초록 ▼

The invention provides vacuum swing adsorption processes that produce an essentially carbon monoxide-free hydrogen or helium gas stream from, respectively, a high-purity (e.g., pipeline grade) hydrogen or helium gas stream using one or two adsorber beds. By using physical adsorbents with high heats

The invention provides vacuum swing adsorption processes that produce an essentially carbon monoxide-free hydrogen or helium gas stream from, respectively, a high-purity (e.g., pipeline grade) hydrogen or helium gas stream using one or two adsorber beds. By using physical adsorbents with high heats of nitrogen adsorption, intermediate heats of carbon monoxide adsorption, and low heats of hydrogen and helium adsorption, and by using vacuum purging and high feed stream pressures (e.g., pressures of as high as around 1,000 bar), pipeline grade hydrogen or helium can purified to produce essentially carbon monoxide-free hydrogen and helium, or carbon monoxide, nitrogen, and methane-free hydrogen and helium.

대표청구항 ▼

The invention claimed is: 1. A process for generating an essentially carbon monoxide-free hydrogen gas stream, the process comprising: (a) (i) feeding a high-purity hydrogen gas feed stream for around 30 minutes or more through a first of two adsorbers that are fluidly connected in parallel or in s

The invention claimed is: 1. A process for generating an essentially carbon monoxide-free hydrogen gas stream, the process comprising: (a) (i) feeding a high-purity hydrogen gas feed stream for around 30 minutes or more through a first of two adsorbers that are fluidly connected in parallel or in series and that are each packed with an adsorbent consisting of a zeolite which is cation exchanged with a metal other than a transition metal and which contains less than about 0.5% by weight of a transition metal, and (ii) recovering a first essentially carbon monoxide-free hydrogen gas stream from the first adsorber; (b) thereafter purging the first adsorber by (1) depressurizing it to less than atmospheric pressure, and by (2) (i) recycling a portion of the first essentially carbon monoxide-free hydrogen gas stream through the first adsorber, and/or (ii) feeding an inert gas stream through the first adsorber; and (c) as the first adsorber is purged, feeding a second portion of the high-purity hydrogen gas feed stream for around 30 minutes or more through the second of the two adsorbers and recovering a second essentially carbon monoxide-free hydrogen gas stream from the second adsorber. 2. The process of claim 1, wherein: (a) the adsorbent has a heat of hydrogen adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; and (b) the high-purity hydrogen gas feed streams are fed to the first and second adsorbers at a pressure of between about 30 to about 1,000 bar. 3. The process of claim 1, wherein the zeolite is selected from the group consisting of zeolites A, low silica X (LSX), X, Y, mordenite, chabazite, erionite, offretite, and clinoptilite. 4. The process of claim 1, wherein at least one of the two adsorbers is also packed with one or more of the following: carbon, alumina, silica gel, or a zeolite which is not cation exchanged. 5. The process of claim 1, wherein the two adsorbers are packed with adsorbent particles having a particle size of between about 0.5 mm to about 5 mm. 6. The process of claim 5, wherein the adsorbent particles are selected from the group consisting of CaLSX and CaX. 7. The process of claim 1, wherein: (a) the two adsorbers are packed with adsorbent particles selected from the group consisting of CaLSX and CaX; (b) the adsorbent particles (i) have a particle size of between about 0.5 mm to about 5 mm and (ii) a heat of hydrogen adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; (c) the first adsorber is purged by depressurizing it to around 0.00001 bar to around 0.5 bar; and (d) an essentially carbon monoxide-free hydrogen gas stream is recovered from the two adsorbers. 8. The process of claim 1, further comprising feeding either or both of the first and second essentially carbon monoxide-free hydrogen gas streams to a hydrogen distribution system. 9. The process of claim 8, wherein the hydrogen distribution system includes a hydrogen fuel station for vehicles. 10. The process of claim 1, wherein the first and second essentially carbon monoxide-free hydrogen gas streams contain around 500 ppm methane and around 1,000 ppm nitrogen. 11. The process of claim 1, wherein the first and second essentially carbon monoxide-free hydrogen gas streams contain around 1 to 10 ppb of total impurities. 12. The process of claim 1, wherein the first and second essentially carbon monoxide-free hydrogen gas streams contain around 100 ppb to around 1,000 ppm of nitrogen. 13. The process of claim 12, wherein the first and second essentially carbon monoxide-free hydrogen gas streams contain around 500 ppm or less of methane. 14. A process for generating an essentially carbon monoxide-free hydrogen gas stream, the process comprising: (a) (i) feeding a high-purity hydrogen gas feed stream for around 30 minutes or more through an adsorber that is packed with an adsorbent consisting of a zeolite which is cation exchanged with a metal other than a transition metal and which contains less than about 0.5% by weight of a transition metal, and (ii) recovering an essentially carbon monoxide-free hydrogen gas stream from the adsorber; and (b) thereafter purging the adsorber by (1) depressurizing it to less than atmospheric pressure, and by (2) (i) recycling a portion of the essentially carbon monoxide-free hydrogen gas stream through the adsorber, and/or (ii) feeding an inert gas stream through the first adsorber. 15. The process of claim 14, wherein: (a) the adsorbent has a heat of hydrogen adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; and (b) the high-purity hydrogen gas feed stream is fed to the first and second adsorber at a pressure of between about 30 to about 1,000 bar. 16. The process of claim 14, wherein the zeolite is selected from the group consisting of zeolites A, low silica X (LSX), X, Y, mordenite, chabazite, erionite, offretite, and clinoptilite. 