Abstract: There is provided a process for the production of pentafluoroethane which comprises contacting a hydrofluorochloroethane having the formula: C.sub.2 H.sub.1 Cl.sub.1+x F.sub.1+y wherein x and y are each independently 0,1,2 or 3 provided x+y is 3 with hydrogen fluoride in the vapor phase and in the presence of a fluorination catalyst which comprises zinc or a compound of zinc and chromia, chromium fluoride or chromium oxyfluoride.

Abstract: There is provided a process for the production of difluoromethane which comprises contacting a dichloromethane with hydrogen fluoride in the presence of a fluorination catalyst comprising zinc or a compound of zinc and metal oxide, fluoride or oxyfluoride.

Abstract: A production method in which reaction processes are divided into two regions comprising one reaction region where mainly perchloroethylene is made to react with HF in a vapor phase in the presence of a catalyst and the other reaction region where HCFC-123 (CF.sub.3 CHCl.sub.2) and/or HCFC-124 (CF.sub.3 CFHCl) is made to react with HF in a vapor phase in the presence of a catalyst, the former region being kept at a higher pressure and the latter region at a lower pressure during the reaction procedure. By this method it is possible to keep the conversion of perchloroethylene at a high level while securing the life of a catalyst, and it is also possible to raise the selectivity of HFC-125. This is a method of producing HFC-125 in which the content of CFC-115 is lowered to not more than 15 vol % of the total amount of HFC-125 and CFC-115, and then CFC-115 is made to react with hydrogen in the presence of a catalyst.

Abstract: This invention relates to a process for the production of 1,1,2,2- and/or 1,1,1,2-tetrafluoroethanes, and in particular to a process for the production of 1,1,1,2-tetrafluoroethane.

Abstract: A method of producing 1,1,1,2-tetrafluoroethane in two separation reaction zones involving (1) reaction of trichloroethylene and hydrogen fluoride to produce l,l,l-trifluoro-2-chloroethane and (2) reaction of the 1,1,1-trifluoro-2-chloroethane and hydrogen fluoride to produce 1,1,1,2-tetrafluoroethane wherein both reactions are carried out at superatmospheric pressure, reaction (2) is carried out at a temperature in the range of 250.degree.-450.degree. C., reaction (1) is carried out at a temperature in the range of 200.degree.-400.degree. C. but below that used in reaction (2) and unconverted 1,1,1-trifluoro-2-chloroethane is recycled for further reaction with hydrogen fluoride.

Abstract: Process for the hydrofluorination of chloro(fluoro)butane of general formula C.sub.4 H.sub.5 Cl.sub.x F.sub.5-x in which x=1 to 5, by means of hydrogen fluoride and in the presence of a catalyst chosen from the derivatives of metals of groups IIIa, IVa, IVb, Va, Vb and VIb of the Periodic Table of the elements.

Abstract: The invention relates to the manufacture of 1,1,1,2-tetrafluoroethane (F134a) by gas-phase catalytic fluorination of 1-chloro-2,2,2-trifluoroethane (F133a).A mixed catalyst is employed, composed of nickel and chromium oxides, halides and/or oxyhalides deposited on a support consisting of aluminium fluoride or of a mixture of aluminium fluoride and alumina.This mixed catalyst makes it possible to obtain an excellent selectivity for F134a with a high production efficiency.

Abstract: There is a method for concurrently producing 1,1,1,2-tetrafluoroethane and pentafluoroethane, which comprises (A) reacting 1,1,1-trifluoro-2-chloroethane, hydrogen fluoride and chlorine in a first reactor in the presence of flurorination catalyst at a temperature in the range of from 300.degree. C. to 450.degree. C.; (B) transfering the products of step (A) together with trichloroethylene to a second reactor and reacting them at a temperature in the range of from 200.degree. C. to 400.degree. C.; (C) separating 1,1,1,2-tetrafluoroethane and pentafluoroethane from the resultant products; and (D) feeding the remaining products from step (C) back to the first reactor, wherein the molar ratio of chlorine/1,1,1-trifluoro-2-chloroethanethe in step (A) is in the range of from 0.001 to 0.

