A heat exchanger includes a shell with a longitudinal axis and helical baffles inside the shell and arranged along the longitudinal axis in an alternating pattern of a first baffle followed by a second baffle of the helical baffles. Each helical baffle includes first holes and second holes that receive tubes. The second holes have a diameter larger than the first holes or there is a clearance between the second holes and the tubes that is greater than a clearance between the first holes and the tubes to intentionally induce an increase in a leakage stream in the spaces between the second holes and the tubes. Such increase in the leakage stream maintains a relatively constant rate of heat transfer while reducing pressure drop, thereby resulting in an improved heat transfer to pressure drop ratio for the heat exchanger.
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 9/00 - CasingsHeader boxesAuxiliary supports for elementsAuxiliary members within casings
A heat exchanger includes a shell with a longitudinal axis and helical baffles inside the shell and arranged along the longitudinal axis in an alternating pattern of a first baffle followed by a second baffle of the helical baffles. Each helical baffle includes first holes and second holes that receive tubes. The second holes have a diameter larger than the first holes or there is a clearance between the second holes and the tubes that is greater than a clearance between the first holes and the tubes to intentionally induce an increase in a leakage stream in the spaces between the second holes and the tubes. Such increase in the leakage stream maintains a relatively constant rate of heat transfer while reducing pressure drop, thereby resulting in an improved heat transfer to pressure drop ratio for the heat exchanger.
F28F 1/36 - 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 obliquely the means being helically-wound fins or wire spirals
3.
FCC PRODUCT VAPOUR SEPARATION METHOD FOR IMPROVED PRODUCT RECOVERY
Systems and processes for separating a mixture of cracked hydrocarbons. A main fractionator separates the mixture of cracked hydrocarbons into an overheads comprising C1 to C6+ hydrocarbons, a side draw, and a bottoms. An overheads condensation and high- pressure separation system partially condenses the overheads and compresses the uncondensed vapor to produce a compressed gas fraction and a compressed liquids fraction. A first distillation column receives the compressed liquids fraction and separates the compressed liquids fraction into a first overheads vapor and a first bottoms. A second distillation column separates the first bottoms into a second overheads and a second bottoms. An absorber receives and contacts in countercurrent flow a portion of the second bottoms fraction and the side draw liquid fraction with the compressed gas fraction, producing an absorber overheads fraction comprising offgas and an absorber bottoms fraction. Such systems are useful in integrating existing FCC/RFCC units with petrochemical complexes.
Systems and processes for separating a mixture of cracked hydrocarbons. A main fractionator separates the mixture of cracked hydrocarbons into an overheads comprising C1 to C6+ hydrocarbons, a side draw, and a bottoms. An overheads condensation and high-pressure separation system partially condenses the overheads and compresses the uncondensed vapor to produce a compressed gas fraction and a compressed liquids fraction. A first distillation column receives the compressed liquids fraction and separates the compressed liquids fraction into a first overheads vapor and a first bottoms. A second distillation column separates the first bottoms into a second overheads and a second bottoms. An absorber receives and contacts in countercurrent flow a portion of the second bottoms fraction and the side draw liquid fraction with the compressed gas fraction, producing an absorber overheads fraction comprising offgas and an absorber bottoms fraction. Such systems are useful in integrating existing FCC/RFCC units with petrochemical complexes.
Systems and processes herein integrate a crude separation unit, a steam cracker unit, a hydrocracker unit, an aromatics processing unit, and a pyrolysis gasoline hydrogenation unit for separating a whole crude oil or other wide boiling hydrocarbon mixtures for producing olefins and aromatics.
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
6.
INTEGRATED PROCESS SOLUTION FOR MAXIMIZING CRUDE TO LIGHT OLEFINS AND CHEMICALS
Systems and processes herein integrate a crude separation unit, a steam cracker unit, a hydrocracker unit, an aromatics processing unit, and a pyrolysis gasoline hydrogenation unit for separating a whole crude oil or other wide boiling hydrocarbon mixtures for producing olefins and aromatics.
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 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 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 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
Methods of and systems for treating the sludge solids of a wastewater stream are provided. The wastewater treatment includes a wet air oxidation (WAO) treatment upstream from an anaerobic sludge digestion. The disclosed methods and systems provide a reduction in the amount of sludge solids requiring disposal, in favor of an increase in the amount of fuel gas produced by the treatment system.
An induction heating system and method includes a work piece that may be a multi-layer pipe. The multi-layer pipe includes an inner layer for conveying effluent and an outer layer surrounding at least a portion of the inner layer. The outer layer has a higher Curie temperature than the inner layer such that the outer layer remains magnetic at or above a reaction temperature of the effluent to maximize hysteresis losses in the pipe up to and beyond the reaction temperature of the effluent. The inner layer may have desirable mechanical, thermal, and chemical properties such that the combination of the outer layer and the inner layer results in a multi-layer pipe that is efficient for induction heating up to and beyond the reaction temperature, while also being mechanically and thermally suitable for hydrocarbon processing applications.
Methods of and systems for treating the sludge solids of a wastewater stream are provided. The wastewater treatment includes a wet air oxidation (WAO) treatment upstream from an anaerobic sludge digestion. The disclosed methods and systems provide a reduction in the amount of sludge solids requiring disposal, in favor of an increase in the amount of fuel gas produced by the treatment system.
An induction heating system and method includes a work piece that may be a multi-layer pipe. The multi-layer pipe includes an inner layer for conveying effluent and an outer layer surrounding at least a portion of the inner layer. The outer layer has a higher Curie temperature than the inner layer such that the outer layer remains magnetic at or above a reaction temperature of the effluent to maximize hysteresis losses in the pipe up to and beyond the reaction temperature of the effluent. The inner layer may have desirable mechanical, thermal, and chemical properties such that the combination of the outer layer and the inner layer results in a multi-layer pipe that is efficient for induction heating up to and beyond the reaction temperature, while also being mechanically and thermally suitable for hydrocarbon processing applications.
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
B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
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
C07C 5/03 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
C07C 6/06 - Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond at a cyclic carbon-to-carbon double bond
C07C 7/00 - Purification, separation or stabilisation of hydrocarbonsUse of additives
C07C 7/09 - Purification, separation or stabilisation of hydrocarbonsUse of additives by fractional condensation
12.
INTEGRATED MIXED PLASTIC PYROLYSIS WITH HEAVY OIL PRODUCT THERMAL CRACKING
Systems and processes for converting waste plastics and other waste materials to useful end products. The systems integrate a plastics pyrolysis reactor and a liquid phase thermal cracking reactor to advantageously process the waste plastics to form various hydrocarbon products.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 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
The present disclosure relates generally to processes and systems for dehydrogenating alkanes. The present disclosure relates specifically to processes and systems for dehydrogenating alkanes in which catalyst beds can be cooled rapidly to prevent runaway.
The present disclosure relates generally to processes and systems for dehydrogenating alkanes. The present disclosure relates specifically to processes and systems for dehydrogenating alkanes in which catalyst beds can be cooled rapidly to prevent runaway. In one aspect, a dehydrogenation process includes, when the temperature of at least one of the hybrid catalyst beds becomes higher than a first threshold value during a number of consecutive cycles greater than a second threshold value, reducing the temperature of the oxygen-containing stream by at least 50° C., the reduction of temperature occurring with a temperature drop of at least 50° C. within three minutes.
C07C 5/32 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
15.
CONVERTING SUPER LIGHT CRUDES, EXTRA LIGHT CRUDES, AND CONDENSATES TO CHEMICALS
Processes and systems for converting a wide boiling hydrocarbon mixture to chemicals herein heating a hydrocarbon feedstock to form a heated hydrocarbon feedstock. The heated hydrocarbon feedstock is separated to recover a vaporized light portion and a remaining liquid portion. The vaporized light portion is superheated and thermally cracked to recover a first cracked effluent, and the remaining liquid portion is heated and stripped to recover a stripped vapor mixture and a residue liquid portion. The stripped vapor mixture is separated to recover a vapor comprising the stripping medium and a stream comprising volatilized hydrocarbons. The volatilized hydrocarbons are heated and mixed with hydrogen then hydroprocessed to form crackable heavy hydrocarbons. The hydroprocessed effluent is separated to recover a hydroprocessed liquid stream comprising crackable heavy hydrocarbons and a hydroprocessed vapor stream comprising unreacted hydrogen. The hydroprocessed liquid stream is superheated and thermally cracked to recover a second cracked effluent.
