CATALYTIC HYDROGENOLYSIS

Abstract: A process is disclosed for the catalytic hydrogenolysis of at least one starting material selected from saturated acyclic halofluorocarbons and hydrohalofluorocarbons containing three or four carbon atoms, and from one to five non-fluorine halogens (each non-fluorine halogen being independently chlorine or bromine) wherein all non-fluorine halogen substituents are contained on end carbons. The process involves reacting the starting material with hydrogen at an elevated temperature of about 300 DEG C or less in the presence if a catalyst containing a catalytically effective amount of palladium supported on carbon to produced a hydrogenolysis product wherein over 80 mole percent of the hydrogenolysis product is a saturated compound having the same distribution of fluorine substituents as the starting material. The carbon support has an ash content of less than about 0.5 % by weight.

Description: ______ CATALYTIC HYDROGENOLYSIS F IELD OF THF. TWVF.W TOW This invention relates to catalytic hydrogenolysis of halofluorocarbons and hydrohalofluorocarbons, and more particularly, to the hydrogenolysis of said materials using palladium-containing catalysts. BACKGROUND Various processes for the catalytic hydrogenolysis of chlorofluorocarbons and hydrochlorofluorocarbons are known. For example, U.S. Patent No. 2,942,036 discloses the reaction of 1,2,2-trichloropentafluoropropane with hydrogen in the presence of palladium on activated carbon catalyst to produce 1,2,2-trihydropentafluoro- propane. The examples show that under the conditions of the experiments one of the products from this reaction is CF3CH=CF2. The carbon support may be treated with aqueous HF prior to depositing palladium on the support for the purpose of removing silica from the carbon. U.S. Patent No. 5,315,048 discloses a process wherein 1,2,3-trichloropentafluoropropane is contacted with hydrogen in the presence of palladium on alumina to produce 1, 1,1,2,3-pentafluoropropane. It is mentioned in this patent that reduction of 1,2,3-trichloropenta- fluoropropane with hydrogen over Pd on carbon gives primarily a mixture of HCF2CHFCF 2 H and HCF 2 CHFCF 2 CI. U.S. Patent No. 4,319,060 discloses a process wherein 1, 1-dichlorotetrafluoroethane contained in mixtures thereof with 1,2-dichlorotetrafluoroethane is selectively degraded to provide 1,2-dichlorotetrafluoro- ethane substantially free of 1,1-dichlorotetrafluoro- ethane. The process includes contacting, in the vapor phase, an organic feed composition containing a major amount of the 1,2-isomer and a minor amount of the 1,1-isomer with hydrogen in the presence of a hydro- dechlorination catalyst. C. Gervasutti et al., J. Fluorine Chem., 19, 1-20 (1981/2) report that 1,1, 1,2-tetrafluoroethane was prepared from isomeric mixtures of dichlorotetrafluoroethanes through selective hydrogenolysis of the CF3CCI 2 F isomer present in the mixture catalyzed by Pd/C. The other isomer CCIF 2 CCIF 2 appeared more stable to hydrogenolysis and was only converted partially to the monohydrogenated derivative CHF2CCIF2. U.S. Patent No. 5,136,113 discloses catalytic hydrogenolysis of fluorohalocarbons and fluorohalohydro- carbons using catalysts of certain metals (e.g., palladium) on low-ash carbon. Various other processes using catalysts containing acid-washed carbon have been studied. A. A. Goleva et al., Russ. J. Phys. Chem., 442, 290-1 (1970) discloses the dehydrochlorination of 1, 1,2,2-tetrachloroethane to the olefin trichloro- ethylene (and HC1) using activated charcoal as the catalyst. Activated charcoal treated with hydrochloric acid proved to be more active than an untreated specimen for the production of trichloroethylene. SUMMARY OF THE INVENTION The present invention provides a process for the catalytic hydrogenolysis of at least one starting material selected from acyclic saturated