Air Products and Chemicals, Inc.

Energy Internet Corporation

Gtlpetrol LLC

Other

8 Rivers Capital, LLC

National Institute for Strategic Technology Acquisition and Commercialization

Technip Usa, Inc.

Niquan Energy LLC

Xiang-dong Peng

John Michael Repasky

William Robert Licht

Jeffrey Raymond Hufton

Steven Gerard Mayorga

Brian Thomas Carvill

Jeffrey Richard Brzozowski

Shankar Nataraj

Xiang-Dong Peng

Diwakar Garg

Shoou-I Wang

Steven Lee Russek

Shankar Ramamurthy

Michael Francis Carolan

Merrill Anderson Wilson

Kurt E Kneidel

Phillip Andrew Armstrong

VanEric Edward Stein

Keith Gerard Rackers

Theodore R Ohrn

Harold W Wahle

Christopher M Chen

James Erik Blake

Rene Hendrik Elias Van Doorn

Kevin Boyle Fogash

Xiaoyi He

Sanjay Mehta

Eugene S Genkin

Hoanh Nang Pham

Robert Roger Broekhuis

Maulik R Shelat

James Richard O'Leary

Michael Enever

Yun Wu

Rodney John Allam

Shivaji Sircar

Paul N Dyer

Jianguo Xu

Guido Peter Pez

John N Armor

Xianming Jimmy Li

Thomas R Gaffney

Robert Quinn

David M Nicholas

Bo Jin

Robert B Moore

Thomas M Roden

David Hon Sing Ying

Eric Stanley Wagner

Arthur Daniel Bixler

Sarah Jane Dulley

Peter De Geest

Thomas Richard Gaffney

Hoanh Pham

Eric S Wagner

Vaneric Edward Stein

Robert Byron Moore

Paul Nigel Dyer

Rene Hendrik Van Doorn

James Richard O'leary

The present disclosure provides systems and methods for hydrogen production as well as apparatuses useful in such systems and methods, including steam generation systems and methods. Hydrogen is produced by reforming of a hydrocarbon in a plurality of reformers to achieve improved reforming efficiency. A COconvective reformer (CCR) and an oxygen secondary reformer (OSR) are used in series to convert hydrocarbon and steam to synthesis gas with substantially complete carbon capture. Steam generation is provided along separate pathways to provide separate steam streams of different composition.

Systems and methods for producing hydrogen with integrated capture of carbon dioxide

Disclosed techniques include liquid purification with pressure vessels. Access to a set of at least two pressure vessels is obtained. The pressure vessels are interconnected using piping and computer-controlled switching valves. A first pressure vessel of the set is filled with a liquid. A second pressure vessel of the set is filled with a pressurized gas. The pressurized gas is sharp interface immiscible with the liquid. Switching valves are controlled to enable the pressurized gas in the second pressure vessel to force the liquid from the first pressure vessel into a purification chamber. Additional switching valves are controlled to enable a third pressure vessel to fill with liquid while a fourth pressure vessel is filled with purification chamber retentate. The liquid is prepurified prior to filling the first pressure vessel. The prepurifying is enabled by compressed air. The purification chamber includes a reverse osmosis chamber.

Liquid purification with pressure vessels

Disclosed techniques include enabling controlled refrigeration and liquefaction and energy management. A liquid is pumped into a closed chamber to compress a vapor. Pressure is increased in the closed chamber by pumping additional liquid into the closed chamber. The increasing pressure enables assimilation of the vapor into the liquid. The heat of compression is removed from the vapor simultaneously with compression. The liquid containing the vapor that was assimilated is withdrawn from the chamber. It is flashed to release at least a portion of the vapor that was assimilated. The flashing results in absorbing a latent heat of vaporization from surfaces in thermal contact with the liquid. A first and second heating/cooling circuit are controlled. Gas within the first heating/cooling circuit is cooled and compressed using a liquid piston. A gas is warmed within the second heating/cooling circuit, and expansion is accomplished using a liquid piston.

Controlled refrigeration and liquefaction using compatible materials for energy management

Disclosed techniques include controlled liquefaction and energy management. A gas within a first pressure containment vessel is pressurized using a column of liquid. The gas that is being pressurized is cooled using a liquid spray, wherein the liquid spray is introduced into the first pressure containment vessel in a region occupied by the gas. The liquid spray keeps the pressurizing to be isothermal. The gas that was pressurized is metered into a second pressure containment vessel, wherein the metering enables liquefaction of the gas. The gas that was pressurized is stored in a gas capacitor prior to the metering. The gas that was liquefied in the second pressure containment vessel is pushed into a holding tank, wherein the holding tank stores a liquefied state of the gas, and wherein the pushing is accomplished by the pressure of the gas that was metered into the second pressure containment vessel.