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
Processes and systems for converting a wide boiling hydrocarbon mixture to chemicals herein heating a hydrocarbon feedstock to form a heated hydrocarbon feedstock. The heated hydrocarbon feedstock is separated to recover a vaporized light portion and a remaining liquid portion. The vaporized light portion is superheated and thermally cracked to recover a first cracked effluent, and the remaining liquid portion is heated and stripped to recover a stripped vapor mixture and a residue liquid portion. The stripped vapor mixture is separated to recover a vapor comprising the stripping medium and a stream comprising volatilized hydrocarbons. The volatilized hydrocarbons are heated and mixed with hydrogen then hydroprocessed to form crackable heavy hydrocarbons. The hydroprocessed effluent is separated to recover a hydroprocessed liquid stream comprising crackable heavy hydrocarbons and a hydroprocessed vapor stream comprising unreacted hydrogen. The hydroprocessed liquid stream is superheated and thermally cracked to recover a second cracked effluent.
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
There are disclosed processes and systems wet air oxidation systems and processes which provide for the combined treatment of a spent caustic with a spent material (e.g., spent carbon, spent biological material, or combinations thereof) to produce a regenerated spent material stream.
Methods and systems for producing high purity methanol and isobutene from crude MTBE feed using multiple divided wall columns are provided. The methods can include purifying the MTBE, dissociating the MTBE to produce isobutene and methanol, purifying the isobutene and recovering/purifying methanol.
C07C 1/22 - 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 reduction
B01D 11/04 - Solvent extraction of solutions which are liquid
C07C 1/20 - 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
C07C 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
C07C 7/08 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation with the aid of auxiliary compounds by extractive distillation
C07C 29/10 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes
C07C 29/58 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by elimination of halogen, e.g. by hydrogenolysis, splitting-off
C07C 29/80 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation
C07C 29/84 - SeparationPurificationStabilisationUse of additives by physical treatment by distillation by extractive distillation
C07C 41/06 - Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
C07C 41/42 - SeparationPurificationStabilisationUse of additives by change of physical state, e.g. by crystallisation by distillation
19.
THERMAL CRACKING OF CRUDES TO CHEMICALS WITH HEAT TRANSFER FLUIDS
Processes and systems for producing olefins from a crude oil include a steam cracking furnace having a radiant heating section and a convective heating section. One or more heating coils are disposed in the convective heating section for heating a heat transfer fluid. A first heat exchanger heats the crude oil with the heated heat transfer fluid, and the heated crude oil is desalted to form a desalted crude. A second heat exchanger heats the desalted crude with the heated heat transfer fluid to form a preheated desalted crude, which is separated in a first separator to recover a hydrocarbon vapor fraction and a hydrocarbon liquid fraction. A heating coil in the convective section superheats the hydrocarbon vapor fraction and a radiant heating coil in the radiant heating section thermally cracks the superheated vapor fraction to recover a first cracked effluent comprising olefins.
C10G 9/40 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by indirect contact with preheated fluid other than hot combustion gases
20.
THERMAL CRACKING OF CRUDES TO CHEMICALS WITH HEAT TRANSFER FLUIDS
Processes and systems for producing olefins from a crude oil include a steam cracking furnace having a radiant heating section and a convective heating section. One or more heating coils are disposed in the convective heating section for heating a heat transfer fluid. A first heat exchanger heats the crude oil with the heated heat transfer fluid, and the heated crude oil is desalted to form a desalted crude. A second heat exchanger heats the desalted crude with the heated heat transfer fluid to form a preheated desalted crude, which is separated in a first separator to recover a hydrocarbon vapor fraction and a hydrocarbon liquid fraction. A heating coil in the convective section superheats the hydrocarbon vapor fraction and a radiant heating coil in the radiant heating section thermally cracks the superheated vapor fraction to recover a first cracked effluent comprising olefins.
C10G 9/40 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by indirect contact with preheated fluid other than hot combustion gases
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
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
21.
OXIDATIVE COUPLING OF METHANE FOR OLEFIN PRODUCTION
The present disclosure provides natural gas and petrochemical processing systems, including oxidative coupling of methane reactor systems that may integrate process inputs and outputs to cooperatively utilize different inputs and outputs in the production of higher hydrocarbons from natural gas and other hydrocarbon feedstocks. The present disclosure also provides apparatuses and methods for heat exchange, such as an apparatus that can perform boiling and steam super-heating in separate chambers in order to reach a target outlet temperature that is relatively constant as the apparatus becomes fouled. A system of the present disclosure may include an oxidative coupling of methane (OCM) subsystem that generates a product stream comprising compounds with two or more carbon atoms, and a dual compartment heat exchanger downstream of, and fluidically coupled to, the OCM subsystem.
C07C 2/84 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
C07C 6/04 - Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond
Systems and processes for the efficient conversion of high concentration isoolefin streams to tertiary alkyl ethers are disclosed. The systems and processes may include a feed system to advantageously divide the high concentration isoolefin feed to multiple fixed bed reactors and a catalytic distillation reactor to control the reaction exotherm and achieve a high isoolefin conversion.
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
C10G 47/10 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
A system includes a discharge subsystem with at least one expander stage operable to expand and heat a high-pressure CO2 stream from an existing CO2 pipeline to generate power and output a low-pressure CO2 stream to a storage media. A charge subsystem includes at least one compression stage operable to compress and cool the low-pressure CO2 stream from the storage media and provide a recycle high-pressure CO2 stream to the existing CO2 pipeline. A thermal integration subsystem is in fluid communication with the at least one expander stage and at least one compression stage to provide heating duty and cooling duty for the heating and cooling operations, respectively. The system relies on the existing CO2 pipeline for storage of high-pressure CO2 to provide the benefits described in the disclosure. Related methods are also contemplated.
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
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 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 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 45/02 - 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
26.
PROCESS FOR HEAVY, WHOLE CRUDE CONVERSION TO VALUABLE CHEMICALS THROUGH INTEGRATED CRUDE CONDITIONING AND STEAM CRACKING
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a solvent deasphalting unit, or an ebullated bed hydrocracking unit. Products from the upgrading operations may be used as feed to a steam cracker.
C10G 67/04 - 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 solvent extraction as the refining step in the absence of hydrogen
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
C10G 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
27.
DEEP SATURATION CATALYSTS AND PROCESS FOR HYDROTREATING WHOLE CRUDES
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
C10G 67/04 - 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 solvent extraction as the refining step 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 9/36 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
C10G 45/02 - 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
28.
INTEGRATED FIXED BED HYDROPROCESSING, DELAYED COKING, AND PYROLYSIS PROCESS TO PRODUCE CHEMICALS AND PETROLEUM COKE
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
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 65/10 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking 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
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, 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
29.
PROCESS FOR HEAVY, WHOLE CRUDE CONVERSION TO VALUABLE CHEMICALS THROUGH INTEGRATED CRUDE CONDITIONING AND STEAM CRACKING
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a solvent deasphalting unit, or an ebullated bed hydrocracking unit. Products from the upgrading operations may be used as feed to a steam cracker.
C10G 67/04 - 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 solvent extraction as the refining step in the absence of hydrogen
A process for converting whole crudes and other heavy hydrocarbon streams to produce ethylene. The process includes feeding a hydroprocessed medium boiling fraction, a hydroprocessed residue fraction, or both, and a light boiling fraction to a steam cracker and recovering a light fraction. The light fraction is fed to a first separator and recovering a C1-C3 stream and a mixed C4 and C4+ stream, comprising isoolefins, olefins, and dienes and feeding the mixed C4 and C4+ stream to a second separator and recovering a mixed C4 stream comprising isoolefins, olefins, and a C4+ stream. A portion of the mixed C4 stream is dimerized in a dimerization unit to produce a dimerized product stream, hydrogenated in a total hydrogenation system, producing a hydrogenated dimer product stream, and cracking the hydrogenated dimer product stream in a thermal cracking reactor system, producing one or more of hydrogen, methane, ethylene, propylene, n-butenes, and isobutene.
