Process for making high purity 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb)
A method for producing 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb) from a reaction composition including a mixture of HCFC-244bb and 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf) by selectively hydrogenating the HCFO-1233xf component of the mixture in a vapor phase in the presence of hydrogen gas and a catalyst to generate a product composition including unreacted HCFC-244bb and hydrogenation products of HCFO-1233xf, such as 2-chloro-1,1,1-trifluoropropane (HCFC-253db), which may be separated from the HCFC-244bb by distillation. The separated HCFC-244bb may then be purified by subsequent acid neutralization and drying steps.
1. A method for producing 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb), comprising the steps of:
providing a reactant stream including a mixture of HCFC-244bb and 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), the amount of HCFO-1233xf between 5 wt. % and 25 wt. % based on a total weight of the reactant stream; and
hydrogenating the HCFO-1233xf of the reactant stream in a vapor phase in the presence of hydrogen gas and a palladium catalyst diluted in an alpha aluminum support to a palladium loading between 0.3 wt. % and 0.5 wt. %, based on the total weight of the palladium catalyst and the alpha aluminum support, to generate a product composition including unreacted HCFC-244bb and 2-chloro-1,1,1-trifluoropropane (HCFC-253db).
2. The method of claim 1 , wherein the reactant stream includes between 75 wt. % and 98 wt. % HCFC-244bb, based on the total weight of the reactant stream.
3. The method of claim 1 , wherein the hydrogenation step further comprises hydrogenating at a temperature between 100° C. and 250° C.
4. The method of claim 1 , wherein the hydrogenation step further comprises hydrogenating at a pressure between 5 psig and 100 psig.
5. The method of claim 1 , further comprising the additional step of separating the HCFC-244bb and the HCFC-253db.
6. The method of claim 5 , further comprising the additional steps of:
subjecting the separated HCFC-244bb to an acid neutralization step; and
drying the acid neutralized HCFC-244bb.
7. The method of claim 6 , wherein, following the drying step, the HCFC-244bb has at least one of:
a purity greater than 95 wt. %;
a water content less than 10 ppm; and
an acid content less than 1 ppm.
8. The method of claim 1 , wherein, in the hydrogenating step, conversion of HCFO-1233xf exceeds 98%.
9. The method of claim 1 , wherein, in the hydrogenating step, selectivity of HCFO-1233xf to HCFC-253db exceeds 60%.
10. A method for producing 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb), comprising the steps of:
providing a reactant stream including a mixture of HCFC-244bb and 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), the amount of HCFO-1233xf between 5 wt. % and 25 wt. % based on a total weight of the reactant stream;
hydrogenating the HCFO-1233xf of the reactant stream in a vapor phase in the presence of hydrogen gas and a palladium metal catalyst diluted in an alpha aluminum support to a palladium loading between 0.3 wt. % and 0.5 wt. %, based on the total weight of the palladium catalyst and the alpha aluminum support, at a temperature between 100° C. and 250° C. to generate a product composition including unreacted HCFC-244bb and 2-chloro-1,1,1-trifluoropropane (HCFC-253db); and
separating the HCFC-244bb and the HCFC-253db.
11. The method of claim 10 , further comprising the additional steps of:
subjecting the separated HCFC-244bb to an acid neutralization step; and
drying the acid neutralized HCFC-244bb.
12. The method of claim 11 , wherein, following the drying step, the HCFC-244bb has a purity greater than 95 wt. %, a water content less than 10 ppm, and an acid content less than 1 ppm.
13. The method of claim 10 , wherein the reactant stream includes between 75 wt. % and 98 wt. % HCFC-244bb, based on the total weight of the reactant stream.
14. The method of claim 10 , wherein the hydrogenation step further comprises hydrogenating at a pressure between 5 psig and 100 psig.
15. The method of claim 10 , wherein, in the hydrogenating step, conversion of HCFO-1233xf exceeds 98%.
16. The method of claim 1 , wherein, in the providing step, the reactant stream is diluted by an inert diluent, the inert diluent present in the reactant stream in an amount between 2 wt. % and 25 wt. %, based on the total weight of the HCFO-1233xf and the HCFC-244bb in the reactant stream.
17. The method of claim 1 , wherein, in the hydrogenating step, the hydrogen gas is diluted by an inert diluent, the inert diluent present in the hydrogen gas in an amount between 2 wt. % and 40 wt. %, based on a total weight of the hydrogen gas.
18. The method of claim 10 , wherein, in the providing step, the reactant stream is diluted by an inert diluent, the inert diluent present in the reactant stream in an amount between 2 wt. % and 25 wt. %, based on the total weight of the HCFO-1233xf and the HCFC-244bb in the reactant stream.
19. The method of claim 10 , wherein, in the hydrogenating step, the hydrogen gas is diluted by an inert diluent, the inert diluent present in the hydrogen gas in an amount between 2 wt. % and 40 wt. %, based on a total weight of the hydrogen gas.