A process for controlling heat transfer in a hydrogenation process is provided. A hydrocarbon feed stream is hydrogenated in a hydrogenation reactor in the presence of hydrogen and a hydrogenation catalyst to produce a hydrogenated effluent. In an embodiment, the hydrogen is green hydrogen. A first feed stream is taken from the hydrogenated effluent and said first feed stream is sent to a steam generator to produce a steam stream. A pressure of the steam stream produced in the steam generator is adjusted to control the temperature of the first feed stream and the first feed stream is then charged to a second reactor.
C07C 5/10 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
F01K 7/16 - Steam engine plants characterised by the use of specific types of enginePlants or engines characterised by their use of special steam systems, cycles or processesControl means specially adapted for such systems, cycles or processesUse of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
F22B 1/16 - Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being hot liquid or hot vapour, e.g. waste liquid, waste vapour
F22G 1/00 - Steam superheating characterised by heating method
2.
PROCESSES FOR REMOVING PERFLUOROALKYL SUBSTANCES AND REGENERATING AN ADSORBENT USED WITH SAME
Processes and apparatuses for degrading PFAS into calcium fluoride, carbon dioxide, and water. PFAS are heated and introduced to a calcium base which will degrade the PFAS. The PFAS may be in a stream that is a PFAS enriched stream formed by desorbing the PFAS from an adsorbent which removed the PFAS from a contaminant stream. The PFAS may be desorbed in the presence of the calcium base. The calcium base may be calcium hydroxide, calcium oxide, calcium carbonate, or combinations thereof.
A62D 3/36 - Detoxification by using acid or alkaline reagents
B01D 15/20 - Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the conditioning of the sorbent material
B01J 20/20 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbonSolid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof comprising inorganic material comprising carbon obtained by carbonising processes
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern to a pressure swing adsorption unit and then to an electrochemical compression unit to produce hydrogen having a purity of above 99.5 mol% to close to 100 mol%.
B01D 53/32 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by electrical effects other than those provided for in group
4.
APPARATUS AND PROCESS FOR PRODUCING A SUPERHEATED STEAM
An apparatus and a process for producing a superheated steam is disclosed. The apparatus comprises a primary heater comprising a radiant section and a convection section. The primary heater comprises a convective heat transfer conduit in communication with a source of water and passing through the convection section to provide a steam stream. The apparatus further comprises a secondary heater. The secondary heater comprises a radiant section and a secondary heat transfer conduit in communication with the convective heat transfer conduit of the primary heater. The secondary heat transfer conduit passes through the radiant section of the secondary heater to provide a superheated steam stream. Further, a process for producing a superheated steam is disclosed.
A hydroprocessing catalyst is provided that is supported hydrotreating catalyst, where the shaped support of 0.36-0.46 void fraction is comprised of a single source of gamma alumina with a medium pore diameter of 10 nm and at least 0.95 cc/g pore volume but not more than 1.10 cc/g, and includes a single, Group IIIb metal dispersed by mulling or mixing in a forming step, and a surface area by nitrogen BET between 230 m2/g and 260 m2/g, and where the finished catalyst can be described in terms of molar ratios relative to aluminum, where the aluminum concentration may vary from 26 to 30 wt%, Al:Group VIb 4.8-5.6, Al:Group VIII 14.9-19.0, Al:Group Va 9.6-12.7, and Al:Group IIIb 112.5-228.2.
A process for converting a feed in a series of reactors is disclosed. The process comprises taking at least two hydrocarbon streams, a first hydrocarbon feed stream and a second hydrocarbon feed stream. The first hydrocarbon feed stream and the second hydrocarbon feed stream are heat exchanged in a heat exchanger with a second product stream from a second reactor. A heat exchanged first hydrocarbon feed stream is charged into a first catalyst bed in a first reactor to produce a first product stream and a heat exchanged second hydrocarbon feed stream is charged into a second catalyst bed in the second reactor to produce the second product stream. The second product stream is at a higher temperature than the first hydrocarbon feed stream and the second hydrocarbon feed stream.
Hydroxymethylfurfural (HMF) is derived from C6 sugars and is a versatile platform chemical with the potential to replace a range of conventional building blocks. It has been found that the remove of certain components such as oxygenated contaminants from C6 sugars can significantly improve the yields of HMF. The oxygenated contaminants may be removed by ion exchange resins, adsorbents, solvent extraction and pH adjustment via addition of base.
A slurry hydrocracking process is disclosed. The process comprises charging a catalyst, a bio-oil stream, a recycle stream, and a hydrogen stream to a slurry hydrocracking reactor. The bio-oil stream, and the recycle stream are hydrocracked in the presence of the catalyst and the hydrogen stream to produce a slurry hydrocracked effluent stream. A recycle stream is taken from the hydrocracked effluent stream. The bio-oil stream is added to the recycle stream which is charged into the slurry hydrocracking reactor.
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
9.
OLEFINS TO FUEL IN A SINGLE-STAGE OLIGOMERIZATION PROCESS
This disclosure describes a process for producing a sustainable aviation fuel including oligomerizing a charge olefin stream over a single oligomerization catalyst to produce an oligomerized stream with greater than about 50% and less than about 99.5% olefins conversion per pass in the charge stream.
A process of producing a fuel stream comprising renewable carbon is disclosed. The process comprises producing an olefinic stream or an alcohol stream from a renewable feedstock. An aromatic stream and an alkylating agent comprising the olefinic stream or the alcohol stream is charged to an alkylation reactor to alkylate the aromatic stream with the alkylating agent to produce an alkylated aromatic product stream. The alkylated aromatic product stream comprises about 0.1 wt % to about 67 wt % renewable carbon.
C10G 69/12 - 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 polymerisation or alkylation step
11.
IMPROVING YIELD OF HYDROXYMETHYLFURFURAL THROUGH PURIFICATION OF SUGAR FEED
Hydroxymethylfurfural (HMF) is derived from C6 sugars and is a versatile platform chemical with the potential to replace a range of conventional building blocks. It has been found that the remove of certain components such as oxygenated contaminants from C6 sugars can significantly improve the yields of HMF. The oxygenated contaminants may be removed by ion exchange resins, adsorbents, solvent extraction and pH adjustment via addition of base.