Abstract: An object is to effectively preparing a fluorinated compound by developing a catalyst which is effective in the fluorination of a halogenated alkane or alkene with hydrogen fluoride by a gas phase fluorination or addition of hydrogen fluoride. To this end, a catalyst which comprises a least one element selected from the group consisting of Ti, V, Zr, Mo, Ge, Sn and Pb, and alumina, aluminum fluoride or partially fluorinated alumina is used. This catalyst is prepared by an impregnation method to support the above element on alumina and the like, or a precipitation method in which the catalyst is co-precipitated from a solution containing an aluminum compound and a compound of the above element.

Abstract: A method for the preparation of 1,1,1,3,3-pentafluoropropane (HFC-245fa) and 1-chloro-3,3,3-trifluoropropene (HCFC-1233). 1,1,1,3,3-pentachloropropane (HCC-240fa) is fluorinated with HF in a vapor phase in the presence of a vapor phase catalyst. The HCFC-1233 and any co-produced 1,3,3,3-tetrafluoropropene (HFC-1234) are recycled for further fluorination by HF for a greater than 99% HCC-240fa conversion.

Abstract: A process for the production of difluoromethane comprising (a) contacting dichloromethane with hydrogen fluoride in the presence of a fluorination catalyst to produce a product stream comprising difluoromethane, monochloromonofluoromethane and unreacted starting materials and (b) separating difluoromethane from the product stream from step (a), wherein sufficient hydrogen fluoride is employed in the process such that during step (b) the molar ratio of hydrogen fluoride to monochloromonofluoromethane is at least about 100:1.

Abstract: A process for co-production of 1,1,1,2-tetrafluoroethane (HFC-134a;CF.sub.3 CH.sub.2 F), pentafluoroethane (HFC-125; CF.sub.3 CHF.sub.2) and 1,1,1 -trifluoroethane (HFC-143a; CF.sub.3 CH.sub.3) by a two-step gaseous reaction comprising the steps of a) reacting 1,1,1-trifluoro-2-chloroethane (CFCH.sub.2 Cl, HCFC-133a) with HF in a first reactor to prepare 1,1,1,2-tetrafluoroethane (HFC-134a; CF.sub.3 CH.sub.2 F), pentafluoroethane (HFC-125; CF.sub.3 CHF.sub.2) and 1,1,1-trifluoroethane (HFC-143a; CF.sub.3 CH.sub.3); b) adding trichloroethylene (TCE:CCl.sub.2 CHCl) to the reaction product of step a) in a second reactor to prepare HCFC-133a; separating HCl, HFC-134a, HFC-125 and HFC-143a from the reaction product of step b) and recycling HCFC-133a to the first reactor, and the stages being performed in the presence of fluorization catalyst obtained by calcining a reaction product which is obtained by reacting ethanol with a mixture of calcium fluoride(CaF.sub.

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: Process for synthesizing 1,1,1-trifluoroethane (143a) in the gaseous phase by reacting 1,1-defluoro-1-chloroethane in gaseous phase in the presence of a Cr catalyst. The process may be run isothermally or adiabatically, without co-feeding air or other oxygen containing gas, in the presence or absence of a Ni, Co, Zn or Mn cocatalyst for the Cr catalyst. The catalyst may be unsupported or supported with a support preferably selected from activated carbon, alumina and fluorided alumina. The formation of olefin byproduct can be kept to less than 10 ppm in accordance with the process of the invention.

Abstract: A chromium-containing fluorination catalyst which comprises an activity-promoting amount of zinc or a compound of zinc, a process for increasing the activity of a chromium-containing fluorination catalyst by introducing an activity promoting amount of zinc or a compound of zinc to the catalyst and a process for the production of fluorinated hydrocarbons, in particular 1,1,1,2-tetrafluoroethane which comprises reacting a hydrocarbon or a halogenated hydrocarbon, in particular 1-chloro-2,2,2-trifluoroethane with hydrogen fluoride in the vapour phase in the presence of the zinc-promoted chromium-containing catalyst.

Abstract: The invention relates to a process for the manufacture of 1,1,1,2-tetrafluoro-2-chloroethane and of pentafluoroethane.The process, which consists of the gas phase catalytic fluorination of at least one pentahaloethane of formula C.sub.2 HX.sub.2-n F.sub.3+n in which X denotes a chlorine or bromine atom and n the number 0 or 1 by means of hydrofluoric acid, is characterized in that there is used a mixed catalyst composed of oxides, halides and/or oxyhalides of nickel and chromium deposited on a support consisting of aluminium fluoride or a mixture of aluminium fluoride and alumina.

