Exxonmobil Chemical Patents Inc.

Paul Hamilton

Stephen Harold Brown

Georges M K Mathys

John Stephen Godsmark

Terrance C Osby

Georges Marie Karel Mathys

Geraldine Tosin

Marc P H Puttemans

Brian W Heins

Jihad Mohammed Dakka

Keith Holroyd Kuechler

Raphael Frans Caers

Marcel J G Janssen

Eddy Theophile Van Driessche

Hans K T Goris

Michael Louis Hergenrother

Robert Piszczek

Yeo-Meng Lim

Mechilium J G Janssen

David E Heather

Jason A Nichols

Zhongcheng Wang

Dion Zhang

Many linear alpha olefin (LAO) syntheses form a range of LAO products when oligomerizing ethylene in the presence of a Ziegler-type catalyst. The range of products typically requires a plurality of distillation columns to separate the LAO products up to a desired carbon count, but such approaches may be energy- and capital-intensive. LAO product separation using at least one dividing wall column may lessen these burdens. Methods for separating LAOs may comprise: providing a pre-processed product stream comprising Cg+ linear alpha olefins (LAOs) to a first of a series of distillation columns, at least one member of the series of distillation columns comprising a dividing wall column; and separating an overhead stream comprising a first LAO from the dividing wall column and one or more side streams from the dividing wall column, each side stream comprising a different LAO that also differs from the first LAO.

Process for the separation of linear alpha-olefins using a dividing wall column

Linear alpha olefins (LAOS) may be formed by oligomerization of ethylene in the presence of a Ziegler-type catalyst. The presence of trace water during oligomerization can result in unwanted formation of insoluble higher oligomers or polymer. Methods for limiting the presence of water during ethylene oligomerization reactions may include separating residual ethylene and 1-butene from an LAO product stream to form a higher LAO-enriched stream comprising CLAOs, separating 1-hexene as an overhead stream from the higher-LAO enriched stream using a first distillation column, obtaining separated solvent as a side stream from the first distillation column or as a side stream from a first of one or more downstream distillation columns, and returning the separated solvent to a reactor in a recycled solvent stream. The recycled solvent stream passes through one or more driers before returning to the reactor.

Methods for limiting water in recycled solvent during linear alpha olefin syntheses

Embodiments of an invention disclosed herein relate to particles made from zeolite catalysts and their use in oligomerization processes. In particular, shaped particles (for example, spheroid particles) are made from compositions including the contact product of at least one zeolite catalyst and at least one binder.

Particles including zeolite catalysts and their use in oligomerization processes

Embodiments of an invention disclosed herein relate to processes utilizing solvent extraction to remove nitrogen containing compounds and optionally other components from feedstreams of olefins and paraffins.

Processes utilizing solvent extraction

Embodiments disclosed herein relate to a process for the oligomerization of olefins, the process including at least one olefin feedstream that includes ammonia and contacting the at least one olefin feedstream with a liquid including alkaline water to remove at least a portion of the ammonia to produce at least one treated olefin feedstream and subsequently contacting the at least one treated olefin feedstream with a catalyst under oligomerization conditions to produce an oligomer product. In several embodiments disclosed herein, the at least one olefin feedstream includes one or more C-Colefins, preferably, C-Colefins, any isomer thereof, one or more paraffins having the same or different carbon number as the olefins, and mixtures thereof.

Processes for treating olefin feedstreams and related oligomerization processes

The startup of a tubular reactor containing fresh or regenerated molecular sieve catalyst and cooled by steam generation on the shell side, as part of an olefin oligomerization process, is improved by, during the startup phase of the reactor, controlling the pressure on the shell side of the reactor at maximum 10 barg. The startup may be further improved by controlling the inlet temperature of the hydrocarbon startup stream to the reactor, by controlling the flow of reactant olefins to the reactor, or by controlling the nature and/or concentration of the olefins in the reactor feed.

Oligomerisation process

The conversion and run length for oligomerization of olefins over a molecular sieve catalyst in a tubular reactor is improved by controlling the peak temperature to not exceed 50 degrees C. above the temperature of the temperature control fluid exiting the shell side outlet of the reactor. A tubular reactor containing molecular sieve catalyst is provided with a multipoint thermocouple in at least one tube, and optionally with a bottom design adapted for fast unloading of the molecular sieve catalyst from the tubular reactor.

Oligomerisation of olefins with zeolite catalyst

In the oligomerization of olefins in a tubular reactor employing a molecular sieve catalyst, the temperature of the reaction is monitored and the space velocity of the olefin feed to the reactor is reduced as the temperature increases. This has been found to increase catalyst life and lead to extended production runs. Further extensions of the production run are achieved by improving reactor operating stability as the end of the production run approaches.

Oligomerisation of olefins

The invention is directed to a reactor system comprising at least one reactor wherein makeup water for said system is preheated by water/steam exiting said reactor. In a preferred embodiment the system comprises plural reactors and the invention provides for each reactor to independently achieve isothermal operating conditions.

Reactor temperature control

The invention is directed to a method of selectively oligomerizing olefin monomers by controlling feedstock composition and reaction conditions. Reaction conditions are chosen to include at least one of: (a) dimer recycle; (b) staged injection of monomer; and (c) utilization of a two catalyst system.

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Brussels, Belgium

Paul Hamilton