Abstract: In a process for separating a feed flow containing hydrogen, carbon dioxide and at least one of the components chosen from the list of carbon monoxide, methane or nitrogen, a feed flow is separated forming a mixture (1) containing predominantly hydrogen, carbon dioxide and at least one of the components chosen from the list of carbon monoxide, methane or nitrogen and the mixture is separated by membrane separation in a membrane system (M1, M2) comprising a turbine (T1, T2) coupled with at least one booster compressor (C1, C2).

Abstract: In a process for separating a mixture containing hydrogen and carbon dioxide, the mixture is compressed to form a compressed mixture, the compressed mixture is separated by partial condensation and/or distillation generating a first CO2-depleted stream, the first CO2-depleted stream is separated by permeation through a membrane system to form a residue of the membrane system which is depleted in hydrogen and carbon dioxide and a portion of the residue is recycled, after expansion, to the compressor to be compressed therein.

Abstract: Method for producing a gas enriched in carbon dioxide from a feed synthesis gas comprising at least one condensable component and in particular hydrogen, characterized in that the method further comprises: a step referred to as a desaturation step during which at least a portion of the condensable component contained in the feed synthesis gas is, upstream of said pressure swing adsorption separation unit, condensed by cooling to a temperature below 10° C., in particular below or equal to 5° C., and separated, producing said desaturated synthesis gas and at least one condensate; the feed synthesis gas exchanging heat with the desaturated synthesis gas so as to heat said desaturated synthesis gas.

Abstract: A process to separate cryogenically a pressurized wet rich CO2 stream with at least 60% CO2 mol % and at least one other light component, including at least the following steps. Separation of water condensates from feed gas Dehydration of feed gas in a dedicated vessel. Condensation of CO2 rich feed gas creating an enriched CO2 liquid and a depleted CO2 gaseous stream. Vaporization of rich liquid CO2 stream. Separation of gaseous stream in membranes thereby creating an enriched CO2 stream and a depleted CO2 stream. Vent to the atmosphere depleted CO2 stream. Compression of enriched CO2 stream. Condensation of stream creating an enriched CO2 liquid and a depleted CO2 gaseous stream. Mixing liquid stream with liquid stream. Mixing gaseous streams.

Abstract: In a process of liquefaction and subcooling of a stream rich in CO2, the stream is liquefied by a closed cycle of refrigerant and subcooled by heat exchange with three streams of liquid CO2 at different pressures.

Abstract: A process for separating a gas mixture, a first item of equipment of the process is heated by a first flow of a first heat producer and supplies heat to a first fluid, the first flow of heat producer being heated upstream of the first item of equipment by a heat source, a second item of equipment of the process heats a second fluid while consuming heat, the heat originating from a second flow of the first heat producer heated by the heat source, which heats the second flow of the first heat producer up to an intermediate temperature lower than the second temperature, and by a heater downstream of the source, which heats the second flow of the first heat producer, which has been heated by the heat source, from the intermediate temperature up to a second temperature higher than the first temperature.

Abstract: The carbon capture process includes, under normal operation: a first stream is compressed, dried, cooled and separated by partial condensation step a phase separator forming a liquid enriched in CO2 and a gas enriched in the at least one component lighter than CO2. And the gas enriched in the component lighter than CO2 is warmed in the heat exchanger and then expanded in a turbine, and then is sent to the atmosphere or to a cooling tower. Under start-up conditions, a phase separator is at a first temperature and a second stream of a gaseous mixture containing CO2 and at least one component lighter than CO2 is expanded in the turbine to produce an expanded gas at a second temperature different from the first temperature, the expanded gas being then warmed in the heat exchanger or sent to be separated in a distillation column of the carbon capture process.