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
31.
INTEGRATED FIXED BED HYDROPROCESSING, DELAYED COKING AND PYROLYSIS PROCESS TO PRODUCE CHEMICALS AND PETROLEUM COKE
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
C10G 47/26 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
C10G 70/04 - Working-up undefined normally gaseous mixtures obtained by processes covered by groups , , , , by physical processes
32.
PROCESS FOR WHOLE CRUDE OIL CONVERSION TO CHEMICALS THROUGH CRUDE CONDITIONING AND STEAM CRACKING TO MAXIMIZE PETROCHEMICALS YIELD
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
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 1/06 - 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
A process for converting whole crudes and other heavy hydrocarbon streams to produce ethylene. The process includes feeding a hydroprocessed medium boiling fraction, a hydroprocessed residue fraction, or both, and a light boiling fraction to a steam cracker and recovering a light fraction. The light fraction is fed to a first separator and recovering a C1-C3 stream and a mixed C4 and C4+ stream, comprising isoolefins, olefins, and dienes and feeding the mixed C4 and C4+ stream to a second separator and recovering a mixed C4 stream comprising isoolefins, olefins, and a C4+ stream. A portion of the mixed C4 stream is dimerized in a dimerization unit to produce a dimerized product stream, hydrogenated in a total hydrogenation system, producing a hydrogenated dimer product stream, and cracking the hydrogenated dimer product stream in a thermal cracking reactor system, producing one or more of hydrogen, methane, ethylene, propylene, n-butenes, and isobutene.
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 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
C07C 2/06 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
C07C 5/02 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
A system includes a discharge subsystem with at least one expander stage operable to expand and heat a high-pressure CO2 stream from an existing CO2 pipeline to generate power and output a low-pressure CO2 stream to a storage media. A charge subsystem includes at least one compression stage operable to compress and cool the low-pressure CO2 stream from the storage media and provide a recycle high-pressure CO2 stream to the existing CO2 pipeline. A thermal integration subsystem is in fluid communication with the at least one expander stage and at least one compression stage to provide heating duty and cooling duty for the heating and cooling operations, respectively. The system relies on the existing CO2 pipeline for storage of high-pressure CO2 to provide the benefits described in the disclosure. Related methods are also contemplated.
F01K 3/12 - Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having two or more accumulators
F01K 25/10 - Plants or engines characterised by use of special working fluids, not otherwise provided forPlants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
Systems and processes for cracking hydrocarbons to produce olefins herein includes heating a hydrocarbon feedstock or a mixture comprising steam and hydrocarbons to a first temperature to form a preheated feed, and also include electrically heating steam to a second, higher, temperature to form a superheated reaction steam. The preheated feed is then mixed with the superheated reaction steam to form a reaction mixture at a cracking temperature, thereby cracking the hydrocarbons to form olefins, producing a reaction effluent. The reaction effluent is then quenched and separated effluent to recover the olefins.
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
B01J 12/00 - Chemical processes in general for reacting gaseous media with gaseous mediaApparatus specially adapted therefor
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor
B01J 19/24 - Stationary reactors without moving elements inside
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
A heater includes a radiant section with a bottom wall and a side wall. A burner is provided on the bottom wall and a primary fuel stream and a primary combustion air stream are provided through the burner to support a primary combustion reaction local to the burner. The primary combustion air stream may be less than the air needed to burn all of the primary fuel stream, resulting in the primary combustion reaction being sub-stochiometric and reducing NOx formation. A remote air pipe injects remote air into the radiant section distal to the burner, and in some cases, spaced from the burner by at least two meters. The remote air addition supports a lean secondary combustion reaction that further minimizes NOx emissions concentration. The heater is suitable for use with high H2 fuel or preheated air, or both, to lower CO2 emissions while meeting NOx emission targets.
F23C 6/04 - Combustion apparatus characterised by the combination of two or more combustion chambers in series connection
F23C 3/00 - Combustion apparatus characterised by the shape of the combustion chamber
F23L 9/04 - Passages or apertures for delivering secondary air for completing combustion of fuel by discharging the air beyond the fire, i.e. nearer the smoke outlet
Systems and processes for cracking hydrocarbons to produce olefins herein includes heating a hydrocarbon feedstock or a mixture comprising steam and hydrocarbons to a first temperature to form a preheated feed, and also include electrically heating steam to a second, higher, temperature to form a superheated reaction steam. The preheated feed is then mixed with the superheated reaction steam to form a reaction mixture at a cracking temperature, thereby cracking the hydrocarbons to form olefins, producing a reaction effluent. The reaction effluent is then quenched and separated effluent to recover the olefins.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
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
A heater includes a radiant section with a bottom wall and a side wall. A burner is provided on the bottom wall and a primary fuel stream and a primary combustion air stream are provided through the burner to support a primary combustion reaction local to the burner. The primary combustion air stream may be less than the air needed to burn all of the primary fuel stream, resulting in the primary combustion reaction being sub-stochiometric and reducing NOx formation. A remote air pipe injects remote air into the radiant section distal to the burner, and in some cases, spaced from the burner by at least two meters. The remote air addition supports a lean secondary combustion reaction that further minimizes NOx emissions concentration. The heater is suitable for use with high H2 fuel or preheated air, or both, to lower CO2 emissions while meeting NOx emission targets.
Embodiments herein relate to solutions to maximize the recovery of ethylene, propylene and aromatics rich naphtha from crude oil processing. The schemes involve treating the effluent from Fluid Catalytic Cracking (FCC) to remove metals like AsH3, PH3, Hg, as well as impurities such as NOx and oxygen, before mixing it with the steam cracker effluent. The combined effluent is then cooled in a cold box and sent to various fractionators for separating the ethylene, propylene, and aromatics rich naphtha.
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
B01D 3/34 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
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 8/24 - 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
B01J 19/24 - Stationary reactors without moving elements inside
40.
METHOD AND APPARATUS FOR STRIPPING NOX, OXYGEN, CO, AND CO2 FROM FCC REGENERATED CATALYST FOR IMPROVING THE SAFETY AND RELIABILITY OF PRODUCT RECOVERY SECTION
Processes for cracking hydrocarbons include contacting hydrocarbon feedstocks with conditioned cracking catalyst in a riser reactor to recover an effluent. The effluent is separated to recover a cracked hydrocarbon stream and a spent catalyst. The spent catalyst is contacted with steam, stripping residual hydrocarbons from the spent catalyst, and the stripped catalyst is fed to a catalyst regenerator and regenerated via combustion of coke contained in the spent catalyst, forming a regenerated catalyst and combustion products. The regenerated catalyst, containing entrained combustion products (e.g., NOx, SOx, and COx) including nitrogen from the regenerator, is fed to a catalyst standpipe hopper. The regenerated catalyst containing entrained combustion products is conditioned in the catalyst standpipe hopper by contacting the regenerated catalyst with steam to recover the conditioned catalyst and a vapor stream comprising steam and the combustion products. The conditioned catalyst, depleted of combustion products, is then fed to the riser reactor.
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 38/06 - Gas or vapour treatingTreating by using liquids vaporisable upon contacting spent catalyst using steam
333, Hg, as well as impurities such as NOx and oxygen, before mixing it with the steam cracker effluent. The combined effluent is then cooled in a cold box and sent to various fractionators for separating the ethylene, propylene, and aromatics rich naphtha.
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 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
42.
