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.

Systems and methods are provided for increasing the portion of a pyrolysis tar fraction that can be hydroprocessed by using a physical particle size reduction process on at least a portion of the pyrolysis tar fraction. The physical particle size reduction process can reduce the percentage of particles in the pyrolysis tar fraction that have a particle size of 75 μm or greater, or 50 μm or greater. It has been unexpectedly discovered that at least a portion of the particles having a size of 75 μm or less, or 50 μm or less, can be effectively hydroprocessed to form products of greater value while still reducing or minimizing the amount of fouling or plugging in a hydroprocessing catalyst bed. By increasing the number of particles having a size of 75 μm or less, or 50 μm or less, while selectively removing larger particles from the SCT fraction, a higher yield of hydrocarbon products can be achieved for a feed containing an SCT fraction. This can reduce or minimize the amount of particulates that are disposed of by incineration or another disposal method for fractions that have a lesser value.

Embodiments of the disclosure provide a system and method for producing a linear alpha olefin. A disulfide, a hydrogen donating compound, and water are combined to produce a mixture. The mixture is introduced to a reactor operated at a pressure equal to or greater than 22.06 MPa and a temperature equal to or greater than 374 deg. C to produce an effluent stream. The effluent stream is separated to produce a product stream including the linear alpha olefin. The disulfide can be a compound of formula R—S—S—R′ where R is a first alkyl group having carbon atoms ranging from 1 to 12 and R′ is a second alkyl group having carbon atoms ranging from 5 to 12. The hydrogen donating compound can include a partially hydrogenated multi-ring aromatic compound.

Embodiments of the disclosure provide a system and method for producing a linear alpha olefin. A disulfide, a hydrogen donating compound, and water are combined to produce a mixture. The mixture is introduced to a reactor operated at a pressure equal to or greater than 22.06 MPa and a temperature equal to or greater than 374 deg. C. to produce an effluent stream. The effluent stream is separated to produce a product stream including the linear alpha olefin. The disulfide can be a compound of formula R—S—S—R′ where R is a first alkyl group having carbon atoms ranging from 1 to 12 and R′ is a second alkyl group having carbon atoms ranging from 5 to 12. The hydrogen donating compound can include a partially hydrogenated multi-ring aromatic compound.

Embodiments of the disclosure provide a system and method for producing a linear alpha olefin. A disulfide, a hydrogen donating compound, and water are combined to produce a mixture. The mixture is introduced to a reactor operated at a pressure equal to or greater than 22.06 MPa and a temperature equal to or greater than 374 deg. C. to produce an effluent stream. The effluent stream is separated to produce a product stream including the linear alpha olefin. The disulfide can be a compound of formula R—S—S—R′ where R is a first alkyl group having carbon atoms ranging from 1 to 12 and R′ is a second alkyl group having carbon atoms ranging from 5 to 12. The hydrogen donating compound can include a partially hydrogenated multi-ring aromatic compound.

A process for producing an upgraded oil blend, the process comprising the steps of introducing the combined stream to a supercritical reactor, wherein a volumetric ratio of water to oil in the combined stream is in the range between 10:1 and 2:1; reacting the combined stream in the supercritical water reactor to produce a reactor effluent, wherein the oil undergoes conversion reactions in the supercritical reactor such that the reactor effluent comprises upgraded bio-oil and upgraded heavy oil; reducing a temperature of the reactor effluent to produce a cooled effluent; operating the soaker to produce a product effluent, wherein a temperature in the soaker is between 250° C. and 350° C., wherein decarboxylation reactions occur in the soaker; and separating the product effluent in the separation unit to produce and the upgraded oil blend, wherein the upgraded oil blend comprises upgraded bio-oil and upgraded heavy oil.

A process for producing an upgraded oil blend, the process comprising the steps of introducing the combined stream to a supercritical reactor, wherein a volumetric ratio of water to oil in the combined stream is in the range between 10:1 and 2:1; reacting the combined stream in the supercritical water reactor to produce a reactor effluent, wherein the oil undergoes conversion reactions in the supercritical reactor such that the reactor effluent comprises upgraded bio-oil and upgraded heavy oil; reducing a temperature of the reactor effluent to produce a cooled effluent; operating the soaker to produce a product effluent, wherein a temperature in the soaker is between 250° C. and 350° C., wherein decarboxylation reactions occur in the soaker; and separating the product effluent in the separation unit to produce and the upgraded oil blend, wherein the upgraded oil blend comprises upgraded bio-oil and upgraded heavy oil.

A facility and a process for hydrotreatment or hydroconversion, in which a fractionation section comprises a stripper which operates on the overhead fraction obtained from a low pressure separator drum.

A facility and a process for hydrotreatment or hydroconversion, in which a fractionation section comprises a stripper which operates on the overhead fraction obtained from a low pressure separator drum.

The present invention relates to an apparatus for the hydroconversion of heavy oil products (the fresh load). Said apparatus comprises: a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle; a stripping column at high pressure and high temperature placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase; lines and means for recirculating the slurry leaving the stripping column; lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor. The stripping column is characterized in that it contains one or more contact devices that allow physical contact to be created between different phases.