A sustainable aviation fuel composition is disclosed. The sustainable aviation fuel composition comprises a T10 of more than about 110° C. and a final boiling point of no more than about 300° C., about 5 to about 25 wt % aromatics, no more than about 15 wt % hydrogen, no more than about 1 wt % oxygen, and has a flash point of at least about 38° C. Further, a process of producing sustainable aviation fuel is disclosed. The sustainable aviation fuel can be used as fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons
C10G 45/16 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing with moving solid particles suspended in the oil, e.g. slurries
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
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
13.
PURIFICATION OF HYDROGEN REMOVED FROM UNDERGROUND STORAGE
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern to a pressure swing adsorption unit and then to an electrochemical compression unit to produce hydrogen having a purity of above 99.5 mol % to close to 100 mol %.
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
B01D 53/32 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by electrical effects other than those provided for in group
A slurry hydrocracking process is disclosed. The process comprises charging a catalyst, a bio-oil stream, a recycle stream, and a hydrogen stream to a slurry hydrocracking reactor. The bio-oil stream, and the recycle stream are hydrocracked in the presence of the catalyst and the hydrogen stream to produce a slurry hydrocracked effluent stream. A recycle stream is taken from the hydrocracked effluent stream. The bio-oil stream is added to the recycle stream which is charged into the slurry hydrocracking reactor.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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 hydrocarbonsHydrofinishing characterised by the catalyst used
15.
OLEFINS TO FUEL IN A SINGLE-STAGE OLIGOMERIZATION PROCESS
This disclosure describes a process for producing a sustainable aviation fuel including oligomerizing a charge olefin stream over a single oligomerization catalyst to produce an oligomerized stream with greater than 50% and less than 99.5% olefins conversion per pass in the charge stream.
A renewable naphtha composition is disclosed. The renewable naphtha composition comprises 0.1 wt% to 15 wt% oxygen, and C4 to C8 hydrocarbons comprising more than 50 wt% cyclic hydrocarbons in the renewable naphtha composition. The renewable naphtha composition has a final boiling point of no more than 420°F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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
17.
PROCESS AND APPARATUS FOR PRODUCING ULTRA PURE CO2 IN A CARBON CAPTURE PROCESS
Processes for producing two CO2 streams having different purities, including one stream comprising ultra high purity CO2. The processes incorporate a second fractionation column in a CO2 fractionation process. The bottoms stream from the first cryogenic fractionation column is sent to the second CO2 fractionation column. The second CO2 fractionation column can produce ultra high purity CO2. The bottoms stream from the first column can be divided and a portion of the bottoms stream can be recovered as a second CO2 product stream having a lower purity than the purity of the product stream.
F25J 3/02 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
A hydroprocessing catalyst is provided that is supported hydrotreating catalyst, where the shaped support of 0.36-0.46 void fraction is comprised of a single source of gamma alumina with a medium pore diameter of 10 nm and at least 0.95 cc/g pore volume but not more than 1.10 cc/g, and includes a single, Group IIIb metal dispersed by mulling or mixing in a forming step, and a surface area by nitrogen BET between about 230 m2/g and 260 m2/g, and where the finished catalyst can be described in terms of molar ratios relative to aluminum, where the aluminum concentration may vary from 26 to 30 wt %, Al: Group VIb 4.8-5.6, Al: Group VIII 14.9-19.0, Al: Group Va 9.6-12.7, and Al: Group IIIb 112.5-228.2.
A process for converting a feed in a series of reactors is disclosed. The process comprises taking at least two hydrocarbon streams, a first hydrocarbon feed stream and a second hydrocarbon feed stream. The first hydrocarbon feed stream and the second hydrocarbon feed stream are heat exchanged in a heat exchanger with a second product stream from a second reactor. A heat exchanged first hydrocarbon feed stream is charged into a first catalyst bed in a first reactor to produce a first product stream and a heat exchanged second hydrocarbon feed stream is charged into a second catalyst bed in the second reactor to produce the second product stream. The second product stream is at a higher temperature than the first hydrocarbon feed stream and the second hydrocarbon feed stream.
B01J 8/18 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles
B01J 8/26 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
C07C 4/00 - Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
A renewable naphtha composition is disclosed. The renewable naphtha composition comprises about 0.1 wt % to about 15 wt % oxygen, and C4 to about C8 hydrocarbons comprising more than about 50 wt % cyclic hydrocarbons in the renewable naphtha composition. The renewable naphtha composition has a final boiling point of no more than about 420° F. The renewable naphtha composition can be used as a fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
21.
APPARATUS AND PROCESS FOR PRODUCING A SUPERHEATED STEAM
An apparatus and a process for producing a superheated steam is disclosed. The apparatus comprises a primary heater comprising a radiant section and a convection section. The primary heater comprises a convective heat transfer conduit in communication with a source of water and passing through the convection section to provide a steam stream. The apparatus further comprises a secondary heater. The secondary heater comprises a radiant section and a secondary heat transfer conduit in communication with the convective heat transfer conduit of the primary heater. The secondary heat transfer conduit passes through the radiant section of the secondary heater to provide a superheated steam stream. Further, a process for producing a superheated steam is disclosed.
F22G 3/00 - Steam superheaters characterised by constructional featuresDetails or component parts thereof
F22G 1/02 - Steam superheating characterised by heating method with heat supply by hot flue gases from the furnace of the steam boiler
F22G 1/16 - Steam superheating characterised by heating method by using a separate heat source independent from heat supply of the steam boiler, e.g. by electricity, by auxiliary combustion of fuel oil
22.
PROCESS OF PRODUCING A FUEL STREAM COMPRISING RENEWABLE CARBON
A process of producing a fuel stream comprising renewable carbon is disclosed. The process comprises producing an olefinic stream or an alcohol stream from a renewable feedstock. An aromatic stream and an alkylating agent comprising the olefinic stream or the alcohol stream is charged to an alkylation reactor to alkylate the aromatic stream with the alkylating agent to produce an alkylated aromatic product stream. The alkylated aromatic product stream comprises 0.1 wt% to 67 wt% renewable carbon.
