Method for the separation of phosphorus pentafluoride from hydrogen chloride
The present invention relates to a process of separating a feed stream comprising HCl and PF 5 into a plurality of streams, wherein a first stream is enriched in PF 5 and a second stream is enriched in HCl, the process comprising the feed stream entering one or more permeable membrane separation modules, wherein the membrane separation module comprises a permeable membrane which is selectively permeable to one of HCl or PF 5 .
1 . A process of separating a feed stream comprising HCl and PF 5 into a plurality of streams, wherein a first stream is enriched in PF 5 and a second stream is enriched in HCl, the process comprising the feed stream entering one or more permeable membrane separation modules, wherein the membrane separation module comprises a permeable membrane which is selectively permeable to one of HCl or PF 5 .
2 . The process according to claim 1 wherein the feed stream is separated into two streams: (i) the first stream enriched in PF 5 ; and (ii) the second stream enriched in HCl.
3 . The process according to claim 1 wherein the feed stream comprises HCl:PF 5 in a molar ratio of greater than 1:1 up to about 15:1, or in a molar ratio of greater than 1:1 up to about 10:1, or in a molar ratio of greater than 1:1 up to about 5:1.
4 . The process according to claim 1 , wherein the process further comprises a step of purifying the first stream and/or second stream so as to produce a purified stream and a waste stream, wherein the purified stream comprises PF 5 and/or HCl in an increased impurity compared to the first and/or second stream, respectively.
5 . The process according to claim 1 , wherein the first stream is enriched with PF 5 so that the molar ratio of PF 5 :HCl is at least 1:1, at least 2:1, at least 5:1, or at least 10:1.
6 . The process according to claim 4 wherein when the first stream is enriched with PF 5 so that the molar ratio of PF 5 :HCl is at least 1:1, the purification step is carried out by distillation.
7 . The process according to claim 4 wherein the process further comprises a step of recycling the waste stream back into the one or more membrane separation modules.
8 . The process according to claim 4 , wherein the first stream and/or the second stream is passed through a further permeable membrane separation module in order to further enrich the amount of PF 5 or HCl in the first or second stream respectively, before the purification step.
9 . The process according to claim 1 wherein the membrane is a microporous, inert polymeric material.
10 . The process according to claim 9 wherein the microporous, inert polymeric material is selected from the group consisting of poly tetrafluoroethene (PTFE), polyvinylidene fluoride (PVDF), fluorinated ethylene-propylene (FEP), sulfonated perfluorovinyl ether-tetrafluoroethene copolymers or a combination thereof.
11 . The process according to claim 9 wherein a pressure gradient across the membrane in one or more of the permeable membrane separation modules is from about 0.1 bar to about 20 bar, from about 0.25 bar to about 15 bar, or from about 0.5 bar to about 10 bar.
12 . The process according to claim 9 wherein the process is carried out in one or more of the permeable membrane separation modules at a temperature of from about −50° C. to about 80° C., from about −30° C. to about 50° C., or from about −20° C. to about 40° C.
13 . The process according to claim 1 wherein the membrane material is selected from a rubbery or glassy polymeric material wherein the solubility of one of PF 5 or HCl is enhanced relative to the other component so that the component with a higher solubility permeates through the membrane at a faster rate than the component with a lower solubility.
14 . The process according to claim 13 wherein the membrane material is selected from the group consisting of fluorinated polymers, polyvinyl chloride, polysiloxanes, poly-methyl-pentene, polysulfones, polyimides, partially fluorinated or substituted polyimides, or a combination thereof.
15 . The process according to claim 14 wherein the polysiloxane is poly dimethyl siloxane.
16 . The process according to claim 14 wherein the polyimide is a fluorinated polyimide, or is 6FDA-6FpDA.
17 . The process according to claim 13 wherein a pressure gradient across the membrane in one or more of the permeable membrane separation modules is from about 0.1 bar to about 20 bar, preferably from about 0.25 bar to about 15 bar, or from about 0.25 bar to about 10 bar.
18 . The process according to claim 13 wherein the process is carried out in one or more of the permeable membrane separation modules at a temperature of from about −80° C. to about 120° C., from about −60° C. to about 80° C., or from about −40° C. to about 40° C.
19 . The process according to claim 13 wherein the membrane is made of a material which has a Hildebrand solubility parameter closer in value to that of HCl (21 (MPa) 1/2 in the temperature range −60° C. to +20° C.) compared to that of PF 5 (11 (MPa) 1/2 in the temperature range −60° C. to +20° C.).
20 . The process according to claim 13 wherein the membrane is made of a material which has a Hildebrand parameter closer in value to that of PF 5 (11 (MPa) 1/2 in the temperature range −60° C. to +20° C.) compared to that of HCl (21 (MPa) 1/2 in the temperature range −60° C. to +20° C.).
21 . The process according to claim 1 wherein the membrane is a flat sheet membrane.
22 . The process according to claim 1 wherein the membrane is a hollow fiber membrane.
23 . The process according to claim 1 wherein the process is carried out in a batchwise or continuous operation.
24 . The process according to claim 1 wherein the one or more streams entering the membrane separation module is in the gaseous or vapour state.
25 . The process according to claim 5 wherein the PF 5 produced in this process is used in a process to synthesis LiPF 6 .