Fina Technology, Inc.

Other

Total Petrochemicals Research Feluy

James T Merrill

James R Butler

Ashim Kumar Ghosh

Xin Xiao

Marcus Ledoux

Adrian M Jacobsen

Edwar Shoukri Shamshoum

Olga Khabashesku

Thomas R Schuler

Joseph Honn Tudor

Thomas Parenteau

Mark Gremillion

Alkylation systems and methods of minimizing alkylation catalyst regeneration are described herein. The alkylation systems generally include a preliminary alkylation system adapted to receive an input stream including an alkyl aromatic hydrocarbon and contact the input stream with a preliminary alkylation catalyst disposed therein to form a first output stream. The preliminary alkylation catalyst generally includes a zeolite catalyst having a SiO/AlOratio of less than about 25. The alkylation systems further include a first alkylation system adapted to receive the first output stream and contact the first output stream with a first alkylation catalyst disposed therein and an alkylating agent to form a second output stream.

Process for the reduction of alkylation catalyst deactivation utilizing low silica to alumina ratio catalyst

Alkylation systems and methods of minimizing alkylation catalyst regeneration are discussed herein. The alkylation systems generally include a preliminary alkylation system adapted to receive an input stream including an alkyl aromatic hydrocarbon and contact the input stream with a first preliminary alkylation catalyst disposed therein to form a first output stream. The first preliminary alkylation catalyst generally includes a Y zeolite. The systems further include a first alkylation system adapted to receive the first output stream and contact the first output stream with a first alkylation catalyst disposed therein and an alkylating agent to form a second output stream.

Processes for the reduction of alkylation catalyst deactivation utilizing stacked catalyst bed

Process for the reduction of alkylation catalyst deactivation

A method for the dehydrogenation of hydrocarbons to alkenes, such as n-pentene to piperylene and n-butane to butadiene at pressures less than atmospheric utilizing a dehydrogenation catalyst are disclosed. Embodiments involve operating the dehydrogenation reactor at a pressure of 1,000 mbar or less.

Dehydrogenation reactions of hydrocarbons to alkenes

Processes for reduction of alkylation catalyst deactivation utilizing stacked catalyst bed

Dehydrogenation of a reactor system of one or more vertically oriented flow reactors equipped with a system for introducing a catalyst extender into the inlet of the reactor. A vertically oriented radial flow reactor comprises inner and outer reactor tubes having perforated wall members extending longitudily of the reactor and defining an annulus containing a dehydrogenation catalyst. A supply line to the reactor is equipped with a rotation vane. An injection nozzle comprising a coaxial flow tube extends into the supply line downstream of the vane. The coaxial flow tube has an interior chamber and an annular chamber surrounding the interior chamber and extending into the supply line along with the interior chamber. The interior chamber is connected to a catalyst extender source and the annular chamber is connected to a source of a carrier gas which is effective to disperse the extender within feedstock flowing into the reactor.

Dehydrogenation of alkyl aromatics

Process for the production of an isoprene containing rubber compound by dehydrogenation of an isoamylene containing feedstock supplied to a dehydrogenation reactor containing a particulate dehydrogenation catalyst comprising iron and potassium and having a pore diameter of at least 500 nanometers. The dehydrogenation reactor is operated at a temperature of at least 570&#xb0; C. to dehydrogenate the isoamylene to produce isoprene. The product containing isoprene and unreacted isoamylene is recovered from the dehydrogenation reactor. Isoprene is polymerized to produce an isoprene containing rubber product. An unreacted feed component containing isoamylene is separated from the rubber product and recycled to the dehydrogenation reactor.

Dehydrogenation and polymerization process

Methods and systems for petrochemical feedstream purification are described herein. The methods generally include providing a petrochemical feedstock, wherein the petrochemical feedstock includes a concentration of polar impurities, contacting the petrochemical feedstock with a washing agent to remove at least a portion of the polar impurities therefrom, separating the washing agent from the petrochemical feedstock to form a purified feedstock and passing the purified feedstock to a petrochemical process. In one embodiment, the petrochemical feedstock includes benzene and the washing agent includes water.

Petrochemical feedstock purification

Process for the catalytic dehydrogenation of a Cor Calkyl aromatic in which a feedstock containing the alkyl aromatic and steam is supplied into the inlet of a tubular reactor containing a dehydrogenation catalyst. Within the reactor, the feedstock flows through at least a portion of the reactor along a spiral flow path extending longitudinally of the reactor. The resulting vinyl aromatic product is then recovered from a downstream or outlet section of the reactor. The spiral flow path through which the feedstock is passed is located at least adjacent the inlet side of the reactor and at least a portion of the spiral flow path contains a particulate dehydrogenation catalyst. The spiral flow path may extend throughout a major portion of the elongated tubular reactor and may contain a particulate dehydrogenation catalyst in a substantial portion there. The feedstock containing the alkyl aromatic and steam is supplied into a plurality of tubular reactors located within the interior of a dehydrogenation reactor vessel and is arranged in a parallel relationship in which the tubular reactors are spaced laterally from one another and from the interior wall of the reaction vessel.

