Kellogg Brown + Root LLC

Avinash Malhotra

Shashi Prakash Singh

David P Mann

Robert Burlingame

Kamal Gursahani

Tim Weeks

Jim Gosnell

James Hanlan Gosnell

Siva Ariyapadi

Kamalkumar Ishwar Gursahani

Yue Jing

Martin John Van Sickels

Stanislaus A Knez

Tufail Ahmad

Bradley Richard Welter

Martin J Van Sickels

Reforming exchangers for syngas production are provided. The reforming exchangers can have a shell-and-tube configuration and include a shift catalyst on the shell side of the exchanger to reduce a carbon monoxide concentration in a shell side product gas mixture. Processes for forming syngas using the reforming exchangers are also provided.

Reforming exchanger with integrated shift conversion

Systems and methods for producing ammonia and/or ammonia products. The ammonia and/or ammonia products can be produced by compressing a gas mixture comprising nitrogen, hydrogen, methane, and argon to produce a compressed gas mixture having a pressure of from about 1,000 kPa (130 psig) to about 10,400 kPa (1,495 psig). All or a portion of the compressed gas mixture can be selectively separated at cryogenic conditions to produce a first gas comprising nitrogen and hydrogen, and a second gas comprising methane, argon, residual hydrogen and nitrogen. At least a portion of the first gas can be reacted at conditions sufficient to produce an ammonia product.

High pressure cyrogenic process and system for producing ammonia products

A reforming exchanger system for syngas production is provided. The reforming exchanger system can have a first and a second reforming exchanger, each with a shell-and-tube configuration, and a shift reactor located intermediate to the first and second reforming exchangers to reduce carbon monoxide concentration in the outlet gas. Processes for forming syngas using the reforming exchanger systems described herein are also provided.

Reforming exchanger system with intermediate shift conversion

A gasification system and method. The system can include a gasifier and a purification unit fluidly coupled to the gasifier, with the purification unit receiving raw syngas from the gasifier and producing waste gas and a syngas product. The system can also include a first reformer fluidly coupled to the purification unit, with the first reformer receiving a first portion of the waste gas and producing reformed hydrocarbon. The system can further include a second reformer having a first inlet fluidly coupled to the purification unit, a second inlet fluidly coupled to the first reformer, and an outlet fluidly coupled to the purification unit. The second inlet can receive the reformed hydrocarbon from the first reformer, and the first inlet can receive a second portion of the waste gas from the purification unit. The second reformer can produce a recovered raw syngas that is directed to the purification unit.

Gasification system and process for maximizing production of syngas and syngas-derived products

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

Low-energy, low-capital hydrogen production is disclosed. A reforming exchangeris placed in parallel with an autothermal reformer (ATR)to which are supplied a preheated steam-hydrocarbon mixture. An air-steam mixture is supplied to the burner/mixer of the ATRto obtain a syngas effluent at 650&#xb0;-1050&#xb0; C. The effluent from the ATR is used to heat the reforming exchanger, and combined reformer effluent is shift converted and separated into a mixed gas stream and a hydrogen-rich product stream. High capital cost equipment such as steam-methane reformer and air separation plant are not required.

Autothermal reformer-reforming exchanger arrangement for hydrogen production

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

A process for manufacturing ammonia from syngas with excess air for reforming and nitrogen removal with low pressure losses is disclosed. Auto-refrigeration for cooling the syngas for cryogenic hydrogen enrichment is provided by expansion of a hydrogen-lean waste fluid stream from a distillation column.

Low-delta P purifier for nitrogen, methane, and argon removal from syngas

Recycling a portion of autothermal reformer effluent into the steam-hydrocarbon feed stream with a thermo-compressor ejector is disclosed, using the preheated feed mixture as motive fluid. Syngas recycle-motive fluid molar ratios are 0.2-1.0, selected to optimize the overall configuration. The recycle introduces hydrogen and steam into the feed, and elevates the feed temperature, for operating the reformer in a soot-free regime. There is some pressure drop between the raw feed steam-natural gas mixture and the reformer feed, which requires the raw feed mixture to be supplied at a higher pressure, but this is offset by the lower pressure drop in the process heater and other upstream and downstream equipment due to lower quantities of steam. The feed pre-heater can have a lower duty, and the upstream and downstream equipment can be reduced in size, while the size of the autothermal reformer is about the same compared to the size needed for operation without effluent recycle.

Growing community of inventors

Sugar Land, TX, United States of America

Avinash Malhotra