C10G 69/12 - 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 polymerisation or alkylation step
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 pointSelective hydrocracking of normal paraffins
A process for dehydrating ethanol to ethylene. The steps include: (a) reacting an ethanol feed stream over a dehydration catalyst to produce ethylene in a dehydration product stream; (b) separating said dehydration product stream into a product liquid stream comprising water and dissolved oxygenates and a product vapor stream of ethylene; (c) taking a bypass stream from said product liquid stream; and, (d) sending the bypass stream to the dehydration reactor bypassing a wastewater stripping column.
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
C07C 7/11 - Purification, separation or stabilisation of hydrocarbonsUse of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
A process for controlling heat transfer in a hydrogenation process is provided. A hydrocarbon feed stream is hydrogenated in a hydrogenation reactor in the presence of hydrogen and a hydrogenation catalyst to produce a hydrogenated effluent. In an embodiment, the hydrogen is green hydrogen. A first feed stream is taken from the hydrogenated effluent and said first feed stream is sent to a steam generator to produce a steam stream. A pressure of the steam stream produced in the steam generator is adjusted to control the temperature of the first feed stream and the first feed stream is then charged to a second reactor.
A sustainable aviation fuel composition is disclosed. The sustainable aviation fuel composition comprises a T10 of more than about 110°C and a final boiling point of no more than about 300°C, about 5 to about 25 wt% aromatics, no more than about 15 wt% hydrogen, no more than about 1 wt% oxygen, and has a flash point of at least about 38°C. Further, a process of producing sustainable aviation fuel is disclosed. The sustainable aviation fuel can be used as fuel stream or a blend stock for blending with a fuel stream or both.
C10L 1/04 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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
26.
PROCESS AND APPARATUS FOR PRODUCING ULTRA PURE CO2 IN A CARBON CAPTURE PROCESS
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
F25J 3/02 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
27.
INTEGRATED FISCHER-TROPSCH AND LINEAR ALKYLBENZENE COMPLEX
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
A semi-permeable cover for a radial flow reactor that is located on top of a bed of catalyst in the reactor. The cover allows for a small portion of process gas to flow therethrough. The semi-permeable cover may be a self-deploying blank with a biasing element or have a spiral seam. The cover may be made from separate pieces. A shroud may be provided to cover an upper end of the center pipe in the reactor.
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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
29.
PROCESS FOR THE PRODUCTION OF A CO-MIXTURE OF PIPERAZINE AND METHYL-SUBSTITUTED PIPERAZINE
Catalytic processes to manufacture piperazine and 2-methyl piperazine simultaneously through co-feeding a linear alkanolamine, or a diol, or an ethyleneamine with an analog of the alkanolamine, or the diol, or the ethyleneamine in the presence of anhydrous ammonia to produce a reaction mixture comprising the piperazine and the methyl-substituted piperazine are described. The catalyst comprises a 10 membered ring zeolite.
C07D 295/023 - PreparationSeparationStabilisationUse of additives
B01J 29/40 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
C07D 241/04 - Heterocyclic compounds containing 1,4-diazine or hydrogenated 1,4-diazine rings not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
C07D 295/027 - Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements containing only one hetero ring
30.
CATALYTIC METHOD FOR SELECTIVE CYCLO-AMINATION OF ALKANOLAMINE AND DIOL TO PRODUCE ON-PURPOSE CYCLIC ETHYLENEAMINES OF PIPERAZINE AND DERIVATIVES
Catalytic processes to produce on purpose piperazine are described. The processes are based on the use of a 10-member ring zeolite, preferably with MFI topology, with tunned morphology and acidity to promote intermolecular or intramolecular cyclization of alkanolamines, ethyleneamines, or diols to cyclic piperazine. The unavoidable byproducts due to thermodynamics can be tuned to favor piperazine upon recycling. The processes can be used to manufacture piperazine which can be used as solvent for post-combustion CO2 capture.
B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups
C07D 295/027 - Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements containing only one hetero ring
Processes and apparatuses for reducing internal damage impairment to an equipment piece in a carbon capture unit after shutdown of the carbon capture unit with a purge gas. Once a shutdown of the carbon capture unit has been detected purge gas is used to displace process fluid within spaces of the equipment piece. The carbon capture unit may be a cryogenic carbon capture unit, a solvent carbon capture unit, a membrane carbon capture unit, a solid adsorbent carbon capture unit, or any combination thereof.
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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 53/30 - Controlling by gas-analysis apparatus
32.
MODIFIED ALUMINOBORATE HAVING INCREASED SURFACE AREA AND METHODS OF MAKING
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al :B in the range of 5 to 8. It has an XRD diffraction pattern different from the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 50°C to 100°C and a solid: liquid ratio of 1 :20 to 1; 100 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
B01J 21/10 - MagnesiumOxides or hydroxides thereof
B01J 23/16 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
222 enriched stream and an evacuation gas stream; and introducing the evacuation gas stream to rotating equipment to displace any particulates in low flow and small clearance areas in the rotating equipment.
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
A semi-permeable cover for a radial flow reactor that is located on top of a bed of catalyst in the reactor. The cover allows for a small portion of process gas to flow therethrough. The semi-permeable cover may be a self-deploying blank with a biasing element or have a spiral seam. The cover may be made from separate pieces. A shroud may be provided to cover an upper end of the center pipe in the reactor.
B01J 8/02 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds
B01J 8/00 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes
35.
PROCESS FOR THE PRODUCTION OF A CO-MIXTURE OF PIPERAZINE AND METHYL-SUBSTITUTED PIPERAZINE
Catalytic processes to manufacture piperazine and 2- methyl piperazine simultaneously through co-feeding a linear alkanolamine, or a diol, or an ethyleneamine with an analog of the alkanolamine, or the diol, or the ethyleneamine in the presence of anhydrous ammonia to produce a reaction mixture comprising the piperazine and the methyl-substituted piperazine are described. The catalyst comprises a 10 membered ring zeolite.
