Sabic Global Technologies B.v.

Other

Robert R Broekhuis

Pankaj Singh Gautam

Vidya Sagar Reddy Sarsani

Tian Gu

Dustin Fickel

David H West

Vijayanand Rajagopalan

Istvan Lengyel

Sagar Sarsani

Lei Chen

Sreekanth Pannala

Emiel Van Kimmenade

Heng Shou

Byeongjin Baek

Hua Bai

Kaushik Anil Gandhi

Ramakumar Allada

Uwaidh Al-Harethi

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (CH, CH, O) to a first reactor system to produce a first effluent stream (CH, CH, O), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactor system is characterized by a first reactor system operating temperature of 270° C.-320° C.; wherein the first reactor system comprises oxidative dehydrogenation (ODH) stage(s); (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, CH, CH, O); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (CH, CH, O); wherein ethylene is not separated from recycle stream and/or first effluent stream; (d) recycling at least a portion of recycle stream to the first reactor system, and a optionally portion of recycle stream to the second reactor.

Process for producing ethylene oxide from ethane by oxidative dehydrogenation and epoxidation using a recycle reactor design

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (CH, CH, O) to a first reactor to produce a first effluent stream (CH, CH, O), wherein the mole fraction of ethylene in first effluent stream is greater than in first reactant mixture; wherein the first reactant mixture is characterized by a molar ratio of ethylene to ethane of ≥1.3; (b) introducing the first effluent stream to a second reactor to produce a second effluent stream (EO, CH, CH, O); (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (CH, CH, O); wherein ethylene is not separated from recycle stream and/or first effluent stream; and (d) recycling at least a portion of recycle stream to the first reactor, and a portion of recycle stream to the second reactor.

Process for producing ethylene oxide from ethane by oxidative dehydrogenation and epoxidation with low ethane concentration in oxidative dehydrogenation effluent

An ethylene oxide (EO) production process comprising (a) introducing a first reactant mixture (CH, O) to a first reactor to produce a first effluent stream (CH, CH, O); (b) introducing a second reactant mixture to a second reactor to produce a second effluent stream (EO, CH, CH, O); wherein the second reactant mixture comprises at least a portion of first effluent stream; (c) separating the second effluent stream into an EO product stream (EO) and recycle stream (CH, CH, O); wherein ethylene is not separated from recycle stream and/or first effluent stream; and (d) recycling a first portion of recycle stream to the first reactor, and a second portion of recycle stream to the second reactor; wherein recycle split ratio <0.6; and wherein recycle split ratio is defined as ratio of volumetric flowrate of first portion of recycle stream divided by the sum of volumetric flowrates of first portion and second portion of recycle stream.

Process for producing ethylene oxide from ethane by oxidative dehydrogenation and epoxidation with split recycle

A process for producing light alkanes and creating a flexible distribution system for those alkanes and related systems are disclosed. The process can include supplying a butane feed stream to a butane conversion unit to produce a light alkane output stream including at least methane, ethane, propane, and hydrogen, separating at least part of the light alkane output stream into separate streams of methane, ethane, and propane and distributing the separated streams as desired. The distribution of the separated streams can include sending the separated ethane and propane streams to downstream processing units which use them as feedstock. The butane containing feed and/or unreacted butane feed can include isobutane, which can be converted to n-butane and then further processed.

Distribution hub for C4 conversion to ethane/propane feedstock network

Processes for the hydrogenolysis of butane are described. A process can include (a) introducing a butane feed and hydrogen to a first hydrogenolysis reactor comprising a hydrogenolysis catalyst, and (b) contacting the butane feed and hydrogen with the hydrogenolysis catalyst at conditions sufficient to produce a first hydrogenolysis product stream. The introduction of the butane feed stream and hydrogen to the first hydrogenolysis reactor can be controlled to maintain a hydrogen to butane molar ratio in the reactor inlet of 0.3:1 to 0.8:1.

Methods of butane hydrogenolysis under hydrogen-lean conditions

A device for mixing two gas streams, the device includes: an inner pipe, wherein: the inner pipe is arranged substantially concentrically within an outer pipe and forms an annulus between an outer diameter of the inner pipe and an inner diameter of the outside pipe; the inner pipe is closed at a downstream end; and the inner pipe comprises a plurality of perforations; and the outer pipe, wherein: a downstream end of the outer pipe extends into a reactor; the outer pipe is closed at the downstream end; and the downstream end of the outer pipe comprises a plurality of perforations. The mixed gas stream can enter the reactor. The reactor can be an Oxidative Coupling of Methane (OCM) reactor.

Two stage gas-gas mixer

A methane conversion process for producing Chydrocarbons comprising (a) introducing a reactant mixture comprising methane (&#x3e;20 mol %) and an inert compound to a reaction unit to produce a reactor effluent stream comprising Chydrocarbons, methane, the inert compound, and water and/or carbon dioxide; (b) removing at least a portion of the water and/or at least a portion of the carbon dioxide from the reactor effluent stream to produce a demethanizer feed stream; (c) feeding at least a portion of the demethanizer feed stream to a demethanizer unit to produce two or more vapor streams (methane rich stream and inert rich stream), and at least one liquid stream (Chydrocarbons); (d) withdrawing at least a portion of the inert rich stream as a purge stream; (e) recycling any remaining portion of the inert rich stream to the reaction unit; and (f) recycling the methane rich stream to the reaction unit.

Growing community of inventors

Sugar Land, TX, United States of America

Robert R Broekhuis