Uop Lcc

Compañia Española De Petroleos, S.a.u.

Cynthia K Zimmerman

Stephen W Sohn

Jeffrey L Pieper

Gavin Paul Towler

Charles P Luebke

Nathan A Siedler

Peter M Bernard

Steven P Lankton

Jacques Meunier

Leopoldo R Alcázar

Processes using mid-column reboilers in at least one benzene separation columns to reduce the heat duty in alkylation processes are provided. The feed to the aromatics removal zone may exchange heat in a mid-column reboiler in the benzene separation column in the alkylbenzene separation zone followed by exchanging heat in a mid-column reboiler in the benzene separation column in the aromatics removal zone. This arrangement minimizes the hot oil duty on the reboilers in both benzene separation columns.

Heat reduction in alkylation process

Processes for removal of heavy aromatic compounds in an alkylated aromatic compounds production complex is disclosed. The processes includes separating a first component from a second component comprising introducing a feed stream comprising the second component and less than about 5 wt % of the first component to one or more top trays of a prefractionation column. The feed stream is separated in the prefractionation column to provide a prefractionation column overhead stream comprising at least about 50 wt % of the second component present in the feed stream and a prefractionation column bottoms stream. A first portion of the prefractionation columns bottom stream is vaporized by heat exchange with a low temperature fluid stream having a temperature of about 150-200&#xb0; C. in a reboiler and passing the vaporized first portion through the prefractionation column.

Alkylaromatic process with removal of aromatic by-products

An adsorption process using a fractionation column including a drying section is described. The drying section dries the desorbent and removes water from the adsorption process resulting in increased capacity for the adsorbent bed.

Sorption process with added drying section

A process for the dehydrogenation of paraffins is presented. The process utilizes a rapid recycling of dehydrogenation catalyst between the dehydrogenation reactor and the catalyst regeneration unit. The process comprises preheating a combined hydrogen and paraffin hydrocarbon feedstream and passing the combined stream to a dehydrogenation reactor. The hydrocarbon feedstream and the catalyst pass through the reactor at a rate to limit the average residence time of the catalyst in the reactor. The catalyst is cycled to a regeneration unit, and passed through the regeneration unit to limit the average residence time of the catalyst in the regeneration unit.

Reactor flowscheme for dehydrogenation of propane to propylene

A process to reduce flush circulation rates in an adsorption separation system is presented. The flush stream is used to improve the capacity of the simulated moving bed system by flushing the contents of the transfer lines containing raffinate material back into the adsorbent column. The flush stream is a material that is used to flush the head chambers in the column, or from the rotary valve flush dome sealant.

Recycling flush streams in adsorption separation process for energy savings

Embodiments of the present invention provide, for an adsorption separation system for separating normal paraffins from a hydrocarbon feed stream, a process for switching the adsorption separation from a triple split desorbent system to a dual split desorbent system, and vice versa. Switching occurs by separating and/or introducing a second flush material in the adsorption separation system. This switching can occur during normal operations.

Process for separating and/or introducing a flush material in an adsorption separation system

A process and system for separating and saturating benzene from a reforming reactor effluent begins with introducing the reforming reactor effluent to a combined stabilizer and naphtha splitter. An overhead stream comprising light ends, a sidecut stream comprising C4&#x2212; C5 compounds, a bottoms stream comprising C7+ compounds and a heart cut stream comprising C4, C5, C6 compounds including benzene are all removed from the combined stabilizer and naphtha splitter. The heart cut stream is introduced to a side stripper to produce a side stripper overhead stream reduced in benzene and a side stripper bottoms stream enriched in benzene. At least a portion of the side stripper bottoms stream enriched in benzene is introduced into a hydrogenation zone to saturate benzene and generate a hydrogenation zone effluent reduced in benzene. The side stripper overhead stream may be recycled to the combined stabilizer and naphtha splitter.

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Palatine, IL, United States of America

Cynthia K Zimmerman