Abstract: The invention relates to a process to prepare tetrahalopropenes, such as 2-chloro-3,3,3-trifluoropropene (1233xf). The process comprises atomizing a feed material, such as 1,1,2,3-tetrachloropropene (1230xa) and the like, and mixing it with superheated HF to form a vaporized composition of feed material and HF with substantially instantaneous contact with a vapor phase fluorination catalyst. The invention extends catalyst life and forestalls catalyst deactivation.

Abstract: The invention relates to a process to produce 244bb from 1233xf in multiple reaction zones whereby the 1233xf starting material is at least 95% converted to 244bb and by-product such as 245cb forms in amounts less than about 2%.

Abstract: The invention relates to a process to prepare tetrahalopropenes, such as 2-chloro-3,3,3-trifluoropropene (1233xf). The process comprises atomizing a feed material, such as 1,1,2,3-tetrachloropropene (1230xa) and the like, and mixing it with superheated HF to form a vaporized composition of feed material and HF with substantially instantaneous contact with a vapor phase fluorination catalyst. The invention extends catalyst life and forestalls catalyst deactivation.

Abstract: The present invention relates, in part, an improved process for the production of certain hydrofluoroolefins, particularly 2,3,3,3-tetrafluoropropene (1234yf). In certain non-limiting embodiments, the invention relates to methods for improving process efficiency during the fluorination of 1,1,2,3-tetrachloropropene, 2,3,3,3-tetrachloropropene, and/or 1,1,1,2,3-pentachloropropane to 2-chloro-3,3,3-trifluoropropene by separating and recycling unreacted HF, unreacted starting materials, and/or certain process intermediates from the 2-chloro-3,3,3-trifluoropropene product stream.

Abstract: Disclosed are methods used to remove HF from a fluorocarbon containing stream, thereby forming a final aqueous HF solution having both a high HF concentration and low dissolved organic content.

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 forming 2,3,3,3-tetrafluoropropene (HFO-1234yf) comprising providing a dehydrochlorination starting material having relatively low concentrations of 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), especially and preferable less than about 8.0% when the dehydrochlorination reaction utilizes no substantial amount of catalyst or catalyst comprising austenitic nickel-based materials.

Abstract: In certain aspects, the present invention relates to methods for increasing the cost efficiency and safety of the hydrogenation of a fluorinated olefin by controlling the reaction conditions and parameters. In further aspects, the hydrogenation reaction is provided in a two stage reaction wherein the reactant amounts, temperature and other parameters are controlled such that the conversion percentage, selectivity, and reaction parameters are all within commercially acceptable levels.

Abstract: This invention relates to a process for the suppression of 3,3,3-trifluoropropyne during the manufacture of fluorocarbons, fluoroolefins, hydrochlorofluoroolefins. More particularly, this invention is directed to a process to suppress the formation of 3,3,3-trifluoropropyne during processes for the manufacture of HCFO-1233zd(E), HCFO-1233zd(Z), HFO-1234ze(E), and/or HFO-1234ze(Z).

Abstract: Disclosed is a method for forming HFO-1234ze, and for forming compositions comprising HFO-1234ze, by (a) converting, preferably by dehydrofluorination, pentafluorpropane (HFC-245), preferably 1,1,1,3,3-pentafluorpropane (HFC-245fa), preferably by contact with a caustic solution, to a reaction product comprising cis-HFO-1234ze and trans-HFO-1234ze; and (b) contacting at least a portion, preferably substantially portion, and in certain embodiments substantially all of said reaction product with at least one isomerization catalyst to convert at least a portion, and preferably at least a substantial portion, of cis-HFO-1234ze in said reaction product to trans-HFO-1234ze.

Abstract: A reactor apparatus is provided having a reaction chamber; a compartmentalizing apparatus including a plurality of compartments, each compartment being open at a top end and bottom end, the compartmentalizing apparatus being disposed within the reaction chamber; and an inlet disposed at an area of the reactor and in fluid communication between the reaction chamber and a feed source. Also provided is a reactor apparatus having an assembly having a reaction chamber; at least one agitator assembly configured to generate mixing within the reaction chamber, the agitator assembly including: a shaft partially lined or coated with a fluoropolymer or other non-metallic corrosion-resistant material, and an impeller lined or coated with the fluoropolymer or other non-metallic corrosion-resistant material; and an inlet disposed at an area of the reactor and in fluid communication between the reaction chamber and a feed source. The provided reactor apparatus can be utilized in hydrofluorination processes.

