Improved process for the manufacture of 1,1,1-trifluorodichloroethane and 1,1,1,2-tetrafluorochloroethane

Abstract: An improved gas-phase process for the manufacture of 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane by contacting a suitable tetrahaloethylene and/or pentahaloethane with hydrogen fluoride in the presence of Cr₂O₃, prepared by pyrolysis of (NH₄)₂Cr₂O₇, the reaction being conducted under controlled conditions whereby the production of pentafluoroethane is minimized.

Description: An improved process for the manufacture of 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane, more particularly, a gas-phase reaction of a suitable tetrahaloethylene and/or pentahaloethane with hydrogen fluoride in the presence of a Cr₂O₃ catalyst prepared by pyrolysis of ammonium dichromate, the reaction being conducted under controlled conditions whereby the production of pentafluoroethane is minimized. Canadian Patent No. 1,196,345 (1985) describes a process for the preparation of CF₃CHXY (X = H, F; Y = H, F, Cl, Br, I) by addition of HF to the corresponding ethylene in the presence of chromium oxyfluoride at 20-200°C, especially 60-180°C. U.S. Patent No. 3,755,477 describes a process for producing fluorinated aliphatic hydrocarbons which comprises fluorinating a halogenated aliphatic hydrocarbon, including tetrachloroethylene and chlorotrifluoroethylene, by reaction in the gas phase with HF in the presence of a steam-treated and calcined chromium oxide catalyst prepared by a multi-step process. Example 23, column 5, shows tetrachloroethylene as a raw material with formation of CF₃CHCl₂ (20%), CF₃CHClF (20%), CF₃CHF₂ (30%), and CF₃CClF₂ (20%) at 10/1 HF/C₂Cl₄ mol ratio, 5.4 seconds contact time and 360°C reaction R-8604 35 temperature. Example 24, column 5, shows chlorotrifluoroethylene as a raw material with formation of CF₂=CF₂ (20%) and CF₃CHClF (13%) at 1.8/1 HF/C₂ClF₃ mol ratio, 4 seconds contact time and 320°C reaction temperature. In these examples, less desirable pentafluorinated products are obtained in a greater amount than the desired tri- and tetrafluoro products. U.S. Patent No. 3,258,500 describes a process for the catalytic vapor phase reaction of HF with halohydrocarbons, including tetrachloroethylene and chlorotrifluoroethylene, employing a catalyst that consists essentially of a heat-activated anhydrous chromium (III) oxide which may be supported on alumina. This catalyst is highly active. Example 17, column 14 showing fluorination of tetrachloroethylene with this catalyst, like that of the above ′477 patent, produces large quantities of the less desirable highly fluorinated pentafluoroethane. At 400°C the product distribution is 35.0% pentafluoroethane, 9.2% 1-chloro-1,2,2,2-tetrafluoroethane, and 3.5% 1,1-dichloro-2,2,2-trifluoroethane. At 300°C the product distribution is 38.3% 1-chloro-1,2,2,2-tetrafluoroethane, 25.4% pentafluoroethane, and 16.0% 1,1-dichloro-2,2,2-trifluoroethane. Example 20, column 15, shows that chlorotrifluoroethylene yields CF₃CHF₂ as the major product at 400°C. GB 1,000,485 describes a process for the preparation of organic fluorinated compounds by fluorination of halo-olefins in the gaseous phase and at a temperature preferably within the range of 200°C to 400°C. The catalyst consists essentially of partially fluorinated alumina impregnated with one or more polyvalent metal halides. The polyvalent metal may be chromium, cobalt, nickel or manganese. The total content of polyvalent metal halide, expressed as oxide, is not more than 15% by weight of the partially fluorinated (70-80%) alumina expressed as alumina. Example 4 (Table 4) shows that reaction of tetrachloroethylene with HF over such catalyst yields CF₃CHCl₂ as the major product at 220-290°C. In addition, the patent states that, if fluorination of the catalyst is excessive, the activity of the catalyst is impaired (page 3, column 2, lines 85-87). The references do not disclose how to favor the production of 1,1,1-trifluorodichloroethane over 1,1,1,2-tetrafluorochloroethane while maximizing the production of these two compounds taken together