Exxon Research and Engineering Company

Primus Green Energy Inc.

Exxon Chemical Patents, Inc.

Exxonmobil Research and Engineering Company

Robert M Koros

Howard L Fang

Jon E Stanat

David C Dankworth

Barry L Tarmy

John T Wyatt

Milind B Ajinkya

Harold Wilbur Margo

Albert Rossi

Salvatore Rea

Cunping Huang

Meifang Qin

Zhong He

Moshe Ben-Reuven

Phiroz M Bhagat

Richard E Boyle

Kenneth Lee Kaufman

Linda Kay Wright

Jacob I Emert

Ramesh Gupta

Jeffrey William Frederick

Keith R Gorda

William D Diana

William B Eckstrom

Joseph V Cusumano

Ramesh R Hemrajani

Salvatore Joseph Rossetti

Jose M Peruyero

Rutton D Patel

Paul D Eichamer

Yiu Wah Wong

Glyndwr A Bessant

Steven R Schieni

Larry A Kaye

William H Cross

Jeffery William Frederick

This invention relates to a new process to directly produce transportation gasoline from synthesis gas containing principally carbon monoxide, carbon dioxide, and hydrogen. The process entails three sequential catalytic stages with intermediate heat exchange to provide the requisite temperature in each stage, but with no interstage separation. The recycle loop enhances the conversion of the synthesis gas to the desired products and also serves as heat sink for the highly exothermic reactions involved in each stage.

Configuration in single-loop synfuel generation

Synthetic fuels are produced from synthesis gas in a four-stage reactor system with a single recycle loop providing the requisite thermal capacity to moderate the high heat release of the reactions and to provide the reactants and reaction environments for the efficient operation of the process. The first reactor converts a portion of the synthesis gas to methanol; the second reactor converts the methanol to dimethylether; the third reactor converts the methanol and dimethylether to fuel; and the fourth reactor converts the high melting point component, durene, and other low volatility aromatic components such as tri- and tetra-methylbenzenes to high octane branched paraffins. A large part of the gas stream of the fourth reactor is recycled to the inlet of the first stage and mixed with the fresh synthesis gas stream. Alternatively, the fresh synthetic gas stream is mixed with the product of the second stage.

Single loop multistage fuel production

Synthetic fuels are produced from synthesis gas in a four-stage reactor system with a single recycle loop providing the requisite thermal capacity to moderate the high heat release of the reactions and to provide the reactants and reaction environments for the efficient operation of the process. The first stage converts a portion of the synthesis gas to methanol, the second stage converts the methanol to dimethylether, the third stage converts the methanol and dimethylether to fuel and the fourth stage converts the high melting point component, durene, and other low volatility aromatic components such as tri- and tetra-methylbenzenes to high octane branched paraffins.

A fixed bed catalytic reactor for converting process fluids having an upper catalyst bed and a lower catalyst bed below the upper catalyst bed for converting process fluids flowing through the upper and lower beds. A mixing zone is located between the upper bed and lower beds, and at least one jet is provided for injecting an inclined fluid jet into the mixing zone against the flow of the process fluids to entrain process fluids within the jet and to radially mix the process fluids across the mixing zone.

Jet mixing of process fluids in fixed bed reactor

An improved process for the homopolymerization and copolymerization of .alpha.-olefins utilizing highly dilute .alpha.-olefin feedstreams to effect high conversions and catalyst efficiencies in the production of non-ethylene copolymers. The instant invention is particularly adaptable to polymerizing the .alpha.-olefin content of commercially available refinery feedstreams such as Raffinate-2.

Dilute process for the polymerization of non-ethylene .alpha.-olefin

An improved process for the copolymerization of ethylene and .alpha.-olefins utilizing highly dilute .alpha.-olefin feedstreams to effect high conversions and catalyst productivities. The instant invention is particularly adaptable to copolymerizing the .alpha.-olefin content of commercially available refinery feedstreams such as Raffinate-2.

