초록 ▼

A method of recovering carbon dioxide from a synthesis gas stream generated within a synthesis gas facility. After the synthesis gas stream is passed through at least one process heat exchanger of the steam generation system located downstream of the water-gas shift reactor, the temperature of the s

A method of recovering carbon dioxide from a synthesis gas stream generated within a synthesis gas facility. After the synthesis gas stream is passed through at least one process heat exchanger of the steam generation system located downstream of the water-gas shift reactor, the temperature of the synthesis gas stream is increased while simultaneously adding steam to the synthesis gas stream. Thereafter, the synthesis gas stream is added to an absorption system having an absorption zone utilizing a solvent to absorb the carbon dioxide and a regeneration zone to disengage the carbon dioxide from the solvent and thereby regenerate the solvent. Heat is transferred from the synthesis gas stream to the regeneration zone to promote disengagement of the carbon dioxide from the steam and such that between about 40 percent and about 90 percent of the carbon dioxide originally present in the synthesis gas stream is recovered.

대표청구항 ▼

We claim: 1. A method of recovering carbon dioxide from synthesis gas stream generated within a facility having a synthesis gas reactor, a water-gas shift reactor and a steam generation system for generating steam for the synthesis gas reactor and for export, said method comprising: extracting a sy

We claim: 1. A method of recovering carbon dioxide from synthesis gas stream generated within a facility having a synthesis gas reactor, a water-gas shift reactor and a steam generation system for generating steam for the synthesis gas reactor and for export, said method comprising: extracting a synthesis gas stream from the facility after the synthesis gas stream has passed through at least one process heat exchanger of the steam generation system wherein at least one process heat exchanger being located downstream of the water-gas shift reactor and the synthesis gas stream upon extraction from the facility having an initial steam content that is at or near dew point; exchanging heat from at least part of a steam stream to the synthesis gas stream, after extraction from the facility, to increase temperature of the synthesis gas stream while simultaneously adding steam to the synthesis gas stream such that a heated synthesis gas stream is produced that has a final steam content that is in a superheated state; introducing the heated synthesis gas stream to an absorption system having an absorption zone utilizing a solvent for absorbing the carbon dioxide contained within the heated synthesis gas stream, thereby to produce a rich liquid containing the carbon dioxide and a treated synthesis gas stream having a lower content of the carbon dioxide than said synthesis gas stream and a regeneration zone operatively associated with the absorption zone for receiving solvent after having absorbed carbon dioxide and disengaging the carbon dioxide from the solvent, thereby to regenerate the solvent and for returning the solvent after having been regenerated to the absorption zone; transferring heat from the heated synthesis gas stream to the regeneration zone for promoting the disengagement of the carbon dioxide from the rich liquid; recovering a carbon dioxide stream composed of the carbon dioxide separated from the rich liquid; and the flow rate of the steam stream being controlled so that between about 40 percent and about 90 percent of the carbon dioxide contained in the synthesis gas stream is recovered in the carbon dioxide stream. 2. The method of claim 1, wherein the steam stream is superheated stream and the heat is transferred to the synthesis gas stream and steam is added thereto by extracting superheated steam from the steam generation system, forming the steam stream from the superheated steam and combining at least part of the steam stream with the synthesis gas stream. 3. The method of claim 1, wherein the steam stream is low pressure steam and the heat is transferred to the synthesis gas stream and steam is added thereto by introducing the synthesis gas stream into a saturator and indirectly transferring heat from the steam stream to a water stream from the saturator and thereafter re-introducing the water stream into the saturator so that the synthesis gas stream and the water stream are counter-currently passed through the saturator and transferring heat to the synthesis gas stream from the steam stream after the addition of the steam thereto through indirect heat exchange with the steam stream. 4. The method of claim 2 or claim 3, wherein: the heated synthesis gas stream is cooled to condense water contained therein, thereby to produce a condensate and the condensate is separated from the heated synthesis gas stream after cooling to produce a lower water content synthesis gas stream; the absorption zone is formed by an absorption column and the lower water content synthesis gas stream and the solvent are counter-currently passed within a first set of mass-transfer contact elements located within the absorption column to absorb the carbon dioxide in the solvent as the solvent descends in the absorption column, thereby to produce the rich liquid as a first liquid column bottoms and the treated synthesis gas as a first tower overhead; the regeneration zone includes a low pressure flash column and the solvent containing the absorbed carbon dioxide is expanded into a low pressure flash column to produce the initial disengagement of a portion of the carbon dioxide from the rich liquid and an intermediate liquid containing the solvent and a further portion of the carbon dioxide, the low pressure flash column including a second set of mass-transfer contact elements to contact the intermediate liquid as it descends through the second set of mass-transfer contact elements with an ascending vapor phase to effect an additional disengagement of the further portion of the carbon dioxide from the intermediate liquid and a liquid column bottoms, thereby to produce a second tower overhead composed of the carbon dioxide and a second liquid column bottoms composed of regenerated solvent; a regenerated solvent stream, made up of the second liquid column bottoms, is extracted from the low pressure flash column, cooled and then pumped back into the absorption column to introduce the solvent into the absorption column to absorb the carbon dioxide; and the carbon dioxide stream is made up of the second tower overhead and is extracted from the low pressure flash column. 5. The method of claim 4, wherein: the solvent functions as both a physical absorbent and a chemisorbent; a water stream is added to the absorption column and washes down any solvent contained in treated synthesis gas used in forming the treated synthesis gas stream; the condensate derived from the heated synthesis gas stream is a first condensate and the water content separated therefrom is a first water content; the carbon dioxide stream is cooled to condense out a second water content of the carbon dioxide stream and thereby to produce a second condensate; and a second condensate stream composed of the second condensate is introduced into the low pressure flash column and washes down any solvent contained in the carbon dioxide produced as the second tower overhead. 6. The method of claim 5, wherein the carbon dioxide stream is compressed in stages with interstage cooling and water removal to form a compressed carbon dioxide stream. 7. The method of claim 5, wherein the heat is transferred to the regeneration zone by indirectly exchanging heat from the heated synthesis gas stream to the second liquid column bottoms so that the ascending vapor phase is formed without boiling the second liquid column bottoms. 8. The method of claim 5, wherein the heat is indirectly transferred from the heated synthesis gas stream to the rich liquid stream prior to being expanded into the low pressure flash column. 9. The method of claim 5, wherein: the steam stream is divided into first and second subsidiary streams; part of the heat is transferred from the first subsidiary stream to the synthesis gas stream while adding steam thereto, thereby to form the heated synthesis gas stream; a remaining part of the heat is transferred from the second subsidiary stream to the second liquid column bottoms so that the ascending vapor phase is formed without boiling the second liquid column bottoms; and heat is indirectly transferred from the heated synthesis gas stream to a rich liquid stream composed of the rich liquid; and the rich liquid stream is expanded into the low pressure flash column. 10. The method of claim 7, wherein the carbon dioxide stream is compressed in stages with interstage cooling and water removal to form a compressed carbon dioxide stream. 11. The method of claim 8, wherein the carbon dioxide stream is compressed in stages with interstage cooling and water removal to form a compressed carbon dioxide stream. 12. The method of claim 9, wherein the carbon dioxide stream is compressed in stages with interstage cooling and water removal to form a compressed carbon dioxide stream.