rate of reactants and cofeeds at the operating temperature and pressure of the process are preferably from about 1 to about 250 seconds more preferably from about 1 to about 50 seconds the reaction product of the gas phase catalytic fluorination step will include in addition to the desired hydrofluoropropene unreacted hydrochlorofluoropropene and fluro and chlorofluor substituted propane such as 245cb and 244bb these byproducts can be separated from the desired hydrofluoropropene in a series of two or more separation columns with the by products being recycled to the gas phase catalytic fluorination reaction the tetrachloropropene feedstock of the present invention can be formed via variety of ways as would be know by a person skilled in the art the data presented in the examples was calculated based upon results obtained in comparable reactions with closely related materials uncatalyzed liquid phase fluorination of 1 1 2 3 tetrachloropropene hco 1230xa to 2 chloro 3 3 3 trifluoropropene hcfo 1233xf 0 28 moles of hco 1230xa can be loaded into a 300 ml hastelloy c autoclave equipped with gas inlet valve mechanical stirrer and an outlet cooling tower 3 5 moles of hf gas can be condensed in the autoclave the reaction mixture would be gradually heated up to 120 u00b0 c with continuous stirring for approximately 1 2 hour excessive gas pressure resulted.