Abstract: A process is disclosed for the preparation of a fluorinated aliphatic olefin having the formulaCH.sub.a F.sub.3-a --CH.sub.2 --CH.sub.b F.sub.3-bwherein a is 0 or the integer 1 or 2 and b is 0 or the integer 1, 2 or 3.In the first step of the process, a chlorinated olefinic hydrocarbon of the formulaCH.sub.c Cl.sub.2-c .dbd.CH--CH.sub.d Cl.sub.3-dwherein c is 0 or the integer 1 and d is 0 or the integer 1 or 2 is reacted with anhydrous hydrogen fluoride for a period of time and at a temperature sufficient to form a chlorofluoro olefin of the formulaCH.sub.e Cl.sub.2-e .dbd.CH--CH.sub.f F.sub.3-fwherein e is 0 or the integer 1 and f is 0 or the integer 1 or 2.The chlorofluoro olefin produced in the first step is then reacted with anhydrous hydrogen fluoride in a second reaction. This second reaction is catalyzed with at least one compound that is a metal oxide or metal halide. Mixtures of said metal oxides, metal halides and metal oxides with metal halides may also be used.

Abstract: 1,1,1,2-tetrafluoroethane (134a) is prepared by reacting, in the gas phase, trichloroethylene with 1,1,1-trifluorochloroethane (133a) and hydrofluoric acid with trichloroethylene/133a molar ratios ranging from 5/95 to 50/50, in the presence of a catalyst consisting of Cr.sub.2 O.sub.3 carried on AlF.sub.3.The process provides 134a yields higher than 90% and permits an exceptionally long life of the catalyst. In this way it is possible to realize a continuous process by recycling the unreacted trichloroethylene and 133a, thereby making up for the relatively low global conversion of the reagents.

Abstract: The subject of the invention is a continuous process for the preparation of 1,1,1,2-tetrafluoroethane (134a) from 2-chloro-1,1,1-trifluoroethane (133a) and hydrofluoric acid in the gaseous phase in the presence of a chromium-based catalysts.According to the invention, the flow of gas leaving the reactor is subjected to a distillation in order to separate at the top a flow containing almost all the HC1 and at least 90% of the 134a produced by the reaction and at the bottom a flow containing at least 90% of the unconverted reactants (133a and HF), and the latter flow is recycled directly to the reactor, without any purifying operation.

Abstract: 1,1,1-Trifluoroethane is produced, in addition to 1,1,-dichloro-1-fluoroethane and/or 1-chloro-1,1-difluoroethane, by hydrofluorination in the liquid phase, using hydrogen fluoride, vinylidene fluoride and at least one chloro compound chosen from vinylidene chloride and 1,1,1-trichloroethane.

Abstract: The invention relates to continuous production of 1,1,1-chlorodifluoroethane from 1,1,1-trichloroethane and hydrofluoric acid by reaction in liquid phase in the presence of at least one fluorination catalyst. According to the invention, the process is carried out under an absolute pressure of between 6 and 30 bars and at a temperature of between 50.degree. and 120.degree. C., the content of catalyst(s) in the reaction mixture, expressed as a percentage by weight of metal, being between 0.05 and 10% and the content of organohalogenated by-products not belonging to series 140 in the reaction mixture being controlled at a value below 40% by weight. This process makes it possible, at the same time, to obtain a high degree of conversion of hydrofluoric acid, to minimize the coproduction of 1,1,1-trifluoroethane and organohalogenated by-products and to facilitate the recovery of the hydrochloric acid formed.

Abstract: An improved process for producing hydrofluorocarbons and hydrochlorofluorocarbons by reacting anhydrous hydrogen fluoride in the vapor phase and in the presence of a fluorination catalyst with an admixture of perchloroethylene and a phenolic inhibitor. The phenolic component is effective to inhibit the formation of an oxidation product in the perchloroethylene while not substantially degrading the fluorination catalyst during the fluorination process. In another embodiment, substantially all of any oxidation inhibitor is removed from the perchloroethylene in-line prior to reacting the hydrogen fluoride with the perchloroethylene.

