Provided is a continuous process for converting waste plastic into recycle for polypropylene 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 naphtha/diesel fraction, a heavy fraction, and char. Pyrolysis oil and wax, comprising naphtha/diesel and heavy fractions, is passed to a refinery FCC unit. A liquid petroleum gas C.sub.3 olefin/paraffin mixture is recovered from the FCC unit. The C.sub.3 paraffins and C.sub.3 olefins are separated into different fractions with the C.sub.3 olefin fraction passed to a propylene polymerization reactor, and the C.sub.3 paraffin fraction passed optionally to a dehydrogenation unit to produce additional propylene.

A two-step process that includes a pyrolytic first step carried out in a mechanically or gravitationally impelled reactor and a catalytic fluid bed second step that upgrades the resulting vapor, for the conversion of waste plastics, polymers, and other waste materials to useful chemical and fuel products such as paraffins, olefins, and aromatics such as BTX is described.

A metal trap for an FCC catalyst include pre-formed microspheres impregnated with an organic acid salt of a rare earth element.

A metal trap for an FCC catalyst include pre-formed microspheres impregnated with an organic acid salt of a rare earth element.

A microspherical fluid catalytic cracking (FCC) catalyst includes Y zeolite and a gamma-alumina.

A microspherical fluid catalytic cracking (FCC) catalyst includes Y zeolite and a gamma-alumina.

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into light and heavy fractions utilizing convection heat from heaters used in steam cracking. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize either an ebullated bed reactor with extrudate catalysts or a slurry hydrocracking reactor using a homogeneous catalyst system, such as a molybdenum based catalysts which may optionally be promoted with nickel. Products from the upgrading operations can be finished olefins and/or aromatics, or, for heavier products from the upgrading operations, may be used as feed to the steam cracker.

Methods for catalytic cracking hydrocarbon mixture have been disclosed. A hydrocarbon mixture having an initial boiling temperature of 30° C. to 70° C. is catalytically cracked in the presence of a catalyst to produce one or more olefins and/or one or more aromatics. The catalytic cracking is conducted such that the amount of coke formed on the catalyst is at least 5 wt. % (based on total weight of spent catalyst). The catalyst from the catalytic cracking step is then regenerated to produce regenerated catalyst.

The present disclosure relates to a device for directing a coking-prone liquid to a high temperature environment, where the device includes an inner tube positioned concentrically within an outer tube, creating a first annular space between an outer wall of the inner tube and an inner wall of the outer tube and a first intermediate tube positioned concentrically around the outer tube, creating a second annular space.

The present disclosure relates to a device for directing a coking-prone liquid to a high temperature environment, where the device includes an inner tube positioned concentrically within an outer tube, creating a first annular space between an outer wall of the inner tube and an inner wall of the outer tube and a first intermediate tube positioned concentrically around the outer tube, creating a second annular space.