Chevron Phillips Chemical Company LP

David W Dockter

Max P McDaniel

Tin-Tack Peter Cheung

Joseph Bergmeister, Iii

Kathy S Clear

Scott G Morrison

Vincent D McGahee

Bruce D Murray

Steven R Horlacher

Reza Khankal

Kenneth Fountain

Ted H Cymbaluk

Dennis L Holtermann

Timothy O Odi

Zongxuan Hong

Anand Ramanathan

Robert L Hise

Christopher D Blessing

Geoffrey E Scanlon

Lawrence E Huff

Jennifer L Nill

Thomas J Gonzales

Charles D Nolidin

Zhihui Gu

Taryn L Huber

Julian Abrego

Marlon L Jordan

Ravindranath Koyyalagunta

Processes for producing activated chromium catalysts such as chromium/silica catalysts and titanated chromium/silica catalysts are disclosed, and these processes utilize a multistep process involving exposure to inert and oxidizing atmospheres at specific temperature conditions. The resulting activated chromium catalysts have unexpectedly high melt index potential and can produce ethylene-based polymers with lower gel counts in addition to higher melt indices. Related activation systems are provided in which the fluidizing gas entering the fluidized bed vessel can be adjusted between an inert gas, an oxygen-containing gas, or a mixture of the inert gas and the oxygen-containing gas to minimize or prevent exotherms.

Systems and methods for chromium catalyst activation

Processes for producing activated chromium catalysts such as titanated chromium/silica catalysts are disclosed, and these processes utilize a multistep process involving exposure to inert and oxidizing atmospheres at specific temperature conditions. The resulting activated chromium catalysts have unexpectedly high melt index potential and can produce ethylene-based polymers with lower gel counts in addition to higher melt indices.

Methods of chromium catalyst activation to reduce gels and improve melt index potential

Pyrolysis processes comprise contacting a waste polyolefin with a solid catalyst at a pyrolysis temperature to form a pyrolysis product containing C-Chydrocarbons. In some instances, the solid catalyst can be a silica-coated alumina, a fluorided silica-coated alumina, or a sulfated alumina, while in other instances, the solid catalyst can be any suitable solid oxide or chemically-treated solid oxide that is characterized by a d50 average particle size from 5 to 12 μm and a particle size span from 0.7 to 1.7. Hydrocarbon compositions are formed from the pyrolysis of waste polyolefins with specific amounts of methane and higher carbon number hydrocarbons.

Solid oxide and chemically-treated solid oxide catalysts for the pyrolysis of polyethylene

A system for processing plastic waste may include a feed line, a feed fractionator, a hydrotreater, a catalytic reforming unit, a heavy oil cracker, and a steam cracker. A pyrolyzed plastics feed is separated into light, medium, and heavy hydrocarbon streams. The hydrotreater removes sulfur, and the catalytic reforming unit produces a circular aromatic-rich stream. The heavy oil cracker generates cracked streams. The steam cracker produces a circular olefin stream from a cracked stream. A system for processing plastic waste may include the feed line, the feed fractionator, the hydrotreater, a medium hydrocarbon fractionator, the catalytic reforming unit, a full-range reforming unit, the heavy oil cracker, and the steam cracker. The medium hydrocarbon fractionator produces two hydrocarbon streams. The full-range naphtha reforming unit produces a second circular aromatic-rich stream.

Systems and processes for processing pyrolysis oil

A process includes hydrogenating, in a reaction zone, a highly unsaturated hydrocarbon received from a hydrocarbon stream to yield a product having an unsaturated hydrocarbon, the hydrogenating step occurring in the presence of a hydrogenation catalyst which has a selectivity for conversion of the highly unsaturated hydrocarbon to the unsaturated hydrocarbon of about 90 mol % or greater based on the moles of the highly unsaturated hydrocarbon which are converted to the product, the hydrogenating step occurring in a reaction zone under conditions which include a flow index (I) in a range of about 0.09 to about 35, wherein the Iis defined as: wherein F is the flow rate of the hydrocarbon stream into the reaction zone in units of kg/h, [CO] is the concentration of carbon monoxide in the hydrocarbon stream in units of mol %, and V is the volume of the reaction zone in units of ft.

Selective hydrogenation using a flow index

A method of removing a metal protective layer from a surface of a reactor component comprising treating the metal protective layer with one or more chemical removal agents to remove at least a portion of the metal protective layer from the reactor component. A method of removing a metal protective layer from a surface of a reactor component comprising treating the metal protective layer to remove the metal protective layer from the reactor component, and determining a thickness of the reactor component following treatment.

Methods of removing a protective layer

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Kingwood, TX, United States of America

David W Dockter