halofluoro- carbons and hydrohalofluorocarbons containing three or four carbon atoms, and from one to five non-fluorine halogens, wherein each non-fluorine halogen is independently selected from the group consisting of chlorine and bromine and wherein all non-fluorine halogen substituents are contained on end carbons (i.e., the first and/or the third carbons of three-carbon compounds and the first and/or fourth carbons of four- carbon compounds) . The process comprises reacting said starting material with hydrogen at an elevated temperature of about 300°C or less in the presence of a catalyst containing a catalytically effective amount of palladium supported on carbon to produce a hydrogenolysis product wherein over 80 mole percent of the hydrogenolysis product is a saturated compound having the same distribution of fluorine substituents as the starting material, said carbon support having an ash content of less than about 0.5% by weight. DETAILED DESCRIPTION The catalysts suitable for the process of this invention comprise palladium and may optionally contain additional Group VIII metals (e.g., Pt, Ru, Rh or Ni) . The palladium is supported on low-ash carbon. The palladium-containing material used to prepare the catalysts is preferably a palladium salt (e.g., palladium chloride) . The other metals, when used, may be added to the support in the conventional manner (e.g., as a soluble salt of the metal). The concentration of palladium supported on low-ash carbon is typically within the range of from about 0.2% to about 5% by weight based on the support. The concentration of additional Group VIII metal, when used, is about 3% by weight, or less, based on the support; but palladium is ordinarily at least 50% by weight of the supported metal (preferably at least 80% by weight of the total metals present on the support) . Low-ash carbon supports can be prepared by a variety of methods. One method is to wash the carbon support with acid prior to deposit of metal. Acid treatment can be performed with more than one acid, but the initial acid treatment typically uses an acid other than hydrofluoric acid. Preferred acids used for the initial acid treatment contain neither phosphorus nor sulfur. Examples of acid that can be used in the initial acid treatment include organic acids such as acetic acid and inorganic acids such as hydrochloric acid or nitric acid. Preferably hydrochloric acid is used. The second acid treatment, when employed, advantageously uses hydrofluoric acid. Normally, the carbon is treated with acid such that after such treatment, the carbon contains less than about 0.5% by weight ash and preferably less than about 0.3% by weight ash. Vegetable-based carbons, such as coconut shell based carbon are preferred for the acid treatment. A preferred embodiment is described below. A carbon support is soaked overnight with gentle stirring in a 1 molar solution of the acid prepared in deionized water. The carbon support is then separated and washed with deionized water or until the pH of the washings is about 3. Preferably, the carbon support is then soaked again with gentle stirring in a 1 molar solution of the acid prepared in deionized water for 12 to 24 hours. The carbon support is then washed with deionized water until the washings are substantially free of the anion of the acid (e.g., Cl" or NO 3 ") , when tested by standard procedures. The carbon support is then separated and dried at 120°C. If necessary, the washed carbon is then soaked in 1 molar HF prepared in deionized water for about 48 hours at room temperature with occasional stirring. The carbon support is separated and washed with deionized water until the pH of the washings is greater than 4. The carbon support is then dried at 150°C in air followed by calcination at 300°C for about 3 hours in air prior to its use as a support. Reference is made to U.S. Patent