Process for the recovery of a concentrated carbon dioxide stream
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IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C01B-003/56
B01D-053/047
출원번호
US-0971308
(2010-12-17)
등록번호
US-8486180
(2013-07-16)
발명자
/ 주소
Chen, Yudong
출원인 / 주소
American Air Liquide, Inc.
인용정보
피인용 횟수 :
1인용 특허 :
8
초록▼
A concentrated carbon dioxide stream is produced during a hydrogen pressure swing adsorption unit cycle by fractionating the carbon dioxide removed from the adsorbent in the adsorption beds during the regeneration of the adsorption beds. Thereby providing a cost efficient process for producing merch
A concentrated carbon dioxide stream is produced during a hydrogen pressure swing adsorption unit cycle by fractionating the carbon dioxide removed from the adsorbent in the adsorption beds during the regeneration of the adsorption beds. Thereby providing a cost efficient process for producing merchant carbon dioxide.
대표청구항▼
1. A process for producing a concentrated carbon dioxide stream for use in the production of merchant carbon dioxide during the regeneration of adsorbent and production of a carbon dioxide containing tail gas in an adsorption bed of a hydrogen pressure swing adsorption unit cycle, the process compri
1. A process for producing a concentrated carbon dioxide stream for use in the production of merchant carbon dioxide during the regeneration of adsorbent and production of a carbon dioxide containing tail gas in an adsorption bed of a hydrogen pressure swing adsorption unit cycle, the process comprising fractionating the carbon dioxide containing tail gas produced during regeneration of the adsorbent in the adsorption bed by counter-currently depressurizing the adsorption bed to desorb a carbon dioxide adsorbed to the adsorbent of the adsorption bed thereby forming a carbon dioxide rich fraction which is withdrawn from the adsorption bed and passed to a first desorption tank followed by purging the adsorption bed to allow for displacement of any residual carbon dioxide from the adsorbent thereby forming a carbon dioxide lean fraction which is withdrawn from the purged first adsorption bed and passed to a second desorption tank, wherein the concentration of carbon dioxide in the carbon dioxide rich fraction is greater than 60 mole %, and wherein during counter-current depressurization, the adsorption bed is reduced to a pressure that ranges from about ambient pressure to about 15 psig. 2. A process for producing a concentrated carbon dioxide stream for use in the production A process for recovering a concentrated carbon dioxide stream during a hydrogen pressure swing adsorption unit cycle, the concentrated carbon dioxide stream to be used in the production of merchant carbon dioxide, the process comprising: subjecting a hydrogen rich feed stream to the cycle of treatment in the hydrogen pressure swing adsorption unit in order to produce a high purity hydrogen stream, a carbon dioxide rich fraction and a carbon dioxide lean fraction, the hydrogen pressure swing adsorption unit including at least two adsorption beds, with each bed running on a cycle that includes the phases of (1) adsorption, (2) co-current depressurization that includes equalization depressurization and depressurization to purge, (3) countercurrent depressurization, (4) purge, and (5) repressurization that includes equalization repressurization and finalizing repressurization, the two or more adsorption beds operating continuously and in a staggered scheme, with each of the adsorption beds including one or more adsorbents for carbon dioxide and for the components carbon monoxide, methane, and trace amounts of water; wherein during the cycle of treatment in the hydrogen pressure swing adsorption unit:i) a first adsorption bed which has been subjected to the adsorption phase is co-currently depressurized by allowing an effluent stream from the first adsorption bed to flow to a second adsorption bed that is in the repressurization phase until near equalization in pressure between the first adsorption bed and the second adsorption bed is reached, then directing the depressurization effluent stream from the first adsorption bed to purge a third adsorption bed that is in the purge phase of the cycle, thereby producing a reduced first adsorption bed;ii) during the counter-current depressurizing phase of the cycle, counter-currently depressurizing the reduced first adsorption bed to desorb carbon dioxide thereby producing a partially desorbed first adsorption bed and forming a carbon dioxide rich fraction which is withdrawn from the partially desorbed first adsorption bed and passed to a first desorption tank that is in communication with each of the adsorption beds;iii) during the purge phase of the cycle, purging the partially desorbed first adsorption bed using the depressurization effluent stream from a still further adsorption bed that is in the depressurization phase to allow for the displacement of the residual carbon dioxide and the remaining components from the one or more adsorbents thereby forming a purged first adsorption bed and a carbon dioxide lean fraction which is withdrawn from the purged first adsorption bed and passed to a second desorption tank that is in communication with each of the adsorption beds;iv) repressurizing the purged first adsorption bed using a depressurization effluent stream from an adsorption bed in the depressurization phase to obtain a partially repressurized first adsorption bed and then further repressurizing the partially repressurized first adsorption bed utilizing a portion of the high purity hydrogen stream from the adsorption phase;iv) withdrawing the carbon dioxide rich fraction from the first desorption tank and compressing this carbon dioxide rich effluent before sending this compressed carbon dioxide rich fraction to be further treated for the recovery of a merchant carbon dioxide product by either subjecting the compressed carbon dioxide rich fraction to cryogenic purification or to carbon dioxide pressure swing adsorption followed by cryogenic purification; andv) withdrawing the carbon dioxide lean fraction from the second desorption tank and recycling the carbon dioxide lean fraction for further use as a make up fuel. 3. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 2, wherein the concentration of carbon dioxide in the carbon dioxide rich fraction is greater than 60 mole %. 4. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 2, wherein the concentration of carbon dioxide in the carbon dioxide rich fraction is from about 60 mole % to about 75 mole %. 5. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 4, wherein the one or more adsorbents are selected from zeolite, activated carbon and activated alumina. 6. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 3, wherein at the beginning of the co-current depressurization phase, the adsorption bed is at a pressure from about 200 psig to about 600 psig. 7. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 6, wherein at the beginning of the repressurization phase, the adsorption bed is at near ambient pressure. 8. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 6, wherein during the counter-current depressurization phase of the cycle, the first adsorption bed is reduced to a pressure that ranges from about ambient to about 15 psig. 9. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 2, wherein the second desorption tank is smaller in size than the first desorption tank. 10. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 2, wherein the hydrogen pressure swing adsorption unit includes from 2 to 12 adsorption beds. 11. A process for producing a concentrated carbon dioxide stream for use in the production A process for recovering high purity gaseous hydrogen and high purity gaseous carbon dioxide from a hydrogen pressure swing adsorption unit, the process comprising: a) providing a hydrogen pressure swing adsorption unit that includes: 1) at least two adsorption beds, with each bed running on a cycle that includes (1) adsorption, (2) co-current depressurization that includes equalization depressurization and depressurization to purge, (3) countercurrent depressurization, (4) purge at low pressure, and (5) repressurization that includes equalization repressurization and finalizing repressurization, at least one of the adsorption beds being in a different phase of the cycle compared to at least one of the remaining adsorption beds being utilized, with each of the adsorption beds including one or more adsorbents for carbon dioxide and for the components carbon monoxide, methane, and trace amounts of water;2) a flow reversible first conduit for receiving feed for each of the adsorption beds,3) a high purity gaseous hydrogen stream flow reversible second conduit for each of the adsorption beds,4) a first desorption stream tank connected to the one or more adsorption beds, and5) a second desorption stream tank connected to the one or more adsorption beds;b) initially increasing the pressure in at least one of the adsorption beds to provide at least one high pressure adsorption bed;c) introducing a feed stream containing carbon dioxide, carbon monoxide, methane, hydrogen and trace amount of water into the flow reversible first conduit for receiving feed of at least one of the adsorption beds and allowing the feed stream to pass over the one or more adsorbents in the one or more adsorption beds in order to allow for the adsorption of the carbon dioxide, carbon monoxide, methane, and trace amounts of water and a portion of the hydrogen from the feed stream to the one or more adsorbents and the concentration of the remaining gaseous hydrogen in the feed stream to form a high purity gaseous hydrogen stream;d) withdrawing the high purity gaseous hydrogen stream via the corresponding high purity gaseous hydrogen stream flow reversible second conduit and passing this high purity gaseous hydrogen stream on for storage;e) during the depressurization phase of the cycle, gradually co-currently depressurizing one or more of the adsorption beds that have been through the adsorption phase by allowing communication with one or more adsorption beds already in the repressurization phase that are at a lower pressure in order to achieve a bed to bed equalization and then further co-currently depressurizing the one or more equalized adsorption beds by withdrawing a depressurization effluent stream from the top of one or more of the equalized adsorption beds and directing this stream to one or more adsorption beds in the purge phase thereby producing one or more reduced adsorption beds;f) counter-currently depressurizing the one or more reduced adsorption beds to allow for the desorption from the one or more adsorbents of carbon dioxide and a portion of the remaining components thereby producing one or more depressurized adsorption beds and forming a carbon dioxide enriched desorbed stream which is passed to the first desorbed stream tank via the flow reversible first conduit;g) purging the one or more depressurized adsorption beds with the depressurization effluent stream of step e) to allow for the desorption of the residual carbon dioxide and the remaining components from the one or more adsorbents to form a carbon dioxide depleted desorbed stream which is passed to the second desorbed stream tank via the flow reversible first conduit thereby producing one or more purged adsorption beds;h) repressurizing the one or more purged adsorption beds by communicating the one or more purged adsorption beds with one or more adsorption beds entering the bed regeneration phase;i) completing the repressurization of the one or more purged adsorption beds by injecting a portion of the high purity gaseous hydrogen stream to achieve a pressure that is close to the pressure of the high pressure feed gas stream;j) compressing the carbon dioxide enriched desorbed steam in the first desorbed stream tank and sending this compressed carbon dioxide enriched desorbed stream for recovery of high purity of carbon dioxide product; andk) recycling the carbon dioxide depleted desorbed stream in the second desorbed stream tank for further use. 12. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 11, wherein the feed gas to the hydrogen pressure swing adsorption unit is obtained from either a coal gasification unit in combination with a water gas shift unit or a steam hydrocarbon reformer unit in combination with a water gas shift unit. 13. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 12, wherein the one or more adsorbents are selected from zeolite, activated carbon and activated alumina. 14. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 13, wherein the hydrogen pressure swing adsorption unit includes from 2 to 12 adsorption beds. 15. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 12, wherein the concentration of carbon dioxide in the carbon dioxide rich fraction is greater than about 60 mole %. 16. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 12, wherein at the beginning of the co-current depressurization phase, the adsorption bed is at a pressure from about 200 psig to about 600 psig. 17. A process for producing a concentrated carbon dioxide stream for use in the production The process of claim 16, wherein at the beginning of the repressurization phase, the adsorption bed is at near ambient pressure.
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