17. The process of claim 14, wherein the adsorber is also packed with one or more of the following: carbon, alumina, silica gel, or a zeolite which is not cation exchanged. 18. The process of claim 14, wherein the adsorber is packed with adsorbent particles having a particle size of between about 0.5 mm to about 5 mm. 19. The process of claim 18, wherein the adsorbent particles are selected from the group consisting of CaLSX and CaX. 20. The process of claim 14, wherein: (a) the adsorber is packed with adsorbent particles selected from the group consisting of CaLSX and CaX; (b) the adsorbent particles (i) have a particle size of between about 0.5 mm to about 5 mm and (ii) a heat of hydrogen adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; (c) the adsorber is purged by depressurizing it to around 0.00001 bar to around 0.5 bar; and (d) an essentially carbon monoxide-free hydrogen gas stream is recovered from the adsorber. 21. The process of claim 14, further comprising feeding the essentially carbon monoxide-free hydrogen gas stream to a hydrogen distribution system. 22. The process of claim 21, wherein the hydrogen distribution system includes a hydrogen fuel station for vehicles. 23. The process of claim 14, wherein the essentially carbon monoxide-free hydrogen gas stream contains around 500 ppm or less methane and around 1,000 ppm or less nitrogen. 24. The process of claim 14, wherein the essentially carbon monoxide-free hydrogen gas stream contains around 1 to 10 ppb of total impurities. 25. The process of claim 14, wherein the essentially carbon monoxide-free hydrogen gas stream contains around 100 ppb to around 1,000 ppm of nitrogen. 26. The process of claim 1, further comprising heating the adsorbent in the first and second adsorbers to a temperature of between about 250�� C. to about 400�� C. before feeding the high-purity hydrogen gas stream to the first or second adsorbers. 27. The process of claim 14, further comprising heating the adsorbent to a temperature of between about 250�� C. to about 400�� C. before feeding the high-purity hydrogen gas stream to the adsorber. 28. The process of claim 1, wherein the zeolite is in binderless form. 29. The process of claim 14, wherein the zeolite is in binderless form. 30. The process of claim 14, wherein the adsorber is purged at a pressure of between about 0.00001 bar to around 0.5 bar. 31. A process for generating an essentially carbon monoxide-free helium gas stream, the process comprising: (a) (i) feeding a high-purity helium gas feed stream for around 30 minutes or more through a first of two adsorbers that are fluidly connected in parallel or in series and that are each packed with an adsorbent consisting of a zeolite which is cation exchanged with a metal other than a transition metal and which contains less than about 0.5% by weight of a transition metal, and (ii) recovering a first essentially carbon monoxide-free helium gas stream from the first adsorber; (b) thereafter purging the first adsorber by (1) depressurizing it to less than atmospheric pressure, and by (2) (i) recycling a portion of the first essentially carbon monoxide-free helium gas stream through the first adsorber, and/or (ii) feeding an inert gas stream through the first adsorber; and (c) as the first adsorber is purged, feeding a second portion of the high-purity helium gas feed stream for around 30 minutes or more through the second of the two adsorbers and recovering a second essentially carbon monoxide-free helium gas stream from the second adsorber. 32. The process of claim 31, wherein: (a) the adsorbent has a heat of helium adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; and (b) the high-purity helium gas feed streams are fed to the first and second adsorbers at a pressure of between about 30 to about 1,000 bar. 33. The process of claim 31, wherein: (a) the two adsorbers are packed with adsorbent particles selected from the group consisting of CaLSX and CaX; (b) the adsorbent particles (i) have a particle size of between about 0.5 mm to about 5 mm and (ii) a heat of helium adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; (c) the first adsorber is purged by depressurizing it to around 0.00001 bar to around 0.5 bar; and (d) an essentially carbon monoxide-free helium gas stream is recovered from the two adsorbers. 34. The process for generating an essentially carbon monoxide-free helium gas stream, the process comprising: (a) (i) feeding a high-purity helium gas feed stream for around 30 minutes or more through an adsorber that is packed with an adsorbent consisting of a zeolite which is cation exchanged with a metal other than a transition metal and which contains less than about 0.5% by weight of a transition metal, and (ii) recovering an essentially carbon monoxide-free helium gas stream from the adsorber; and (b) thereafter purging the adsorber by (1) depressurizing it to less than atmospheric pressure, and by (2) (i) recycling a portion of the essentially carbon monoxide-free helium gas stream through the adsorber, and/or (ii) feeding an inert gas stream through the first adsorber. 35. The process of claim 34, wherein: (a) the adsorbent has a heat of helium adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; and (b) the high-purity helium gas feed stream is fed to the first and second adsorber at a pressure of between about 30 to about 1,000 bar. 36. The process of claim 34, wherein: (a) the adsorber is packed with adsorbent particles selected from the group consisting of CaLSX and CaX; (b) the adsorbent particles (i) have a particle size of between about 0.5 mm to about 5 mm and (ii) a heat of helium adsorption of less than about 5 kcal/mole, a heat of carbon monoxide adsorption of between about 8 to about 12 kcal/mole, and a heat of nitrogen adsorption of greater than about 5 kcal/mole; (c) the adsorber is purged by depressurizing it to around 0.00001 bar to around 0.5 bar; and (d) an essentially carbon monoxide-free helium gas stream is recovered from the adsorber.