Recovery of NF3 from adsorption operation
View Patent ↗During the conventional temperature swing adsorption (TSA) process, NF 3 co-adsorbed with the impurities is vented during regeneration. This invention is a novel TSA cycle in which the co-adsorbed NF 3 is recovered. In this novel TSA cycle, a control scheme is used to stop the adsorption prior to the saturation of the adsorber with impurities and use a recovery purge gas (either co-current or counter-current) to release the co-adsorbed NF 3 off the saturated adsorber. The effluent of the inert purge gas can be combined with the effluent of the on-stream vessel or can be recycled to the feed of the on-stream vessel. 10%-100% of the co-adsorbed NF 3 is recovered and made available as product in this novel TSA cycle. Thus the overall process yield of NF 3 is increased. The removing of the co-adsorbed NF 3 from the adsorber also prevents adsorber degradation thus prolonging the useful life of the adsorber.
1. A process for removing at least one impurity from a crude NF 3 gas stream in a system having at least two vessels each containing an adsorber, comprising steps of:
flowing the crude NF 3 gas stream through the first adsorber in the first vessel to selectively adsorb the at least one impurity;
redirecting the flow of the crude NF 3 gas stream through the second adsorber in the second vessel after a predetermined time or when effluent of the first adsorber reaches a predetermined level of the at least one impurity;
flowing a recovery purge gas through the first adsorber to selectively desorb co-adsorbed NF 3 from the first adsorber;
discontinuing the flow of the recovery purge gas when a predetermined time or when effluent of the recovery purge gas reaches a predetermined level of the at least one impurity or a predetermined percentage of co-adsorbed NF 3 ;
flowing a regeneration purge gas through the first adsorber to purge adsorbed at least one impurity and remaining co-adsorbed NF 3 from the first adsorber; and
discontinuing the flow of the regeneration purge gas.
2. The process of claim 1 is a temperature swing adsorption (TSA).
3. The process of claim 1 wherein the effluent of the recovery purge gas from the first adsorber is combined with (1) effluent of the second adsorber; or (2) the crude NF 3 gas stream directed to the second adsorber when the effluent of the recovery purge gas reaches a predetermined level of the at least one impurity.
4. The process of claim 1 wherein the at least one impurities is selected from the group consisting of N 2 O, CO 2 , H 2 O, OF 2 , SF 6 , CF 4 , C 2 F 6 and combinations thereof.
5. The process of claim 1 wherein the adsorber is an aluminosilicate zeolite having a framework selected from the group consisting of FAU, MOR, CHA, OFF, ERI, FER, GME, LEV, EMT, BEA, MAZ, LTA, LTL, MFI, MEL, MTW, MEI, MFS, NES and combinations thereof.
6. The process of claim 5 wherein the adsorber is selected from the group consisting of Na-MOR, Ca-LTA, Na-FAU, and combinations thereof.
7. The process of claim 1 wherein the recovery purge gas is selected from the group consisting of helium, nitrogen and argon, and the regeneration purge gas is selected from the group consisting of helium, nitrogen and argon.
8. The process of claim 1 wherein the flowing of the recovery purge gas through the first adsorber is in the same direction (cocurrent flow) as the flowing of the crude NF 3 gas stream through the first adsorber.
9. The process of claim 1 wherein the flowing of the recovery purge gas through the first adsorber is in the opposite direction (countercurrent flow) as the flowing of the crude NF 3 gas stream through the first adsorber.
10. The process of claim 1 wherein the flowing of the regeneration purge gas through the first adsorber is in the same direction (cocurrent flow) as the flowing of the crude NF 3 gas stream through the first adsorber.
11. The process of claim 1 wherein the flowing of the regeneration purge gas through the first adsorber is in the opposite direction (countercurrent flow) as the flowing of the crude NF 3 gas stream through the first adsorber.
12. The process of claim 1 wherein the the recovery purge gas has a temperature ranging from −20 to 120° C.
13. The process of claim 12 wherein the the recovery purge gas has a temperature ranging from 4 to 65° C.
14. The process of claim 12 wherein the the recovery purge gas has a temperature ranging from 4 to 30° C.
15. The process of claim 1 wherein the the regeneration purge gas has a temperature ranging from 35 to 450° C.
16. The process of claim 1 wherein the the recovery purge gas has a molar mass velocity ranging from 0.2 to 40 kg-mol/m 2 hr and a residence time ranging from 0.1 to 25 minutes.
17. The process of claim 16 wherein the the recovery purge gas has a molar mass velocity ranging from 0.5 to 15 kg-mol/m 2 hr and a residence time ranging from 0.3 to 10 minutes.
18. The process of claim 16 wherein the the recovery purge gas has a flow rate ranging from 1 to 7 kg-mol/m 2 hr and a residence time ranging from 0.7 to 5 minutes.
19. The process of claim 1 wherein 10-100% of the co-adsorbed NF 3 is desorbed from the first adsorber in the step of flowing the recovery purge gas through the first adsorber.
20. The process of claim 1 further comprising steps of:
redirecting the flow of the crude NF 3 gas stream back through the first adsorber in the first vessel after a predetermined time or when effluent of the second adsorber reaches a predetermined level of the at least one impurity;
flowing a recovery purge gas through the second adsorber to selectively desorb co-adsorbed NF 3 from the second adsorber;
discontinuing the flow of the recovery purge gas when a predetermined time or when effluent of the recovery purge gas reaches a predetermined level of the at least one impurity or a predetermined percentage of co-adsorbed NF 3 ;
flowing a regeneration purge gas through the second adsorber to purge adsorbed at least one impurity and remaining co-adsorbed NF 3 from the second adsorber; and
discontinuing the flow of the regeneration purge gas.