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Clayton Colin Sadler

Mark D Moser

Michael Jerome Vetter

Mary Jo Wier

Charles P Luebke

David A Wegerer

Manuela Serban

Laurence O Stine

Christopher Naunheimer

Bryan James Egolf

Christian D Freet

Paolo Palmas

Peter Kokayeff

Vasant P Thakkar

Mark Paul Lapinski

Rajeswar R Gattupalli

Kenneth David Peters

Daniel Robert Johnson

Christopher D DiGiulio

Quan Yuan

Vedula Kasipati Murty

Gregory J Gajda

Xin X Zhu

Christopher D Gosling

David James Shecterle

Steven Lee Krupa

Matthew Lippmann

Kurt M VandenBussche

Louis A Lattanzio

Elizabeth Carter

Matthew C Cole

Tokhanh Ngo

Gregory James Nedohin

Keyur Y Pandya

Mohamed Sami Elganiny

Vedula K Murty

Catalysts and processes for a selective conversion of hydrocarbons. The catalyst comprises: a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; and a support forming a catalyst particle comprising a plurality of pores. The catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle.

Dehydrogenation catalyst with optimum modifier profile index

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500&#xb0;-645&#xb0; C.

Dehydrogenation process at reduced hydrogen to hydrocarbon ratios

An apparatus for heating a process fluid is presented. The apparatus is for improving the foot-print of a fired heater and to reduce the fired heater volume. The apparatus includes a W-shaped process coil to provide for a smaller single-cell fired heater, and a fired heater with a lower profile, providing flexibility in positioning relative to downstream reactors.

Reactor and heater configuration synergies in paraffin dehydrogenation process

A process for cleaning a reactor, the reactor comprising a shell including catalyst for selectively converting hydrocarbons. The process includes removing catalyst from the reactor and deploying a robot into the reactor. A cleaner from the robot is applied onto a surface within the shell of the reactor that includes a foulant. The cleaner is adapted to remove the foulant from the surface within the shell of the reactor. The cleaner may be one of light radiation, heat radiation, ultra-high pressure fluid, and liquid nitrogen.

Process for removing foulants from reactor internal spaces

Large pill dehydrogenation catalysts and large screens slot width are combined in dehydrogenation units to reduce the pressure drop across the catalyst bed and reactor screens compared to conventional screen and catalyst size combinations. The catalyst has an average pill diameter in the range of 1.6 mm to 3.0 mm, and the slot width of the screen is in the range of about 30% to about 60% of the pill diameter.

Dehydrogenation process

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500&#xb0;-645&#xb0; C. The process uses a low coke catalyst.

A process and apparatus uses a flash drum to separate light hydrocarbons from heavy oligomerate from an oligomerization zone. The heavy oligomerate can bypass a fractionation column in the oligomerate recovery section and be recycled to the oligomerization zone or other zones. Costs are saved by avoiding repeatedly transporting and processing the heavier recycled oligomerate.

Process and apparatus for recovering oligomerate

A process for adsorbing hydrogen chloride (HCl) from a regeneration vent gas. The regeneration vent gas is cooled from a catalyst regeneration zone. The cooled regeneration vent gas is passed to an adsorption zone that is spaced apart from the catalyst regeneration zone. HCl from the regeneration vent gas is adsorbed onto a sorbent in the adsorption zone to enrich the sorbent with HCl to provide HCl-rich sorbent and deplete HCl from the regeneration vent gas to provide HCl-lean regeneration vent gas. HCl-lean regeneration vent gas is purged as an effluent gas. HCl-rich sorbent is passed from the adsorption zone to a sorbent regeneration zone. HCl from the HCl-rich sorbent in the sorbent regeneration zone is desorbed to provide a regenerated sorbent. The regenerated sorbent is transferred to the adsorption zone.

Process for adsorbing hydrogen chloride from a regeneration vent gas

Embodiments of a hydrocarbon conversion apparatus are provided, as are embodiments of a hydroprocessing conversion process. In one embodiment, the hydrocarbon conversion apparatus includes a reaction vessel having a reaction chamber and a feed distribution chamber. A riser fluidly couples the feed distribution chamber to the reaction chamber, and a catalyst recirculation standpipe fluidly couples the reaction chamber to the feed distribution chamber. The catalyst recirculation standpipe forms a catalyst recirculation circuit with the reaction chamber, the feed distribution chamber, and the riser. A catalyst is circulated through the catalyst recirculation circuit during operation of the hydrocarbon conversion apparatus.

Hydrocarbon conversion apparatus including fluid bed reaction vessel and related processes

Process for adsorbing a species from a feed gas stream. Feed gas stream is introduced to an adsorption zone having a sorbent. Species from the feed gas stream is adsorbed onto the sorbent at an adsorbing temperature to enrich the sorbent with the species and deplete the species from the feed gas stream. Species-lean product gas stream is output. Species-rich sorbent from the adsorption zone is passed to a regeneration zone. Regenerant gas at a regenerating temperature greater than the adsorbing temperature is introduced into the regeneration zone to strip the species from the species-rich sorbent. Regenerated sorbent from the regeneration zone passes to a cooling zone disposed below the regeneration zone. Regenerated sorbent is cooled at a cooling temperature below the regenerating temperature. Cooled sorbent is transferred to the adsorbent zone.

Moving bed temperature swing adsorption process

A process and apparatus that uses a debutanizer with a side stripper can recover a light stream, an intermediate stream and a liquid stream. One of the intermediate stream and the liquid stream can be recycled to oligomerization or to fluid catalytic cracking.

Apparatus for recovering oligomerate

A process and apparatus is provided to produce desulfurized diesel at low pressure with high cetane rating. A hydrotreated stream is stripped and fed to a saturation reactor. The saturated stream is stripped again and fractionated to provide diesel product. Unconverted oil may be hydrocracked and stripped with the saturated product.

Process and apparatus for producing diesel with high cetane

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Arlington Heights, IL, United States of America

Clayton Colin Sadler