The present disclosure relates to a method for producing trifluoroiodomethane (CF.sub.3I) from iodine (I.sub.2) and trifluoroacetic anhydride (TFAA) under photochemical conditions using ultraviolet (UV) light.

Disclosed is a process for producing a chlorinated C3-6 alkane comprising providing a reaction mixture comprising an alkene and carbon tetrachloride in a principal alkylation zone to produce chlorinated C3-6 alkane in the reaction mixture, and extracting a portion of the reaction mixture from the principal alkylation zone, wherein: a) the concentration of the chlorinated C3-6 alkane in the reaction mixture in the principal alkylation zone is maintained at a level such that the molar ratio of chlorinated C3-6 alkane:carbon tetrachloride in the reaction mixture extracted from the alkylation zone does not exceed 95:5 when the principal alkylation zone is in continuous operation; and/or b) the reaction mixture extracted from the principal alkylation zone additionally comprises alkene and the reaction mixture is subjected to a dealkenation step in which at least about 50% or more by weight of the alkene present in the reaction mixture is extracted therefrom and at least about 50% of the extracted alkene is fed back into the reaction mixture provided in the principal alkylation zone; and/or c) the reaction mixture present in the principal alkylation zone and extracted from the principal alkylation zone additionally comprises a catalyst, and the reaction mixture extracted from the principal alkylation zone is subjected to an aqueous treatment step in which the reaction mixture is contacted with an aqueous medium in an aqueous treatment zone, a biphasic mixture is formed and an organic phase comprising catalyst is extracted from the biphasic mixture.

Disclosed is a process for producing a chlorinated C3-6 alkane comprising providing a reaction mixture comprising an alkene and carbon tetrachloride in a principal alkylation zone to produce chlorinated C3-6 alkane in the reaction mixture, and extracting a portion of the reaction mixture from the principal alkylation zone, wherein: a) the concentration of the chlorinated C3-6 alkane in the reaction mixture in the principal alkylation zone is maintained at a level such that the molar ratio of chlorinated C3-6 alkane:carbon tetrachloride in the reaction mixture extracted from the alkylation zone does not exceed 95:5 when the principal alkylation zone is in continuous operation; and/or b) the reaction mixture extracted from the principal alkylation zone additionally comprises alkene and the reaction mixture is subjected to a dealkenation step in which at least about 50% or more by weight of the alkene present in the reaction mixture is extracted therefrom and at least about 50% of the extracted alkene is fed back into the reaction mixture provided in the principal alkylation zone; and/or c) the reaction mixture present in the principal alkylation zone and extracted from the principal alkylation zone additionally comprises a catalyst, and the reaction mixture extracted from the principal alkylation zone is subjected to an aqueous treatment step in which the reaction mixture is contacted with an aqueous medium in an aqueous treatment zone, a biphasic mixture is formed and an organic phase comprising catalyst is extracted from the biphasic mixture.

Disclosed is a process for producing a chlorinated C3-6 alkane comprising providing a reaction mixture comprising an alkene and carbon tetrachloride in a principal alkylation zone to produce chlorinated C3-6 alkane in the reaction mixture, and extracting a portion of the reaction mixture from the principal alkylation zone, wherein: a) the concentration of the chlorinated C3-6 alkane in the reaction mixture in the principal alkylation zone is maintained at a level such that the molar ratio of chlorinated C3-6 alkane:carbon tetrachloride in the reaction mixture extracted from the alkylation zone does not exceed 95:5 when the principal alkylation zone is in continuous operation; and/or b) the reaction mixture extracted from the principal alkylation zone additionally comprises alkene and the reaction mixture is subjected to a dealkenation step in which at least about 50% or more by weight of the alkene present in the reaction mixture is extracted therefrom and at least about 50% of the extracted alkene is fed back into the reaction mixture provided in the principal alkylation zone; and/or c) the reaction mixture present in the principal alkylation zone and extracted from the principal alkylation zone additionally comprises a catalyst, and the reaction mixture extracted from the principal alkylation zone is subjected to an aqueous treatment step in which the reaction mixture is contacted with an aqueous medium in an aqueous treatment zone, a biphasic mixture is formed and an organic phase comprising catalyst is extracted from the biphasic mixture.