Abstract: In a method for liquefying a gas rich in carbon dioxide, the gas is compressed to a first pressure greater than its critical pressure in a compressor to form a compressed gas, the compressed gas is cooled through heat exchange with a refrigerant to a variable temperature to form a cooled compressed gas with a density between 370 and 900 kg/m3, the cooled compressed gas is cooled at supercritical pressure in a first heat exchanger to a temperature below the critical temperature, the gas cooled below the critical temperature is expanded to a second pressure between 45 and 60 bara to form a diphasic fluid which is separated in a phase separator to form a liquid and a gas, and a liquid portion originating from the phase separator provides cold to the first heat exchanger.

Abstract: An apparatus for separation of a flow containing at least 95 mol % of carbon dioxide and also at least one impurity lighter than carbon dioxide by distillation comprises a heat exchanger (20), a distillation column (30), expansion means (V3), means for sending the flow to be cooled in the heat exchanger, means for sending the cooled flow to be separated in the distillation column, means for withdrawing at the bottom of the column a liquid flow containing at least 99 mol % of carbon dioxide, means for sending at least a portion (12) of the liquid flow to be cooled in the heat exchanger to form a subcooled liquid (3), means for sending at least a portion of the subcooled liquid to the expansion means to produce a two-phase flow, a phase separator (40) for separating the two-phase flow to form a gas and a liquid, means for sending at least a portion (14) of the liquid from the phase separator to be vaporized in the heat exchanger and means for taking a portion (4) of the liquid from the phase separator.

Abstract: Two streams containing CO2 with different purities are separated in a common distillation column, without having been compressed or purified of water together.

Abstract: A process for membrane separation of a mixture containing as main, or even major, components hydrogen and carbon dioxide and also at least one other component, for example chosen from the following group: carbon monoxide, methane and nitrogen, including: heating of the mixture in the heat exchanger, permeation of the reheated mixture in a first membrane separation unit making it possible to obtain a first permeate which is a hydrogen and carbon dioxide enriched relative to the mixture, and a first residue which is hydrogen and carbon dioxide lean, permeation of the first residue in a second membrane separation unit making it possible to obtain a second residue, at least one portion of the first permeate is compressed in a booster compressor and the second residue is expanded in a turbine, the booster compressor being driven by the turbine.

Abstract: Apparatus for separation of a gaseous mixture containing CO2, hydrogen and water includes a compressor for compressing the gaseous mixture to a first pressure between 20 to 60 bara, a temperature swing adsorption unit for drying the compressed gas mixture comprising at least two adsorbent beds, a separation unit for separation of the dry and compressed gaseous mixture in by at least one of the following techniques: partial condensation, distillation, washing and solidification to produce at least two streams, being a rich CO2 liquid enriched in CO2 and depleted in at least one of methane and hydrogen and carbon monoxide as compared with the gaseous mixture and a first residual gas depleted in CO2 and enriched in at least one of methane and hydrogen and carbon monoxide as compared with the gaseous mixture, a pressure swing adsorption unit for separation of the first residual gas depleted in CO2 by at least one pressure swing adsorption unit in order to produce at least one gas richer in CO2 than the first resi

Abstract: A heat integration method, including providing a hot gas stream, wherein the hot gas stream includes carbon dioxide and at least one gas from the following: carbon monoxide, nitrogen, and oxygen. Recovering waste heat from the hot gas stream by producing a steam stream by indirect heat exchange, and utilizing the steam stream in a carbon capture system, wherein the carbon capture system includes a cryogenic partial condensation step. Wherein the carbon capture system produces a product carbon dioxide stream.

Abstract: A facility for recovering carbon dioxide from a feed gas flow, including a unit for treating the feed gas flow in order to produce, from feed gas flow, a carbon dioxide-rich gas flow and a nitrogen-rich gas flow, a compression stage for compressing the feed gas flow, an expansion stage capable of outputting mechanical energy generated by the expansion of the nitrogen-rich gas flow, a thermal device arranged to enable heat transfers to take place between the gas flow leaving the compression stage and the nitrogen-rich gas flow prior to expansion, and a device for utilising the mechanical energy output by the expansion stage.

