Saudi Arabian Oil Company

Sabic Global Technologies B.v.

Vinod Ramaseshan

Omer Refa Koseoglu

Bruce Richard Beadle

Robert Peter Hodgkins

Rakan Sulaiman Bilaus

Ki-Hyouk Choi

Mohnnad H Alabsi

Vishvedeep Bhat

Hiren Shethna

Yufeng He

Mohammed A AlWohaibi

Mazin M Fathi

Yuv Raj Mehra

Marcus J Killingworth

Ali Hasan Al-Abdulal

Mohamed Sabri Abdelghani

Nicolas Goyheneix

Hatem Belfadhel

Ali H Al-Abdul'al

Timothy Abbott

Mohammed A Al-Wohaibi

Hisham T Al-Bassam

Abdulaziz S Al-Ghamdi

Eric Wei

Donald Saunders

Emad Al Subaie

Hector Infante

Rustam Ismagilov

Jesse Williams

Ashok Kumar Choudhary

Jurgen Kleibergen

Abdalaziz A Al-Balawi

A process for reverse isomerization of a light naphtha feedstock containing branched C-Cparaffins. The process includes feeding a mixed feed stream including the light naphtha feedstock to a separation unit to generate an iso-paraffin stream and one or more normal paraffin streams. The process further includes mixing hydrogen gas and a hydrocarbon feed stream containing the iso-paraffin stream to form a hydrogen-enriched liquid feed stream which is provided to a reverse isomerization reactor. The hydrogen-enriched liquid feed stream is contacted with a solid reverse isomerization catalyst for reverse hydroisomerization in a substantially two-phase liquid-solid reverse isomerization fixed-bed reaction zone convert iso-paraffins to normal paraffins. The isomerization effluent stream is provided to a stabilization column to generate a stabilized isomerate stream which is combined with the light naphtha feedstock to generate the mixed feed stream. An associated system for performing the process is also provided.

Reverse isomerization process using feedstock containing dissolved hydrogen

Provided is a system to upgrade an input stream of a straight run vacuum residue or a cracked feedstock that includes a vacuum column, a hydrocracking unit, a high lift solvent deasphalting unit, a low lift solvent deasphalting unit, and a bitumen blowing unit or a pitch pelletizing unit, and optionally a hydrotreating reactor. The system and components thereof may pass a distillate and naphtha product, a light ends product, an asphaltene-lean heavy deasphalted oil stream, an asphaltene-rich pitch stream, a light deasphalted oil that is a lube base feed stock, a heavy oil stream, a bitumen and asphalt stream or a solid fuel. Further provided is a process, including introducing a straight run vacuum residue or a cracked feed stock into a system, and operating the system including a step of fractionating, a step of solvent stage deasphalting, and a step of hydrocracking.

Process scheme for maximum heavy oil conversion with stage asphaltene rejection

A process for upgrading a hydrocarbon feed includes contacting the hydrocarbon feed with hydrogen in the presence of a ring opening catalyst in a naphthene conversion unit, the contacting causing naphthenes in the hydrocarbon feed to react to produce a converted effluent comprising isoparaffins and normal paraffins. The process includes separating the converted effluent in a paraffin separation system to produce an isoparaffin-rich stream and an n-paraffin-rich stream. The process includes contacting the isoparaffin-rich stream with hydrogen in the presence of an isomerization catalyst in a reverse isomerization unit, the contacting causing isomerization to produce an isomerate comprising an equilibrium mixture of normal paraffins and isoparaffins. The process include separating the isomerate in the paraffin separation system to produce the isoparaffin-rich stream and the n-paraffin-rich stream, and passing the n-paraffin-rich stream to a steam cracker to produce a cracker effluent comprising olefins.

Systems and processes for producing ethylene from naphtha and butanes

A method for producing a diesel having improved cold flow properties, the method comprising the steps of introducing a crude oil to a distillation column, separating the crude oil in the distillation unit to produce a light gas oil, and a light vacuum gas oil, where the light gas oil has a T95% cut point in the range between 300 deg C. and 340 deg C., where the light vacuum gas oil has a T95% cut point in the range between 400 deg C. and 430 deg C., processing the light vacuum gas oil in the supercritical water unit to produce an upgraded vacuum gas oil, separating the upgraded vacuum gas oil in the fractionator to produce an upgraded light fraction, an upgraded light gas oil, and upgraded heavy fraction, introducing the upgraded light gas oil into a diesel pool, and blending the light gas oil into the diesel pool.

