A process and a system for reforming and upgrading a heavy naphtha feedstock may include dehydrogenating naphthenes in the heavy naphtha feedstock to form a first effluent stream comprising aromatics and then separating the aromatics via extraction from the produced first effluent stream to produce a second effluent stream containing raffinate paraffins. The process may then include subjecting the second effluent stream to cyclization reactions to produce a third effluent stream comprising aromatics and then combining the first effluent stream and the third effluent stream prior to extraction.

A method is described for revamping an ammonia production facility said ammonia production facility having a front end comprising one or more reformers fed with a hydrocarbon feedstock at a hydrocarbon feed stock feed rate and a high-temperature shift reactor fed with a reformed gas obtained from said one or more reformers and containing a fixed bed of iron-containing water-gas shift catalyst, said front end operating at a first steam-to-carbon ratio and a first pressure drop, said method comprising the steps of (i) replacing the iron-containing water-gas shift catalyst with a low-steam water-gas shift catalyst to form a modified front end, (ii) operating the modified front end at a second steam-to-carbon ratio and a second pressure drop, wherein the second steam-to-carbon ratio is at least 0.2 less than the first steam-to-carbon ratio and the second pressure drop is less than the first pressure drop, and (iii) increasing the hydrocarbon feed stock feed rate to said one or more reformers.

A method is described for revamping an ammonia production facility said ammonia production facility having a front end comprising one or more reformers fed with a hydrocarbon feedstock at a hydrocarbon feed stock feed rate and a high-temperature shift reactor fed with a reformed gas obtained from said one or more reformers and containing a fixed bed of iron-containing water-gas shift catalyst, said front end operating at a first steam-to-carbon ratio and a first pressure drop, said method comprising the steps of (i) replacing the iron-containing water-gas shift catalyst with a low-steam water-gas shift catalyst to form a modified front end, (ii) operating the modified front end at a second steam-to-carbon ratio and a second pressure drop, wherein the second steam-to-carbon ratio is at least 0.2 less than the first steam-to-carbon ratio and the second pressure drop is less than the first pressure drop, and (iii) increasing the hydrocarbon feed stock feed rate to said one or more reformers.

The invention relates to hydrocarbon conversion, to equipment and materials useful for hydrocarbon conversion, and to processes for carrying out hydrocarbon conversion, e.g., hydrocarbon pyrolysis processes. The hydrocarbon conversion is carried out in a reactor which includes at least one channeled member that comprises refractory and has an open frontal area≤55%. The refractory can include non-oxide ceramic.

The invention relates to hydrocarbon conversion, to equipment and materials useful for hydrocarbon conversion, and to processes for carrying out hydrocarbon conversion, e.g., hydrocarbon pyrolysis processes. The hydrocarbon conversion is carried out in a reactor which includes at least one channeled member that comprises refractory and has an open frontal area≤55%. The refractory can include non-oxide ceramic.

A method and apparatus for processing a hydrocarbon stream are described. The method includes heating a feed stream in a convective bank. The heated feed stream is reacted in a first reaction zone to form a first effluent, which is heated in a first radiant cell. The first radiant cell combusts fuel to heat the first effluent and forms a first exhaust gas. The first exhaust gas is contacted with the convective bank to heat the feed stream. The outlet temperature the heated feed stream from the convective bank is controlled by introducing an additional gas stream into the convective bank. There can be additional reaction zones and radiant heaters.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Provided in one embodiment is a continuous process for converting waste plastic into recycle for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a pyrolysis oil and optionally wax comprising a naphtha/diesel and heavy fraction, and char. The pyrolysis oil is passed to a refinery FCC unit from which a liquid petroleum gas C.sub.3 olefin/paraffin mixture fraction is recovered, as well as a C.sub.4 olefin/paraffin mixture fraction. The liquid petroleum gas C.sub.3 olefin/paraffin mixture fraction is passed to a steam cracker for ethylene production. The C.sub.4 olefin/paraffin mixture fraction is passed to a refinery alkylation unit, from which a n-butane and naphtha feed for a stream cracker to produce ethylene is recovered.

Provided in one embodiment is a continuous process for converting waste plastic into recycle for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a pyrolysis oil and optionally wax comprising a naphtha/diesel and heavy fraction, and char. The pyrolysis oil is passed to a refinery FCC unit from which a liquid petroleum gas C.sub.3 olefin/paraffin mixture fraction is recovered, as well as a C.sub.4 olefin/paraffin mixture fraction. The liquid petroleum gas C.sub.3 olefin/paraffin mixture fraction is passed to a steam cracker for ethylene production. The C.sub.4 olefin/paraffin mixture fraction is passed to a refinery alkylation unit, from which a n-butane and naphtha feed for a stream cracker to produce ethylene is recovered.

A device (110) for heating a fluid is proposed. The device comprises at least one electrically conductive pipeline (112) and/or at least one electrically conductive pipeline segment (114) for receiving the fluid, and at least one DC current and/or DC voltage source (126), wherein respectively one DC current or DC voltage source (126) is assigned to each pipeline (112) and/or each pipeline segment (114), said DC current and/or DC voltage source being connected to the respective pipeline (112) and/or the respective pipeline segment (114), wherein the respective DC current and/or DC voltage source (126) is embodied to produce an electric current in the respective pipeline (112) and/or in the respective pipeline segment (114), said electric current warming up the respective pipeline (112) and/or the respective pipeline segment (114) by Joule heating, which arises when the electric current passes through conductive pipe material, for the purposes of heating the fluid.