No. 5,136,113 for further details relating to producing acid-washed carbon catalysts. The present invention provides high selectivity to product compounds having the same distribution (i.e., the same number and the same relative position) of fluorine substituents as the starting compound. The invention includes the hydrogenolysis of chlorofluoro- carbons which contain three carbons and no more than four chlorines in the molecule (e.g., CCI 3 CF2CCIF2, CCI 2 FCF 2 CCI 2 F, CCI 2 FCF 2 CCIF 2 , CCI 3 CF 2 CF 3 , CCI2FCF2CF 3 , CCIF2CF 2 CCIF 2 and CCIF2CF2CF3) . This invention also includes the hydrogenolysis of hydrochlorofluorocarbons which contain three carbons and (i) no more than three chlorines and one hydrogen in the molecule (e.g., CHCI 2 CF 2 CCIF 2 , CHCIFCF2CCI2F, CCI2FCF2CHF2, CCI3CF2CHF2, CHC1FCF 2 CC1F 2 , CHCI 2 CF 2 CF 3 , CHF 2 CF CC1F2 and CHCIFCF2CF3) ; (ii) two chlorines and two hydrogens in the molecule (e.g., CHCIFCF2CHCIF, CHCI 2 CF 2 CHF 2 and CCIF 2 CF 2 CH 2 CI) ; (iii) one chlorine and two hydrogens in the molecule (e.g., CHCIFCF2CHF2, CH2FCF 2 CCIF 2 and CH2CICF2CF3) ; or (iv) one chlorine and three hydrogens in the molecule (e.g., CH2CICF2CHF2, CH 2 FCF 2 CHC1F and CH3CF2CCIF2) . This invention further includes the hydrogenolysis of chlorofluorocarbons containing four carbons and no more than five chlorines in the molecule (e.g., CCIF2CF2CF2CCIF2 and CCI 2 FCF 2 CF 2 CF3) and the hydrogenolysis of hydrochlorofluorocarbons which contain four carbon atoms and no more than four chlorines and one hydrogen in the molecule (e.g., CCIF 2 CF 2 CF 2 CHF 2 , CHCIFCF 2 CF 2 CF 3 and CCIF 2 CF 2 CHFCF3) . The valencies not satisfied by chlorine or hydrogen are satisfied by fluorine. Of note are embodiments where both end carbons contain non-fluorine halogen. Also of note are embodiments where only one carbon contains non-fluorine halogen. Use of suitable temperatures, contact times and intermediate recycle (where applicable) in accordance with this invention can result in production of hydrogenolysis product wherein all chlorines of a starting material have been replaced by hydrogen, with high selectivity (i.e., over 80 mole percent based on the amount of starting material converted) . For example, the present invention provides a process for reacting CCI 2 FCF 2 CCIF 2 with hydrogen to produce CH 2 FCF 2 CHF 2 with high selectivity; a process for reacting CCI3CF 2 CF3 with hydrogen to produce CH3CF2CF3 with high selectivity; a process for reacting CCI 2 FCF 2 CF 3 with hydrogen to produce CH 2 FCF 2 CF 3 with high selectivity; a process for reacting CCIF 2 CF 2 CCIF 2 with hydrogen to produce CHF 2 CF 2 CHF 2 with high selectivity; a process for reacting CCIF 2 CF 2 CF 2 CCIF 2 with hydrogen to produce CHF 2 CF 2 CF 2 CHF 2 with high selectivity; a process for reacting CHF2CF 2 CF2CCIF2 with hydrogen to produce CHF 2 CF 2 CF 2 CHF 2 with high selectivity; a process for reacting CCI3CF2CCIF2 with hydrogen to produce CH3CF 2 CHF 2 with high selectivity; a process for reacting CCI2FCF2CCI2F with hydrogen to produce CH 2 FCF 2 CH 2 F with high selectivity; a process for reacting CCIF 2 CF 2 CF 3 with hydrogen to produce CHF 2 CF 2 CF3 with high selectivity; a process for reacting CHCI2CF 2 CCIF 2 with hydrogen to produce CH 3 CF 2 CHF 2 with high selectivity; a process for reacting CHCIFCF 2 CCI 2 F with hydrogen to produce CH 3 CF 2 CHF 2 with high selectivity; a process for reacting CCI 3 CF2CHF2 with hydrogen to produce CH3CF 2 CHF 2 with high selectivity; a process for reacting CHCIFCF 2 CCIF 2 with hydrogen to produce CH2FCF 2 CHF 2 with high selectivity; a process for reacting CCI 2 FCF 2 CHF 2 with hydrogen to produce CH2FCF2CHF2 with high selectivity; a process for reacting CHCI 2 CF 2 CF3 with hydrogen to produce CH3CF 2 CF 3 with high selectivity; a process for reacting CHF 2 CF2CCIF 2 with hydrogen to