METHOD AND APPARATUS FOR STRIPPING NOX, OXYGEN, NITROGEN, CO, AND CO2 FROM FCC REGENERATED CATALYST FOR IMPROVING THE PERFORMANCE, SAFETY, AND RELIABILITY OF PRODUCT RECOVERY SECTION
Processes for cracking hydrocarbons include contacting hydrocarbon feedstocks with conditioned cracking catalyst in a riser reactor to recover an effluent. The effluent is separated to recover a cracked hydrocarbon stream and a spent catalyst. The spent catalyst is contacted with steam, stripping residual hydrocarbons from the spent catalyst, and the stripped catalyst is fed to a catalyst regenerator and regenerated via combustion of coke contained in the spent catalyst, forming a regenerated catalyst and combustion products. The regenerated catalyst, containing entrained combustion products (e.g., NOx, SOx, and COx) including nitrogen from the regenerator, is fed to a catalyst standpipe hopper. The regenerated catalyst containing entrained combustion products is conditioned in the catalyst standpipe hopper by contacting the regenerated catalyst with steam to recover the conditioned catalyst and a vapor stream comprising steam and the combustion products. The conditioned catalyst, depleted of combustion products, is then fed to the riser reactor.
C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
A method of treating a quantity of water that includes a first level of a contaminant and is discharged from a process includes mixing the water with an effluent having a second level of the contaminant to produce a condensate having a third level of contaminant, the second level being greater than the first level. The method further includes passing the condensate through a reverse osmosis system to produce a permeate having a fourth level of the contaminant and a concentrate having a fifth level of the contaminant that is greater than the fourth level. The method also includes oxidizing the concentrate in an electro-oxidation system to generate the effluent and directing the effluent to a point upstream of the reverse osmosis system to perform the mixing step.
Catalytic material having catalysts supported by hibonite-type supports are provided. The catalytic materials include a first catalytic material comprising an oxidative coupling methane catalyst for oxidative coupling of methane (OCM) and a second selective oxidation catalytic material comprising a selective oxidation catalyst that preferentially oxidizes hydrogen and carbon monoxide over methane. Systems comprising the first and second catalytic materials for performing an OCM reaction using a low temperature feedstock gas mixture and methods of using the same to prepare C2+ compounds are also provided.
C07C 2/84 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
An apparatus including a radiant heating section and a flue gas stack; one or more process coils disposed within the radiant heating section; one or more fuel-fired burners disposed within the radiant heating section, the one or more fuel-fired burners configured for combusting a fuel and producing the combustion gas; one or more electrical heating elements disposed within the radiant heating section, the one or more electrical heating elements arranged to provide a second radiant energy to a lower elevation of the one or more process coils; and an internal baffle located at an elevation between the upper elevation and the lower elevation, the internal baffle arranged to provide shielding of the one or more electrical heating elements from flame and combustion gases from the one or more fuel-fired burners.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
F24H 1/14 - Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium by tubes, e.g. bent in serpentine form
A system for recovery of heat from a cracked gas product includes a heat exchanger with one or more coiled tube bundles including a mandrel, tubes wound in concentric layers around the mandrel, and tube sheets. The tubes and tube sheets define one or more tube circuits. A cracked gas product is provided to the heat exchanger and flows on a shell side of the exchanger around an outside of the tubes without a substantial change in direction of the cracked gas product. A feed stream and one or more process streams flow inside the tubes, and more specifically, through separate tube circuits. The feed stream and process streams are heated by indirect heat transfer against the cracked gas product, which enables simultaneous heating of separate fluid streams without a convection section. Related methods for heat recovery are also disclosed.
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
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
F28D 7/02 - 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 the conduits being helically coiled
F28D 21/00 - Heat-exchange apparatus not covered by any of the groups
48.
METHOD AND APPARATUS FOR HEAT RECOVERY FROM CRACKED GAS
A system for recovery of heat from a cracked gas product includes a heat exchanger with one or more coiled tube bundles including a mandrel, tubes wound in concentric layers around the mandrel, and tube sheets. The tubes and tube sheets define one or more tube circuits. A cracked gas product is provided to the heat exchanger and flows on a shell side of the exchanger around an outside of the tubes without a substantial change in direction of the cracked gas product. A feed stream and one or more process streams flow inside the tubes, and more specifically, through separate tube circuits. The feed stream and process streams are heated by indirect heat transfer against the cracked gas product, which enables simultaneous heating of separate fluid streams without a convection section. Related methods for heat recovery are also disclosed.
Systems and processes for the production of a high purity isobutylene stream, a high purity isooctene stream or for the co-production of a high purity isobutylene and a high purity isooctene. The systems and processes advantageously process mixed C4 hydrocarbon streams via etherification, back cracking, isomerization, and/or dimerization, along with various separation systems, to produce the desired high purity streams.
C07C 2/06 - Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
B01D 3/00 - Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
B01J 19/24 - Stationary reactors without moving elements inside
C07C 1/22 - 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 reduction
C07C 7/09 - Purification, separation or stabilisation of hydrocarbonsUse of additives by fractional condensation
An apparatus including a radiant heating section and a flue gas stack; one or more process coils disposed within the radiant heating section; one or more fuel-fired burners disposed within the radiant heating section, the one or more fuel-fired burners configured for combusting a fuel and producing the combustion gas; one or more electrical heating elements disposed within the radiant heating section, the one or more electrical heating elements arranged to provide a second radiant energy to a lower elevation of the one or more process coils; and an internal baffle located at an elevation between the upper elevation and the lower elevation, the internal baffle arranged to provide shielding of the one or more electrical heating elements from flame and combustion gases from the one or more fuel-fired burners.
Systems and processes for the production of a high purity isobutylene stream, a high purity isooctene stream or for the co-production of a high purity isobutylene and a high purity isooctene. The systems and processes advantageously process mixed C4 hydrocarbon streams via etherification, back cracking, isomerization, and/or dimerization, along with various separation systems, to produce the desired high purity streams.
C07C 1/20 - 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
Electrical heater systems including one or multiple electrical heaters and a stack for combusting materials leaked into and vented from the electrical heaters. Configurations may include fluid conduits, pressure doors and other equipment for controlling a flow of leaked process fluid between the heater enclosure and the stack. Configurations may also include a purge gas distribution system for purging heater enclosures and preventing thermal shock of electrical heating elements.
F23G 7/06 - Methods or apparatus, e.g. incinerators, specially adapted for combustion of specific waste or low grade fuels, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
F23G 7/08 - Methods or apparatus, e.g. incinerators, specially adapted for combustion of specific waste or low grade fuels, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases using flares, e.g. in stacks
Electrical heater systems including one or multiple electrical heaters and a stack for combusting materials leaked into and vented from the electrical heaters. Configurations may include fluid conduits, pressure doors and other equipment for controlling a flow of leaked process fluid between the heater enclosure and the stack. Configurations may also include a purge gas distribution system for purging heater enclosures and preventing thermal shock of electrical heating elements.
An apparatus for heating petroleum, petrochemical, chemical process fluids, and boiler feed water or steam generation with a combination, or individual operation, of electrical elements and fired burners. The apparatus includes a radiant heating section and a flue gas stack for exhausting a combustion gas to the atmosphere. The radiant section includes one or more process coils, one or more fuel-fired burners for combusting a fuel and producing the combustion gas, where the one or more fuel-fired burners are arranged to provide radiant energy to a first area of the one or more process coils, and one or more electrical heating elements arranged to provide radiant energy to a second area of the one or more process coils. The one or more electrical heating elements are configured to provide 5% or more of a combined maximum energy output of the fuel-fired burners and the electrical heating elements.
B01J 19/00 - Chemical, physical or physico-chemical processes in generalTheir relevant apparatus
F27D 99/00 - Subject matter not provided for in other groups of this subclass
F24H 1/14 - Continuous-flow heaters, i.e. heaters in which heat is generated only while the water is flowing, e.g. with direct contact of the water with the heating medium in which the water is kept separate from the heating medium by tubes, e.g. bent in serpentine form
F22B 1/02 - Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
An apparatus for heating petroleum, petrochemical, chemical process fluids, and boiler feed water or steam generation with a combination, or individual operation, of electrical elements and fired burners. The apparatus includes a radiant heating section and a flue gas stack for exhausting a combustion gas to the atmosphere. The radiant section includes one or more process coils, one or more fuel-fired burners for combusting a fuel and producing the combustion gas, where the one or more fuel-fired burners are arranged to provide radiant energy to a first area of the one or more process coils, and one or more electrical heating elements arranged to provide radiant energy to a second area of the one or more process coils. The one or more electrical heating elements are configured to provide 5% or more of a combined maximum energy output of the fuel-fired burners and the electrical heating elements.