C07D 295/023 - PreparationSeparationStabilisationUse of additives
C07D 241/04 - Heterocyclic compounds containing 1,4-diazine or hydrogenated 1,4-diazine rings not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including fats, oils and greases (FOGs) to fuel, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
C10G 67/02 - 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
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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 hydrocarbonsHydrofinishing
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including, hydroprocessing, and naphtha to ethane and propane to ethylene and propylene, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
C10G 67/02 - 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
C10G 67/16 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural parallel stages only
C10G 73/02 - Recovery of petroleum waxes from hydrocarbon oilsDe-waxing of hydrocarbon oils
C10G 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 45/60 - 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 pointSelective hydrocracking of normal paraffins characterised by the catalyst used
Organic chlorides are removed from bio-oils, including vegetable oils and animal fats, that are to be coprocessed to meet sustainability goals. The organic chlorides are removed by using active materials such as silica-alumina containing adsorbents. The bio-oils that are targeted for treatment contain greater than 5 ppmw chlorides and are planned for more than 10% of the feedstream that is being processed.
xyzabb where M is a trivalent framework element, B is boron, O is oxygen, N is nitrogen and H is hydrogen, x is 3-8, y is 1-5, z is 16-25, a is 1 and b is 10-15. This composition is effective in removing per- and polyfluoroalkyl substances from water.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 1.5 to 2.5, and it has an XRD diffraction pattern substantially similar to the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 20° C. to 40° C. and a solid:liquid ratio of 1:20 to 1:100, or temperatures in the range of 50 to 100° C. and a solid:liquid ratio of 1:10 to 1:40 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 5 to 8. It has an XRD diffraction pattern different from the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 50° C. to 100° C. and a solid:liquid ratio of 1:20 to 1:100 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
Processes for displacing particulates from low flow and small clearance areas in rotating equipment associated with a carbon capture unit, the process comprising compressing, in a compressor, a flue gas stream to provide a compressed flue gas stream; processing, in a CO2 separation zone in a carbon capture unit, the compressed flue gas stream and providing a CO2 enriched stream and an evacuation gas stream; and introducing the evacuation gas stream to rotating equipment to displace any particulates in low flow and small clearance areas in the rotating equipment.
B08B 9/00 - Cleaning hollow articles by methods or apparatus specially adapted thereto
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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 vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
43.
PROCESSES AND APPARATUSES FOR REDUCING INTERNAL DAMAGE IMPAIRMENT TO AN EQUIPMENT PIECE IN A CARBON CAPTURE UNIT
Processes and apparatuses for reducing internal damage impairment to an equipment piece in a carbon capture unit after shutdown of the carbon capture unit with a purge gas. Once a shutdown of the carbon capture unit has been detected purge gas is used to displace process fluid within spaces of the equipment piece. The carbon capture unit may be a cryogenic carbon capture unit, a solvent carbon capture unit, a membrane carbon capture unit, a solid adsorbent carbon capture unit, or any combination thereof.
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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
44.
ENERGY EFFICIENT NON-FLAMMABLE REFRIGERATION FOR CO2-RICH PROCESS STREAMS
Processes for chilling CO2 rich streams are described. The processes combine the use of a refrigerant mixture comprising CO2 and a first refrigerant capable of depressing the freezing point of CO2 to less than or equal to −60° C. and a series of flash drums which reduce the temperature and pressure of the refrigerant mixture and concentrate the first refrigerant.
F25J 3/02 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
A process for dehydrating ethanol to ethylene. The steps include: (a) reacting an ethanol feed stream over a dehydration catalyst to produce ethylene in a dehydration product stream; (b) separating said dehydration product stream into a product liquid stream comprising water and dissolved oxygenates and a product vapor stream of ethylene; (c) taking a bypass stream from said product liquid stream; and, (d) sending the bypass stream to the dehydration reactor bypassing a wastewater stripping column.
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
46.
INTEGRATED FISCHER-TROPSCH AND LINEAR ALKYLBENZENE COMPLEX
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
Organic chlorides are removed from bio-oils, including vegetable oils and animal fats, that are to be coprocessed to meet sustainability goals. The organic chlorides are removed by using active materials such as silica-alumina containing adsorbents. The bio-oils that are targeted for treatment contain greater than 5 ppmw chlorides and are planned for more than 10% of the feedstream that is being processed.
B01J 20/28 - Solid sorbent compositions or filter aid compositionsSorbents for chromatographyProcesses for preparing, regenerating or reactivating thereof characterised by their form or physical properties
A process for producing light olefins is disclosed. The process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to produce a hydrocracked stream. A reforming charge stream is taken from the hydrocracked stream. The reforming charge stream is reformed over a reforming catalyst in a reforming reactor to convert naphthenes to aromatics and produce a reformed stream. The reformed stream is charged to an NEP reactor to convert the reformed stream over an NEP catalyst in the presence of NEP hydrogen to produce a light paraffinic stream. Ethylene and propylene can be produced from the light paraffinic stream.
A marine fuel oil composition is disclosed. The marine fuel oil composition comprises an acid number of less than about 2.5 mg KOH/g, a flash point temperature greater than about 140° F., and an oxygen concentration of at least about 2 wt %. Further, a process for producing marine fuel oil is disclosed.
Salt modified aluminoborates and processes of producing them are described. The salt modified aluminoborate has a weight ratio of Al:B in the range of 1.5 to 2.5, and it has an XRD diffraction pattern substantially similar to the XRD pattern of known aluminoborates. It can be produced using temperatures in the range of 20°C to 40°C and a solid: liquid ratio of 1:20 to 1:100, or temperatures in the range of 50 to 100 °C and a solid: liquid ratio of 1:10 to 1:40 will produce a salt modified aluminoborate with the properties described below. Calcining the salt modified aluminoborate produces different XRD diffraction patterns depending on the temperature used for the calcining.
2222 to less than or equal to -60°C and a series of flash drums which reduce the temperature and pressure of the refrigerant mixture and concentrate the first refrigerant.
F25J 1/00 - 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
F25B 1/10 - Compression machines, plants or systems with non-reversible cycle with multi-stage compression
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
53.