produce CHF 2 CF 2 CHF 2 with high selectivity; a process for reacting CHCIFCF 2 CF 3 with hydrogen to produce CH 2 FCF 2 CF 3 with high selectivity; a process for reacting CCI 2 FCF 2 CF 2 CF 3 with hydrogen to produce CH2FCF2CF 2 CF3 with high selectivity; and a process for reacting CHCIFCF 2 CF 2 CF 2 CF 3 with hydrogen to produce CH 2 FCF 2 CF 2 CF 3 with high selectivity. Mixtures of starting materials may also be used. For example, a mixture of CCI 2 FCF 2 CF3 and CCIF2CF 2 CCIF2 may be reacted with hydrogen to produce a mixture of CHF 2 CF2CHF2 and CH2FCF2CF3 with high selectivity. The present invention also provides a process for a selective two-step hydrogenolysis of a mixture of CCI 2 CF2CF3 and CCIF 2 CF 2 CCIF 2 (e.g., in a ratio of from 1:9 to 9:1) . In the first step of the two-step process the CCI 2 FCF 2 CF 3 is selectively reacted with hydrogen at a temperature less than about 200°C to provide a mixture containing CH 2 FCF 2 CF3 and CCIF2CF 2 CCIF2. In the second step the CCIF2CF 2 CCIF 2 is reacted with hydrogen at a temperature greater than about 200°C to provide CHF 2 CF 2 CHF2. It is ordinarily preferable to recover the CH 2 FCF2CF3 of the first step prior to carrying out the second step. Typically, the first step produces some CHCIFCF2CF3 and CF 2 CICF2CHF2; and these may be included in the second step reactants. The product from both steps of the reaction are essentially saturated compounds containing the same number of fluorine atoms as the respective initial starting compound and contains less than 10% of olefinic co-product and product containing less fluorine than the initial starting materials. The hydrogenolysis of the present invention is conducted at an elevated temperature. Ordinarily the temperature is about 300°C or less. Typically, satisfactory reaction rates are achieved at operating temperatures of about 150° to 250°C. Generally, in order to provide substantial hydrogenolysis product yields, the amount of hydrogen used is at least about 0.5 mole per mole of the organic starting material. To provide yields desired in many embodiments, at least stoichiometric amounts of hydrogen are used. A considerable excess of hydrogen can also be advantageously employed to provide the yields desired in many embodiments in addition to serving as a heat sink to reduce the overall temperature rise in the reactor. Pressure is not critical. Atmospheric and superatmospheric pressures are the most convenient and are therefore preferred. Practice of the invention will become further apparent from the following non-limiting examples. EXAMPLE 1 Carbon Support The carbon support used in the examples was a 4 x 8 mesh (about 4.7 mm x 2.4 mm) commercial grade coconut shell carbon which had (before washing) an ash content of about 2.6 weight percent. After hydrochloric acid washing, the carbon support had an ash content of less than about 0.1 weight percent. Preparation of an isomeric mixture of CCIF 2 CF2CCIF 2 and CCI2FCF 2 CF3 A 400 mL Hastelloy™ nickel alloy shaker tube was charged with CCl3F-modified anhydrous aluminum chloride (3.0 g) prepared as illustrated in U.S. Patent No. 5,157,171. The tube was sealed, cooled to -78°C and evacuated and purged with nitrogen. It was then charged with CCI 2 F 2 (50 g, 0.41 mole) . The cold shaker tube was placed in a barricade and charged with 25 g (0.25 mole) of tetrafluoroethylene. The reactor was warmed to 60°C over the course of 15 minutes during which time the pressure rose to 80 psig (653 kPa) . The temperature was maintained for an additional 1.3 hours at 60°C and then raised to 80°C and held for one hour at which time the pressure rose to 112-115 psig (873-894 kPa) . After cooling and discharge there was obtained 54.7 g of a clear supernatant liquid. Analysis of this liquid by 19 F NMR showed that the product contained 13.9% CCIF 2 CF 2 CCIF 2 and 53.5% CCI 2 FCF 2 