Systems and methods for producing light olefins and BTX (benzene, toluene, and xylene). Crude oil is first separated to produce light naphtha and heavy naphtha. Light naphtha is fed to a steam cracking unit and heavy naphtha is fed to a catalytic cracking unit. The effluent from the steam cracking unit and the effluent from the catalytic cracking unit are flowed into an oil quench tower and are further separated in a separation unit to produce an ethylene stream, a propylene stream, and a BTX stream. The C.sub.4 hydrocarbons, ethane, and propane from the effluent of the steam cracking unit and the effluent from the catalytic cracking unit are recycled to the steam cracking unit. The non-BTX C.sub.6+ hydrocarbons from the effluent of the steam cracking unit and the effluent from the catalytic cracking unit are recycled to the catalytic cracking unit.

Systems and methods for producing light olefins and BTX (benzene, toluene, and xylene). Crude oil is first separated to produce light naphtha and heavy naphtha. Light naphtha is fed to a steam cracking unit and heavy naphtha is fed to a catalytic cracking unit. The effluent from the steam cracking unit and the effluent from the catalytic cracking unit are flowed into an oil quench tower and are further separated in a separation unit to produce an ethylene stream, a propylene stream, and a BTX stream. The C.sub.4 hydrocarbons, ethane, and propane from the effluent of the steam cracking unit and the effluent from the catalytic cracking unit are recycled to the steam cracking unit. The non-BTX C.sub.6+ hydrocarbons from the effluent of the steam cracking unit and the effluent from the catalytic cracking unit are recycled to the catalytic cracking unit.

A dividing wall column is used in an alkylation process flow scheme to fractionate an alkylate reactor effluent to produce an iso-butane-rich stream as a recycle feed for the alkylation reactor while also separating iso-butane, normal butane and alkylate as separate product streams depending on the reactor effluent composition. In an optional embodiment, the scheme may contain propane.

A process for treating effluent streams in a naphtha complex is described. One or more of the sour water stripping unit for the NHT sour water from the NHT, the amine treatment unit and the caustic treatment unit for the NHT stripper off-gas, the caustic scrubber unit or other chloride treatment unit for the off-gas from the C.sub.5-C.sub.6 isomerization zone and the C.sub.4 isomerization zone, and the caustic scrubber unit or other chloride treatment unit for the regenerator off-gas are replaced with a thermal oxidation system.

A process for treating effluent streams in a renewable transportation fuel production process is described. One or more of the sour water stream and an acid gas stream are treated directly in thermal oxidation section. The process allows the elimination or size reduction of a sour water stripper unit, waste water treatment plant, and sulfur recovery unit.

The present disclosure relates to a process for treating a feedstock containing tall oil, the process including separation of a light stream from the feedstock, followed by removal of a heavy fraction from the feedstock, in which process the separation of the light stream from the feedstock a fractionator is used and at least one product is collected from the light stream. The disclosure also relates to an apparatus for use in the process and use of a fractionator in dehydration of a feedstock containing tall oil.

The present disclosure relates to a process for treating a feedstock containing tall oil, the process including separation of a light stream from the feedstock, followed by removal of a heavy fraction from the feedstock, in which process the separation of the light stream from the feedstock a fractionator is used and at least one product is collected from the light stream. The disclosure also relates to an apparatus for use in the process and use of a fractionator in dehydration of a feedstock containing tall oil.

A method of cleaning a condensate thermosyphon reboiler including modifying a flow rate of a hot oil stream introduced into the tube-side of a first condensate thermosyphon reboiler, modifying a flow rate of a condensate hydrocarbon stream introduced into the shell-side of the first condensate thermosyphon reboiler, and maintaining an operation of the condensate stabilizer system until the value of an overhead temperature of the first condensate thermosyphon reboiler is detected to have been modified from the first overhead temperature to a second overhead temperature. The method further includes modifying the flow rate of the condensate hydrocarbon stream from the second condensate flow rate to the first condensate flow rate, and modifying the flow rate of the hot oil stream from the second hot oil flow rate to the first hot oil flow rate.

Method for crude petroleum oil processing in Crude Distillation Unit is provided to eliminate the stripping steam in an Atmospheric Distillation Column (VDC) of CDU for a significant reduction in the CDU's operating cost and alleviating the corrosion in the overhead section of ADC. The present invention relates to a method of separating the components of crude petroleum oil. The proposed method utilizes the innovative application of process hydrocarbon vapour consisting of a lighter fraction of crude and natural gas. The conceptualized new schemes for downstream processing the Light and Heavy gas oil (LGO and HGO) distillates to meet their boiling specifications are also disclosed.

The present disclosure provides for organic solvent production via distillation and dehydration by: directing portions of a feed stream to a first and second distillation columns operating at a different pressures from each other, wherein the organic solvent is preferably an alcohol and more preferably ethanol; generating, in the first distillation column, a vaporous first overhead stream; directing the vaporous first overhead stream directly to a rectification system; generating, in the second distillation column, a vaporous second overhead stream; forming a condensed second overhead stream from the vaporous second overhead stream; directing, at least a portion of the condensed second overhead stream to the rectification system; generating, via the rectification system, a third overhead stream; directing at least a portion of the third overhead stream to a separation system; and generating, in the separation system, an enriched solvent stream.