The present invention relates to an integrated hydro-processing reaction vessel which comprises of all the reactor, separator and stabilization sections integrated in a single vessel or system for hydro-processing of low boiling vapour phase hydrocarbon feed; as primary stream undergoing multitude of mass transfer stages with the heavy boiling liquid phase hydrocarbon feed; as secondary stream.

A process for the hydrotreatment of a feed obtained from renewable sources in which the total stream of feed F is divided into a number of different part-streams of feed F1 to Fn equal to the number of catalytic zones n, where n is 1 to 10. The mass flow rate of hydrogen sent to the first catalytic zone represents more than 80% by weight of the total mass flow rate of hydrogen used. The effluent from the reactor outlet undergoes at least one separation step. A portion of the liquid fraction is recycled to the catalytic zones in a manner such that the local recycle ratio for each of the beds is 2 or less, and the local dilution ratio over each of the beds is less than 4.

Systems and methods are provided for fixed bed hydroprocessing of deasphalter rock. Instead of attempting to process vacuum resid in a fixed bed processing unit, vacuum resid is deasphalted to form a deasphalted oil and deasphalter residue or rock. The rock can then be hydroprocessed in a fixed bed reaction zone, optionally after combining the rock with an aromatic co-feed and/or a hydroprocessing solvent. This can allow for improved conversion of the deasphalter rock and/or improved combined conversion of the deasphalter rock and deasphalted oil.

Vapor and liquid flow concurrently down through a vertical vessel. A horizontal scale collection and predistribution tray is located in the vessel to remove solid contaminants and to redistribute the liquid to a fine distribution tray. The scale collection and predistribution tray consists of a tray plate with a scale collection zone where the solid contaminants settle and deposit. In one embodiment, an upstanding permeable wall forms the scale collection zone, and liquid is filtered as it flows through the permeable wall, leaving the solid contaminants trapped upstream from the permeable wall. The predistribution tray has a rim provided with a slotted weir. Liquid from the scale collection zone forms a liquid level in a trough located between the permeable wall and the weir. Due to the uniform liquid level in the trough, liquid flow rates through the slots in the weir are nearly equal. Because of the polygonal shape of the tray, the liquid exits the slots in a direction along lanes defined between distribution units on the fine distribution tray, and the amount of liquid entering the vapor inlets of the distribution units is therefore small. Vapor by-passes the scale collection and pre-distribution tray through the area between the reactor wall and the permeable wall, and through the area between the reactor wall and the weir to the fine distribution tray. The scale collection and predistribution tray protects the fine distribution tray and the catalyst bed from fouling, pre-distributes liquid to the fine distribution tray to minimize level gradients on this tray, and reduces flow velocities to ensure calm flow conditions on the fine distribution tray.

An apparatus for converting heavy hydrocarbons to light hydrocarbons includes an inlet capable of supplying a pre-foaming mixture comprising a hydrocarbon to be processed and a processing gas, wherein the processing gas is dissolved in the hydrocarbon to be processed; a foam generator configured to receive the pre-foaming mixture at a first pressure, compress the pre-foaming mixture to a second pressure that is higher than the first pressure by routing it through a nozzle; and generate a foam by allowing the pre-foaming mixture at the second pressure to expand in a chamber at a third pressure that is lower than the first or second pressures; a plasma reactor, wherein the plasma reactor is capable of receiving the foam and comprises at least one pair of spark gap electrodes capable of subjecting the foam to a plasma discharge to yield a processed mixture; and an outlet capable of receiving the processed mixture.

The present invention relates to a process for producing olefins from a hydrocarbon feedstock 11 having a sulfur content of at least 0.1 weight %, an initial boiling point of at least 180 C. and a final boiling point of at least 600 C.

Systems and methods are provided for hydroprocessing of bio-derived feeds, such as bio-oils and/or other types of feeds including triglycerides, fatty acids, and/or fatty acid derivatives. The systems and methods can assist with maintaining a desired temperature profile within a reactor while performing hydroprocessing on a feed with substantial oxygen content. In various aspects, the initial bed of the reactor can be exposed to 30 vol % or less of the total fresh feed. The remaining portions of the fresh feed can be introduced below one or more of the catalyst beds in the reactor. By reducing or minimizing the amount of fresh feed introduced upstream from the initial catalyst bed that contains a catalyst with hydrodeoxygenation activity, the net amount of product recycle can be reduced or minimized while still maintaining a target temperature profile across individual catalyst beds and/or across the reactor.

A process and a process plant for production of a hydrocarbon composition useful as a transportation fuel from a hydrocarbonaceous feedstock, including the steps of a. directing a hydrocarbonaceous feedstock to hydrotreatment in one or more steps providing an intermediate product including less than 0.1 wt % oxygen and a specific gravity, for the fraction boiling in the range defined by the commercial transportation fuel specification, above the upper limit of specific gravity under the commercial transportation fuel specification, b. providing a hydrotreated hydrocarbon stream for hydroconversion from the intermediate product, wherein a fraction for hydroconversion has a T50 being below T95 of the commercial transportation fuel specification, c. directing the stream for hydroconversion to contact a hydroconversion catalyst under hydroconversion conditions to provide a hydroconverted hydrocarbon stream, d. fractionating said hydroconverted hydrocarbon stream to provide at least said hydrocarbon composition useful as a transportation fuel.

A fluid mixer for a reactor of a hydrocarbon processing plant includes a substantially cylindrical mixing chamber, at least one first inlet for conducting first fluid to the mixing chamber from above the mixing chamber and along a side wall of the mixing chamber to produce a spiral stream in the mixing chamber, at least one second inlet for conducting second fluid tangentially into the spiral stream, and an outlet channel for conducting the first and second fluids downwards out from the mixing chamber. The outlet channel is concentric to the mixing chamber and includes a mixing structure for enhancing mixing of the first and second fluids. At least a part of the mixing structure is located below an upper edge of the outlet channel and produces turbulence in a stream of the first and second fluids flowing in the outlet channel.

The invention relates to a process for treating a plastics and/or solid recovery fuel pyrolysis oil, comprising: a) optionally, selective hydrogenation of the feedstock; b) hydroconversion in an ebullated bed, in an entrained bed and/or in a moving bed, to obtain a hydroconverted effluent; c) hydrotreatment of said hydroconverted effluent from step b) to obtain a hydrotreated effluent, without any intermediate separation step between steps b) and c), c) optionally, hydrocracking of said effluent from step c), c) separation of the effluent from step c) or c) in the presence of an aqueous stream, to obtain a gaseous effluent, an aqueous liquid effluent and a liquid hydrocarbon effluent; d) optionally a fractionation to obtain at least one gas stream and one cut with a boiling point of less than or equal to 175 C. and one cut with a boiling point of greater than 175 C.