Sabic Global Technologies B.v.

Saudi Arabian Oil Company

King Abdullah University of Science and Technology

Consejo Superior De Investigaciones Cientificas

Universitat Politécnica De Valência

Khalid A Al-Majnouni

Ahmed Al-Zenaidi

Wei Xu

Raed H Abudawoud

Avelino Corma Canós

Nabil Al-Yassir

Wojciech Andrzej Supronowicz

Ahmed Alzenaidi

Naif Aldalaan

Nabil Alyasser

Ahmad M Al-Shehri

Motaz Khawaji

Avelino Corma Canos

Ola S Ali

Mohamed Elanany

Ibrahim M Al-Zahrani

M Teresa Portilla Ovejero

M Cristina Martinez Sanchez

Vicente J Margarit Benavent

M Teresa Navarro Villalba

Vidya Sagar Guggilla

Jorge Gascon Sabate

Talal Aldugman

Debdut S Roy

Abdulaziz S Alarifi

Khalid Almusaiteer

Nabil Al-Yasser

Naif A Al-Dalaan

Talal Alshammari

Abdulaziz A Alarifi

Nandini Pechimuthu

Mª Teresa Navarro Villalba

Mª Teresa Portilla Ovejero

Mª Cristina MARTÍNEZ SÁNCHEZ

Raed Hasan Abudawoud

Systems and methods for producing light olefin(s) are disclosed. The method includes contacting a catalyst with a coke precursor to form a light olefin selective catalyst, and contacting the light olefin selective catalyst with a hydrocarbon feed under conditions sufficient to catalytically crack at least a portion of the hydrocarbon feed to form a products stream containing a light olefin, here the light olefin selective catalyst is more selective than the catalyst in catalyzing formation of the light olefin by the catalytic cracking of the hydrocarbon feed.

Light olefins yield improvement over light olefin selective catalyst

Systems and methods of producing olefins via catalytic cracking are disclosed. Hydrocarbons of a naphtha stream are isomerized by converting straight chain Cn hydrocarbons to branched Cn hydrocarbons, thereby forming an isomerized naphtha stream. The isomerized naphtha stream is subsequently fed to a catalytic cracking unit such that the hydrocarbons of the isomerized naphtha stream form olefins. In the catalytic cracking process, the reaction temperature can be kept lower than 680° C., thereby increasing the reactivity and minimizing catalyst deactivation in the catalytic cracking process.

Process of producing light olefins from isomerized straight run naphtha

System and method for producing olefins are disclosed. The method includes using a radial flow moving bed reactor system to catalytically crack paraffins, in multiple stages with continuous catalyst regeneration, to form olefins. The system includes inter-stage heaters to facilitate increase in yield of olefins.

Process for catalytic cracking of naphtha using multi-stage radial flow moving bed reactor system

Systems and methods for the catalytic cracking of light hydrocarbons, such as naphtha, to form light olefins and aromatics is disclosed. The systems and methods may include a catalytic cracking process that involves mixing catalyst with a gas and then this mixture is used to contact a hydrocarbon feed, e.g., light straight run naphtha or heavy straight run naphtha. The hydrocarbon feed may be mixed with dry gas such as methane and/or hydrogen to dilute the hydrocarbon feed, before the hydrocarbon feed is contacted with the catalyst/gas mixture.

Process integration for cracking light paraffinic hydrocarbons

Systems and methods for processing full range naphtha to produce light olefins are disclosed. The systems and methods include separating the full range naphtha into a light naphtha stream and a heavy naphtha stream and integrating a catalytic cracking with a naphtha reforming to process the light naphtha and heavy naphtha streams.

Process of producing light olefins and aromatics from wide range boiling point naphtha

A multi-zoned fluidized bed reactor system may include a multi-zoned fluidized bed reactor and at least one catalyst regeneration loop. The multi-zoned fluidized bed reactor comprising a housing, a fluid bed distributor plate positioned at the bottom of the housing, a fluidized catalyst bed disposed vertically above the fluid bed distributor plate and a condensation zone disposed vertically above the fluidized catalyst bed. The at least one catalyst regeneration loop may be fluidly coupled to the stripping zone and a reaction zone. The at least one catalyst regeneration loop may be operable to withdraw a portion of spent catalyst from the stripping zone, regenerate the portion of spent catalyst to produce regenerated catalyst, and return the regenerated catalyst to the reaction zone. A method of regenerating catalyst in a multi-zoned fluidized bed reactor may include passing a portion of spent catalyst from a stripping zone to a catalyst regeneration loop.

Integrated loop systems for catalyst regeneration in multi-zone fluidized bed reactors and methods of using the same

A method of producing olefins by catalytic cracking of hydrocarbons is disclosed. The method may include catalytic cracking hydrocarbons in a feed stream that includes the hydrocarbons and the dry gas diluent. The catalytic cracking may be carried out in a process using a train of fixed bed reactors while one or more other trains of fixed bed reactors are being regenerated or are on standby after being regenerated. When the train of fixed bed reactors being used needs regenerating, it is taken out of service and the one or more other trains of fixed bed reactors put in service to carry out the catalytic cracking process. Dry gas instead of steam may be used to reduce the partial pressure of hydrocarbons.

Naphtha catalytic cracking for light olefins production over cyclic regenerative process with dry gas diluent

Processes to produce olefins from a hydrocarbons stream obtained from a catalytic cracking unit are described. The process includes the integration of metathesis of Colefin process and a hydrocarbon catalytically cracking process to produce commercially valuable products (for example, Colefins and a Cgasoline hydrocarbons).

Process to produce olefins from a catalytically cracked hydrocarbons stream

A method of catalytically cracking liquid hydrocarbons is disclosed. The method includes the use of one or more radial flow moving bed reactors. The method may include mixing a liquid hydrocarbon stream comprising primarily C5 and C6 hydrocarbons with water or a dry gas to form a feed mixture and flowing the feed mixture into the one or more radial flow moving bed reactors in a manner so that the feed mixture flows radially inward or radially outward through the moving catalyst bed and thereby contacts the catalyst particles under reaction conditions to produce a hydrocarbon stream comprising light olefins (C2 to C4 olefins).

Process for catalytic cracking of naphtha using radial flow moving bed reactor system

A method that integrates a catalytic cracking process with a crude oil conversion to chemicals process is disclosed. The method may include contacting, in a catalytic cracking reactor, a mixture of the hydrocarbon stream comprising primarily Cand Chydrocarbons from crude oil processing and a Cto Chydrocarbon stream produced in a steam cracking unit with a catalyst under reaction conditions sufficient to produce an effluent comprising olefins.

Integration of catalytic cracking process with crude conversion to chemicals process

A method of forming a composite zeolite catalyst includes combining a silicon source and an aqueous organic structure directing agent having a polyamino cation compound to form a silica intermediary gel, introducing an aluminum precursor to the silica intermediary gel to form a catalyst precursor gel, evaporating water in the catalyst precursor gel to form a catalyst gel, and heating the catalyst gel to form a composite zeolite catalyst particle having an intergrowth region with a mixture of both Beta crystals and ZSM-5 crystals. An associated method of making xylene includes feeding heavy reformate to a reactor, the reactor containing the composite zeolite catalyst, and producing xylene by simultaneously performing dealkylation and transalkylation of the heavy reformate in the reactor, where each composite zeolite catalyst particle is able to catalyze both the dealkylation and transalkylation reactions.

Methods of producing composite zeolite catalysts for heavy reformate conversion into xylenes

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Riyadh, Saudi Arabia

Khalid A Al-Majnouni