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
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
B01J 19/24 - Stationary reactors without moving elements inside
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 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
C10G 45/32 - Selective hydrogenation of the diolefin or acetylene compounds
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 47/26 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
C10G 47/30 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised bed" technique
C10G 49/02 - 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
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
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
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
A process for producing olefins may include dehydrogenating a first alkane in a first reactor to produce a first effluent comprising at least one of a first n-olefin or a first diolefin; removing the first effluent from the first reactor; and regenerating the first reactor. The first reactor may include a first dehydrogenation catalyst and a first phase change material.
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 8/06 - 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 in tube reactorsChemical 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 solid particles being arranged in tubes
A system for steam cracking a whole crude that may include a volatilization device, a control system, a separator, and a steam pyrolysis reactor. The volatilization device may be configured to separate a vapor phase from a liquid phase. The control system may be configured to maintain a flow rate of the whole crude and steam, at an initial relative velocity of less than 30 m/s. The separator may be fluidly connected to the volatilization device and configured to separate the liquid phase into a second vapor phase, and a second liquid phase. The steam pyrolysis reactor may include a convection section and a steam pyrolysis heater section, the convection section configured to heat the vapor phase, the liquid phase, and the second vapor phase, and the steam pyrolysis heater section configured to steam crack hydrocarbons in the vapor phase thereby generating a cracked hydrocarbon product.
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
B01J 19/24 - Stationary reactors without moving elements inside
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 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
C10G 45/32 - Selective hydrogenation of the diolefin or acetylene compounds
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 47/26 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
C10G 47/30 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised bed" technique
C10G 49/02 - 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
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
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
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
59.
PROCESS AND PLANT FOR TREATMENT OF WASTEWATER STREAM FROM ACRYLIC ACID AND/OR ACRYLATE PRODUCTION PLANT
Provided is a process for treatment of at least one wastewater stream from an acrylic acid and/or acrylate production plant. The process for treatment comprises the steps of: (a) introducing the least one wastewater stream from the acrylic acid and/or acrylate production plant into a bioreactor (510), (b) reacting the at least one wastewater stream in the bioreactor (510) under conditions of anaerobic microbiological decomposition of undesired organic components in the presence of at least one microorganism suitable for decomposition of undesired organic components to afford methane and carbon dioxide, (c) discharging from the bioreactor (510) a treated wastewater stream depleted in undesired organic components relative to the at least one wastewater stream introduced into the bioreactor (510), and (d) incinerating a methane-and carbon dioxide-containing product gas stream discharged from the bioreactor (510), in the incineration plant (512) with an incineration air stream and an optional auxiliary fuel stream.
C02F 1/66 - Treatment of water, waste water, or sewage by neutralisationTreatment of water, waste water, or sewage pH adjustment
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
C02F 103/36 - Nature of the water, waste water, sewage or sludge to be treated from the chemical industry not provided for in groups from the manufacture of organic compounds
45 - Legal and security services; personal services for individuals.
Goods & Services
Licensing of oil refining and petrochemical technologies;
consultation services in the field of the licensing of oil
refining and petrochemical technology; licensing of
technologies for the manufacture and configuration of
ethylene production systems; licensing of technologies for
the manufacture of ethylene from ethanol, including
bio-derived ethanol; licensing of specialized equipment and
chemical and petrochemical processes to third party oil
refineries and chemical, petrochemical, oil and other
process and industrial plants and facilities; licensing of
specialized equipment and chemical and petrochemical
processes to third party facilities; licensing of
specialized equipment and chemical and petrochemical
processes to third party facilities for the processing and
production of biofuels and chemicals derived from bio-based
and recycled feedstocks; licensing of specialized equipment
and chemical and petrochemical processes to third party oil
refineries and chemical, petrochemical, oil and other
process and industrial plants and facilities for the
processing and production of ethylene from ethanol,
including bio-derived ethanol; licensing services, namely,
licensing of and consultancy relating to the licensing of
rights to equipment and industrial, refining and chemical
processes for use in third party oil refineries and
chemical, petrochemical, oil and other process and
industrial plants and facilities; licensing of intellectual
property; licensing of technologies and processes for the
production of chemicals, biochemicals, polymers, olefins,
fuels, and biofuels; consultation services in the field of
the licensing of production of chemicals, polymers, and
fuels.
61.
PROCESS FOR CONVERSION OF VERY LIGHT, SWEET CRUDE OIL TO CHEMICALS
Systems and processes for converting light or very light sweet crudes and condensates to chemicals and petrochemicals. The process includes providing a hydrocarbon feedstock comprising a crude oil or condensate having an API gravity of at least 35, a sulfur content of less than 0.2 wt%, and less than 10 wt% of hydrocarbons having a normal boiling point above 575°C. The hydrocarbon feedstock is heated and separated to recover a light fraction, a middle fraction, and optionally a heavy fraction. The light fraction is steam cracked to produce a cracked light fraction and the middle fraction is separately steam cracked to produce a cracked middle fraction. The cracked light fraction and the cracked middle fraction are then separated to recover one or more product fractions including an ethylene fraction and a propylene fraction.
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 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
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
62.
SELECTIVE TREATMENT OF FCC GASOLINE FOR REMOVAL OF SULFUR, NITROGEN, AND OLEFIN COMPOUNDS WHILE MAXIMIZING RETENTION OF AROMATIC COMPOUNDS
Systems and processes for the treatment of a naphtha range hydrocarbon feedstock comprising sulfur-containing compounds, nitrogen-containing compounds, olefins, diolefins, and aromatics. The systems and processes are configured to treat the naphtha range hydrocarbon feedstock to convert the sulfur-containing compounds, nitrogen-containing compounds, and olefins, diolefins while less than 2 wt% aromatics are hydrogenated, producing an olefin lean overheads fraction comprising less than 0.2 wt% olefins and less than 100 mg/kg sulfur and an aromatics rich fraction comprising less than 50 ppmw olefins, less than 0.5 ppmw sulfur and less than 0.5 ppmw nitrogen.
C10G 65/04 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
C10G 65/06 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
A process for dehydrogenating a paraffinic feedstock, producing olefins and/or dienes. The process includes feeding a paraffinic hydrocarbon feedstock comprising one or more C2+ paraffinic hydrocarbons and a fuel gas stream to a dehydrogenation reactor preheater, combusting the fuel gas stream in the dehydrogenation reactor preheater and heating the paraffinic hydrocarbon feedstock to a temperature in the range of 500-650°C, producing a heated paraffinic feedstock, feeding the heated paraffinic feedstock to a first dehydrogenation reactor operating in a reaction mode and containing an active dehydrogenation catalyst and at least one first electrical heating element, heating the heated paraffinic feedstock in the first dehydrogenation reactor using the at least one first electrical heating element, and contacting the heated paraffinic feedstock with the active dehydrogenation catalyst and the at least one electrical heating element thereby producing an olefinic product stream comprising one or more olefins.
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 8/04 - 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
An electric air heater system including a first electric air heater module. The first electric air heater module including an outer casing having an inner surface, a first end, and a second end; a refractory insulation layer in tight communication with the outer casing; an inner cavity within the refractory insulation layer; and a plurality of tubes extending through the inner cavity from the first end to the second end, the plurality of tubes each having an exterior surface. Each tube is fixed relative to the outer casing at the first end, and each tube has an electrical connection disposed at the first end. The plurality of tubes is arranged into one or more bundles of tubes, where each bundle includes two or more tubes having a plurality of fins extending radially from the exterior surface, and a heating element axially through a hollow interior of the tube.
