The invention relates to a method of separating and purifying products from a high pressure processing system adapted for processing a feed stream comprising carbonaceous material at a pressure of at least 150 bar and a temperature of at least 300° C., where the converted feed stream (product mixture) is cooled to a temperature in the range 50 to 250° C., and depressurized to a pressure in the range 1 to 150 bar, the method comprising separating the depressurized product mixture in gas phase, an oil phase (liquid hydrocarbon), and a water phase comprising water soluble organics, dissolved salts and optionally suspended particles in a first phase separator and purifying the oil phase from the first phase separator by mixing it with one or more washing agents, at least one of which comprises water, and separating the oil phase from the one or more washing agents in a further separation step.

A system for liquid hydrocarbon desulfurization having at least one reaction subsystem including at least one high intensity mixer and a stripping station. Multiple reaction subsystems can be utilized. A method is likewise disclosed for liquid hydrocarbon desulfurization.

A method to demetal and de-ash oil feedstock. The method includes adding direct steam and sulfuric acid to oil feedstock to form acid treated oil, the sulfuric acid to strip the oil feedstock of metals, adding de-emulsifier to the acid treated oil feedstock to aid in phase separation, and settling the acid treated oil feedstock to separate into clarified oil, water, and a rag layer. The method includes centrifuging the clarified oil with a centrifuge running in a 3 phase configuration to remove water and solids from the clarified oil, and ensuring proper temperature and adding triethanol amine (TEA) to the centrifuged clarified oil to flocculate asphaltenes in the centrifuged clarified oil, creating TEA treated oil. The method includes centrifuging the TEA treated oil with a centrifuge running in a 2 phase configuration to remove the asphaltenes from the TEA treated oil and create marine fuel.

A method to demetal and de-ash oil feedstock. The method includes adding direct steam and sulfuric acid to oil feedstock to form acid treated oil, the sulfuric acid to strip the oil feedstock of metals, adding de-emulsifier to the acid treated oil feedstock to aid in phase separation, and settling the acid treated oil feedstock to separate into clarified oil, water, and a rag layer. The method includes centrifuging the clarified oil with a centrifuge running in a 3 phase configuration to remove water and solids from the clarified oil, and ensuring proper temperature and adding triethanol amine (TEA) to the centrifuged clarified oil to flocculate asphaltenes in the centrifuged clarified oil, creating TEA treated oil. The method includes centrifuging the TEA treated oil with a centrifuge running in a 2 phase configuration to remove the asphaltenes from the TEA treated oil and create marine fuel.

Hydrocracked bottoms fractions are treated to separate HPNA compounds and/or HPNA precursor compounds and produce a reduced-HPNA hydrocracked bottoms fraction effective for recycle, in a configuration of a single-stage hydrocracking reactor, series-flow once through hydrocracking operation, or two-stage hydrocracking operation. A process for separation of HPNA and/or HPNA precursor compounds from a hydrocracked bottoms fraction of a hydroprocessing reaction effluent comprises contacting the hydrocracked bottoms fraction with an effective quantity of a sulfonation agent to produce corresponding sulfonated HPNA compounds and/or sulfonated HPNA precursor compounds, and to form a sulfonated hydrocracked bottoms fraction. The sulfonated hydrocracked bottoms fraction is separated into an HPNA-reduced hydrocracked bottoms portion and a sulfonated HPNA portion. All or a portion of the HPNA-reduced hydrocracked bottoms portion is recycled within the hydrocracking operation.

A light naphtha feedstock containing olefins is introduced with hydrogen sulfide into a mercaptanization zone for conversion of the olefins into a mercaptan stream that is substantially free of olefins, after which the mercaptans are sent with an alkali caustic solution into a mercaptan oxidation treatment unit (MEROX) to produce a spent caustic stream and sweet light naphtha product stream that is substantially free of olefins and of mercaptans. Disulfide oils are produced from the wet air oxidation of the spent caustic, and the disulfide oils can be further processed to provide high purity olefin building blocks.

A light naphtha feedstock containing olefins is introduced with hydrogen sulfide into a mercaptanization zone for conversion of the olefins into a mercaptan stream that is substantially free of olefins, after which the mercaptans are sent with an alkali caustic solution into a mercaptan oxidation treatment unit (MEROX) to produce a spent caustic stream and sweet light naphtha product stream that is substantially free of olefins and of mercaptans. Disulfide oils are produced from the wet air oxidation of the spent caustic, and the disulfide oils can be further processed to provide high purity olefin building blocks.

A process, a system, and an apparatus for separation of an oxygenate from a stream is provided. More specifically, a stream comprising the oxygenate is introduced to a quench tower along with a caustic outlet stream comprising a metal salt. Contact between the oxygenate and the metal salt results in conversion of a portion of the oxygenate into a derivative salt. The derivative salt and unconverted oxygenate are condensed by quenching and substantially removed from the quench tower as an oxygenate outlet stream. The gaseous components of the stream, minus a substantial portion of the oxygenate, are removed from the quench tower as a quench outlet stream.

A process, a system, and an apparatus for separation of an oxygenate from a stream is provided. More specifically, a stream comprising the oxygenate is introduced to a quench tower along with a caustic outlet stream comprising a metal salt. Contact between the oxygenate and the metal salt results in conversion of a portion of the oxygenate into a derivative salt. The derivative salt and unconverted oxygenate are condensed by quenching and substantially removed from the quench tower as an oxygenate outlet stream. The gaseous components of the stream, minus a substantial portion of the oxygenate, are removed from the quench tower as a quench outlet stream.

The invention relates to a method of separating and purifying products from a high pressure processing system adapted for processing a feed stream comprising carbonaceous material at a pressure of at least 150 bar and a temperature of at least 300 C., where the converted feed stream (product mixture) is cooled to a temperature in the range 50 to 250 C., and depressurized to a pressure in the range 1 to 150 bar, the method comprising separating the depressurized product mixture in gas phase, an oil phase (liquid hydrocarbon), and a water phase comprising water soluble organics, dissolved salts and optionally suspended particles in a first phase separator and purifying the oil phase from the first phase separator by mixing it with one or more washing agents, at least one of which comprises water, and separating the oil phase from the one or more washing agents in a further separation step.