CF3 and other products. The product isomer mix was then recovered from this reaction mixture by distillation. Hydrogenolysis of an isomeric mixture of CCIF 2 CF 2 CCIF 2 and CCI 2 FCF 2 CF3 The starting material was prepared from two different runs by the procedure described above and combined for the hydrogenolysis experiment. They were present in the ratio of 41.3% CC1F 2 CF 2 CC1F 2 (CFC-216ca) and 58.7% CCI 2 FCF 2 CF3 (CFC-216cb) . This liquid isomeric mixture of CFC-216ca and CFC-216cb, 0.3 mL/minute, was vaporized and mixed with 300 cc/minute of hydrogen. This vaporized mixture was passed through a 1" O.D. x 13" reactor (25.4 mm x 330 mm) containing containing 46 g of 2 weight percent palladium supported on 4 x 8 mesh (4.7 mm x 2.4 mm) low-ash, acid-washed carbon heated to 150°C in a fluidized sand bath. About four hours after start of the reaction, organic product analysis using conventional gas chromatography indicated that CCI 2 FCF 2 CF 3 conversion was essentially complete with about 6% of CCIF2CF2CCIF2 being converted to the monohydrogenolysis product (i.e., HCFC-226cb or CF 2 CICF 2 CF 2 H) . The temperature of the reactor was then increased to 275°C for a period of about four hours with the organic starting material and hydrogen flowing through the reactor. At the end of this period, the reactor temperature was brought back down to 150°C. After about eight hours of operation at 150°C, organic product analysis indicated that CCI 2 FCF 2 CF 3 conversion was still essentially complete, with about 70% selectivity to 1, 1-dihydrohexafluoropropane (HFC-236cb) and about 23% selectivity to 1-hydro-l-chlorohexafluoropropane (HCFC-226ca) . The conversion of CCIF 2 CF2CCIF2 was essentially zero and products arising from loss of fluorine from the starting substrates was less than about 5%. Comparative Hydrogenolysis of CF 3 CCI 2 CF 3 Liquid CF3CCI 2 CF 3 , 3 mL/hour, was vaporized and mixed with 10 cc/minute of hydrogen. This vapor mixture was sent through a 0.5" O.D. x 8" (12.7 mm x 203 mm) Hastelloy™ nickel alloy reactor containing 7.2 g of 0.5 weight percent palladium supported on acid washed carbon maintained at 150°C using a fluidized sand bath. Organic product analysis using conventional gas chromatography indicated that about 90% of the starting material had been converted. The hydrogen-containing products included 15.7% 2,2-dihydrohexafluoropropane (HFC-236fa), 54.3% 2-chloro-2-hydrohexafluoropropane (HCFC-226da) , 12.3% 2-hydropentafluoropropene, and 1.7% 1,2,2-trihydropentafluoropropane (HFC-245fa) and small quantities of other compounds. This example was repeated except that the hydrogen flowrate was increased to 30 cc/minute. Organic product analysis using conventional gas chromatography indicated that the starting material conversion was essentially complete. The hydrogen-containing products included 24.8% 2,2-dihydrohexafluoropropane (HFC-236fa) , 54.6% 2-chloro-2-hydrohexafluoropropane (HCFC-226da) and 19.8% 1,2,2-trihydropentafluoropropane (HFC-245fa) and small quantities of other compounds. This experiment illustrates that when using palladium supported on acid washed carbon as catalyst and where the two chlorines of the starting compound are on the internal carbon, an olefin and/or a saturated product containing one less fluorine than the starting compound can be produced in significant amounts. EXAMPLE 2 CHF2CF2CF2CCIF2 (HCFC-3281CC) → CHF2CF2CF2CHF2 (HFC-338pcc) Liquid HCFC-3281cc (2 mL/hr) was vaporized, mixed with hydrogen (10 cc/min) and sent through a 6" x 0.5" (152 mm x 12.7 mm) Hastelloy™ nickel alloy reactor containing 4.0 g of 0.3 wt% palladium on acid-washed carbon maintained at 275°C in a fluidized sand bath. After about five hours of operation, organic product analysis using conventional gas chromatography indicated about 38% HCFC-3281cc, 59% HFC-338pcc, and small amounts of other products.

