Kellogg Brown + Root LLC

Phillips Petroleum Company

David P Mann

Shashi Prakash Singh

Avinash Malhotra

Anant Pisut

Alan D Eastman

John Abughazaleh

Robert B Eldridge

Kenneth Lewis Blanchard

Simon G Kukes

Ronald G Abbott

Richard L Anderson

Daniel M Coombs

Fu-Ming Lee

Siva Ariyapadi

Martin John Van Sickels

Kenneth L Blanchard

Stanislaus A Knez

Robert J Mitchell

Michael J Sandefur

Edwin V Reece

Shashi P Singh

Martin J Van Sickels

Mike Sandefur

Methods, systems, and apparatus for mass flow are provided. The apparatus can include a housing, an inlet disposed at a first end of the housing, and an outlet disposed at a second end of the housing. The housing can include a first section and a second section. The second section can have at least one tapered sidewall that slopes away from an inner surface of the first section toward the outlet. The apparatus can also include a divider disposed at least partially within the first and second sections of the housing. The divider can have at least one tapered surface disposed proximate the at least one tapered sidewall of the second section. An edge of the divider can be located between the outlet and a point within the second section where the cross-sectional area of the second section is about three times or less a cross-sectional area of the outlet.

Lock hopper mass flow arrangement

Systems and methods for producing a synthetic gas are provided. A feedstock can be gasified within a gasifier to produce a raw syngas. The raw syngas can be processed within a processing device to produce a processed syngas. The processed syngas can be separated into a vapor phase, an organic phase, and an aqueous phase within a separator. The organic phase can be introduced to the gasifier. The aqueous phase can be introduced to a stripper to provide steam and a condensate, and the steam can then be introduced to the gasifier.

Recycling organic compounds from gasifier syngas condensate

Systems and methods for contacting a liquid, gas, and/or a multi-phase mixture with particulate solids. The system can include a body having a first head and a second head disposed thereon. Two or more discrete fixed beds can be disposed across a cross-section of the body. One or more unobstructed fluid flow paths can bypass each fixed bed, and one or more baffles can be disposed between the fixed beds.

Split flow contactor

Systems and processes for producing syngas are provided. A first hydrocarbon can be partially oxidized in the presence of an oxidant and one or more first catalysts at conditions sufficient to partially combust a portion of the first hydrocarbon to provide carbon dioxide, non-combusted first hydrocarbon, and heat. At least a portion of the non-combusted first hydrocarbon can be reformed in the presence of at least a portion of the heat generated in the partial oxidation step and the one or more first catalysts to provide a first syngas. The first syngas can comprise hydrogen, carbon monoxide, and carbon dioxide. Heat can be indirectly exchanged from the first syngas to a second hydrocarbon to reform at least a portion of the second hydrocarbon in the presence of steam and one or more second catalysts to provide a second syngas. The second syngas can comprise hydrogen, carbon monoxide, and carbon dioxide.

Catalytic partial oxidation reforming

Systems and methods for producing syngas are provided. A first hydrocarbon can be partially oxidized in the presence of an oxidant and one or more first catalysts at conditions sufficient to partially combust a portion of the first hydrocarbon to provide carbon dioxide, non-combusted first hydrocarbon, and heat. The non-combusted first hydrocarbon can be reformed in the presence of the heat generated in the partial oxidation step and the one or more first catalysts to provide a first syngas. Heat can be indirectly exchanged from the first syngas to a second hydrocarbon to reform at least a portion of the second hydrocarbon in the presence of steam and one or more second catalysts to provide a second syngas. A syngas, which can include the at least a portion of the first syngas, at least a portion of the second syngas, or a mixture thereof can be converted to provide one or more Fischer-Tropsch products, methanol, derivatives thereof, or combinations thereof.

Catalytic partial oxidation reforming for syngas processing and products made therefrom

An ammonia converter and method are disclosed. The reactor can alter the conversion of ammonia by controlling the reaction temperature of the exothermic reaction along the length of the reactor to parallel the equilibrium curve for the desired product. The reactorcan comprise a shelland internal catalyst tubes. The feed gas stream enters the reactor, flows through the shell, and is heated by indirect heat exchange with the catalyst tubes. The catalyst tubescomprise reactive zoneshaving catalyst and reaction limited zonesthat can comprise inert devices that function to both separate the reactive zones, increase heat transfer area, and reduce the temperature of the reaction mixture as the effluent passes through the catalyst tube

Maximum reaction rate converter process for exothermic reactions

An ammonia converter is disclosed. The converter can alter the conversion of ammonia by controlling the reaction temperature of the exothermic reaction along the length of the reactor to parallel the equilibrium curve for the desired product. The converter can comprise a shelland internal catalyst tubes. The feed gas stream enters the reactor, flows through the shell, and is heated by indirect heat exchange with the catalyst tubes. The catalyst tubescomprise reactive zoneshaving catalyst and reaction limited zonesthat can comprise inert devices that function to both separate the reactive zones, increase heat transfer area, and reduce the temperature of the reaction mixture as the effluent passes through the catalyst tube

Maximum reaction rate converter for exothermic reactions

An ammonia converter system and method are disclosed. The reactor can alter the conversion of ammonia by controlling the reaction temperature of the exothermic reaction along the length of the reactor to parallel the equilibrium curve for the desired product. The reactorcan comprise a shelland internal catalyst tubes. The feed gas stream enters the reactor, flows through the shell, and is heated by indirect heat exchange with the catalyst tubes. The catalyst tubescomprise reactive zoneshaving catalyst and reaction limited zonesthat can comprise inert devices that function to both separate the reactive zones, increase heat transfer area, and reduce the temperature of the reaction mixture as the effluent passes through the catalyst tube

Maximum reaction rate converter system for exothermic reactions

Low-energy hydrogen production is disclosed. A reforming exchanger is placed in parallel with a partial oxidation reactor in a new hydrogen plant with improved efficiency and reduced steam export, or in an existing hydrogen plant where the hydrogen capacity can be increased by as much as 20&#x2013;30 percent with reduced export of steam from the hydrogen plant.

Partial oxidation reformer-reforming exchanger arrangement for hydrogen production

Disclosed is a process for removing acid soluble oils, produced as an undesirable by-product of an HF catalyzed alkylation reaction, from a liquid containing a sulfone compound. The process includes the use of a solvent to extract the acid soluble oils from a sulfone-containing fluid that has previously been neutralized by a treating step.

Alkylation catalyst regeneration

Disclosed is a process for removing acid soluble oils, produced as an undesirable by-product of an HF catalyzed alkylation reaction, from a liquid containing a sulfone compound. The process includes the use of water to induce the formation of the two immiscible liquid phases of ASO and sulfone with water. The two immiscible phases can subsequently be separated from each other.

The process described uses a C.sub.2 -C.sub.10 hydrocarbon solvent and an organophosphorous compound to extract metals from metal containing oils. Preferably, the extraction is performed above the critical conditions of the solvent.

Growing community of inventors

Katy, TX, United States of America

David P Mann