Fluor Technologies Corporation

Fluor Technologies Corporaticn

Paul M Mathias

Satish Reddy

Joseph Yonkoski

Ravi Ravikumar

Sanjiv Dabee

Paul E Koppel

A system for carbon dioxide capture from a gas mixture comprises an absorber that receives a lean solvent system stream (containing a chemical solvent, physical-solvent, and water) from the stripper, a stripper that receives the rich solvent stream from the absorber and produces the product carbon dioxide and the lean solvent through the use of a reboiler in fluid communication with a lower portion of the stripper, a condenser in fluid communication with a vapor outlet of the stripper, a cross-exchanger in fluid communication with a rich solvent system outlet from the absorber and a rich solvent system inlet on the stripper, and a splitter. The splitter is configured to separate the rich solvent system stream into a first portion and second portion, where the first portion directly passes to the stripper and the second portion passes through the cross-exchanger prior to passing to the stripper.

Methods and systems for improving the energy efficiency of carbon dioxide capture

A system for carbon dioxide capture from a gas mixture comprises a lean solvent comprising 3-amino-1-propanol (AP), 2-dimethylamino-2-methyl-1-propanol (DMAMP), and water; an absorber containing at least a portion of the lean solvent, wherein the absorber is configured to receive the lean solvent and a gaseous stream comprising carbon dioxide, contact the lean solvent with the gaseous stream, and produce a rich solvent stream and a gaseous stream depleted in carbon dioxide; a stripper, wherein the stripper is configured to receive the rich solvent stream; a cross-exchanger fluidly coupled to a rich solvent outlet on the absorber and a rich solvent inlet on the stripper; a reboiler fluidly coupled to a lower portion of the stripper; and a condenser fluidly coupled to a vapor outlet of the stripper.

Systems and methods of COdesublimation are presented in which refrigeration content is retained within the system. Most preferably, refrigeration content is recycled by providing the refrigeration content of a CO-lean feed gas to the CO-containing feed gas and to pre-cooling of a desublimator, and/or by providing refrigeration of effluent of a desublimator in regeneration to a refrigerant in a closed refrigeration cycle for deep-cooling of another desublimator.

Configurations and methods of COcapture from flue gas by cryogenic desublimation

A method of producing hydrogen comprising receiving a sour gas comprising CO, HS, and ammonia from a sour water stripper; introducing the sour gas to an absorption system to produce an ammonia rich gas and a sulfide rich gas, wherein the ammonia rich gas comprises ammonia and CO, and wherein the sulfide rich gas comprises HS and CO; compressing the ammonia rich gas in a compressing unit to a pressure of 400-600 psig to produce a compressed ammonia rich gas; introducing the compressed ammonia rich gas to an ammonia cracker unit comprising a catalyst to produce a cracked gas, wherein the ammonia cracker unit is characterized by a cracking temperature of 450-550&#xb0; C., and wherein the cracked gas comprises hydrogen, nitrogen, and CO; and introducing the cracked gas to a PSA unit to produce hydrogen and a PSA tail gas, wherein the PSA tail gas comprises nitrogen and CO.

Production of pure hydrogen from ammonia rich sour water stripper overhead

A system for carbon dioxide capture from a gas mixture comprises an absorber that receives a lean solvent system stream (containing a chemical solvent, physical-solvent additive, and water) from the stripper, a stripper that receives the rich solvent stream from the absorber and produces the product carbon dioxide and the lean solvent through the use of a reboiler in fluid communication with a lower portion of the stripper, a condenser in fluid communication with a vapor outlet of the stripper, a cross-exchanger in fluid communication with a rich solvent system outlet from the absorber and a rich solvent system inlet on the stripper, and a splitter. The splitter is configured to separate the rich solvent system stream into a first portion and a second portion, where the first portion directly passes to the stripper and the second portion passes through the cross-exchanger prior to passing to the stripper.

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Systems and methods for pre-treatment of acid gas are presented in which ammonium is removed from the acid gas in an absorber that is operated at significantly elevated temperature using dilute phosphoric acid. While seemingly incompatible, absorbing ammonia at high heat in the absorber will allow for production of a diammonium phosphate product that is ultra-low in residual sulfurous compounds and prevent crystallization of phosphate salts due to the increased solubility of the salts in the hot diluted solvent.

Claus plant preprocessing systems and methods for removal of ammonia from claus plant feed gases

Systems and methods are described for selectively removing an acid gas from a feed stream to reduce co-absorption of CO. The system can include an absorber configured to contact at least a portion of the feed stream with a caustic solution or other basic solvents to produce a clean stream substantially depleted of the acid gas. To reduce co-absorption of COby the caustic solution to less than 10% of the COpresent in the feed stream, the absorber can be further configured to receive a driver gas that is substantially non-reactive with the caustic solution.

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Aliso Viejo, CA, United States of America

Paul M Mathias