Production of high quality diesel by supercritical water process

Systems and methods for crude oil separation and upgrading, which include the ability to reduce aromatic complex bottoms content in gasoline and higher-quality aromatic compounds. In some embodiments, aromatic complex bottoms are recycled for further processing. In some embodiments, aromatic complex bottoms are separated for further processing.

Process to recover gasoline and diesel from aromatic complex bottoms

Methods and systems for producing light olefins are disclosed. A feedstock comprising crude oil is distilled to produce a plurality of streams including a naphtha stream and a vacuum residue stream. The naphtha is fed to a steam cracking unit to produce light olefins, Chydrocarbons, pyrolysis gasoline and pyrolysis oil. The vacuum residue stream is hydrocracked to produce additional naphtha and heavy unconverted oil. The heavy unconverted oil and the pyrolysis oil from steam cracking unit can be deasphalted to produce deasphalted oil and pitch product. The deasphalted oil can be further hydrocracked to produce naphtha. The pitch product can be gasified to produce synthesis gas, which is further used to produce methanol. The methanol can be used to react with isobutylene of the Chydrocarbon stream from steam cracker to produce methyl tert-butyl ether (MTBE).

Optimizing the simultaneous production of high-value chemicals and fuels from heavy hydrocarbons

Systems and methods for hydrodearylation of a hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons, the method including supplying a hydrogen feed to the hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons; mixing the hydrogen feed with the hydrocarbon feed stream to saturate the hydrocarbon feed stream with hydrogen gas to create a hydrogen-enriched liquid hydrocarbon stream; passing the hydrogen-enriched liquid hydrocarbon stream to a hydrodearylation reactor without a separate gaseous phase of hydrogen; allowing the hydrogen-enriched liquid hydrocarbon stream to react in presence of a catalyst under specific reaction conditions to produce a product stream comprising a reduced concentration of di-aromatic compounds and an increased concentration of mono-aromatic compounds compared to the hydrocarbon feed stream comprising non-condensed alkyl-bridged multi-aromatic hydrocarbons; and recovering, from the hydrodearylation reactor, a product stream for a downstream process, wherein the non-condensed alkyl-bridged multi-aromatic hydrocarbons include at least two benzene rings connected by an alkyl bridge group having at least two carbons, wherein the benzene rings are connected to different carbons of the alkyl bridge group.

Catalytic hydrodearylation of heavy aromatic streams containing dissolved hydrogen with fractionation

A system for processing a stream including fuel oil includes an atmospheric flash column for receiving the stream as feedstock and separate the stream into an atmospheric flash distillate stream and an atmospheric flash residue stream. The system includes a vacuum flash column for receiving the atmospheric flash residue stream and separating the atmospheric flash residue stream into a vacuum flash distillate stream, a vacuum flash residue stream, and a vacuum gas oil stream. The system includes a first hydrocracking unit for receiving and processing at least a portion of the vacuum flash residue stream to produce an intermediate stream and a slurry. The system includes a second hydrocracking unit for receiving and processing the vacuum gas oil stream and the intermediate stream to produce a naphtha product and a light ends product. The system includes a pelletization unit for receiving and processing the slurry to produce a pelletized product.

Fuel oil conversion

An integrated upgrading process for upgrading a heavy oil, the process comprising the steps of introducing a heavy oil to a visbreaker unit; processing the heavy oil in the visbreaker unit to produce a visbreaker product stream; feeding the visbreaker product stream to a fractionator; separating the visbreaker product stream in the fractionator to produce a bottoms stream, a gas oil stream, a naphtha stream, and a gas product stream; feeding the bottoms stream to a supercritical water unit; and processing the bottoms stream in the supercritical water unit to produce an upgraded bottoms stream.

Supercritical water process integrated with visbreaker

Techniques for processing residuum include receiving a feed stream that includes a residuum hydrocarbon fraction at an ebullated bed hydroconversion reactor; contacting the residuum hydrocarbon fraction with hydrogen and a hydroconversion catalyst in the ebullated bed hydroconversion reactor to produce a partially converted reactor effluent product; separating, in a first separation zone, the partially converted reactor effluent product into a distillate stream and a heavy hydrocarbon stream; feeding the distillate stream to a bottom portion of an integrated hydrocracking/hydrofinishing reactor; and feeding the heavy hydrocarbon stream to a top portion of the hydrofinishing reactor.

Integrated residuum hydrocracking and hydrofinishing

Growing community of inventors

Ras Tanura, Saudi Arabia

Vinod Ramaseshan