A metal cyclopentadienyl complex has the formula:

##STR00001##

wherein m≥0; M is a Group I, II or III main group metal, alkali or transition metal; C.sub.5H.sub.4 represents a Cp ring where two hydrogens are substituted by M and R(F).sub.m; R(F).sub.m is connected to any one of the carbon atoms of the Cp and selected from a hydrocarbyl, fluorohydrocarbyl, silyl group [SiR′.sub.3], or amino group [—NR.sup.1R.sup.2]. The metal cyclopentadienyl complexes include Li(C.sub.5H.sub.4-2-C.sub.5H.sub.11) (CAS No: 2413046-23-6), K(C.sub.5H.sub.4-2-C.sub.5H.sub.11), Na(C.sub.5H.sub.4-2-C.sub.5H.sub.11), K(C.sub.5H.sub.4-1-F—C.sub.4H.sub.10), K(C.sub.5H.sub.4-1,1,1-3F—C.sub.4H.sub.6), Li(C.sub.5H.sub.4-2-C.sub.4H.sub.9), or In(C.sub.5H.sub.4-2-C.sub.5H.sub.11) (CAS No.: 2364634-67-1).

A mono-substituted cyclopentadiene has the formula:

##STR00002##

wherein m≥0; C.sub.5H.sub.5 represents the Cp ring where one hydrogen is substituted R(F).sub.m; R(F).sub.m is connected to any one of the carbon atoms of the Cp and selected from a hydrocarbyl, fluorohydrocarbyl, silyl group [SiR′.sub.3], or amino group [—NR.sup.1R.sup.2]. The mono-substituted cyclopentadienes include C.sub.5H.sub.5-1-F—C.sub.4H.sub.10, C.sub.5H.sub.5-2-C.sub.5H.sub.11, C.sub.5H.sub.5-2-C.sub.4H.sub.9, or C.sub.5H.sub.5-1,1,1-3F—C.sub.4H.sub.6.

Provided is a method for storing a fluoro-2-butene by which isomerization reaction is unlikely to proceed during storage. A fluoro-2-butene represented by general formula C.sub.4H.sub.xF.sub.y where x is 0 or more and 7 or less, y is 1 or more and 8 or less, and x+y is 8 contains or does not contain at least one of chromium, molybdenum, iron, zinc, and aluminum as a metal impurity. The fluoro-2-butene is stored in a container in which the total concentration of chromium, molybdenum, iron, zinc, and aluminum is 1,000 ppb by mass or less when containing at least one of chromium, molybdenum, iron, zinc, and aluminum.

Provided is a method for storing a fluoro-2-butene by which isomerization reaction is unlikely to proceed during storage. A fluoro-2-butene represented by general formula C.sub.4H.sub.xF.sub.y where x is 0 or more and 7 or less, y is 1 or more and 8 or less, and x+y is 8 contains or does not contain at least one of chromium, molybdenum, iron, zinc, and aluminum as a metal impurity. The fluoro-2-butene is stored in a container in which the total concentration of chromium, molybdenum, iron, zinc, and aluminum is 1,000 ppb by mass or less when containing at least one of chromium, molybdenum, iron, zinc, and aluminum.

The present invention relates to a process for purifying olefin feed comprising R-5 1234yf, R-40, R-134a, R-134, R-1225zc, and OFCB, comprising the step of separating different ternary and binary azeotrope compositions comprising 1234yf. The olefin feed is obtained from the pyrolysis of tetrafluoroethylene/chlorodifluoromethane with chloromethane/methane, optionally in presence of initiator.

The present invention relates to a process for purifying olefin feed comprising R-5 1234yf, R-40, R-134a, R-134, R-1225zc, and OFCB, comprising the step of separating different ternary and binary azeotrope compositions comprising 1234yf. The olefin feed is obtained from the pyrolysis of tetrafluoroethylene/chlorodifluoromethane with chloromethane/methane, optionally in presence of initiator.

The present invention relates to a process for purifying olefin feed comprising R-5 1234yf, R-40, R-134a, R-134, R-1225zc, and OFCB, comprising the step of separating different ternary and binary azeotrope compositions comprising 1234yf. The olefin feed is obtained from the pyrolysis of tetrafluoroethylene/chlorodifluoromethane with chloromethane/methane, optionally in presence of initiator.