Saudi Arabian Oil Company

Yufeng He

Vinod Ramaseshan

Hiren Shethna

Mohammed A AlWohaibi

Qi Xu

Rohit Patwardhan

Abdullah Al Ghazal

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

A method of forming C-Caromatics may include selectively dealkylating a Fluid Catalytic Cracking (FCC) heavy cut naphtha that has at least Caromatics to selectively crack Calkyl chains from the Caromatics, thereby forming the C-Caromatics. The selectively de-alkylated heavy cut naphtha is then combined with a FCC middle cut naphtha, and aromatics including the C-Caromatics are separated from the combined stream. A system for forming C-Caromatics may include a fluid catalytic cracking unit for producing a FCC heavy cut naphtha comprising at least Caromatics; a de-alkylation reactor for selectively cracking Calkyl chains from the Caromatics, thereby forming the C-Caromatics; and an aromatic extraction unit for extracting at least a portion of the C-Caromatics.

Producing C6-C8 aromatics from FCC heavy naphtha

Increased paraxylene production through the use of a split feed reforming process, wherein hydrotreated naphtha is split into light, middle and heavy fractions. Each fraction is reformed separately to generate streams containing aromatic compounds. These streams can further be processed and can undergo dealkylation, transalkylation, disproportionation, isomerization, and separation steps to maximize paraxylene production. In addition, some streams are recycled or recombined in order to maximize paraxylene production.

Paraxylene production from naphtha feed

Sales gas output from a glycol dehydration unit in a gas plant is flown into a sales gas pipeline. One or more operational parameters of the glycol dehydration unit are received. One or both of an amount of glycol carryover and an amount of water carryover in sales gas output from the glycol dehydration unit in the gas plant are determined based on the one or more operational parameters of the glycol dehydration unit. An amount of glycol and water co-condensation in the sales gas pipeline is determined based on one or more operational parameters of the sales gas pipeline and the one or both of the amount of glycol carryover and the amount of water carryover. An amount of black powder formation of the sales gas is determined based on the amount of glycol and water co-condensation.

Evaluating black powder formation of hydrocarbon gas flowed through pipelines

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 integrated hydrocracking/hydrofinishing reactor.

Growing community of inventors

Al Khobar, Saudi Arabia

Yufeng He