Methods and apparatuses for processing hydrocarbons are provided. In one embodiment, a method for processing a hydrocarbon stream including lighter hydrocarbons and heavier hydrocarbons includes hydrocracking the lighter hydrocarbons in a hydrocracking reactor. After hydrocracking the lighter hydrocarbons, the method hydrocracks the heavier hydrocarbons in the hydrocracking reactor. The method includes removing from the hydrocracking reactor a hydrocracking effluent comprising a mixture of components formed by hydrocracking the lighter hydrocarbons and hydrocracking the heavier hydrocarbons.

The present invention relates to a process for producing benzene comprising the steps of: a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and alkylbenzenes into a first feedstream comprising a higher proportion of benzene than the source feedstream and a second feedstream comprising a lower proportion of benzene than the source feedstream and subsequently, b) contacting the first feedstream in the presence of hydrogen with a first hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under first process conditions to produce a first product stream comprising benzene, wherein the first process conditions include a temperature of 425-580 C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h.sup.1, and c) contacting the second feedstream with hydrogen under second process conditions to produce a second product stream comprising benzene, wherein i) the second process conditions are suitable for hydrocracking and step (c) involves contacting the second feedstream in the presence of hydrogen with a second hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under the second process conditions which include a temperature of 300-600 C., a pressure of 300-5000 kPa gauge and a Weight Hourly space Velocity of 0.1-15 h.sup.1, ii) the second process conditions are suitable for toluene disproportionation and involve contracting the second feedstream with a toluene disproportionation catalyst, or iii) the second process conditions are suitable for hydrodealkylation.

Embodiments herein relate to a process flow scheme for the processing of gas oils and especially reactive gas oils produced by thermal cracking of residua using a split flow concept. The split flow concepts disclosed allow optimization of the hydrocracking reactor seventies and thereby take advantage of the different reactivities of thermally cracked gas oils versus those of virgin gas oils. This results in a lower cost facility for producing base oils as well as diesel, kerosene and gasoline fuels while achieving high conversions and high catalyst lives.

Embodiments herein relate to a process flow scheme for the processing of gas oils and especially reactive gas oils produced by thermal cracking of residua using a split flow concept. The split flow concepts disclosed allow optimization of the hydrocracking reactor seventies and thereby take advantage of the different reactivities of thermally cracked gas oils versus those of virgin gas oils. This results in a lower cost facility for producing base oils as well as diesel, kerosene and gasoline fuels while achieving high conversions and high catalyst lives.

Hydrocarbon oil obtained by Fischer-Tropsch (FT) synthesis reaction using a catalyst within a slurry bed reactor is fractionated into a distilled oil and a column bottom oil in a rectifying column, part of the column bottom oil is flowed into a first transfer line that connects a column bottom of the rectifying column to a hydrocracker, at least part of the column bottom oil is flowed into a second transfer line branched from the first transfer line and connected to the first transfer line downstream of the branching point, the amount of the catalyst fine powder to be captured is monitored while the catalyst fine powder in the column bottom oil that flows in the second transfer line are captured by a detachable filter provided in the second transfer line, and the column bottom oil is hydrocracked within the hydrocracker.

The present invention relates to a process for upgradation of cracked residual hydrocarbons. More specifically, the present invention relates to a process for upgradation of cracked residual hydrocarbons into distillates in the presence of a catalyst in a slurry hydrocracking reactor (7). The slurry hydrocracking reactor (7) maximizes the conversions of hydrocarbons to distillate products and reduces the bottom unconverted fraction. The slurry hydrocracking reactor (7) enhances residue conversions to greater than 97% with reduced purge.

The present invention relates to a process for upgradation of cracked residual hydrocarbons. More specifically, the present invention relates to a process for upgradation of cracked residual hydrocarbons into distillates in the presence of a catalyst in a slurry hydrocracking reactor (7). The slurry hydrocracking reactor (7) maximizes the conversions of hydrocarbons to distillate products and reduces the bottom unconverted fraction. The slurry hydrocracking reactor (7) enhances residue conversions to greater than 97% with reduced purge.