PROCESS FOR PRODUCING A SINGLE PHASE IMMERSION COOLING FLUID FROM FISCHER-TROPSCH OIL
Processes for converting Fischer-Tropsch products into a single-phase immersion cooling fluid and optionally aviation fuel are described. Processes for converting Fischer-Tropsch products to sustainable aviation fuel can be modified and tailored to co-produce an immersion cooling base oil which can be used to generate a fluid with the required properties for single-phase immersion cooling.
Processes for converting Fischer-Tropsch products into linear alkyl benzene (LAB) are described. By selecting a portion of the Fischer-Tropsch product stream, it can be fed to the alkylation reaction zone. Some pretreatment steps can be eliminated or reduced. Unreacted paraffins can be dehydrogenated and recycled to the alkylation reaction zone.
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 57/00 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
A marine fuel oil composition is disclosed. The marine fuel oil composition comprises an acid number of less than about 2.5 mg KOH/g, a flash point temperature greater than about 140°F, and an oxygen concentration of at least about 2 wt%. Further, a process for producing marine fuel oil is disclosed.
Processes for converting Fischer-Tropsch products into a single-phase immersion cooling fluid and optionally aviation fuel are described. Processes for converting Fischer-Tropsch products to sustainable aviation fuel can be modified and tailored to co-produce an immersion cooling base oil which can be used to generate a fluid with the required properties for single-phase immersion cooling.
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern, a depleted gas field or a saline aquifer to a pressure swing adsorption unit and then to a membrane unit to produce hydrogen having a purity of above 99.5 mol %.
Integrated processes for producing p-xylene from biomass are described. The biomass is converted to sugars which are converted to 5-hydroxymethylfurfural (HMF) which is converted to dimethylfuran (DMF). The biomass derived DMF is reacted with internally generated de-watered, unpurified ethylene to form the p-xylene. The de-watered, unpurified ethylene is also derived from sugars made from the biomass.
C07C 2/86 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
C07D 307/36 - Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, directly attached to ring carbon atoms
C07D 307/46 - Doubly bound oxygen atoms, or two oxygen atoms singly bound to the same carbon atom
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
C07C 1/24 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as hetero atoms by elimination of water
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including fats, oils and greases (FOGs) to fuel, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
Processes integrating product streams from Fischer-Tropsch processes with other hydrocarbon processes, including, hydroprocessing, and naphtha to ethane and propane to ethylene and propylene, are described. In some cases, the Fischer-Tropsch product stream is separated into two or more streams before being sent to the later process, while in other cases the entire Fischer-Tropsch product stream is sent to the subsequent process.
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
A high selectivity and high CO2 plasticization resistant polymer comprises a plurality of repeating units of formula (I) for gas separation applications. The polymer may be synthesized from a superacid catalyzed poly(hydroalkylation) reaction.
Membranes made from the polymer and gas separation processes using the membranes made from the polymer are also described.
C08G 61/12 - Macromolecular compounds containing atoms other than carbon in the main chain of the macromolecule
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
B01D 71/62 - Polycondensates having nitrogen-containing heterocyclic rings in the main chain
A process for converting plastics is disclosed. The process comprises pyrolyzing a plastic feed stream in a first pyrolysis reactor to produce a pyrolysis vapor stream. The pyrolysis vapor stream is pyrolyzed in a second pyrolysis reactor to produce a pyrolysis product stream. The first pyrolysis reactor may be operated at a higher temperature than the second pyrolysis reactor. The plastic feed stream may be separated from a mixed-plastic stream.
C08J 11/12 - Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
B29B 17/02 - Separating plastics from other materials
63.
PROCESS FOR CONVERTING OLEFINS TO DIESEL WITH BLENDING
We have formulated a process for oligomerizing an olefin stream to distillate fuel that meets appropriate distillate requirements. We have found that diesel produced by oligomerizing a charge olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream followed by saturation may have a viscosity that exceeds requirements. The process comprises blending jet fuel with diesel fuel to enable the diesel fuel to meet viscosity qualifications.
C10G 69/12 - 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 polymerisation or alkylation step
C10G 50/00 - Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
A process for recovery of hydrogen from underground storage is provided. The process involves sending a hydrogen stream stored in an underground cavern, a depleted gas field or a saline aquifer to a pressure swing adsorption unit and then to a membrane unit to produce hydrogen having a purity of above 99.5 mol%.
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
A process for producing light olefins is disclosed. The process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to produce a hydrocracked stream. A reforming charge stream is taken from the hydrocracked stream. The reforming charge stream is reformed over a reforming catalyst in a reforming reactor to convert naphthenes to aromatics and produce a reformed stream. The reformed stream is charged to an NEP reactor to convert the reformed stream over an NEP catalyst in the presence of NEP hydrogen to produce a light paraffinic stream. Ethylene and propylene can be produced from the light paraffinic stream.
C10G 69/08 - 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 reforming naphtha
66.
INTEGRATED BIO-REFINERY FOR BIO-P-XYLENE WITH INTERNAL BIO-ETHYLENE PRODUCTION
Integrated processes for producing p-xylene from biomass are described. The biomass is converted to sugars which are converted to 5-hydroxymethylfurfural (HMF) which is converted to dimethylfuran (DMF). The biomass derived DMF is reacted with internally generated de-watered, unpurified ethylene to form the p-xylene. The de-watered, unpurified ethylene is also derived from sugars made from the biomass.
C07C 2/86 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
Processes for converting Fischer-Tropsch products into synthetic paraffinic kerosene which can be used to make aviation. The process schemes provide the possibility of different degrees of isomerization of an unconverted oil recycle to maximize the distillate yields. Different process schemes can be employed depending on the type of Fischer-Tropsch feed, e.g., the distillate to wax ratio in the Fischer-Tropsch oil. The present invention provides routes to produce sustainable aviation fuel (SAF) from a Fischer-Tropsch complex with a lower level of isomerization leading to better SAF yields.
