Abstract: A method for producing 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene using a single set of four unit operations, the unit operations being (1) hydrogenation of a starting material comprising hexafluoropropene and optionally recycled 1,1,1,2,3-pentafluoropropene; (2) separation of the desired intermediate hydrofluoroalkane, such as 1,1,1,2,3,3-hexafluoropropane and/or 1,1,1,2,3-pentafluoropropane; (3) dehydrofluorination of the intermediate hydrofluoroalkane to produce the desired 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene, followed by another separation to isolate the desired product and, optionally, recycle of the 1,1,1,2,3-pentafluoropropene.

Abstract: A method for producing 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene using a single set of four unit operations, the unit operations being (1) hydrogenation of a starting material comprising hexafluoropropene and optionally recycled 1,1,1,2,3-pentafluoropropene; (2) separation of the desired intermediate hydrofluoroalkane, such as 1,1,1,2,3,3-hexafluoropropane and/or 1,1,1,2,3-pentafluoropropane; (3) dehydrofluorination of the intermediate hydrofluoroalkane to produce the desired 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene, followed by another separation to isolate the desired product and, optionally, recycle of the 1,1,1,2,3-pentafluoropropene.

Abstract: A method for producing 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene using a single set of four unit operations, the unit operations being (1) hydrogenation of a starting material comprising hexafluoropropene and optionally recycled 1,1,1,2,3-pentafluoropropene; (2) separation of the desired intermediate hydrofluoroalkane, such as 1,1,1,2,3,3-hexafluoropropane and/or 1,1,1,2,3-pentafluoropropane; (3) dehydrofluorination of the intermediate hydrofluoroalkane to produce the desired 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene, followed by another separation to isolate the desired product and, optionally, recycle of the 1,1,1,2,3-pentafluoropropene.

Abstract: An integrated process for the manufacture of HFO trans-1,3,3,3-tetrafluoropropene (HFO trans-1234ze) by first catalytically dehydrofluorinating 1,1,1,3,3-pentafluoropropane to thereby produce a mixture of cis-1,3,3,3-tetrafluoropropene, trans-1,3,3,3-tetrafluoropropene and hydrogen fluoride. Then optionally recovering hydrogen fluoride, catalytically isomerizing cis-1234ze into trans-1234ze, and recovering trans-1,3,3,3-tetrafluoropropene.

Abstract: A method for producing 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3 -pentafluoropropene using a single set of four unit operations, the unit operations being (1) hydrogenation of a starting material comprising hexafluoropropene and optionally recycled 1,1,1,2,3-pentafluoropropene; (2) separation of the desired intermediate hydrofluoroalkane, such as 1,1,1,2,3,3-hexafluoropropane and/or 1,1,1,2,3-pentafluoropropane; (3) dehydrofluorination of the intermediate hydrofluoroalkane to produce the desired 1,1,1,2-tetrafluoropropene and/or 1,1,1,2,3-pentafluoropropene, followed by another separation to isolate the desired product and, optionally, recycle of the 1,1,1,2,3-pentafluoropropene.

Abstract: An integrated process for the manufacture of HFO trans-1,3,3,3-tetrafluoropropene (HFO trans-1234ze) by first catalytically dehydrofluorinating 1,1,1,3,3-pentafluoropropane to thereby produce a mixture of cis-1,3,3,3-tetrafluoropropene, trans-1,3,3,3-tetrafluoropropene and hydrogen fluoride. Then optionally recovering hydrogen fluoride, catalytically isomerizing cis-1234ze into trans-1234ze, and recovering trans-1,3,3,3-tetrafluoropropene.

Abstract: An integrated process for the manufacture of HFO trans-1,3,3,3-tetrafluoropropene (HFO trans-1234ze) by first catalytically dehydrofluorinating 1,1,1,3,3-pentafluoropropane to thereby produce a mixture of cis-1,3,3,3-tetrafluoropropene, trans-1,3,3,3-tetrafluoropropene and hydrogen fluoride. Then optionally recovering hydrogen fluoride, catalytically isomerizing cis-1234ze into trans-1234ze, and recovering trans-1,3,3,3-tetrafluoropropene.

Abstract: An integrated process for the manufacture of HFO trans-1,3,3,3-tetrafluoropropene (HFO trans-1234ze) by first catalytically dehydrofluorinating 1,1,1,3,3-pentafluoropropane to thereby produce a mixture of cis-1,3,3,3-tetrafluoropropene, trans-1,3,3,3-tetrafluoropropene and hydrogen fluoride. Then optionally recovering hydrogen fluoride, catalytically isomerizing cis-1234ze into trans-1234ze, and recovering trans-1,3,3,3-tetrafluoropropene.

Abstract: A process for preparing a fluorination catalyst using a low pressure activating step followed by a high pressure activating step.

Abstract: A process for preparing a fluorination catalyst using a low pressure activating step followed by a high pressure activating step.

Abstract: A process for preparing halogenated ethanes, particularly pentafluoroethane, from a mixture produced by the reaction of perchloroethylene, hydrogen fluoride and a recycle stream. The preferred process utilizes phase separation techniques to ensure that less than the azzeotropic amount of HF is included in the product stream, thereby minimizing the hydrogen fluoride that is carried off with the desired products after they are separated from the reaction mixture, and at the same time prevents undesirable byproducts from being recycled to the reaction.

