Embodiments of methods and apparatuses for hydrotreating hydrocarbons are provided. An exemplary method includes hydrotreating a hydrocarbon feed comprising heating a hydrotreating zone effluent to produce a heated hydrotreating zone effluent. An indirect heat exchange takes place between the heated hydrotreating zone effluent and hydrocarbon feed to provide a heated hydrocarbon feed.

A process for conversion of a hydro-carbonaceous feed including ionic halides to a hydrocarbon product stream by hydrotreatment, wherein the stream is combined with wash water, the weight ratio between wash water and hydrocarbon product stream water is between 1:10 and 10:1, wherein the combined hydrocarbon product stream and wash water are separated in a non-polar stream of hydrocarbon product and a polar stream of wash water including ionic halides, such that from 50% of the ionic halides are transferred from the hydrocarbon product stream to the polar stream of wash water including ionic halides, wherein the polar stream of wash water is directed to a means of concentrating, to provide a stream of purified water and a stream of brine having a concentration of ionic halides being more than 2 times and less than 100 times above that of the polar stream of waste water including ionic halides.

A method of producing aromatic hydrocarbons including: supplying a raw material stream to a C6 separation column, supplying an upper discharge stream from the C6 separation column to a first gasoline hydrogenation unit, and supplying a lower discharge stream from the C6 separation column to a C7 separation column; supplying an upper discharge stream from the C7 separation column to the first gasoline hydrogenation unit and supplying a lower discharge stream from the C7 separation column to a C8 separation column; separating benzene and toluene from a discharge stream from the first gasoline hydrogenation unit; removing a lower discharge stream from the C8 separation column and supplying an upper discharge stream from the C8 separation column to a second extractive distillation column; and separating styrene from a lower discharge stream from the second extractive distillation column and separating xylene from an upper discharge stream from the second extractive distillation column.

A process and apparatus is for recycling LCO and/or HCO to an FCC unit to recover additional distillate. Spent catalyst recycle in the FCC unit may be used to improve distillate yield. A hydroprocessing zone may saturate cycle oil aromatics for cracking in an FCC unit. The recycle cracked stream may be recycled to a downstream hydroprocessing zone to avoid a first hydroprocessing zone for hydrotreating feed to the FCC unit. Additional recovery of cycle oil for recycle is obtained by heating slurry oil prior to vacuum separation.

The invention relates to a process and system arrangement to generate benzene, toluene and xylenes in a refinery. The process relies on recycling a C.sub.9+ aromatic bottoms stream from an aromatic recovery complex back to rejoining a hydrotreated naphtha stream as it enters a catalytic reformer. The aromatic bottoms can be further reacted through both the reformer and the subsequent aromatic recovery complex to transform to higher value compounds, thereby reducing waste or reducing bottoms' presence in gasoline pools.

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

Integrated processes for upgrading crude shale-derived oils, such as those produced by oil shale retorting or by in situ extraction or combinations thereof. Processes disclosed provide for a split-flow processing scheme to upgrade whole shale oil. The split flow concepts described herein, i.e., naphtha and kerosene hydrotreating in one or more stages and gas oil hydrotreating in one or more stages, requires additional equipment as compared to the alternative approach of whole oil hydrotreating. While contrary to conventional wisdom as requiring more capital equipment to achieve the same final product specifications, the operating efficiency vis a vis on-stream time efficiency and product quality resulting from the split flow concept far exceed in value the somewhat incrementally higher capital expenditure costs.

In the hydrocarbon oil production method, mixed oil containing atmospheric residue and deasphalted oil is brought into contact with a demetallizing catalyst in the presence of a hydrogen gas, and the mixed oil subjected to the demetallizing process is brought into contact with a desulfurizing catalyst in the presence of a hydrogen gas. The demetallizing catalyst optionally includes a low-reactivity catalyst. A part of a metallic composition contained in the mixed oil is a decomposable metallic composition. The amount of vanadium in the decomposable metallic composition is x % relative to the amount of vanadium in a whole vanadium-containing compound, the volume of the low-reactivity catalyst is y vol % relative to the total demetallizing catalyst:
0<x100, 0<y≦100, and x−50≦y2.6x−99.

In the hydrocarbon oil production method, mixed oil containing atmospheric residue and deasphalted oil is brought into contact with a demetallizing catalyst in the presence of a hydrogen gas, and the mixed oil subjected to the demetallizing process is brought into contact with a desulfurizing catalyst in the presence of a hydrogen gas. The demetallizing catalyst optionally includes a low-reactivity catalyst. A part of a metallic composition contained in the mixed oil is a decomposable metallic composition. The amount of vanadium in the decomposable metallic composition is x % relative to the amount of vanadium in a whole vanadium-containing compound, the volume of the low-reactivity catalyst is y vol % relative to the total demetallizing catalyst:
0<x100, 0<y≦100, and x−50≦y2.6x−99.

A process for producing hydrocarbons is disclosed in which a first feed substream and a second feed substream are obtained from a hydrocarbonaceous feed stream, of which the first feed substream is converted by means of partial oxidation or autothermal reforming to a first synthesis gas stream and the second feed substream is converted by means of steam reforming to a second synthesis gas stream and subsequently combined with the first synthesis gas stream to give a third synthesis gas stream, of which at least a first portion is converted by Fischer-Tropsch synthesis to a crude product stream comprising hydrocarbons of different chain lengths, from which light hydrocarbons are separated in a tail gas, in order to recycle them and use them in the partial oxidation or autothermal reforming. The characteristic feature here is that unsaturated hydrocarbons are separated from at least a portion of the tail gas.