C10G 67/02 - 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
A process for converting plastics is disclosed. The process comprises pyrolyzing a plastic feed stream in a first pyrolysis reactor to produce a pyrolysis vapor stream. The pyrolysis vapor stream is pyrolyzed in a second pyrolysis reactor to produce a pyrolysis product stream. The first pyrolysis reactor may be operated at a higher temperature than the second pyrolysis reactor. The plastic feed stream may be separated from a mixed-plastic stream.
C10G 1/02 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
C10B 47/30 - Other processes in rotary ovens or retorts
C10B 53/07 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of synthetic polymeric materials, e.g. tyres
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
A process for producing monomers is disclosed. The process comprises hydrocracking a pyrolysis oil stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open rings present in said pyrolysis oil stream to produce a hydrocracked effluent stream. The hydrocracked effluent stream is fractionating in a fractionation column to provide a naphtha stream. The naphtha stream is contacted with a NEP catalyst and hydrogen to produce a light paraffinic stream or with a reforming catalyst to produce an aromatics stream.
C10G 69/04 - 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 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C07C 5/327 - Formation of non-aromatic carbon-to-carbon double bonds only
C07C 6/12 - Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
C07C 7/09 - Purification, separation or stabilisation of hydrocarbonsUse of additives by fractional condensation
We have formulated a process for oligomerizing an olefin stream to distillate fuel that meets appropriate distillate requirements. We have found that diesel produced by oligomerizing a charge olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream followed by saturation may have a viscosity that exceeds requirements. The process comprises blending jet fuel with diesel fuel to enable the diesel fuel to meet viscosity qualifications.
Processes for converting Fischer-Tropsch products into synthetic paraffinic kerosene which can be used to make aviation. The process schemes provide the possibility of different degrees of isomerization of an unconverted oil recycle to maximize the distillate yields. Different process schemes can be employed depending on the type of Fischer-Tropsch feed, e.g., the distillate to wax ratio in the Fischer-Tropsch oil. The present invention provides routes to produce sustainable aviation fuel (SAF) from a Fischer-Tropsch complex with a lower level of isomerization leading to better SAF yields.
C10G 67/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
C10G 73/02 - Recovery of petroleum waxes from hydrocarbon oilsDe-waxing of hydrocarbon oils
C10G 45/60 - 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 pointSelective hydrocracking of normal paraffins characterised by the catalyst used
C10G 47/02 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used
A process for producing monomers is disclosed. The process comprises hydrocracking a pyrolysis oil stream in a hydrocracking reactor over a hydrocracking catalyst in the presence of a hydrocracking hydrogen stream at hydrocracking conditions to open rings present in said pyrolysis oil stream to produce a hydrocracked effluent stream. The hydrocracked effluent stream is fractionating in a fractionation column to provide a naphtha stream. The naphtha stream is contacted with a NEP catalyst and hydrogen to produce a light paraffinic stream or with a reforming catalyst to produce an aromatics stream.
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
C07C 7/10 - Purification, separation or stabilisation of hydrocarbonsUse of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
C07C 51/16 - Preparation of carboxylic acids or their salts, halides, or anhydrides by oxidation
C07C 67/39 - Preparation of carboxylic acid esters by oxidation of groups which are precursors for the acid moiety of the ester
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
A process for upgrading a bio-oil stream is disclosed. The process comprises discharging spent hydrotreating catalyst fines from a hydrotreating reactor. The hydrotreating catalyst fines comprise a metal from Group IVB, Group VB, Group VIB, Group VIIB, and Group VIII metals on an inorganic support. A bio-oil stream is reacted with hydrogen in the presence of the spent hydrotreating catalyst fines in a bio-oil reactor to produce an upgraded bio-oil stream. The spent hydrotreating catalyst fines can be characterized by a D90 particles size of 1000 microns.
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
76.
PROCESSES AND APPARATUSES FOR TREATING NOX SEPARATED FROM CARBON DIOXIDE
Processes and apparatuses for treating NOx from a carbon dioxide stream. Prior to separating carbon dioxide and NOx, NOx is converted to nitrogen gas in an NOx conversion zone, which may include an SCR reactor and/or CO boiler. A carbon separation zone which may include one or more fractionation columns produces a CO2 stream and an NOx stream. The NOx is passed back to the NOx conversion zone.
A process for upgrading a bio-oil stream is disclosed. The process comprises discharging spent hydrotreating catalyst fines from a hydrotreating reactor. The hydrotreating catalyst fines comprise a metal from Group IVB, Group VB, Group VIB, Group VIIB, and Group VIII metals on an inorganic support. A bio-oil stream is reacted with hydrogen in the presence of the spent hydrotreating catalyst fines in a bio-oil reactor to produce an upgraded bio-oil stream. The spent hydrotreating catalyst fines can be characterized by a D90 particles size of about 1000 microns.
C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
78.
METHODS AND SYSTEM FOR PRODUCING CO2 ENRICHED STREAMS FROM AIR STREAMS
Processes and systems for providing a CO2 enriched stream from an air stream, by: selectively adsorbing, in a first separation zone, CO2 and H2O in an air stream and providing a CO2 and H2O depleted gas stream; separating, in a second separation zone, the CO2 and H2O depleted gas stream and providing an N2 enriched stream, an O2 enriched stream, and an N2 enriched regeneration stream; heating the N2 enriched regeneration stream to provide a heated N2 enriched regeneration stream; selectively desorbing, in the first separation zone, the CO2 and H2O using the heated N2 enriched regeneration stream and providing a spent regeneration gas stream; drying the spent regeneration gas stream to remove H2O and providing a dried spent regeneration gas stream; and separating, in a third separation zone, the CO2 from the dried spent regeneration gas stream to provide a CO2 enriched stream.
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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
A method for monitoring and analyzing the operation of a battery energy storage system (BESS) comprises, entering data parameters from one or more subsystems of a field installed BESS into a correlation matrix and extracting target correlations from the correlation matrix. The target correlations along with independent data parameters are entered into a relational coefficient matrix to identify data features. The method further includes extracting the data features from the relational coefficient matrix to a generative and adversarial artificial intelligence network model, where the extracted data features are used to train the model with data from the field installed BESS solution.
