초록 ▼

Disclosed herein are processes for separation of 2,3,3,3-tetrafluoropropene and hydrogen fluoride using azeotropic distillation. Additionally, disclosed are processes for separating mixtures of 2,3,3,3-tetrafluoropropene, hydrogen fluoride and 1,1,1,2,3-pentafluoropropane (HFC-245eb) and/or 1,1,1,2,

Disclosed herein are processes for separation of 2,3,3,3-tetrafluoropropene and hydrogen fluoride using azeotropic distillation. Additionally, disclosed are processes for separating mixtures of 2,3,3,3-tetrafluoropropene, hydrogen fluoride and 1,1,1,2,3-pentafluoropropane (HFC-245eb) and/or 1,1,1,2,2-pentafluoropropane (HFC-245cb) by azeotropic distillation.

대표청구항 ▼

1. A process for separating a mixture comprising HF and HFC-1234yf, said process comprising: a. feeding the mixture comprising HF and HFC-1234yf to a first distillation column;b. removing an azeotrope composition comprising HF and HFC-1234yf as a first distillate and either i) HF or ii) HFC-1234yf a

1. A process for separating a mixture comprising HF and HFC-1234yf, said process comprising: a. feeding the mixture comprising HF and HFC-1234yf to a first distillation column;b. removing an azeotrope composition comprising HF and HFC-1234yf as a first distillate and either i) HF or ii) HFC-1234yf as a first column bottoms composition;c. decanting the first distillate to form 2 liquid phases, being i) an HF-rich phase and ii) an HFC-1234yf-rich phase; andd. recycling a first liquid phase enriched in the same compound that is removed as the first column bottoms, said first liquid phase being either i) HF-rich phase or ii) HFC-1234yf-rich phase, back to the first distillation column; wherein the first distillation column is operated at a pressure of from about 14.7 psia (101 kPa) to about 300 psia (2068 kPa), with a top temperature of from about −50° C. to about 200° C. and a bottom temperature from about −30° C. to about 220° C. 2. The process of claim 1, further comprising feeding a second liquid phase not recycled in step (d), said second liquid phase being either i) HF-rich phase or ii) HFC-1234yf-rich phase, to a second distillation column. 3. The process of claim 1, wherein said HFC-1234yf in the mixture is present in a concentration greater than the azeotrope composition for hydrogen fluoride and said HFC-1234yf, and wherein the first column bottoms composition is HFC-1234yf that is essentially free of hydrogen fluoride, and wherein said first liquid phase is enriched in HFC-1234yf. 4. The process of claim 3, further comprising: i. feeding the hydrogen fluoride-rich phase from the decanter to a second distillation column;ii. recovering hydrogen fluoride essentially free of HFC-1234yf from the bottom of the second distillation column; andiii. recycling a second distillate composition to the two liquid phases in the decanter. 5. The process of claim 1, wherein hydrogen fluoride is present in a concentration greater than the azeotrope concentration for hydrogen fluoride and said HFC-1234yf, and wherein the first column bottoms composition is hydrogen fluoride essentially free of HFC-1234yf, and wherein said first liquid phase is enriched in hydrogen fluoride. 6. The process of claim 5 further comprising: i. feeding the HFC-1234yf-rich phase from the decanter to a second distillation column;ii. recovering HFC-1234yf essentially free of hydrogen fluoride from the bottom of the second distillation column; andiii. recycling a second distillate composition to the two liquid phases in the decanter. 7. A process for the purification of an HFC-1234yf from a mixture comprising HFC-1234yf and HF, said process comprising: a. adding an entrainer to the mixture comprising HFC-1234yf and HF thus forming a second mixture;b. distilling said second mixture in a first distillation step to form a first distillate composition comprising HF, HFC-1234yf, and entrainer, and a first bottoms composition comprising either i) HFC-1234yf, or ii) HF;c. condensing said first distillate composition to form two liquid phases, being i) an HF-rich phase and ii) an entrainer-rich phase; andd. optionally recycling a first liquid phase back to the first distillation step, wherein said first liquid phase being either i) the HF-rich phase when the first bottoms composition comprises HF or ii) the entrainer-rich phase when the first bottoms composition comprises HFC-1234yf. 8. The process of claim 7, wherein said HFC-1234yf is present in said mixture in a concentration greater than the azeotrope concentration for said HFC-1234yf and HF; and wherein said first bottoms composition comprises HFC-1234yf; said process further comprising feeding the entrainer-rich phase to a second distillation step and forming a second distillate composition comprising entrainer, HFC-1234yf and HF and a bottoms composition comprising HF essentially free of entrainer. 9. The process of claim 7, wherein said HF is present in said mixture in a concentration greater than the azeotrope concentration for said HFC-1234yf and HF; and wherein said first bottoms composition comprises HF; said process further comprising feeding the HF-rich phase to a second distillation step and forming a second distillate composition comprising entrainer, HFC-1234yf and HF and a bottoms composition comprising entrainer essentially free of HF. 10. The process of claim 8 or 9, further comprising recycling said second distillate composition back to the two liquid phases. 11. A process for the separation of HFC-1234yf from a mixture of HFC-1234yf, HF, and at least one of HFC-245cb or HFC-245eb, said process comprising: a. subjecting said mixture to a first distillation step, wherein additional HFC-1234yf is fed from a second distillation step, to form a first distillate comprising an azeotrope of HFC-1234yf and HF and a first bottoms composition comprising at least one of HFC-245cb or HFC-245eb;b. feeding said first distillate to a second distillation step to form a second distillate comprising an azeotrope of HFC-1234yf and HF and a second bottoms composition comprising HFC-1234yf essentially free of HF;c. decanting said second distillate to form two liquid phases, being i) an HF-rich phase and ii) an HFC-1234yf-rich phase; andd. recycling the HFC-1234yf-rich phase from (c) back to the first distillation step. 12. The process of claim 11 further comprising feeding the HF-rich phase to a third distillation step to form a third distillate comprising an azeotrope of HFC-1234yf and HF and a third bottoms composition comprising HF essentially free of HFC-1234yf. 13. A process for separating HF from a mixture comprising HFC-1234yf, HF, and at least one of HFC-245cb or HFC-245eb, said process comprising: a. adding an entrainer to the mixture comprising HFC-1234yf, HF, and at least one of HFC-245cb or HFC-245eb thus forming a second mixture;b. distilling said second mixture in a first distillation step to form a first distillate composition comprising HF and entrainer and a first bottoms composition comprising HFC-1234yf and at least one of HFC-245cb or HFC-245eb;c. condensing said first distillate composition to form two liquid phases, being (i) an entrainer-rich phase and (ii) an HF-rich phase; andd. recycling the entrainer-rich phase back to the first distillation step. 14. The process of claim 13 further comprising feeding the HF-rich phase to a second distillation step and forming a second distillate composition comprising an azeotrope of entrainer and HF and a second bottoms composition comprising HF essentially free of entrainer. 15. The process of claim 14 further comprising recycling said second distillate composition back to the two liquid phases. 16. The process of claim 7 or 13, wherein said entrainer is selected from the group consisting of hydrocarbons, chlorocarbons, chlorofluorocarbons, hydrochlorofluorocarbons, hydrofluorocarbons, perfluorocarbons, fluoroethers, HFPO, SF6, chlorine, hexafluoroacetone, and mixtures thereof.