Dilute process for the polymerization of ethylene/.alpha.-olefin

A continuous process for functionalizing olefins, especially polymer olefins in a CSTR or pipe reactor. Esters are preferably produced by continuous reaction of the olefin with carbon monoxide and a nucleophilic trapping agent. The liquid-filled pipe reactor operates in plug flow with static mixers and the CSTR is operated in the substantial absence of air at constant liquid level.

Continuous process for production of functionalized olefins

The uniform distribution of mixed phase fluid stream on to the top of a contact bed in a reactor chamber is provided by a horizontal tray with a plurality of spaced-apart, vertically disposed chimneys extending through the tray. These chimneys have a first end to receive liquid and gas above the tray and a second end for distributing the liquid and gas downwardly below the tray. Importantly, the second end is provided with a spray generating device located below the tray for producing a conical downward spray of the mixed fluid phase onto the top surface of a bed of contact material positioned below the tray. The spray generating devices for producing the conical spray are located at positions so that the spray of the mixed fluid stream from one spray generating device as it impinges on the top surface of the fixed bed, will overlap the spray from an adjacent spray generating device.

Mixed phase fixed bed reactor distributor

A reactor housing having a plurality of reaction tubes vertically disposed therein for conducting slurry phase hydrocarbon synthesis reactions under substantially plug flow conditions, and wherein provision is made for uniformly distributing gas bubbles in slurry liquid into the reaction tubes.

Bubble column, tube side slurry process and apparatus

The distribution of fluid flowing through a packed bed reactor is determined by placing a plurality of fiber optic sensors at desired locations within the packed bed reactor. A light analyzable tracer component is injected into the fluid flowing through the reactor. Light is supplied to each of the sensors causing any tracer component in the vicinity of the sensor to emit electromagnetic radiation. The emitted electromagnetic radiation is detected at each fiber optic sensor, thereby permitting the amount of tracer in the vicinity of each sensor to be determined, and consequently providing a measure of the distribution of fluid flowing through the reactor.

In-situ localized tracer injection/fiber optic detection for measurement

In its simplest sense, the present invention provides a method for improving the contacting of plural, distinct phases in a vertically disposed vessel containing distinct fluid phases by injecting a stream of dispersed distinct phases together into the phases contained in the vessel at a sufficient velocity to force the fluid in the vessel to circulate downwardly through a central region in the vessel and upwardly in the annular region surrounding the central region.

High interfacial area multiphase reactor (RM-1069)

High interfacial area multiphase reactor

In its simplest sense, the present invention provides a method and apparatus for improving the contacting of plural, distinct phases in a circulatory reactor containing a liquid-immersed circulation tube by injecting a stream of dispersed distinct phases together into the circulation tube of the circulatory reactor. Sufficient fluid movement will force the fluid in the reactor to circulate downwardly through the circulation tube and upwardly in the annular space between the tube and the reactor wall.

The interzone mixing device of the present invention is positioned in a multi-zoned vessel for flow of fluid generally vertically therethrough. The interzone mixing device includes a horizontally disposed first plate that has a central opening in it and a cylindrical cap extending upwardly from the first plate and sized and positioned to cover the central opening therein. The cap has a plurality of angular slots in the side wall to direct the flow of fluid passing therethrough in a swirling direction toward the central opening in the first plate. The interzone mixing device also includes a horizontally disposed second plate which has a plurality of openings in an annular ring around the periphery of the second plate. Additionally, a horizontally disposed circular table is positioned on the second plate and is aligned with the central opening in the first plate. A third horizontally disposed plate, having a central opening therein, is spaced apart from the second plate and defines a jet stirred mixing zone therebetween. A horizontally disposed fluid distribution plate is spaced apart from the third plate. A conduit for introducing a quench fluid is also provided in this apparatus.

Interzone mixing device

Growing community of inventors

Westfield, NJ, United States of America

Robert M Koros