Dehydrogenation process

A process for the reduction of a phenylacetylene contaminant in the presence of a styrene monomer. A styrene monomer stream containing a minor amount of phenylacetylene is supplied to a hydrogenation reactor. A hydrogenation gas comprising hydrogen is also supplied to the hydrogenation reactor. The styrene monomer stream and the hydrogen are brought into contact with a catalyst bed containing a catalyst comprising a reduced copper compound on a theta alumina support. The hydrogenation reactor is operated at a temperature of at least 60&#xb0; C. and a pressure of at least 30 psig to hydrogenate phenylacetylene to styrene. A product is recovered from the hydrogenation reactor having a substantially reduced phenylacetylene content and an enhanced styrene content. The hydrogenation gas comprises a mixture of nitrogen and hydrogen.

Process for the selective hydrogenation of phenylacetylene

Disclosed is the observation that 7-aryl-quinone methides and 4-tert-butylcatechol, when used in combination in a vinyl aromatic monomer to inhibit polymerization,do not inhibit polymerization to the same extend as each would if used separately. Stated another way, a phenomenon has been observed that when these two compounds are used together, they can, to a large extent, render each other unable to inhibit polymerization in a vinyl aromatic monomer. Also disclosed are methods of preventing adverse results of this interaction when undesired and a method of using this interaction to prepare a reactive vinyl aromatic monomer having a concentration of 4-tert-butylcatechol that would otherwise inhibit polymerization. The invention is disclosed to be useful with the production and storage of any vinyl aromatic monomer and is disclosed to be particularly useful with the production and storage of styrene monomer.

Method for stabilizing vinyl aromatic monomers using selected polymerization inhibitors and polymers prepared therewith

A process for the transalkylation of polyalkylated aromatic compounds over a high porosity zeolite-Y molecular sieve having a surface area of no more than 500 m/g. A feedstock comprising a polyalkylated aromatic component, including polyalkylbenzenes in which the predominant alkyl substituents contain from 2 to 4 carbon atoms, is supplied to a transalkylation reaction zone containing the high porosity zeolite-Y catalyst. Benzene is also supplied to the transalkylation zone, and the reaction zone is operated under temperature and pressure conditions to maintain the polyalkylated aromatic component in the liquid phase and which are effective to cause disproportionation of the polyalkylated aromatic component to arrive a disproportionation product having a reduced polyalkylbenzene content and an enhanced monoalkylbenzene content. An alkylation reaction zone is provided which contains a molecular sieve aromatic alkylation catalyst having an average pore size which is less than the average pore size of the average pore size of the high porosity zeolite-Y. A feedstock comprising benzene in a C-Calkylating agent is supplied to the alkylation reaction zone which is operated under conditions to produce alkylation of the benzene by the alkylating agent in the presence of the molecular sieve alkylation catalyst. The alkylation product from the alkylation reaction zone is supplied to an intermediate recovery zone for the separation and recovery of a monoalkylbenzene, e.g. ethylbenzene, from the alkylation product; together with the recovery of a polyalkylated aromatic component employing a dialkylbenzene, e.g. diethylbenzene. The polyalkylated aromatic component is employed in at least a portion of the feedstream supplied to the transalkylation reactor.

Aromatic conversion process employing low surface area zeolite Y

The alkylation of benzene-containing feedstock over a zeolite beta alkylation catalyst which is formulated with a silica binder and has an average regeneration coefficient of at least 95% for at least three regenerations. The alkylation reaction is carried out in the liquid phase or supercritical region with a C-Calkylating agent, specifically ethylene. The catalyst exhibits a regeneration coefficient of at least 95% after ethylation of the benzene with ethylene at a benzene/ethylene mole ratio of less than 10. The ethylation of benzene occurs at an initial designated primary activity. The operation of the reaction zone is continued until the activity of the catalyst for the ethylation of benzene decreases by a value of at least 0.1% and not more 1% from the initial designated primary activity. The operation of the reaction for alkylation is terminated and a regeneration procedure is instituted in which the catalyst is regenerated in an oxidizing environment at an average temperature of no more than 500&#xb0; C. At the conclusion of the regeneration procedure, the operation of the alkylation zone is reinstituted with the reaction zone again operated under conditions as described above followed by regeneration.

Silica-supported alkylation catalyst

Process for the catalytic dehydrogenation of a C or C alkyl aromatic in which a feedstock containing the alkyl aromatic and steam is supplied into the inlet of a tubular reactor containing a dehydrogenation catalyst. Within the reactor, the feedstock flows through at least a portion of the reactor along a spiral flow path extending longitudinally of the reactor. The resulting vinyl aromatic product is then recovered from a downstream or outlet section of the reactor. The spiral flow path through which the feedstock is passed is located at least adjacent the inlet side of the reactor and at least a portion of the spiral flow path contains a particulate dehydrogenation catalyst. The spiral flow path may extend throughout a major portion of the elongated tubular reactor and may contain a particulate dehydrogenation catalyst in a substantial portion there. The feedstock containing the alkyl aromatic and steam is supplied into a plurality of tubular reactors located within the interior of a dehydrogenation reactor vessel and is arranged in a parallel relationship in which the tubular reactors are spaced laterally from one another and from the interior wall of the reaction vessel.

Growing community of inventors

Katy, TX, United States of America

James T Merrill