Controlled liquefaction and energy management

Disclosed techniques include desalination using pressure vessels. Access to a set of at least three pressure vessels is obtained. The pressure vessels are interconnected using piping and computer-controlled switching valves. A first pressure vessel of the set is filled with a prepurified liquid. A second pressure vessel of the set is filled with a pressurized gas. The pressurized gas is sharp interface immiscible with the prepurified liquid. The switching valves are controlled to enable the pressurized gas in the second pressure vessel to force the prepurified liquid from the first pressure vessel into a reverse osmosis chamber. The switching valves are controlled to enable a third pressure vessel of the set to fill with additional prepurified liquid. The switching valves are controlled to enable the pressurized gas that entered the first pressure vessel to force the additional prepurified liquid from the third pressure vessel into the reverse osmosis chamber.

Desalination using pressure vessels

Reactive diluent fluid () is introduced into a stream of synthesis gas (or 'syngas') produced in a heat-generating unit such as a partial oxidation ('POX') reactor () to cool the syngas and form a mixture of cooled syngas and reactive diluent fluid. Carbon dioxide and/or carbon components and/or hydrogen in the mixture of cooled syngas and reactive diluent fluid is reacted () with at least a portion of the reactive diluent fluid in the mixture to produce carbon monoxide-enriched and/or solid carbon depleted syngas which is fed into a secondary reformer unit () such as an enhanced heat transfer reformer in a heat exchange reformer process. An advantage of the invention is that problems with the mechanical integrity of the secondary unit arising from the high temperature of the syngas from the heat-generating unit are avoided.

Process and apparatus for the production of synthesis gas

Reactive diluent fluid () is introduced into a stream of synthesis gas (or 'syngas') produced in a heat-generating unit such as a partial oxidation ('PDX') reactor () to cool the syngas and form a mixture of cooled syngas and reactive diluent fluid. Carbon dioxide and/or carbon components and/or hydrogen in the mixture of cooled syngas and reactive diluent fluid is reacted () with at least a portion of the reactive diluent fluid in the mixture to produce carbon monoxide-enriched and/or solid carbon depleted syngas which is fed into a secondary reformer unit () such as an enhanced heat transfer reformer in a heat exchange reformer process. An advantage of the invention is that problems with the mechanical integrity of the secondary unit arising from the high temperature of the syngas from the heat-generating unit are avoided.

A system is set forth for the exothermic generation of soot depleted syngas comprising (i) reacting a hydrocarbon-containing fuel with an oxygen containing gas in a first reactor to produce the syngas and byproducts comprising CO, HO and soot; and (ii) introducing the syngas and byproducts into a second reactor containing a non-carbonaceous material that traps the soot for a sufficient time such that the majority of the byproduct soot is gasified via reaction with the byproduct COand/or HO to produce a syngas stream that is depleted in the soot. The system is particularly suitable for the practice of heat exchange reforming wherein a portion of the heat is recovered from the soot depleted syngas stream and used as at least a portion of the heat to facilitate the additional production of syngas via the (endothermic) catalytic reforming of natural gas and steam.

In-situ gasification of soot contained in exothermically generated syngas stream

A steam-hydrocarbon reforming process and apparatus wherein reformate from a prereformer is reacted in a gas heated reformer which is heated by reformed gas from a primary reformer. Reformate from the gas heated reformer is passed to the primary reformer as feed gas.

Steam-hydrocarbon reforming with limited steam export

A tubular reactor for producing a product mixture in a tubular reactor where the tubular reactor comprises an internal catalytic insert with cup-shaped structures having orifices for forming fluid jets for impinging the fluid on the tube wall. Jet impingement is used to improve heat transfer between the fluid in the tube and the tube wall in a non-adiabatic reactor. The tubular reactor and method may be used for endothermic reactions such as steam methane reforming and for exothermic reactions such as methanation.

Tubular reactor with jet impingement heat transfer

A process for producing a hydrogen-containing product gas by catalytic steam-hydrocarbon reforming with an overall steam-to-carbon molar ratio between 1.5 and 2.4 for the process. The process stream is reacted in at least two prereformers prior to reaction in catalyst-containing tubes in a top-fired reformer furnace. The process stream is reacted adiabatically in the first prereformer, while the process stream is heated prior to being introduced into the second prereformer and/or the second prereformer is heated. The process avoids carbon formation on the catalyst in the catalyst-containing tubes in the primary reformer.

Process for producing a hydrogen-containing product gas

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Allentown, PA, United States of America

Shankar Nataraj