Abstract: A liquid phase fluorination process for producing difluoromethane without corrosion is provided. In the process of this invention, methylene chloride and hydrogen fluoride are reacted in a reactor made of fluorinated polymer to produce a reaction product while a vaporized and superheated recycle stream of process reactants is fed into the reactor.

Abstract: The invention relates to an improvement in a process in which chlorine and difluoromethane are present in a distillation column, for example, a fluorination reaction. By controlling the chlorine feed such that the concentration of chlorine relative to difluoromethane in the distillation column is maintained below about 22 weight percent (the flammability threshold for chlorine in a mixture of difluoromethane and chlorine), formation of a flammable difluoromethane/chlorine mixture may be minimized or avoided. The invention is particularly useful in a process for the preparation of difluoromethane wherein at least one distillation column separates difluoromethane from unreacted starting materials such as methylene chloride, hydrogen fluoride and monochloromonofluoromethane.

Abstract: A liquid and vapor phase processes for the production of difluoromethane in which the risk of exposure to, and equipment fouling from, chlorofluoromethane is reduced. This reduction is accomplished from removing a sidestream containing monochloromonofluoromethane from a fluorination process distillation column.

Abstract: The present invention provides a method for separating dichlorodifluoromethane from difluoromethane. More specifically, a process is provided for separating dichlorodifluoromethane and difluoromethane using azeotropic distillation.

Abstract: A process for minimizing the compositional changes that occur in a non-azeotropic composition during the withdrawal of an amount of the composition from a storage vessel. The process of the invention provides for the minimization of compositional changes by cooling the non-azeotropic composition.

Abstract: This invention relates to a process for producing 1,1,1,2-tetrafluoroethane (HFC-134a). The process reacts, 1,1,1-trifluoro-2-chloroethane (HCFC-133a) and hydrogen fluoride in a first reactor. The product resulting from the first reaction step is brought to a second reactor together with trichloroethylene and hydrogen fluoride. The second reaction is conducted at a higher temperature than the first reactor. Optionally, HCl is removed prior to removal of the crude HFC-134a product. Unreacted HCFC-133a, trichloroethylene and hydrogen fluoride may be recycled back to the first reactor.

Abstract: A process for regenerating a catalyst which involves washing a catalyst with a liquid at a temperature within the range of about 50.degree. C. to about 70.degree. C. for a time sufficient to remove foulants thereby recovering catalyst activity. The wash liquid is preferably a member selected from the group consisting of ethers, alcohols and mixtures of ethers and alcohols wherein the ether is a tertiary alkyl ether, preferably selected from the group consisting of tertiary amyl methyl ether and methyl tertiary butyl ether, and wherein the alcohol is preferably selected from the group consisting of tertiary butyl alcohol and methanol. The catalyst is preferably a clay treated with an acid selected from the group consisting of hydrofluoric acid, hydrochloric acid and mixtures of hydrofluoric and hydrochloric acid, wherein the clay is preferably selected from the group consisting of montmorillonite, kaolinite, attapulgite, bentoninte and natural clay.

Abstract: A method for increasing the ratio of 2-methyl-2-butene (2MB2) to 2-methyl-1-butene (2MB1) in isoamylenes involves fractionating a feedstream containing tertiary amyl methyl ether (TAME) and isoamylenes including 2MB2 and 2MB1 in a ratio of about 2:1 to effect a separation between an overhead hydrocarbon fraction of isoamylenes including 2MB2 and 2MB1 in a ratio of about 1:1, a bottoms fraction including TAME, and a sidestream hydrocarbon fraction consisting essentially of isoamylenes including 2MB2 and 2MB1 in a ratio of about 6 to 12:1, recovering the sidestream hydrocarbon fraction, and recycling the overhead hydrocarbon fraction of isoamylenes to form a mixture which is subsequently reacted to form the feedstream. Prior to fractionation, the feedstream is formed by passing isoamylene, and optionally TAME, in a vapor phase over an ether cracking catalyst which isomerizes isoamylene and converts 2MB1 to 2MB2, i.e., the feedstream for fractionating, which contains 2MB2 and 2MB1 in a ratio of 2 to 5:1.

Abstract: A process for regenerating a catalyst which involves washing a catalyst with a liquid at a temperature within the range of about 50.degree. C. to about 70.degree. C. for a time sufficient to remove foulants thereby recovering catalyst activity. The wash liquid is preferably a member selected from the group consisting of ethers, alcohols and mixtures of ethers and alcohols wherein the ether is a tertiary alkyl ether, preferably selected from the group consisting of tertiary amyl methyl ether and methyl tertiary butyl ether, and wherein the alcohol is preferably selected from the group consisting of tertiary butyl alcohol and methanol. The catalyst is preferably a clay treated with an acid selected from the group consisting of hydrofluoric acid, hydrochloric acid and mixtures of hydrofluoric and hydrochlorica acid, wherein the clay is preferably selected from the group consisting of montmorillonite, kaolinite, attapulgite, bentonite and natural clay.