Abstract: CF.sub.3 CHFCHF.sub.2 production is disclosed which involves reacting CF.sub.3 CF.dbd.CHF with HF at an elevated temperature over a catalyst selected from the group consisting of aluminum fluoride, fluorided alumina, metals supported on aluminum fluoride, metals supported on fluorided alumina and catalysts comprising trivalent chromium. Also disclosed is enrichment of CF.sub.3 CF.dbd.CHF from a starting mixture containing CF.sub.3 CF.dbd.CHF and CF.sub.3 CH.dbd.CF.sub.2 which involves reacting said starting mixture with HF at an elevated temperature over a catalyst consisting essentially carbon, a catalyst consisting essentially of metal halides supported on carbon, a catalyst consisting essentially of Cr.sub.2 O.sub.3, or mixtures thereof (provided that when Cr.sub.2 O.sub.3 is present the temperature is about 250.degree. C. or less) to produce a product mixture containing CF.sub.3 CH.sub.2 CF.sub.3 and unreacted CF.sub.3 CF.dbd.CHF wherein the mole ratio of CF.sub.3 CF.dbd.CHF to CF.sub.3 CH.dbd.CF.sub.

Abstract: A method of producing 1,1,1,2-tetrafluoroethane in two separation reaction zones involving (1) reaction of trichloroethylene and hydrogen fluoride to produce 1,1,1-trifluoro-2-chloroethane and (2) reaction of the 1,1,1- trifluoro-2-chloroethane and hydrogen fluoride to produce 1,1,1,2-tetrafluoroethane wherein both reactions are carried out at superatmospheric pressure, reaction (2) is carried out at a temperature in the range of 250.degree.-450.degree. C., reaction (1) is carried out at a temperature in the range of 200.degree.-400.degree. C. but below that used in reaction (2) and unconverted 1,1,1-trifluoro-2-chloroethane is recycled for further reaction with hydrogen fluoride.

Abstract: A process is disclosed for producing 1,1,1,3,3,3-hexafluoropropane. The process involves contacting 1,1,1,3,3,3-hexachloropropane with hydrogen fluoride in the vapor phase at a temperature of from about 250.degree. C. to 400.degree. C. in the presence of a catalyst of trivalent chromium supported on carbon. The carbon has an ash content sufficiently low to produce CF.sub.3 CH.sub.2 CF.sub.3 with a selectivity of at least about 70 percent based upon the amount of 1,1,1,3,3,3-hexachloropropane reacted with HF.

Abstract: A process is disclosed for producing a product comprising CCl.sub.2 FCF.sub.3 substantially free of CClF.sub.2 CClF.sub.2. The process includes (i) contacting a mixture of perhalogenated hydrocarbons which is essentially free of CClF.sub.2 CClF.sub.2 and comprises from 20 to 80 mole percent CCl.sub.3 CF.sub.3 and from 5 to 80 mole percent total of at least one compound selected from the group consisting of CCl.sub.2 .dbd.CCl.sub.2, CCl.sub.3 CCl.sub.2 F, CCl.sub.2 FCCl.sub.2 F and CClF.sub.2 CCl.sub.3 with HF and optionally Cl.sub.2 (provided that when the mixture comprises CCl.sub.2 .dbd.CCl.sub.2, Cl.sub.2 is supplied in a mole ratio of Cl.sub.2 to CCl.sub.2 .dbd.CCl.sub.2 of at least 1:2) over a fluorination catalyst at an elevated temperature no higher than 375.degree. C., to provide a product mixture comprising CCl.sub.2 FCClF.sub.2 and C.sub.2 Cl.sub.2 F.sub.4 wherein the ratio of CClF.sub.2 CClF.sub.2 to CCl.sub.2 FCF.sub.3 is less than about 1:50; (ii) recovering said C.sub.2 Cl.sub.2 F.sub.

Abstract: In an improved process and plant for carrying out liquid phase fluorination in the presence of a catalyst, consisting in reacting hydrofluoric acid and an organic starting material in a reaction zone, and in separating, in a separating zone, reactional mixture and at least one light fraction containing the desired fluorinated organic products and at least a first part of the sub-fluorinated organic products formed, and a heavy fraction that includes the remainder of the sub-fluorinated organic products formed, and further comprising partial condensation of the said light fraction in order to obtain a gaseous phase containing the desired fluorinated organic products and a liquid phase containing said first part of the said sub-fluorinated organic products, said heavy fraction being returned to said reaction zone and said liquid phase being returned as a reflux to the top of the separation zone, intermediate recovery is carried out at, or in the proximity of, the lower portion of said separation zone.

