A process for forming a petroleum product includes introducing a feed stream of a petroleum feedstock to a supercritical water reactor. The feed stream is reacted with supercritical water in the supercritical water reactor, thereby forming a supercritical water reactor effluent. The supercritical water reactor effluent is introduced to a separator to separate the supercritical water reactor effluent into a light stream and a heavy stream. At least a portion of the light stream is introduced to a reformer to concentrate aromatics in the at least a portion of the light stream, thereby forming a reformer effluent. The reformer effluent is mixed with the heavy stream.

A process for forming a petroleum product includes introducing a feed stream of a petroleum feedstock to a supercritical water reactor. The feed stream is reacted with supercritical water in the supercritical water reactor, thereby forming a supercritical water reactor effluent. The supercritical water reactor effluent is introduced to a separator to separate the supercritical water reactor effluent into a light stream and a heavy stream. At least a portion of the light stream is introduced to a reformer to concentrate aromatics in the at least a portion of the light stream, thereby forming a reformer effluent. The reformer effluent is mixed with the heavy stream.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

In some examples, a vapor phase product and a liquid phase product can be separated from a heated mixture that can include steam and a hydrocarbon. The liquid phase product can be catalytically cracked in the presence of a fluidized catalyst to produce a catalytically cracked effluent. A bottoms product can be separated from the catalytically cracked effluent. The bottoms product can be hydroprocessed to produce a hydroprocessed product. For example, the bottoms product can be hydroprocessed under pre-treater hydroprocessing conditions to produce a pre-treated bottoms product and the pre-treated bottoms product can be hydroprocessed under bottoms product hydroprocessing conditions to produce the hydroprocessed product. A hydroprocessor heavy product can be separated from the hydroprocessed product. The vapor phase product can be steam cracked to produce a steam cracker effluent. A tar product and an upgraded steam cracker effluent can be separated from the steam cracker effluent.

A processing facility is provided that includes a feedstock separation system configured to separate a feed stream into a lights stream and a heavies stream, a hydrogen production system configured to produce hydrogen and carbon dioxide from the lights stream, and a carbon dioxide conversion system configured to produce synthetic hydrocarbons from the carbon dioxide. The processing facility includes a hydroprocessing system configured to process the heavies stream.

Processes and apparatus for preparing a liquid hydrocarbon product are provided. In one embodiment, a process for prepreparing a liquid hydrocarbon product includes thermally-treating a tar to produce a first tar composition and blending the tar composition with a utility fluid to form a tar-fluid mixture. The process includes separating the tar-fluid mixture to form a first lower-density portion and a first higher-density portion containing solids. The process further includes thermally-treating the first higher-density portion to form a thermally-treated first higher-density portion to convert at least a portion of the solids to liquid.

Processes and apparatus for preparing a liquid hydrocarbon product are provided. In one embodiment, a process for prepreparing a liquid hydrocarbon product includes thermally-treating a tar to produce a first tar composition and blending the tar composition with a utility fluid to form a tar-fluid mixture. The process includes separating the tar-fluid mixture to form a first lower-density portion and a first higher-density portion containing solids. The process further includes thermally-treating the first higher-density portion to form a thermally-treated first higher-density portion to convert at least a portion of the solids to liquid.

A process for producing a hydrocarbon stream with reduced CS.sub.2 content, comprising contacting a hydrocarbon stream containing CS.sub.2 with a solid reactive CS.sub.2-scavenger which contains primary and/or secondary amino group-bearing hydrocarbon residues attached to a solid support, at a temperature in the range of from 0 to 300° C., and separating the obtained reaction product of and reactive CS.sub.2-scavenger from the hydrocarbon stream.

Systems and methods are provided for integration of a reactor for polyolefin pyrolysis with the effluent processing train for a steam cracker. The polyolefins can correspond to, for example, polyolefins in plastic waste. Integrating a process for polyolefin pyrolysis with a steam cracker processing train can allow a mixture of polymers to be converted to monomer units while reducing or minimizing costs and/or equipment footprint. This can allow for direct conversion of polyolefins to the light olefin monomers in high yield while significantly lowering capital and energy usage due to integration with a steam cracking process train. The integration can be enabled in part by selecting feeds with appropriate mixtures of various polymer types and/or by limiting the volume of the plastic waste pyrolysis product relative to the volume from the steam cracker(s) in the steam cracking process train. By selecting plastic waste and/or other polyolefin sources with an appropriate mixture of polyolefins as the feedstock, the resulting polyolefin pyrolysis product can be separated in a steam cracking process train to produce separate fractions for various polymer grade small olefin products.