A process for treating a plastics pyrolysis oil: a) selective hydrogenation of feedstock in the presence of hydrogen and at least one selective hydrogenation catalyst, at 100 to 150 C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.1, to obtain a hydrogenated effluent; b) hydrotreatment of hydrogenated effluent in the presence of hydrogen and at least one hydrotreatment catalyst, at 250 to 370 C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.1, to obtain a hydrotreatment effluent; c) separation of hydrotreatment effluent obtained from b) in the presence of an aqueous stream, at a temperature of 50 to 370 C., to obtain at least one gaseous effluent, an aqueous liquid effluent and a hydrocarbon liquid effluent.

A method for enabling gas exchange and chemical reactions with one or more liquid streams contained in a reactive process vessel are provided. One or more exchange layers within the process vessel can be composed of both collector media and releaser media. The exchange layers allow elements to facilitate increased performance of vessel operations by promoting gas component mixing and diffusion. Improved rates of gas component exchange mean less coking and more gas components available for reaction.

The present invention relates to producing hydrocarbon products from a polymer feed. In particular, the present invention relates to producing waxes from a polymer feed by pyrolysis and hydrogenation of a fluid product stream from the pyrolysis.

Electrical power derived from a renewable energy source is used to perform water electrolysis to produce oxygen and hydrogen. A flue gas and heat are produced from combustion of a fuel using at least a portion of the oxygen generated by electrolysis. A feed stream including hydrocarbon oil is hydroprocessed using the generated heat and at least a portion of the hydrogen generated by electrolysis to produce a product including a saturated hydrocarbon. At least a portion of the flue gas is hydrogenated using at least a portion of the hydrogen generated by electrolysis to produce a second product stream including a hydrocarbon, an oxygenate, or both.

A multi-phase combination reaction system has at least one fixed bed hydrogenation reactor. The fixed bed hydrogenation reactor has, arranged from top to bottom, a first hydrogenation reaction area, a gas-liquid separation area, a second hydrogenation reaction area and a third hydrogenation reaction area. The gas-liquid separation area is provided with a raw oil inlet. A hydrogen inlet is provided between the second hydrogenation reaction area and the third hydrogenation reaction area. The system is capable of simultaneously obtaining two fractions in one hydrogenation reactor.

The invention relates to a method for producing C2-C4 olefins from methanol and ethanol, said method having the steps of: A) feeding a methanol- and optionally ethanol-containing feed flow A into a dimethyl ether fixed-bed reactor and catalytically reacting methanol to form dimethyl ether, wherein a product flow A1 containing dimethyl ether, methanol, ethanol and steam is obtained; B) mixing the flow A1 with at least one hydrocarbon return flow R containing C2-C6 hydrocarbons and catalytically reacting the mixture in an olefin fixed-bed reactor to form a raw product flow B containing C2-C4 olefins, C5-C6 hydrocarbon and C7+ hydrocarbons; C) cooling the raw product flow B, wherein a hydrocarbon raw product flow C is obtained; D) separating the hydrocarbon raw product flow C in a propylene-containing value product flow, optionally an ethylene-containing value product flow, a butene-containing value product flow, at least one C5-C6 hydrocarbon-containing return flow and at least one C6+ hydrocarbon-containing auxiliary product flow; E) returning a part of the C2-C4 olefins and at least a part of the C5-C6 hydrocarbons as one or more hydrocarbon return flows in step B); F) recovering a propylene-containing value product flow, an ethylene-containing value product flow and optionally a butene-containing value product flow; G) discharging the C6+ hydrocarbon-containing auxiliary product flow; characterised in that the flow A, in relation to methanol and ethanol, contains <1 wt. % or 30 to 50 wt. % ethanol, wherein, in relation to 100 wt. % of the C2-C4 olefins recovered as value products, 30 to 60 wt. % ethylene, 30 to 60 wt. % propylene, and 0 to 30 wt. % butene are recovered as value products, and, in relation to the C2-C4 olefins contained in the raw product flow B, 0 to 40% of the ethylene, 40 to 90% of the propylene, and 0 to 100% of the butene are fed back in step B), or the flow A, in relation to methanol and ethanol, contains 1 to 30 wt. % ethanol, wherein, in relation to 100 wt. % of the C2-C4 olefins recovered as value products, 0 to 20 wt. % ethylene, 70 to 100 wt. % propylene, and 1 to 20 wt. % butene are recovered as value products, and, in relation to the 40 C2-C4 olefins contained in the raw product flow B, 0 to 100% of the ethylene, 0 to 20% of the propylene and 40 to 100% of the butene are fed back in step B).

A multi-zone filtration device for a down-flow catalytic hydroprocessing reactor is disclosed. The filtration device may be used in the petroleum and chemical processing industries in catalytic reactions of hydrocarbonaceous feedstocks in the presence of hydrogen, at an elevated temperature and pressure, to remove contaminants from mixed gas and liquid feedstreams to reactor catalyst beds. The filtration device may be provided as a horizontal installation at the top of a reactor, whereby feedstream liquid is passed through filtration media zones in a radial flow direction. In one zone, the flow is radially outward from the center of a zone of the filtration device to the wall of the reactor. In another zone, the flow is radially inward from the wall of the reactor to the center of a zone of the filtration device. The liquid flows to the reactor catalyst bed after passing through the filtration device. Among the benefits provided are the minimization of scale and small/fine particulates that reach the catalyst bed below the device, reduced pressure drop through the reactor, even when the filter is completely fouled, the potential for added catalyst volume due to the reduced need to use catalyst grading materials, and the improved potential for reduced maintenance needs during reactor operation, e.g., top bed skimming or filtration media replacement, thereby extending the reactor run time length.