Abstract: A process for the preparation of one or more of CHClFCF.sub.3 (HCFC-124), CHF.sub.2 CClF.sub.2 (HCFC-124a) and CHF.sub.2 CF.sub.3 (HFC-125) by reaction of perchloroethylene with hydrogen fluoride in a single stage reaction vessel in the presence of a fluorination catalyst. These compounds are useful in a variety of industrial applications including blowing agents, refrigerants, sterilant gases and solvent applications. Distilling the reaction product produces a distillate comprising HCl, CHClFCF.sub.3, CHF.sub.2 CClF.sub.2 and CHF.sub.2 CF.sub.3 and a minor amount of HF which distillate is scrubbed to remove the acids. The bottoms product comprises perchloroethylene, hydrogen fluoride and organic by-products which is phase separated to sequester the hydrogen fluoride from the mixture of perchloroethylene and organic by-products. The hydrogen fluoride and mixture of perchloroethylene with organic by-products are then preferably re-mixed at a controlled rate and recycled to the reaction vessel.

Abstract: The invention relates to mass catalysts based on chromium and nickel oxides, obtained from a sol of chromium and nickel hydroxides.These catalysts, in which the Ni/Cr atomic ratio is between 0.05 and 5, may be used from the fluorination of halogenated hydrocarbons by HF in the gas phase.

Abstract: A process is disclosed for the preparation of pentafluoroethane from chlorotetrafluoroethane (the yield of pentafluoroethane is at least 50 mole percent based upon the amount of chlorofluoroethane reacted with HF) with particularly low levels of chlorofluoroethanes. The process involves providing sufficient pretreatment (where necessary) of a Cr.sub.2 O.sub.3 catalyst with at least one agent selected from the group consisting of CO, H.sub.2, H.sub.2 O and mixtures thereof in the gaseous state such that the total chlorofluoroethane content of said product stream is less than 1 mole percent. Certain high surface area catalysts may be used without such pretreatment.

Abstract: In a process for preparing 1,1,1-trifluorochloroethane by reacting, in a gas phase, trichloroethylene and hydrogen fluoride, when the reactant gases are diluted with a gas which is inactive to the reaction, it is very easy to control a reaction temperature, and when a generated gas from the reaction of 1,1,1-trifluorochloroethane and hydrogen fluoride is used as a diluent gas, generation of 1,1-difluoroethylene is suppressed to a very low level while not influencing the reaction between trichloroethylene and hydrogen fluoride.

Abstract: 1,1,1,2-tetrafluoroethane (134a) is prepared by reacting, in the gas phase, trichloroethylene with 1,1,1-trifluorochloroethane (133a) and hydrofluoric acid with trichloroethylene/133a molar ratios ranging from 5/95 to 50/50, in the presence of a catalyst consisting of Cr.sub.2 O.sub.3 carried on AlF.sub.3.The process provides 134a yields higher than 90% and permits an exceptionally long life of the catalyst. In this way it is possible to realize a continuous process by recycling the unreacted trichloroethylene and 133a, thereby making up for the relatively low global conversion of the reagents.

Abstract: The invention relates to the purification of pentafluoroethane (F125) containing chloropentafluoroethane (F15).The F-125-F115 mixture to be purified is subjected to a fluorination stage to convert F115 into hexafluoroethane (F116) which is then separated from F125, for example by distillation.

Abstract: A process is disclosed for producing a product comprising CCl.sub.2 FCF.sub.3 substantially free of CClF.sub.2 CClF.sub.2. The process includes (i) contacting a mixture of perhalogenated hydrocarbons which is essentially free of CClF.sub.2 CClF.sub.2 and comprises from 20 to 80 mole percent CCl.sub.3 CF.sub.3 and from 5 to 80 mole percent total of at least one compound selected from the group consisting of CCl.sub.2 .dbd.CCl.sub.2, CCl.sub.3 CCl.sub.2 F, CCl.sub.2 FCCl.sub.2 F and CClF.sub.2 CCl.sub.3 with HF and optionally Cl.sub.2 (provided that when the mixture comprises CCl.sub.2 .dbd.CCl.sub.2, Cl.sub.2 is supplied in a mole ratio of Cl.sub.2 to CCl.sub.2 .dbd.CCl.sub.2 of at least 1:2) over a fluorination catalyst at an elevated temperature no higher than 375.degree. C. to provide a product mixture comprising CCl.sub.2 FCClF.sub.2 and C.sub.2 Cl.sub.2 F.sub.4 wherein the ratio of CClF.sub.2 CClF.sub.2 to CCl.sub.2 FCF.sub.3 is less than about 1:50; (ii) recovering said C.sub.2 Cl.sub.2 F.sub.

Abstract: A single step, vapor phase process for the chlorofluorination of methane forms trifluoromethane and/or tetrafluoromethane in high yield. A Cr.sub.2 O.sub.3 catalyst is preferred.

Abstract: In the production of 1,1,1,2-tetrafluoroethane by reacting trichloroethylene with hydrogen fluoride, crude 1,1,1,2-tetrafluoroethane is highly purified by a method comprising subjecting the crude 1,1,1,2-tetrafluoroethane to preliminary purification to remove hydrogen chloride to a concentration of not higher than 2%, and bring the preliminarily purified 1,1,1,2-tetrafluoroethane containing one or more unsaturated impurities and hydrogen fluoride in an amount at least equimolar to the unsaturated impurities into contact with a fluorination catalyst in a vapor phase to decrease the content of the unsaturated impurities.

Abstract: A process is disclosed for producing 1,1,1,3,3,3-hexafluoropropane with high selectivity. 1,1,1,3,3,3-hexachloropropane is contacted with hydrogen fluoride in the vapor phase at a temperature of from about 200.degree. C. to 400.degree. C. in the presence of a catalyst comprising trivalent chromium, to produce a fluorinated product containing CF.sub.3 CH.sub.2 CF.sub.3 and its haloprecursors (i.e., compounds which may be recycled for further reaction with HF) with a total selectivity of at least about 95 percent; and a sufficient amount of said haloprecursors is reacted with hydrogen fluoride in the vapor phase at a temperature of from 200.degree. C. to 400.degree. C. in the presence of a catalyst comprising trivalent chromium to provide an overall selectivity to 1,1,1,3,3,3-hexafluoropropane of at least about 95 percent based upon the amount of 1,1,1,3,3,3-hexachloropropane initially reacted with HF.

Abstract: A process for the reactivation of a chromium-based fluorination catalyst, in particular chromia, by contacting the deactivated chromium-based fluorination catalyst with an atmosphere containing water vapour at elevated temperature, preferably above 300.degree. C.

Abstract: An improved process for the manufacture of CF.sub.3 CHF.sub.2 by contacting CF.sub.3 CHCl.sub.2 or CF.sub.3 CHClF with HF in the presence of a Cr.sub.2 O.sub.3 catalyst prepared by pyrolysis of ammonium dichromate, the reaction being conducted under controlled conditions whereby the production of CF.sub.3 CHF.sub.2 is maximized, and the formation of chloropentafluoroethane (CF.sub.3 CClF.sub.2) and other perhalo derivatives is minimized. The subject hydrogen-containing compound is useful as a blowing agent, propellant, refrigerant, fire extinguishing agent, or sterilant carrier gas.

Abstract: 1,1,1,2-tetrafluoroethane (HFA 134a) is manufactured from trichloroethylene by a two-stage process comprising reacting trichloroethylene with hydrogen fluoride under superatmospheric pressure in a first reaction zone to form 1,1,1-trifluoro-2-chloroethane (133a) and reacting the 1,1,1-trifluoro-2-chloroethane with hydrogen fluoride in a second reaction zone to form 1,1,1,2-tetrafluoroethane; the entire product stream from the 133a reaction zone together with additional HF of required is fed through the 134a reaction zone. The two reaction zones may be provided within a single reaction vessel.

Abstract: In a process for preparing 1,1,1-trifluorochloroethane by reacting, in a gas phase, trichloroethylene and hydrogen fluoride, when the reactant gases are diluted with a gas which is inactive to the reaction, it is very easy to control a reaction temperature, and when a generated gas from the reaction of 1,1,1-trifluorochloroethane and hydrogen fluoride is used as a diluent gas, generation of 1,1-difluoroethylene is suppressed to a very low level while not influencing the reaction between trichloroethylene and hydrogen fluoride.

Abstract: A chlorofluorination process is disclosed which employs a catalyst comprising chromium oxide for producing halohydrocarbons of the formula CHXFCF.sub.3 (where X is selected from Cl and F). The process is characterized by feeding a combination of components comprising (i) at least one halohydrocarbon starting compound selected from CHCl.dbd.CCl.sub.2 and CH.sub.2 ClCF.sub.3, (ii) hydrogen fluoride and (iii) chlorine, to a reaction zone; contacting said combination of compounds in said reaction zone with a catalyst comprising chromium oxide at an elevated temperature to produce reaction zone products containing halohydrocarbons of the formula CHXFCF.sub.3 together with halohydrocarbon reaction products of the formula CHYClCF.sub.3 (wherein Y is selected from Cl and H); and recovering at least a portion of the reaction zone products from the reaction zone including at least one halohydrocarbon of the formula CHXFCF.sub.3.