Systems and processes for the treatment of a naphtha range hydrocarbon feedstock comprising sulfur-containing compounds, nitrogen-containing compounds, olefins, diolefins, and aromatics. The systems and processes are configured to treat the naphtha range hydrocarbon feedstock to convert the sulfur-containing compounds, nitrogen-containing compounds, and olefins, diolefins while less than 2 wt % aromatics are hydrogenated, producing an olefin lean overheads fraction comprising less than 0.2 wt % olefins and less than 100 mg/kg sulfur and an aromatics rich fraction comprising less than 50 ppmw olefins, less than 0.5 ppmw sulfur and less than 0.5 ppmw nitrogen.
C10G 63/04 - Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only including at least one cracking step
C10G 47/32 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions in the presence of hydrogen-generating compounds
66.
PROCESS FOR CONVERSION OF VERY LIGHT, SWEET CRUDE OIL TO CHEMICALS
Systems and processes for converting light or very light sweet crudes and condensates to chemicals and petrochemicals. The process includes providing a hydrocarbon feedstock comprising a crude oil or condensate having an API gravity of at least 35, a sulfur content of less than 0.2 wt %, and less than 10 wt % of hydrocarbons having a normal boiling point above 575° C. The hydrocarbon feedstock is heated and separated to recover a light fraction, a middle fraction, and optionally a heavy fraction. The light fraction is steam cracked to produce a cracked light fraction and the middle fraction is separately steam cracked to produce a cracked middle fraction. The cracked light fraction and the cracked middle fraction are then separated to recover one or more product fractions including an ethylene fraction and a propylene fraction.
C10G 51/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
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
An electric air heater system including a first electric air heater module. The first electric air heater module including an outer casing having an inner surface, a first end, and a second end; a refractory insulation layer in tight communication with the outer casing; an inner cavity within the refractory insulation layer; and a plurality of tubes extending through the inner cavity from the first end to the second end, the plurality of tubes each having an exterior surface. Each tube is fixed relative to the outer casing at the first end, and each tube has an electrical connection disposed at the first end. The plurality of tubes is arranged into one or more bundles of tubes, where each bundle includes two or more tubes having a plurality of fins extending radially from the exterior surface, and a heating element axially through a hollow interior of the tube.
F24H 3/06 - Air heaters with forced circulation the air being kept separate from the heating medium, e.g. using forced circulation of air over radiators
F27D 99/00 - Subject matter not provided for in other groups of this subclass
A process for dehydrogenating a paraffinic feedstock, producing olefins and/or dienes. The process includes feeding a paraffinic hydrocarbon feedstock comprising one or more C2+ paraffinic hydrocarbons and a fuel gas stream to a dehydrogenation reactor preheater, combusting the fuel gas stream in the dehydrogenation reactor preheater and heating the paraffinic hydrocarbon feedstock to a temperature in the range of 500-650° C., producing a heated paraffinic feedstock, feeding the heated paraffinic feedstock to a first dehydrogenation reactor operating in a reaction mode and containing an active dehydrogenation catalyst and at least one first electrical heating element, heating the heated paraffinic feedstock in the first dehydrogenation reactor using the at least one first electrical heating element, and contacting the heated paraffinic feedstock with the active dehydrogenation catalyst and the at least one electrical heating element thereby producing an olefinic product stream comprising one or more olefins.
A heater includes a convection section with columns and tube sheets coupled to the columns with tubes received in the tube sheets. The convection section includes a space between the tube sheets associated with corresponding pairs of columns. A structural frame is coupled to the columns and positioned in the space to slidably receive one or more catalyst support beds for loading or unloading a catalyst into the convection section through a lateral side of the convection section of the heater. The structural frame may include beams, struts, slide plates, and other frame elements that assist with supporting the catalyst support beds and enable sliding of the catalyst support beds with respect to the structural frame.
A heater includes a convection section with columns and tube sheets coupled to the columns with tubes received in the tube sheets. The convection section includes a space between the tube sheets associated with corresponding pairs of columns. A structural frame is coupled to the columns and positioned in the space to slidably receive one or more catalyst support beds for loading or unloading a catalyst into the convection section through a lateral side of the convection section of the heater. The structural frame may include beams, struts, slide plates, and other frame elements that assist with supporting the catalyst support beds and enable sliding of the catalyst support beds with respect to the structural frame.
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 15/00 - Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet materialApparatus specially adapted therefor
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
F23J 15/02 - Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
71.
SELECTIVE CATALYTIC REDUCTION CATALYST MODULE SUPPORT SYSTEM AND INSTALLATION METHOD
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
F23J 15/02 - Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
72.
HEAT EXCHANGER CLOSURE ASSEMBLIES AND METHODS OF USING AND INSTALLING THE SAME
A heat exchanger assembly including an elongated tubular heat exchanger enclosure defining an interior chamber. A tube sheet is positioned within the interior chamber of the heat exchanger enclosure separating the interior chamber into a shell side and a channel side. The interior portion is configured to removably receive a tube bundle positioned within the shell side of the interior chamber. An annular sleeve member is positioned within the channel side of the interior chamber of the heat exchanger enclosure. An annular elastic torsion member is positioned within the channel side of the interior chamber of the heat exchanger such that the sleeve member is positioned between the tube sheet and the elastic torsion member. The elastic torsion member has an inner circumference deflectable relative to its outer circumference for torsioning the elastic torsion member.
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 9/00 - CasingsHeader boxesAuxiliary supports for elementsAuxiliary members within casings
F28F 9/013 - Auxiliary supports for elements for tubes or tube-assemblies
F28F 21/00 - Constructions of heat-exchange apparatus characterised by the selection of particular materials
A heat exchanger includes a shell with a longitudinal axis with a first portion of the shell on a first side of a plane through the shell and a second portion on a second side of the plane opposite to the first side. A first heat transfer surface is arranged in the first portion of the shell and a second heat transfer surface is arranged in the second portion of the shell. The first and second heat transfer surfaces may be coiled tube bundles with one of the coolant streams interfacing with the heat transfer surfaces being the reactor feed stream. The tubes in the bundle have a radial spacing between tubes that is considerably larger than an axial spacing between tubes. A reactor effluent flows through the shell without a substantial change in direction while the first and second heat transfer surfaces cool the effluent.
F28D 7/02 - 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 the conduits being helically coiled
F28D 21/00 - Heat-exchange apparatus not covered by any of the groups
Processes and systems for converting waste plastics include feeding a waste plastic to a melt tank, and in the melt tank, heating the waste plastic to form a molten plastic. The molten plastic is withdrawn from the melt tank and fed to a pyrolysis reactor. In the pyrolysis reactor, the molten plastic is heated to a pyrolysis temperature, producing a pyrolysis oil product and a liquid pitch product. The pyrolysis oil is then separated into a pyrolysis gas fraction, a light pyrolysis oil fraction, a medium pyrolysis oil fraction, and a heavy pyrolysis oil fraction.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
B09B 3/40 - Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
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
C10B 31/06 - Charging devices for coke ovens for charging horizontally
B09B 3/70 - Chemical treatment, e.g. pH adjustment or oxidation
A method of thermally cracking a hydrocarbon feed (105) includes feeding the hydrocarbon feed (105) into at least one coil (130) in a reaction section (112) of an electric heater (110), using electrical energy to heat the hydrocarbon feed (105) in the electric heater (110) to a reaction temperature, and directing a reaction output from the electric heater (110) to at least one exchanger (150) to cool the reaction output.
An inline static mixer (100) includes an outer tube (112) and an inner tube (104) positioned inside the outer tube and arranged coaxially with respect to the outer tube with a space (104) between the inner and outer tubes. The inner tube is operable to receive and convey a hydrocarbon stream and the outer tube is operable to receive and convey a diluent stream. At least one baffle (114) extends from the inner tube toward the outer tube and through at least a portion of the space that is operable to generate a twisted diluent flow from the diluent stream. The twisted diluent flow and the hydrocarbon stream are mixed downstream of an outlet of the inner tube with the twisted diluent flow forming a boundary layer along an internal surface of the outer tube to minimize fouling from liquid or liquid droplets of the hydrocarbon stream after mixing.
