial channels for the separate introduction of the different gas streams, the burner being located at the top of the reaction vessel, wherein the hydrogen and oxygen in the hydrogen rich gas stream and oxygen rich gas stream undergo a combustion reaction upon entering the reaction vessel, thereby providing the heating energy required for the reverse water-gas shift reaction; and (d) the temperature in the reaction vessel is maintained in the range of 1000 to 1500 °C by varying the molar ratio of hydrogen to oxygen, which are introduced into the reaction vessel in the hydrogen rich gas stream and oxygen rich gas stream, respectively.

IPC Classes  ?

• C01B 3/12 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
• C10K 3/02 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
• C25B 1/04 - Hydrogen or oxygen by electrolysis of water

Abstract

Methods for production of ethanol, distiller's corn oil, and enhanced co-products are disclosed. Methods include obtaining a mixture of one or more co-products of an alcohol production process, which may include wet cake, performing hydrolysis of polysaccharides in the mixture to generate fermentable sugars, fermenting the fermentable sugars in the mixture to produce alcohol, distilling the mixture to remove alcohol from the mixture thereby producing alcohol-containing distillate and enhanced whole stillage, removing released oil from the fermented mixture before distillation and/or from the enhanced whole stillage after distillation, and recovering enhanced wet distiller's grains, enhanced thin stillage, and/or enhanced dried distiller's grains. Compositions disclosed herein include enhanced dried distiller's grains having a crude protein content of at least 45% on a dry weight basis and having a total fat content of less than 10% on a dry weight basis.

IPC Classes  ?

• A23K 10/38 - Animal feeding-stuffs from material of fungal origin, e.g. mushrooms from waste material from distillers' or brewers' waste
• C12P 7/08 - Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
• C12P 7/10 - Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material

Abstract

The invention relates to a safety device for releasably locking the output member of a linear drive, the device comprising the following: a coupling rod (12) that can be coupled with the output member of the linear drive; a blocking unit (21), through which the coupling rod (12) passes in a linearly displaceable manner, which blocking unit is movable between a blocking position (30) blocking a lifting of the coupling rod (12), and a release position (31) allowing a linear movement of the coupling rod (12) relative to a housing (13); a spring device (28) for pretensioning the blocking unit (21) into the blocking position (30); a locking device (41) for locking the blocking unit (21) in the release position (31), wherein the locking device (41) has locking roller bodies (34a-c) accommodated in the housing (13), and a support sleeve (42), through which the coupling rod (12) passes in a linearly displaceable manner; an electromagnetic device (18), which, when energized, holds the support sleeve (42) in the supporting position (43) counter to the actuating force of at least one trigger spring (48) of a trigger spring device (49).

IPC Classes  ?

• F16K 31/00 - Operating means; Releasing devices
• F16K 31/56 - Mechanical actuating means without stable intermediate position, e.g. with snap action

Abstract

The invention relates to a process for preparing a catalyst for alkane oxidative dehydrogenation and/or alkene oxidation, which catalyst is a mixed metal oxide catalyst containing molybdenum, vanadium, niobium and optionally tellurium, wherein the process comprises: a) preparing a catalyst precursor containing molybdenum, vanadium, niobium and optionally tellurium; b) optionally contacting the catalyst precursor obtained in step a) with oxygen and/or an inert gas at an elevated temperature; c) contacting the catalyst precursor obtained in step a) or step b) with a gas mixture comprising ammonia and water, which gas mixture further comprises oxygen and/or an inert gas, at an elevated temperature; and d) optionally contacting the catalyst precursor obtained in step c) with an inert gas at an elevated temperature. Further, the invention relates to a catalyst obtainable by said process and to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms wherein said catalyst is used.

IPC Classes  ?

• B01J 23/28 - Molybdenum
• B01J 37/08 - Heat treatment
• C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
• C07C 11/04 - Ethene
• C07C 11/06 - Propene

Abstract

The invention relates to a process for the production of ethylene by oxidative dehydrogenation of ethane, comprising: a) subjecting a stream comprising ethane to oxidative dehydrogenation conditions, resulting in a stream comprising ethylene, unconverted ethane and light components; b) subjecting ethylene, unconverted ethane and light components from the stream resulting from step a) to distillation, resulting in a stream comprising ethylene and light components and a stream comprising unconverted ethane; c) optionally recycling unconverted ethane from the stream comprising unconverted ethane resulting from step b) to step a); and d) subjecting ethylene and light components from the stream comprising ethylene and light components resulting from step b) to distillation at a top column pressure which is higher than the top column pressure in step b), resulting in a stream comprising light components and a stream comprising ethylene.

IPC Classes  ?

• C07C 11/04 - Ethene
• C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• C07C 7/04 - Purification, separation or stabilisation of hydrocarbons; Use of additives by distillation

Abstract

The invention relates to a process of the oxidative dehydrogenation of an alkane containing 2 to 6 carbon atoms and/or the oxidation of an alkene containing 2 to 6 carbon atoms, wherein the alkane and/or alkene is contacted with oxygen in the presence of a catalyst comprising a mixed metal oxide and one or more diluents selected from the group consisting of carbon dioxide, carbon monoxide and steam, and wherein the conversion of the alkane and/or alkene is at least 40%.

IPC Classes  ?

• C07C 5/48 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
• C07C 11/04 - Ethene
• C07C 11/06 - Propene
• C07C 51/215 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
• C07C 51/25 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring