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Saudi Arabian Oil Company

Mary Jo Wier

Clayton Colin Sadler

Gregory J Gajda

Laurence O Stine

Christopher Naunheimer

Ka Leung Lok

Bryan K Glover

David A Wegerer

Mark D Moser

Gregory A Funk

Mark Paul Lapinski

Kurt M VandenBussche

Alexander V Sabitov

Alakananda A Bhattacharyya

Tom N Kalnes

Andrea G Bozzano

Manuela Serban

Hayim Abrevaya

Christopher D Gosling

John Anthony Petri

Dean E Rende

Paul R Cottrell

Michael Jerome Vetter

Stuart Smith

William Yanez

Bryan James Egolf

Pengfei Chen

Guy B Woodle

Mohamed S Shakur

Larry D Richardson

Charles T Ressl

Jennifer J Ozmen

Gary A Dziabis

Gautam Tavanappa Kalghatgi

Kyle P Austin

Jorge Charr

Michael A Moore

David M Kazell

Richard Gaicki

James A Szczurek

Yue Zhu

Ernest J Boehm, Jr

Catalysts used for catalytic reforming are treated with organic chloride to condition the catalysts. Chloride treaters may be located in the product streams to remove the chloride contaminants. The continuous catalyst reforming process, including the catalyst reformer unit and chloride treaters, may be monitored in order to predict when adsorbent replacement or regeneration is needed. For example, one or more sensors and measurement devices may be used to monitor certain conditions or parameters. A system may be configured to take one or more actions in response to certain conditions or parameters being met.

Remote monitoring of chloride treaters using a process simulator based chloride distribution estimate

Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Process for producing a naphtha stream

GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26&#xb0; C. to about 38&#xb0; C. and a final boiling point in a range of about 193&#xb0; C. to less than 250&#xb0; C., a density of about 0.72 kg/l to about 0.8 kg/l at 15&#xb0; C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

Fuel composition for GCI engines and method of production

Apparatuses and methods are provided for regenerating catalyst particles. In one embodiment, a method for regenerating catalyst particles includes passing the catalyst particles through a halogenation zone and a drying zone. The method feeds drying gas to the drying zone and passes a first portion of the drying gas from the drying zone to the halogenation zone. The method includes removing a second portion of the drying gas from the drying zone and injecting a halogen gas into the second portion of the drying gas. Further, the method includes delivering the halogen gas and the second portion of the drying gas to the halogenation zone. In the method, substantially all of the drying gas fed to the drying zone enters the halogenation zone.

Methods and apparatuses for regenerating catalyst particles

A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of Cand Cparaffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Flexible gasoline process using multiple feedstocks

A process for increasing the yields of light olefins and the yields of aromatics from a hydrocarbon stream is presented. The process includes a first separation to direct the light components that are not reformable to a cracking unit, with the remainder passed to a second separation unit. The second separation unit extracts normal components from the hydrocarbon stream to pass to the cracking unit. The resulting hydrocarbon stream with reduced light ends and reduced normals is passed to a reforming unit.

Naphtha cracking

A process for regenerating a catalyst used in a reaction zone. In a regeneration zone, the catalyst may be cooled before passing into a chloride rich zone. The regeneration zone may also receive a heated ambient oxygen in a catalyst heating zone. The regeneration zone may also receive recovered chloride from a chloride recovering zone which removes and recovers chloride from regeneration gas taken from the regeneration zone. Heated ambient oxygen may also be introduced into a chlorination zone.

Processes for the continuous regeneration of a catalyst

Processes for producing aromatics from a naphtha feedstream are provided. An exemplary process includes passing the feedstream to a fractionation unit, thereby generating a first stream including hydrocarbons having less than 8 carbon atoms and a second stream including hydrocarbons having at least 8 carbon atoms. The first stream is passed to a first reformer operated at a first set of reaction conditions to generate a first product stream. The first set of reaction conditions includes a first temperature and a first pressure. The second stream is passed to a second reformer operated at a second set of reaction conditions to generate a second product stream. The second set of reaction conditions includes a second temperature and a second pressure. The first pressure is lower than the second pressure.

Process for increasing aromatics production

A process is presented for the increasing the yields of aromatics from reforming a hydrocarbon feedstream. The process includes splitting a naphtha feedstream into a light hydrocarbon stream, and a heavier stream having a relatively rich concentration of naphthenes. The heavy stream is reformed to convert the naphthenes to aromatics and the resulting product stream is further reformed with the light hydrocarbon stream to increase the aromatics yields. The process includes passing a catalyst stream in a counter-current flow relative to the hydrocarbon process stream.

Counter-current catalyst flow with split feed and two reactor train processing

The invention involves a process that reduces the potential for catalyst fluidization in a reduction vessel of a continuous catalyst regeneration system. The gas exit area from the catalyst reduction zone is increased by ventilating the cylindrical baffle of the upper reduction zone. This provides an increased exit cross-sectional area for the upper reduction gas to escape and reduce the overall exit velocity of the combined upper and lower reduction gases and reduces the potential for catalyst fluidization.

Process to reduce catalyst fluidization in regeneration units

A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Systems and processes for the alkylation of a hydrocarbon are provided that utilize a plurality of moving bed radial flow reactors. An olefin injection point can be provided prior to each reactor by providing a mixer that mixes olefin with a hydrocarbon feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed radial flow reactors can be stacked in one or more reactor stacks.

Solid catalyst hydrocarbon alkylation using stacked moving bed radial flow reactors

Systems and processes for hydrocarbon conversion are provided that utilize a plurality of moving bed reactors. The reactors may be moving bed radial flow reactors. Optional mixers that mix a portion of a second hydrocarbon feed with the effluent stream from an upstream reactor, to produce reactor feed streams may be employed, and the reactor feed streams may be introduced at injection points prior to each reactor. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed reactors can be stacked in one or more reactor stacks.

Solid catalyst hydrocarbon conversion process using stacked moving bed reactors

Systems and processes for the hydroprocessing of a hydrocarbonaceous feed are provided that utilize a plurality of moving bed reactors. The reactors may be moving bed radial flow reactors. A hydrogen injection point can be provided prior to each reactor by providing a mixer that mixes hydrogen with a hydrocarbonaceous feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed reactors can be stacked in one or more reactor stacks.

Solid catalyst liquid phase hydroprocessing using moving bed reactors

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Des Plaines, IL, United States of America

Mary Jo Wier