over the production of more highly fluorinated products. The process of the instant invention achieves the desired high degree of selectivity by minimizing the formation of the pentafluoroethane through catalyst selection and control of the reaction variables, as discussed below and illustrated in the Examples. What has been discovered is a process for the preparation of 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane by fluorination of a tetrahaloethylene, C₂Cl 4-x F x , wherein x = 0 to 3, and/or a pentahaloethane, C₂HCl 5-x F x , wherein x = 0 to 2, comprising contacting in the gaseous phase at effective temperature, mol ratio, and contact time, said tetrahaloethylene and/or pentahaloethane with HF and Cr₂O₃, said Cr₂O₃ prepared by pyrolysis of (NH₄)₂Cr₂O₇ and having a potassium content of 100 ppm or less, said contacting producing a product stream containing 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane and pentafluoroethane, wherein the amount of said 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane is greater than the amount of pentafluoroethane produced, and, thereafter, separating the 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane from the product stream. The tetrahaloethylene of this invention is defined by the formula C₂Cl 4-x F x , wherein x = 0 to 3, and includes CCl₂=CCl₂, CClF=CCl₂, CClF=CClF, CF₂=CCl₂, and CF₂=CClF and mixtures of these. The pentahaloethanes of this invention are defined by the formula C₂HCl 5-x F x , wherein x = 0 to 2, and includes CCl₃CHCl₂, CCl₂FCHCl₂, CCl₃CHClF, CClF₂CHCl₂, and CCl₂FCHClF and mixtures of these. The tetrahaloethylenes and pentahaloethanes of this invention are known to the art. The Cr₂O₃ catalyst of this invention is prepared by pyrolysis of ammonium dichromate. By pyrolysis is meant heating ammonium dichromate to a sufficient temperature and for a sufficient time to cause the following reaction to occur to substantial completion: (NH₄)₂Cr₂O₇----→Cr₂O₃ + 4 H₂O + N₂ For example, ammonium dichromate may be heated in a continuous kiln at 500-700°C, preferably 540-640°C, for 5-20 minutes so that it will undergo an internal oxidation-reduction reaction to produce mainly water, nitrogen and Cr₂O₃. After the water and nitrogen are driven off, the remaining fine powder of Cr₂O₃ may be cooled and compacted so as to increase its bulk density for ease of handling. For example, a bulk density of approximately 400-560 kg/m³ may be desirable, preferably 448-512 kg/m³. The Cr₂O₃ obtained may contain low levels of contaminants which are present as a result of the manufacturing process for the original (NH₄)₂Cr₂O₇. Although not totally destructive of catalyst efficacy, potassium as a contaminant has an adverse effect on the activity and life of the catalyst of this invention. It is necessary for potassium levels to be 100 ppm by weight or less. The level may be reduced by a water washing step. While the conditions are not critical, the water washing step can include forming a slurry containing 5-15% Cr₂O₃, preferably 10%, and deionized water. Stirring of this water slurry can be carried out at 35-65°C for at least one hour, preferably two or more hours. The solids are then recovered by filtration, suitably on a plate and frame filter press. The filter cake can be analyzed for potassium. If its level is 100 ppm by weight or less (dry basis), the solids are, thereafter, dried. If not, the washing step can be repeated to obtain a desired level of potassium. The form of the catalyst is not critical and may be used as pellets, powders or granules. For example, if the catalyst is desired to be in the pellet form, 5-15%, preferably 10%, of chromium acetate and 1-5%, preferably 2%, of graphite can be added to the dried solids as pelletization aids. The chromium acetate can be added in aqueous solution of 30-70%, preferably 50% concentration. The resultant paste can be mulled to mix the ingredients and then pelletized to the desired size, preferably 0.32 cm x 0.32 cm cylinders. The pellets can be dried at 80-120°C, preferably 105°C, for 8-48 hours, preferably 16-24 hours. The Cr₂O₃ pellets then have a bulk density of 1120-1440 kg/m³ for the preferred pellet size and a surface area of 40-57 m²/g, preferably 45-55 m²/g. Pore volume is 0.15-0.3 cc/g, the potassium content is 100 ppm or less. Generally, the resulting Cr₂O₃ will be pretreated with HF. It is thought that this converts some of the surface chrome oxide to chrome oxy-fluoride. This pretreatment can be accomplished by placing the Cr₂O₃ in a suitable container, which can be the reactor to be used to perform the reaction of the instant invention, and thereafter, passing HF over the pyrolyzed and dried Cr₂O₃ so as to partially saturate the Cr₂O₃ with HF. This is conveniently carried out by passing HF over the Cr₂O₃ for a period of time of, for example, 15 to 300 minutes at a temperature of, for example, 200°C to 450°C. The purpose of this pretreatment is to prevent damage to the catalyst due to possible high temperature excursions and resultant coking of the catalyst if the reactants, tetrahaloethylene and/or pentahaloethane, were contacted with the catalyst without first having conditioned some of the surface chrome oxide with HF. Nevertheless, this pretreatment is not essential; initial process conditions and equipment could be selected so as to avoid the problem of high temperature and coking of the catalyst. The contacting of the reactants with HF in the presence of the catalyst, preferably pretreated, of the instant invention is performed at effective temperature, mol ratio and contact time. By effective temperature, mol ratio and contact time is meant the temperatures, mol ratios, and contact times which produce a product stream which contains an amount of 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane which is greater than the amount of pentafluoroethane produced. The temperature is 225°C to 400°C, preferably 225°C to 250°C, with a contact time, of 0.1 to 100 seconds, preferably 10 to 90 seconds, and most preferably 15 to 90 seconds. The molar ratio of HF to the reactants is from 1/1 to 20/1, preferably 3/1 to 10/1, and most preferably, 4/1 to 6/1. In general, the higher the temperature, the greater the HF/reactant mol ratio, and the longer the contact time, the greater is the conversion of the reactants to fluorinated products and the greater is the degree of fluorination of the raw material. The above variables can be balanced, one against the other, so that formation of CF₃CHCl₂ is favored over CF₃CHClF, and the production of these two compounds taken together is maximized and that of more highly fluorinated products minimized. A key feature of the invention is that through catalyst selection and process control, as described herein, the desired tri- and tetrafluoro products can be obtained as the major products at high reactant conversions, normally greater than 30%. Preferably, the reaction variables are controlled so as to keep the production of the pentafluoro product below 10 area percent, as determined gas chromatographically, of the products produced. Thus, as illustrated in the Examples with tetrachloroethylene, the tri- and tetrafluoro products are obtained in very high yields while the production of higher fluorinated products is minimized, even at high conversions of tetrachloroethylene. Intermediates formed during the course of the reaction, such as CHClFCClF₂ , CHCl₂CClF₂, CClF=CCl₂ and CHCl₂CCl₂F can be recycled to the reactor for the production of additional CF₃CHCl₂ and CF₃CHClF. In addition, CF₃CHCl₂ can be recycled to the reactor for the production of additional CF₃CHClF when this is desired. The reaction of the reactants with HF may be conducted in any suitable reactor, including fixed and fluidized bed reactors. The reaction vessel should be constructed from materials which are resistant to the corrosive effects of hydrogen fluoride such as Hastelloy" (reg. trademark) and "Inconel" (reg. trademark). The pentachloroethane may be fed directly to the reactor or may be prepared in-situ in the reactor by contemporaneously feeding trichloroethylene, chlorine and HF to the reactor containing the catalyst of this invention. Pressure is not