A process for hydrocracking a hydrocarbon feed is provided. The process comprises hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream, separating the first hydrocracking product stream to form a gas stream and a liquid stream, hydrocracking the liquid stream to produce a second hydrocracking product stream, separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C.sub.9+ hydrocarbon, or a combination comprising at least one of the foregoing, purifying the gas stream to form a purified gas stream, and separating the purified gas stream to form at least two of a hydrogen stream, C.sub.1 stream, C.sub.2 stream, C.sub.3 stream, C.sub.4 stream, C.sub.5+ stream, or a combination comprising at least one of the foregoing.

The present invention relates to a process for converting the waste plastic along with the petroleum residue feedstock in a Delayed Coker unit employed in refineries. The invented process aims to convert any type of waste plastic including polystyrene, polypropylene, polyethylene etc. including metal additized multilayer plastics along with the petroleum residue material from crude oil refining such as reduced crude oil, vacuum residue etc. Value added light distillate products like motor spirit, LPG, middle distillates etc. are produced upon co-conversion in the invented process and is recovered and treated along with the products of thermal cracking of hydrocarbon residues. The residual metals in the metal additized plastics upon co-conversion in the invented process will be deposited in the solid petroleum coke.

The present invention relates to the extraction of gasoline from a gas G, with (a) a step of extracting gasoline from the gas to be treated comprising methanol GM obtained from step (d), (b) a step of separating said fluid GL1 partially condensed in step (a), producing a first aqueous liquid phase Al , a first liquid phase H1 of hydrocarbon(s) a gaseous phase G1 obtained from the gas G; (c) a step of contacting a portion of the gas G to be treated with said first aqueous liquid phase A1, producing a second aqueous liquid phase A2, a gaseous phase of gas to be treated comprising methanol GM; (d) a step of mixing said gaseous phase of gas to be treated comprising methanol GM with the remainder of the gas G to be treated, producing a gas to be treated comprising methanol GM, (e) a step of stabilizing said first liquid phase H1 of hydrocarbon(s).

The present invention relates to a process for the conversion of a feedstock comprising at least 50 wt % related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into hydrogen, olefins, dienes, aromatics, gasoline, diesel fuel, jet fuel, naphtha and liquefied petroleum gas comprising: a) introducing of said feedstock in a first reactor to produce linear paraffins in presence of a hydrodesulfurization catalyst and hydrogen, b) separating the effluent of said first reactor in at least three parts to produce at least a first stream comprising part of said linear paraffins and at least a second stream comprising part of said linear paraffins, and at least a third stream comprising part of said linear paraffins c) sending said first stream to a steam cracker to produce hydrogen, olefins, dienes, aromatics and gasoline, diesel fuel being further fractionated; d) introducing said second stream into a second reactor in presence of a hydrocracking or hydroisomerization catalyst to produce a mixture comprising diesel fuel, jet fuel, naphtha and liquefied petroleum gas being further fractionated e) blending said third stream with the diesel fuel obtained at said step d)
wherein said feedstock of said first reactor is diluted in order to limit the temperature increase within said first reactor; and wherein before entering the first reactor said dilution is performed with a weight ratio diluent:feedstock being 1:1, and wherein said diluent comprises at least part of said paraffins obtained at step b).

Treatment of hydrocarbon streams, and in one non-limiting embodiment refinery distillates, with reducing agents, such as borohydride and salts thereof, alone or together with at least one co-solvent results in reduction of the sulfur compounds such as disulfides, mercaptans, thiophenes, and thioethers that are present to give easily removed sulfides. In one non-limiting embodiment, the treatment converts the original sulfur compounds into hydrogen sulfide or low molecular weight mercaptans that can be extracted from the distillate with caustic solutions, hydrogen sulfide or mercaptan scavengers, solid absorbents such as clay or activated carbon or liquid absorbents such as amine-aldehyde condensates and/or aqueous aldehydes.

The present disclosures and inventions relate to a catalyst composition for the selective conversion of a hydrogen/carbon monoxide mixture (syngas) to C2+ hydrocarbons.

The present disclosure relates to an additive and a catalyst composition for a catalytic cracking process of vacuum gas oil for preparing cracked run naphtha having reduced liquid olefin content, and increased propylene and butylene yields in the LPG fraction. The process makes use of a catalyst composition which is a mixture of an FCC equilibrated catalyst and an additive comprising a zeolite, phosphorus and a combination of metal promoters. The process is successful in achieving high propylene and butylene yields in the LPG fraction along with a lower liquid olefin content and increased aromatic content with increase in RON unit in the resultant cracked run naphtha, as compared to that achieved using an FCC equilibrated catalyst alone.

This invention describes a novel and efficient processing scheme that can be used to transform a vacuum residue feedstock into 0.5 wt % sulfur bunker fuel that fulfills the specifications required by the International Maritime Organization (IMO).

Method of producing hydrocarbon fuels from polyolefin waste materials, wherein: polyolefin waste materials are subjected to continuous depolymerisation in a tower flow reactor with a movable packing, which comprises a heating system for heating the lower half of the reaction chamber, where products of depolymerisation are collected in a gaseous state through an outlet in the upper half of the reaction chamber; and the obtained products of depolymerisation are subjected to catalytic hydrogenation and isomerization in an atmosphere of synthesis gas, under atmospheric pressure, to obtain a mixture of hydrocarbon fuels; characterised in that: polyolefin waste materials are mixed with heated elements constituting the packing of the reactor until the surface of the packing elements is coated with a thin layer of plasticised material, wherein in the depolymerisation process that obtained mixture is fed as a stream into the reaction chamber from the top of the chamber, whereas a synthesis gas is fed in a counter current from the bottom, the gas comprising carbon monoxide (CO) and hydrogen (H.sub.2) with the molar ratio CO:H.sub.2 being from 0.25 to 1.5: from 0.5 to 3.

Direct conversion of syngas produces liquid fuels and light olefins. The catalytic reaction is conducted on a fixed bed or a moving bed. The catalyst comprises A and B components. The component A is composed of active metal oxides, and the active ingredients of the component B are zeolites with a MEL structure. The distance between the geometric centers of catalyst A and catalyst B particles is 2 nm-10 mm; a weight ratio of the catalyst A to the catalyst B is 0.1-20. The pressure of the syngas is 0.1-10 MPa; reaction temperature is 300-600 C.; and space velocity is 300-10000 h.sup.1. The reaction mainly produces gasoline with high octane number, and co-generates light olefins. Meanwhile, the selectivity for a methane byproduct is low (less than 10%).