Claims: WHAT IS CLAIMED IS: 1. A process for the catalytic hydrogenolysis of at least one starting material selected from acyclic saturated halofluorocarbons and hydrohalofluorocarbons containing three or four carbon atoms, and from one to five non-fluorine halogens wherein each non-fluorine halogen is independently selected from the group consisting of chlorine and bromine, and wherein all non- fluorine halogen substituents are contained on end carbons, comprising: reacting said starting material with hydrogen at an elevated temperature of about 300°C or less in the presence of a catalyst containing a catalytically effective amount of palladium supported on carbon to produce a hydrogenolysis product wherein over 80 mole percent of the hydrogenolysis product is a saturated compound having the same distribution of fluorine substituents as the starting material, said carbon support having an ash content of less than about 0.5% by weight. 2. The process of Claim 1 wherein the starting material is selected from the group consisting of CCI3CF2CCIF 2 , CCI 2 FCF2CCI 2 F, CC1 2 FCF 2 CC1F 2 , CC1 3 CF 2 CF 3/ CCI2FCF2CF3, CCIF 2 CF 2 CCIF2 and CCIF 2 CF 2 CF 3 . 3. The process of Claim 1 wherein the starting material is selected from the group consisting of CHCI2CF2CCIF2, CHCIFCF2CCI 2 F, CCI 2 FCF2CHF2, CCI3CF2CHF2, CHCIFCF 2 CCIF 2 , CHCI 2 CF 2 CF3, CHF 2 CF 2 CCIF 2 and CHCIFCF2CF 3 . 4. The process of Claim 1 wherein the starting material is selected from the group consisting of CHCIFCF 2 CHCIF, CHCI 2 CF 2 CHF2 and CCIF 2 CF 2 CH 2 CI. 5. The process of Claim 1 wherein the starting material is selected from the group consisting of CHCIFCF2CHF2, CH2FCF2CCIF2 and CH2CICF2CF3. 6. The process of Claim 1 wherein the starting material is selected from the group consisting of CH2CICF2CHF2, CH2FCF2CHCIF and CH3CF2CCIF2. 7. The process of Claim 1 wherein the starting material is selected from the group consisting of CCIF 2 CF2CF2CCIF2 and CCI 2 FCF2CF2CF3. 8. The process of Claim 1 wherein the starting material is selected from the group consisting of CCIF2CF2CF2CHF2, CHCIFCF2CF2CF3 and CCIF2CF2CHFCF3. 9. The process of Claim 1 for the hydrogenolysis of a mixture of CCI 2 CF2CF3 and CCIF 2 CF 2 CCIF 2 wherein in a first step the CCI 2 FCF 2 CF 3 is selectively reacted with hydrogen at a temperature less than about 200°C to provide a mixture containing CH 2 FCF 2 CF3 and CCIF2CF2CCIF2; and in a second step the CCIF 2 CF2CCIF 2 is reacted with hydrogen at a temperature greater than about 200°C to provide CHF 2 CF 2 CHF 2 . 10. The process of Claim 9 wherein CH 2 FCF2CF3 of the first step is recovered prior to carrying out the second step.

Inventors: KELLNER CARL STEPHEN, RAO VELLIYUR NOTT MALLIKARJUNA, SIEVERT ALLEN CAPRON, KELLNER, CARL, STEPHEN, RAO, VELLIYUR, NOTT, MALLIKARJUNA, SIEVERT, ALLEN, CAPRON
Applicants: DU PONT, E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1995
Main classification: C07C17
IPC codes: B01J23, C07B61, C07C17, C07C19