Abstract: A process for separating CO2 from a feed stream containing at least CO2 and at least one lighter component chosen among oxygen, nitrogen, argon, methane, CO and hydrogen and at least one component heavier than CO2, comprises cooling the feed stream in a heat exchanger (E1) to a temperature less than 30° C., separation of the cooled feed stream producing a first liquid enriched in CO2 and a first gas depleted in CO2, expanding at least part of the first liquid, producing a second liquid, vaporizing the second liquid in the heat exchanger (E1) producing a second gas, sending the compressed cooled second gas to the bottom of a scrubber column (K2) and removing a top gas of the scrubber column depleted in the at least one heavier component.

Abstract: A facility for cooling a gas flow containing CO2, water and at least one other component includes a scrubbing tower, a pipe for conveying the gas flow at a first temperature to the bottom of the tower, a pipe for conveying water at a second temperature, which is lower than the first temperature, to a first level at the top of the scrubbing tower, a pump, a pipe being connected to the tank of the column for removing tank water and to the pump for pressurizing the water removed from the tank, and means for withdrawing water downstream of the pump, these means being connected to the tower thereby conveying the pressurized water at a third temperature to an indirect heat exchanger located in the tower at the second level above the first level, the third temperature being higher than the second temperature, but lower than the first temperature.

Abstract: An apparatus for separation of a flow containing at least 95 mol % of carbon dioxide and also at least one impurity lighter than carbon dioxide by distillation comprises a heat exchanger (20), a distillation column (30), expansion means (V3), means for sending the flow to be cooled in the heat exchanger, means for sending the cooled flow to be separated in the distillation column, means for withdrawing at the bottom of the column a liquid flow containing at least 99 mol % of carbon dioxide, means for sending at least a portion (12) of the liquid flow to be cooled in the heat exchanger to form a subcooled liquid (3), means for sending at least a portion of the subcooled liquid to the expansion means to produce a two-phase flow, a phase separator (40) for separating the two-phase flow to form a gas and a liquid, means for sending at least a portion (14) of the liquid from the phase separator to be vaporized in the heat exchanger and means for taking a portion (4) of the liquid from the phase separator.

Abstract: In a process for separating a mixture containing hydrogen and carbon dioxide, the following steps are present: a) cooling of the mixture in a heat exchanger by sending the mixture to the heat exchanger, resulting in the partial condensation of the mixture into a liquid phase enriched in carbon dioxide and a gas phase depleted in carbon dioxide, a gaseous fluid which is heated in the heat exchanger by indirect heat exchange, b) separating the liquid phase from the gas phase in a separator vessel, c) heating of the gas phase originating from at least one of the separator vessels in the heat exchanger, d) sending of the at least one heated part from step c) to a membrane separation unit, generating a residue depleted in hydrogen and carbon dioxide and e) expansion of the at least one residue in a turbine producing an expanded fluid, f) the expanded fluid constituting the gaseous fluid of step a) which is heated in the heat exchanger by indirect heat exchange.

Abstract: In a process for separating a mixture containing hydrogen and carbon dioxide, the mixture is compressed to form a compressed mixture, the compressed mixture is separated by partial condensation and/or distillation generating a first CO2-depleted stream, the first CO2-depleted stream is separated by permeation through a membrane system to form a residue of the membrane system which is depleted in hydrogen and carbon dioxide and a portion of the residue is recycled, after expansion, to the compressor to be compressed therein.

Abstract: In a method for separating a flow containing at least 95 mol % of carbon dioxide and at least one impurity lighter than carbon dioxide by distillation, the flow is cooled to a first intermediate temperature between those of the cold end and the hot end of a heat exchange means in order to form a liquid flow at a first temperature and a first pressure and it is split into at least two to form a first fraction and a second fraction, the first fraction is expanded to the pressure of a distillation column, referred to as second pressure, which is lower than the first pressure, and it is sent to an intermediate level of the distillation column, the second fraction is cooled in the heat exchange means to the cold end thereof, it is expanded to the pressure of the distillation column and is sent to a level of the distillation column above the point of arrival of the first fraction, a liquid flow containing at least 99 mol % of carbon dioxide is withdrawn from the bottom of the column, and a fraction of the liquid fl