Abstract: The present invention is directed to a combination reactor system for exothermic reactions comprising a trickle-bed reactor and a shell-and-tube reactor. This combination allows the system to efficiently remove heat while also providing the ability to control both the temperature and/or reaction progression. The trickle-bed reactor removes heat efficiently from the system by utilizing latent heat and does not require the use of a cooling or heating medium. The shell-and-tube reactor is used to further progress the reaction and provides a heat exchanger in order to introduce fluid at the desired temperature in the shell-and-tube reactor. Also, additional reactant or reactants and/or other fluids may be introduced to the shell-and-tube section of the reactor under controlled temperature conditions.

Abstract: The present invention is directed to a combination reactor system for exothermic reactions comprising a trickle-bed reactor and a shell-and-tube reactor. This combination allows the system to efficiently remove heat while also providing the ability to control both the temperature and/or reaction progression. The trickle-bed reactor removes heat efficiently from the system by utilizing latent heat and does not require the use of a cooling or heating medium. The shell-and-tube reactor is used to further progress the reaction and provides a heat exchanger in order to introduce fluid at the desired temperature in the shell-and-tube reactor. Also, additional reactant or reactants and/or other fluids may be introduced to the shell-and-tube section of the reactor under controlled temperature conditions.

Abstract: The present invention relates, in part, an improved process for the production of certain hydrofluoroolefins, particularly 2,3,3,3-tetrafluoropropene (1234yf). In certain non-limiting embodiments, the invention relates to methods for improving process efficiency during the fluorination of 1,1,2,3-tetrachloropropene, 2,3,3,3-tetrachloropropene, and/or 1,1,1,2,3-pentachloropropane to 2-chloro-3,3,3-trifluoropropene by separating and recycling unreacted HF, unreacted starting materials, and/or certain pro cess intermediates from the 2-chloro-3,3,3-trifluoropropene product stream.

Abstract: A method for forming 2,3,3,3-tetrafluoropropene (HFO-1234yf) comprising providing a dehydrochlorination starting material having relatively low concentrations of 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf), especially and preferable less than about 8.0% when the dehydrochlorination reaction utilizes no substantial amount of catalyst or catalyst comprising austenitic nickel-based materials.

Abstract: The invention relates to a process to prepare tetrahalopropenes, such as 2-chloro-3,3,3-trifluoropropene (1233xf). The process comprises atomizing a feed material, such as 1,1,2,3-tetrachloropropene (1230xa) and the like, and mixing it with superheated HF to form a vaporized composition of feed material and HF with substantially instantaneous contact with a vapor phase fluorination catalyst. The invention extends catalyst life and forestalls catalyst deactivation.

Abstract: The invention relates to a process to produce 244bb from 1233xf in multiple reaction zones whereby the 1233xf starting material is at least 95% converted to 244bb and by-product such as 245cb forms in amounts less than about 2%.

Abstract: In certain aspects, the present invention relates to methods for increasing the cost efficiency and safety of the hydrogenation of a fluorinated olefin by controlling the reaction conditions and parameters. In further aspects, the hydrogenation reaction is provided in a two stage reaction wherein the reactant amounts, temperature and other parameters are controlled such that the conversion percentage, selectivity, and reaction parameters are all within commercially acceptable levels.

Abstract: This invention relates to a process for the suppression of 3,3,3-trifluoropropyne during the manufacture of fluorocarbons, fluoroolefins, hydrochlorofluoroolefins. More particularly, this invention is directed to a process to suppress the formation of 3,3,3-trifluoropropyne during processes for the manufacture of HCFO-1233zd(E), HCFO-1233zd(Z), HFO-1234ze(E), and/or HFO-1234ze(Z).

Abstract: Disclosed is a process for the manufacture of HFO-1234yf from TCP in three integrated steps that include hydrofluorination of TCP (tetrachloropropene) to HCFC-1233xf in the vapor phase followed by hydrofluorination of HCFC-1233xf to HCFC-244bb in the liquid phase which is then followed by dehydrochlorination in liquid or vapor phase to produce HFO-1234yf. The vapor phase hydrofluorination is carried out at a higher pressure than the liquid phase hydrofluorination, thereby eliminating the need for compression and/or intermediate recovery. Also, any HCl generated from this reaction is fed to the liquid phase hydrofluorination section to promote agitation and mixing. This results in a more economical process from an initial capital and operating cost versus conducting the 3-steps sequentially.