Abstract: Process for the preparation of 1,1,1,2-tetrafluoroethane by reaction of hydrogen fluoride with a trihaloethylene according to which trifluoroethylene is chosen as trihaloethylene and the reaction is carried out in the liquid phase.

Abstract: 1,1,1,2-tetrafluoroethane (HFA 134a) is manufactured from trichloroethylene by a two-stage process comprising reacting trichloroethylene with hydrogen fluoride in one reactor to form 1,1,1-trifluoro-2-chloroethane (133a) and reacting the 1,1,1-trifluoro-2-chloroethane with hydrogen fluoride in another reactor to form 1,1,1,2-tetrafluoroethane. The invention is characterized by reversing the reactor sequence and passing the entire product stream from the HFA 134a reactor together with trichloroethylene through the 133a reactor and separating 134a and hydrogen chloride from the recycle stream between the 133a reactor and the 134a reactor.

Abstract: 1,1,1.Trifluoro-2-fluoroethane (HFC 134A), respectively 1,1,1-trifluoro-2, 2-dichloroethane (HCFC 123) 1,1,1-trifluoro-2-chloro, 2-fluoroethane (HCFC 124) and pentafluoroethane (HFC 125), are purified from impurities respectively consisting of 1,1-difluoro-2-chloroethylene (HCFC 1122) and of difluorodichloroethylene (CFC 1112A and CFC 1112), by reacting in the liquid state respectively HFC 134A or HCFC 123, HCFC 124 and HFC 125 containing the relative impurities, with elemental fluorine, at temperatures ranging from -80.degree. to -40.degree. C.

Abstract: A process for preparing 1,1,1-trifluoro-2,2-dichloroethane by hydrofluorination,in the gas phase, of perchloroethylene in the presence of a catalyst comprising chrome oxides supported on AlF.sub.3 in the gamma and/or beta form.

Abstract: The invention relates to a process for the manufacture of 1,1,1,2-tetrafluorochloroethane and of pentafluoroethane.The process which consists of gas phase catalytic fluorination of at least one pentahaloethane of formula C.sub.2 HX.sub.2-n F.sub.3+n in which X denotes a chlorine or bromine atom and n the number 0 or 1, by hydrofluoric acid, is characterized in that a catalyst is employed consisting of a catalytic quantity of chromium in an oxidation state equal to or greater than 3 and of an activated charcoal as support.The selectivity for 1,1,1,2-tetrafluorochloroethane and pentafluoroethane reaches approximately 95% and even more.

Abstract: A process for producing 1,1,1,2-tetrafluoroethane from trichloroethylene and HF, which comprises introducing products of a reaction of trichloroethylene with HF, and products of a reaction of 1,1,1-trifluoro-2-chloroethane with HF into a first distillation column either separately or as a mixture thereof, recovering HCl as a distillate from the top of the first distillation column, and introducing the remainder into a second distillation column.

Abstract: An improved process for the vapor phase fluorination, especially fluorination of 1,1,1-trifluoro-2-chloroethane (CFC-133a) with HF to produce 1,1,1,2-tetrafluoroethane (HFC-134a) employs a catalyst which preferably consists essentially of boehmite and Cr(OH)Cl.sub.2.2H.sub.2 O, combined and extruded to form particulates and then heated in nitrogen.

Abstract: Water present in a hot gaseous product stream from a reactor system A,B (FIG. 1 ) containing hydrogen fluoride is separated from the stream in order to eliminate a potentially corrosive combination of water and HF. The water is removed by contacting the gaseous product stream with liquid HF in a distillation column so as to obtain a bottoms product containing liquid HF and water and a top product containing dry HF and the product to be recovered. The invention encompasses the separation process, a vessel for carrying out the process (FIGS. 2 to 4), a control system for the liquid HF supply to the distillation column (FIGS. 5 and 6) and a recovery system for recovering HF employed during operation of the reactor system in different regimes employing HF as a fluorination agent, as a diluent during catalyst regeneration and/or catalyst prefluorination (FIG. 7 ).