1211' followed by a nucleophilic substitution reaction or a grafting reaction, and optionally an acidification reaction. Formula (I). Proton-exchange membranes and membrane electrode assemblies made from the polymer are also described.
C25B 13/08 - DiaphragmsSpacing elements characterised by the material based on organic materials
C25B 1/04 - Hydrogen or oxygen by electrolysis of water
H01M 8/103 - Polymeric electrolyte materials characterised by the chemical structure of the main chain of the ion-conducting polymer having nitrogen, e.g. sulfonated polybenzimidazoles [S-PBI], polybenzimidazoles with phosphoric acid, sulfonated polyamides [S-PA] or sulfonated polyphosphazenes [S-PPh]
H01M 8/1004 - Fuel cells with solid electrolytes characterised by membrane-electrode assemblies [MEA]
A proton-conducting polymer comprises a plurality of repeating units of formula (I) for electrochemical reactions. The polymer may be synthesized from a super acid catalyzed polyhydroxyalkylation reaction of monomers Ar1′, Ar2′, and X1′ followed by a nucleophilic substitution reaction or a grafting reaction, and optionally an acidification reaction.
A proton-conducting polymer comprises a plurality of repeating units of formula (I) for electrochemical reactions. The polymer may be synthesized from a super acid catalyzed polyhydroxyalkylation reaction of monomers Ar1′, Ar2′, and X1′ followed by a nucleophilic substitution reaction or a grafting reaction, and optionally an acidification reaction.
A proton-conducting polymer comprises a plurality of repeating units of formula (I) for electrochemical reactions. The polymer may be synthesized from a super acid catalyzed polyhydroxyalkylation reaction of monomers Ar1′, Ar2′, and X1′ followed by a nucleophilic substitution reaction or a grafting reaction, and optionally an acidification reaction.
Proton-exchange membranes and membrane electrode assemblies made from the polymer are also described.
C25B 9/23 - Cells comprising dimensionally-stable non-movable electrodesAssemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
C25B 13/08 - DiaphragmsSpacing elements characterised by the material based on organic materials
H01M 8/1004 - Fuel cells with solid electrolytes characterised by membrane-electrode assemblies [MEA]
82.
SPENT CAUSTIC TREATMENT USING AN ELECTROCHEMICAL ROUTE
Processes for treating spent caustic in a hydrocarbon process utilizing HCl are described. The processes include sending the spent caustic to a caustic scrubbing system. HCl rich off gases are routed to the scrubbing system. This process is designed to deplete the NaOH in the spent caustic and form a brine solution. The brine is sent to an electrochemical cell to convert the NaCl to NaOH while generating chlorine and hydrogen gas. The NaOH generated from the electrochemical reaction is recycled back to the caustic scrubber, while the chlorine and hydrogen gas are combined and recycled back to the reaction zone.
A process for hydroprocessing a sustainable feedstock is disclosed. The process comprises contacting a feed stream with a selective saturation catalyst to saturate olefins to provide a selectively saturated stream. The selective saturation catalyst may comprise a metal on an alumina support. The selectively saturated stream is hydrodeoxygenated over a hydrodeoxygenation catalyst to produce a hydrodeoxygenated stream. The hydrodeoxygenation catalyst has a smaller mean pore diameter than the selective saturation catalyst.
C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
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 pointSelective hydrocracking of normal paraffins
C10G 69/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
84.
SPENT CAUSTIC TREATMENT USING AN ELECTROCHEMICAL ROUTE
Processes for treating spent caustic in a hydrocarbon process utilizing HCI are described. The processes include sending the spent caustic to a caustic scrubbing system. HCI rich off gases are routed to the scrubbing system. This process is designed to deplete the NaOH in the spent caustic and form a brine solution. The brine is sent to an electrochemical cell to convert the NaCI to NaOH while generating chlorine and hydrogen gas. The NaOH generated from the electrochemical reaction is recycled back to the caustic scrubber, while the chlorine and hydrogen gas are combined and recycled back to the reaction zone.
2233 molar ratio of 2.0-2.15, and a crystal size in the range of 4-6 μm and of 400-600 nm. The present disclosure also provides a method for preparing said low-silica-alumina-ratio X-type zeolite molecular sieve and the use thereof. The method of the present disclosure employs readily available raw materials and features simple steps, and the prepared zeolite molecular sieve exhibits excellent adsorption performance.
A process for hydroprocessing a sustainable feedstock is disclosed. The process comprises contacting a feed stream with a selective saturation catalyst to saturate olefins to provide a selectively saturated stream. The selective saturation catalyst may comprise a metal on an alumina support. The selectively saturated stream is hydrodeoxygenated over a hydrodeoxygenation catalyst to produce a hydrodeoxygenated stream. The hydrodeoxygenation catalyst has a smaller mean pore diameter than the selective saturation catalyst.
A low cost, sandwich-structured thin film composite (TFC) anion exchange membrane for redox flow batteries, fuel cells, electrolysis, and other electrochemical reaction applications is described. The sandwich-structured TFC anion exchange membrane comprises a microporous substrate membrane, a first hydrophilic ionomeric polymer coating layer on the surface of the microporous substrate layer, a cross-linked protonated polyamine anion exchange polymer coating layer on top of the first hydrophilic ionomeric polymer coating layer, and a second hydrophilic ionomeric polymer protective layer on top of the cross-linked protonated polyamine anion exchange polymer coating layer. Methods of making the TFC anion exchange membrane comprises a microporous substrate membrane and redox flow battery system incorporating the TFC anion exchange membrane comprises a microporous substrate membrane are also described.
Processes for recovery of carbon dioxide from a gas stream are described. The processes reduce dehydration cost in CO2 capture systems and minimize the formation of COS and H2O and enable water removal with an enhanced solvent-based absorbent operating at a lower temperature. This allows low residual water levels to be achieved in the dried gas. Also, feed streams containing high levels of CO2 and H2S can be treated in an integrated system comprising a cryogenic CO2 fractionation system, an overhead pressure swing adsorption (PSA) unit, and a CO2 temperature swing adsorption (TSA) unit. The processes allow recovery of helium and methane as well as CO2 and H2S.