B01F 25/313 - Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
B01F 25/313 - Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
An inline static mixer includes an outer tube and an inner tube positioned inside the outer tube and arranged coaxially with respect to the outer tube with a space between the inner and outer tubes. The inner tube is operable to receive and convey a hydrocarbon stream and the outer tube is operable to receive and convey a diluent stream. At least one baffle extends from the inner tube toward the outer tube and through at least a portion of the space that is operable to generate a twisted diluent flow from the diluent stream. The twisted diluent flow and the hydrocarbon stream are mixed downstream of an outlet of the inner tube with the twisted diluent flow forming a boundary layer along an internal surface of the outer tube to minimize fouling from liquid or liquid droplets of the hydrocarbon stream after mixing.
B01F 25/435 - Mixing tubes composed of concentric tubular members
B01F 25/431 - Straight mixing tubes with baffles or obstructions that do not cause substantial pressure dropBaffles therefor
B01F 25/4314 - Straight mixing tubes with baffles or obstructions that do not cause substantial pressure dropBaffles therefor with helical baffles
B01F 23/232 - Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
B01F 35/91 - Heating or cooling systems using gas or liquid injected into the material, e.g. using liquefied carbon dioxide or steam
Processes and systems for the production of heavy isoparaffinic hydrocarbons include feeding hydrogen and a mixed isoolefin stream, including C8-C12 olefins, isoolefins, and oligomers, and C8-C12+ hydrogenated hydrocarbons to a trickle-bed reactor system. The hydrogen and mixed isoolefin are reacted over a hydrogenation catalyst, producing a liquid effluent comprising hydrogenated hydrocarbons and unreacted olefins and oligomers, and a vapor effluent comprising hydrogenated hydrocarbons, hydrogen and unreacted olefins and oligomers. The liquid effluent is fed to a first heat exchanger, producing a cooled liquid effluent stream, which is combined with the vapor effluent, producing a mixed phase effluent. The mixed phase effluent is cooled in a second heat exchanger, producing a partially condensed effluent, which is fed to a drum, producing a vent stream, a hydrogenated product stream having greater than 95 wt % C8-C12 saturated hydrocarbons, and a hydrogenated recycle stream. The hydrogenated product stream may be provided to downstream blending systems.
C07C 5/03 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
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
Processes and systems for the production of heavy isoparaffinic hydrocarbons include feeding hydrogen and a mixed isoolefin stream, including C8-C12 olefins, isoolefins, and oligomers, and C8-C12+ hydrogenated hydrocarbons to a trickle-bed reactor system. The hydrogen and mixed isoolefin are reacted over a hydrogenation catalyst, producing a liquid effluent comprising hydrogenated hydrocarbons and unreacted olefins and oligomers, and a vapor effluent comprising hydrogenated hydrocarbons, hydrogen and unreacted olefins and oligomers. The liquid effluent is fed to a first heat exchanger, producing a cooled liquid effluent stream, which is combined with the vapor effluent, producing a mixed phase effluent. The mixed phase effluent is cooled in a second heat exchanger, producing a partially condensed effluent, which is fed to a drum, producing a vent stream, a hydrogenated product stream having greater than 95wt% C8-C12 saturated hydrocarbons, and a hydrogenated recycle stream. The hydrogenated product stream may be provided to downstream blending systems.
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 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
Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.
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
B01J 19/24 - Stationary reactors without moving elements inside
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 21/00 - Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
C10G 45/32 - Selective hydrogenation of the diolefin or acetylene compounds
C10G 45/44 - Hydrogenation of the aromatic hydrocarbons
C10G 47/26 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
C10G 47/30 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions with moving solid particles according to the "fluidised bed" technique
C10G 49/02 - 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
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
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
C10L 1/08 - Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
Systems and processes for converting waste plastics and other waste materials to useful end products. The systems integrate a plastics pyrolysis reactor and a liquid phase thermal cracking reactor to advantageously process the waste plastics to form various hydrocarbon products.
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
83.
Integrated mixed plastic pyrolysis with heavy oil product thermal cracking
Systems and processes for converting waste plastics and other waste materials to useful end products. The systems integrate a plastics pyrolysis reactor and a liquid phase thermal cracking reactor to advantageously process the waste plastics to form various hydrocarbon products.
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 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
A system may include a turbine and a recuperative heat exchanger system. The recuperative heat exchanger system is configured to receive exhaust gases from the turbine. The recuperative heat exchanger system may include a precool section to cool the exhaust gases, a major heating section to receive the cooled the exhaust gases, and a minor heating section to receive the cooled the exhaust gases.
F01N 3/02 - Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for cooling, or for removing solid constituents of, exhaust
F01N 5/02 - Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy the devices using heat
F28D 1/04 - Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with the heat-exchange conduits immersed in the body of fluid with tubular conduits
F28D 21/00 - Heat-exchange apparatus not covered by any of the groups
85.
INTEGRATED MIXED PLASTIC PYROLYSIS WITH HEAVY OIL PRODUCT THERMAL CRACKING
Systems and processes for converting waste plastics and other waste materials to useful end products. The systems integrate a plastics pyrolysis reactor and a liquid phase thermal cracking reactor to advantageously process the waste plastics to form various hydrocarbon products.
C10G 1/10 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
C10G 1/00 - Production of liquid hydrocarbon mixtures from oil shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
Systems and processes for external combustion air preheating for providing preheated combustion air to a furnace. The furnace systems convective heating section includes multiple heating coils for waste heat recovery. The heating coils may be used for preheating a feed (feed preheat coils), heating a boiler feed water, superheating steam, or heating or superheating a feed stream prior to the feed being fed to the radiant coil. The waste heat in the combustion gas is also used to heat a heat transfer fluid, which may be used to pre-heat combustion air or for other purposes within the plant.
An electrically heated furnace including one or more unit cells. Each unit cell includes a radiant heating section, one or more process coils disposed within the radiant heating section, and a quench unit for cooling a cracked product from the one or more process coils and producing a quenched reaction product. The furnace also includes one or more electrical heating elements disposed within the radiant heating section, the one or more electrical heating elements are arranged to provide radiant energy to the one or more process coils. Further, the electrically heated furnace includes a first area corresponding to a heating area of the one or more electrical heating elements, a second area corresponding to a wall area of the wall on which the one or more electrical heating elements are disposed, and a third area corresponding to a surface area of the one or more process coils.
A process including preheating a hydrocarbon feed in a first preheat zone of a convection section, recovering a preheated hydrocarbon stream; heating the preheated hydrocarbon stream in a secondary transferline exchanger, recovering a heated hydrocarbon stream; feeding the heated hydrocarbon stream to a second preheat zone of the convection section to vaporize a portion of heated hydrocarbon stream, recovering a cracking feedstream; cracking hydrocarbons in the cracking feedstream in one or more coils in a radiant section, recovering a cracked hydrocarbon product; and cooling the cracked hydrocarbon product in the secondary transferline exchanger in indirect heat exchange with the preheated hydrocarbon stream, recovering a cooled hydrocarbon product stream.
A process including preheating a hydrocarbon feed in a first preheat zone of a convection section, recovering a preheated hydrocarbon stream; heating the preheated hydrocarbon stream in a secondary transferline exchanger, recovering a heated hydrocarbon stream; feeding the heated hydrocarbon stream to a second preheat zone of the convection section to vaporize a portion of heated hydrocarbon stream, recovering a cracking feedstream; cracking hydrocarbons in the cracking feedstream in one or more coils in a radiant section, recovering a cracked hydrocarbon product; and cooling the cracked hydrocarbon product in the secondary transferline exchanger in indirect heat exchange with the preheated hydrocarbon stream, recovering a cooled hydrocarbon product stream.
C10G 9/14 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
C10G 9/24 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
C10G 9/00 - Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
Systems and processes for external combustion air preheating for providing preheated combustion air to a furnace. The furnace systems convective heating section includes multiple heating coils for waste heat recovery. The heating coils may be used for preheating a feed (feed preheat coils), heating a boiler feed water, superheating steam, or heating or superheating a feed stream prior to the feed being fed to the radiant coil. The waste heat in the combustion gas is also used to heat a heat transfer fluid, which may be used to preheat combustion air or for other purposes within the plant.
An electrically heated furnace including one or more unit cells. Each unit cell includes a radiant heating section, one or more process coils disposed within the radiant heating section, and a quench unit for cooling a cracked product from the one or more process coils and producing a quenched reaction product. The furnace also includes one or more electrical heating elements disposed within the radiant heating section, the one or more electrical heating elements are arranged to provide radiant energy to the one or more process coils. Further, the electrically heated furnace includes a first area corresponding to a heating area of the one or more electrical heating elements, a second area corresponding to a wall area of the wall on which the one or more electrical heating elements are disposed, and a third area corresponding to a surface area of the one or more process coils.
A process for regenerating a catalyst in an olefin production reactor. The process includes feeding a compressed, pre-heated air stream to a heating zone comprising an electrical heater, electrically heating the compressed, pre-heated air stream in the heating zone to a temperature in the range of 500-800°C, producing a regeneration air stream, feeding the regeneration air stream to the olefin production reactor, regenerating the catalyst using the regeneration air, producing a hot air stream, and feeding the hot air stream to a waste heat recovery unit configured to pre-heat a compressed air stream, producing the compressed, pre-heated air stream and a waste air stream.
B01J 38/04 - Gas or vapour treatingTreating by using liquids vaporisable upon contacting spent catalyst
B01J 8/06 - 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 in tube reactorsChemical 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 solid particles being arranged in tubes
A process for converting isobutane to propylene. The process including dehydrogenating isobutane to produce a mixed product stream comprising isobutane and isobutene, skeletal isomerizing the mixed product stream comprising isobutane and isobutene to convert isobutene to n-butenes including 1-butene and 2-butenes and to recover a skeletal isomerization reaction product comprising isobutane, isobutene, butadiene, 1-butene, and 2-butenes. The process further including fractionating the skeletal isomerization reaction product, isomerizing the 1-butene contained therein to 2-butenes, recovering an overhead fraction comprising isobutane, a side draw fraction comprising isobutane and isobutene, and a bottoms fraction comprising 2-butenes, and combining the bottoms fraction with ethylene and converting the ethylene and 2-butenes to produce a reaction effluent comprising propylene.
A process for converting isobutane to propylene. The process including dehydrogenating isobutane to produce a mixed product stream comprising isobutane and isobutene, skeletal isomerizing the mixed product stream comprising isobutane and isobutene to convert isobutene to n-butenes including 1 -butene and 2-butenes and to recover a skeletal isomerization reaction product comprising isobutane, isobutene, butadiene, 1 -butene, and 2- butenes. The process further including fractionating the skeletal isomerization reaction product, isomerizing the 1 -butene contained therein to 2-butenes, recovering an overhead fraction comprising isobutane, a side draw fraction comprising isobutane and isobutene, and a bottoms fraction comprising 2-butenes, and combining the bottoms fraction with ethylene and converting the ethylene and 2-butenes to produce a reaction effluent comprising propylene.
C07C 6/04 - Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond
C07C 5/373 - Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen with simultaneous isomerisation
A process for regenerating a catalyst in an olefin production reactor. The process includes feeding a compressed, pre-heated air stream to a heating zone comprising an electrical heater, electrically heating the compressed, pre-heated air stream in the heating zone to a temperature in the range of 500-800° C., producing a regeneration air stream, feeding the regeneration air stream to the olefin production reactor, regenerating the catalyst using the regeneration air, producing a hot air stream, and feeding the hot air stream to a waste heat recovery unit configured to pre-heat a compressed air stream, producing the compressed, pre-heated air stream and a waste air stream.
B01J 38/12 - Treating with free oxygen-containing gas
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
45 - Legal and security services; personal services for individuals.
Goods & Services
Licensing of oil refining and petrochemical technologies; consultation services in the field of the licensing of oil refining and petrochemical technology; licensing of technologies for the manufacture and configuration of ethylene production systems; licensing of technologies for the manufacture of ethylene from ethanol, including bio-derived ethanol; licensing of specialized equipment and chemical and petrochemical processes to third party oil refineries and chemical, petrochemical, oil and other process and industrial plants and facilities; licensing of specialized equipment and chemical and petrochemical processes to third party facilities; licensing of specialized equipment and chemical and petrochemical processes to third party facilities for the processing and production of biofuels and chemicals derived from bio-based and recycled feedstocks; licensing of specialized equipment and chemical and petrochemical processes to third party oil refineries and chemical, petrochemical, oil and other process and industrial plants and facilities for the processing and production of ethylene from ethanol, including bio-derived ethanol; licensing services, namely, licensing of and consultancy relating to the licensing of rights to equipment and industrial, refining and chemical processes for use in third party oil refineries and chemical, petrochemical, oil and other process and industrial plants and facilities; licensing of technologies and processes for the production of chemicals, biochemicals, polymers, olefins, fuels, and biofuels; consultation services in the field of the licensing of production of chemicals, polymers, and fuels; none of the foregoing for use in the fields of entertainment, audiovisual content, television, or film
97.
PROCESS FOR THE EFFICIENT PRODUCTION OF BIO HIGH PURITY ISOBUTENE FROM RENEWABLES
A process and system for converting bio ethanol to high purity isobutene is provided. The system includes a dehydration unit configured to receive a bio ethanol containing stream, convert the bio ethanol to bio ethylene, and produce a bio ethylene containing stream, a dimerization unit configured to receive the bio ethylene stream, dimerize ethylene, and produce an n-butenes containing stream, a skeletal isomerization unit configured to receive the n-butenes containing stream, convert n-butenes to produce a skeletal isomerization stream comprising an isobutene, isobutane, n-butenes, and n-butane, and a catalytic separation unit configured to receive the skeletal isomerization stream, convert olefins and/or isoolefins contained therein to produce a converted skeletal isomerization reaction product, and to fractionate the skeletal isomerization reaction product and produce bio isobutene.
C07C 5/327 - Formation of non-aromatic carbon-to-carbon double bonds only
C07C 7/148 - Purification, separation or stabilisation of hydrocarbonsUse of additives by treatment giving rise to a chemical modification of at least one compound
A wet air oxidation system includes a reactor including an inlet and an outlet. The reactor is operable to oxidize a portion of a two-phase process fluid and to discharge a hot oxidized fluid from the outlet. A heat exchanger includes a plurality of tubes that extend along a long axis of the heat exchanger and cooperate to define a hot fluid inlet coupled to the outlet to receive the hot oxidized fluid and a hot fluid outlet, a shell that surrounds the plurality of tubes and defines a process fluid inlet arranged to receive the two-phase process fluid, and a process fluid outlet arranged to discharge a preheated two-phase process fluid to the inlet of the reactor, wherein the long axis of the heat exchanger is arranged in a non-horizontal direction.
A process and system for converting bio ethanol to high purity isobutene is provided. The system includes a dehydration unit configured to receive a bio ethanol containing stream, convert the bio ethanol to bio ethylene, and produce a bio ethylene containing stream, a dimerization unit configured to receive the bio ethylene stream, dimerize ethylene, and produce an n-butenes containing stream, a skeletal isomerization unit configured to receive the n-butenes containing stream, convert n-butenes to produce a skeletal isomerization stream comprising an isobutene, isobutane, n-butenes, and n-butane, and a catalytic separation unit configured to receive the skeletal isomerization stream, convert olefins and/or isoolefins contained therein to produce a converted skeletal isomerization reaction product, and to fractionate the skeletal isomerization reaction product and produce bio isobutene.
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 7/04 - Purification, separation or stabilisation of hydrocarbonsUse of additives by distillation
Systems and processes for pyrolyzing waste plastics, including, in one or more heating stages, heating a waste plastic from an initial temperature to a peak pyrolysis temperature, and, in a final pyrolysis stage, providing heat input sufficient to maintain a temperature of the waste plastic at a pyrolysis reaction temperature less than the peak pyrolysis temperature and maintaining the waste plastic at the pyrolysis reaction temperature for a time period to convert a portion of the waste plastic to a pyrolyzed product and a pitch. The process further includes recovering the pyrolyzed product and recovering the pitch.
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 1/10 - 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