F25J 3/06 - Processes or apparatus for separating the constituents of gaseous mixtures involving the use of liquefaction or solidification by partial condensation
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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 vapoursRecovering vapours of volatile solvents from gasesChemical 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 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
C10L 3/10 - Working-up natural gas or synthetic natural gas
89.
METHOD FOR PRODUCING HYDROISOMERIZED AND/OR HYDROCRACKED HYDROCARBONS WITH HIERARCHICAL ZEOLITIC MATERIALS
Methods for converting hydrocarbonaceous feedstocks to value added products via a hydroisomerization/hydrocracking catalyst that contains at least two or more zeolitic materials comprising hierarchical porosity, each material having a mesostructure between 2-50 nm are described. Specifically, the improved acid function in these catalysts is obtained by mesoporizing a first zeolite and blending the mesoporized first zeolite with an as-synthesized mesoporous second zeolite; or mesoporizing a first zeolite; mesoporizing a second zeolite, and blending the mesoporized first zeolite with the mesoporized second zeolite; or blending a first zeolite and a second zeolite; and mesoporizing the blend of the first zeolite and the second zeolite; wherein the first zeolite comprises Y zeolite, and the second zeolite comprises a one-dimensional, 10-ring zeolite.
C10G 49/08 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
B01D 53/00 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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
91.
METHOD FOR PRODUCING HYDROISOMERIZED AND/OR HYDROCRACKED HYDROCARBONS WITH HIERARCHICAL ZEOLITIC MATERIALS
Methods for converting hydrocarbonaceous feedstocks to value added products via a hydroisomerization/hydrocracking catalyst that contains at least two or more zeolitic materials comprising hierarchical porosity, each material having a mesostructure between 2-50 nm are described. Specifically, the improved acid function in these catalysts is obtained by mesoporizing a first zeolite and blending the mesoporized first zeolite with an as-synthesized mesoporous second zeolite; or mesoporizing a first zeolite; mesoporizing a second zeolite, and blending the mesoporized first zeolite with the mesoporized second zeolite; or blending a first zeolite and a second zeolite; and mesoporizing the blend of the first zeolite and the second zeolite; wherein the first zeolite comprises Y zeolite, and the second zeolite comprises a one-dimensional, 10-ring zeolite.
C10G 45/64 - 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 pointSelective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
92.
PROCESSES AND APPARATUSES FOR PROVIDING A HYDROGEN STREAM
Processes and apparatuses for producing a hydrogen stream by: producing an effluent stream in a reaction zone comprising a reactor, the effluent stream comprising hydrogen and oxygen; selectively adsorbing oxygen from the effluent stream in a separation zone, the separation zone comprising a plurality of vessels containing an adsorbent configured to selectively adsorb oxygen and provide a purified hydrogen stream; and regenerating spent adsorbent in a vessel from the plurality of vessels of the separation zone with at least a portion of the purified hydrogen stream to desorb oxygen as water.
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
B01D 53/04 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical 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
93.
PROCESS FOR OPTIMUM HYDROGEN RECOVERY DOWNSTREAM OF A SOLVENT-BASED CO2 REMOVAL UNIT
22 removal units having decreased carbon emissions in the fuel gas and reduced buildup of inert gases are described. The processes incorporate a hydrogen pressure swing adsorption (PSA) unit and a second separation unit, which can be a membrane separation unit, or a PSA unit. The membrane separation unit can be combined with a second PSA unit.
C01B 3/34 - 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
C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
94.
PROCESSES AND APPARATUSES FOR CONTROLLING A TEMPERATURE OF A REACTOR
Processes and apparatuses for controlling a temperature of a reactor. Oxygen and hydrogen are reacted in a reactor which contains a catalyst configured to catalyze a reaction between oxygen and hydrogen and produce an effluent comprising water. Water is removed from the effluent in a separation zone having a plurality of vessels containing an adsorbent configured to adsorb water and provide a purified product stream, the purified product stream comprises oxygen or hydrogen. An exotherm of the reactor is controlled by recycling a recycled stream which comprises a portion of the effluent stream or a portion of the purified product stream.
Processes and apparatuses for controlling a temperature of a reactor. Oxygen and hydrogen are reacted in a reactor which contains a catalyst configured to catalyze a reaction between oxygen and hydrogen and produce an effluent comprising water. Water is removed from the effluent in a separation zone having a plurality of vessels containing an adsorbent configured to adsorb water and provide a purified product stream, the purified product stream comprises oxygen or hydrogen. An exotherm of the reactor is controlled by recycling a recycled stream which comprises a portion of the effluent stream or a portion of the purified product stream.
B01J 8/04 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
Processes and apparatuses for producing a hydrogen stream by: producing an effluent stream in a reaction zone comprising a reactor, the effluent stream comprising hydrogen and oxygen; selectively adsorbing oxygen from the effluent stream in a separation zone, the separation zone comprising a plurality of vessels containing an adsorbent configured to selectively adsorb oxygen and provide a purified hydrogen stream; and regenerating spent adsorbent in a vessel from the plurality of vessels of the separation zone with at least a portion of the purified hydrogen stream to desorb oxygen as water.
B01D 53/02 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by adsorption, e.g. preparative gas chromatography
C25B 15/08 - Supplying or removing reactants or electrolytesRegeneration of electrolytes
97.
PROCESS FOR OPTIMUM HYDROGEN RECOVERY DOWNSTREAM OF A SOLVENT-BASED CO2 REMOVAL UNIT
Hydrogen production processes with solvent-based CO2 removal units having decreased carbon emissions in the fuel gas and reduced buildup of inert gases are described. The processes incorporate a hydrogen pressure swing adsorption (PSA) unit and a second separation unit, which can be a membrane separation unit, or a PSA unit. The membrane separation unit can be combined with a second PSA unit.
B01D 53/14 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by absorption
B01D 53/22 - Separation of gases or vapoursRecovering vapours of volatile solvents from gasesChemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases or aerosols by diffusion
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 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
C01B 3/56 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solidsRegeneration of used solids