critical. Atmospheric and superatmospheric pressures are the most convenient and are therefore preferred. The fluorinated alkanes produced by the instant invention have utility as blowing agents, propellants and refrigerants. They can also be used as starting materials for the preparation of other useful compounds. For example, CF₃CHClF can be used to prepare 1,1,1,2-tetrafluoroethane. EXAMPLES In the following illustrative Examples all parts and percentages ore by weight and all temperatures are Centigrade unless otherwise stated. All reactions used commercial HF containing only trace amounts of water. The pyrolyzed Cr₂O₃ catalyst used in the following Examples was prepared using ammonium dichromate having the following specifications: (NH₄)₂Cr₂O₇ 99.5% Insolubles less than 0.2% Iron less than 100 ppm Chloride less than 100 ppm Sulfate less than 500 ppm Alkali less than 2000 ppm pH (8 wt % aqueous sol) 3.2-4.0 The preparation, drying and compacting of the Cr₂O₃ used in the following Examples were performed according to the following procedure: A rotating continuous kiln, 0.457 m (18 inches) in diameter and 5.18 m (17 feet) long, was electrically heated to 570-620°C. At this point the heater was turned off and ammonium dichromate was fed into the kiln at a feed rate of 127 kg/hr (280 lb/hr) (residence time = 8 minutes). The conversion of ammonium dichromate to Cr₂O₃ was essentially quantitative. The heat generated from the internal oxidation-reduction reaction to produce water, nitrogen and Cr₂O₃ was sufficient to maintain the desired reaction temperature. After the water and nitrogen were driven off, the remaining fine powder of Cr₂O₃ was cooled and compacted to a bulk density of approximately 448-512 kg/cubic meter. Procedure for Pretreatment The reactor (0.0127 m (0.5 inch) ID, 0.3 m (12 inch) long "Inconel" pipe) was charged with the amount of catalyst as described in the following Examples and placed in a sand bath. The bath was gradually heated to 400° while nitrogen gas at a flow rate of 50 ml/minute was passed through the reactor to remove traces of water. The temperature was lowered to 200°, and HF and nitrogen gas (1:4 molar ratio) were passed through the reactor. The nitrogen flow was decreased with time until neat HF was being passed through the reactor. At this point, the temperature was gradually raised to 450° and maintained there for 15 to 300 minutes. Procedure for Fluorination The temperature was then decreased, while maintaining the HF flow, to the indicated values and, thereafter, CCl₂=CCl₂ flow was started. The flows of HF and CCl₂=CCl₂ were adjusted to give the indicated molar ratios and contact times. The reactor effluent was scrubbed with aqueous potassium hydroxide to remove HCl and HF, and sampled on-line with a gas chromatograph using a 6.1 m (20 foot) long 3.175 mm (one-eighth inch) diameter column containing "Krytox" (reg. trademark) perfluorinated polyether on an inert support and a helium carrier gas flow of 35 cc/minute. EXAMPLES 1-7 The Procedures for Pretreatment and Fluorination were followed using 38.1 g (30 cc) of Cr₂O₃ with a potassium content of 60 ppm as the initial catalyst charge in the form of crushed pellets 0.37 - 0.175 mm = 40 - 80 mesh). The results are given in the Table.

Claims: A process for the preparation of 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane by fluorination of a tetrahaloethylene, C₂Cl 4-x F x , wherein x = 0 to 3, and/or pentahaloethane, C₂HCl 5-x F x , wherein x = 0 to 2, comprising contacting in the gaseous phase at temperature of 225° to 400°C., mol ratio of 1/1 to 20/1 of HF to the reactants and contact time of 0.1 to 100 seconds, said tetrahaloethylene and/or pentahaloethane with HF and Cr₂O₃, said Cr₂O₃ prepared by pyrolysis of (NH₄)₂Cr₂O₇, and having a potassium content of 100 ppm or less, said contacting producing a product stream containing 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane and pentafluoroethane, wherein the amount of said 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane produced is greater than the amount of pentafluoroethane produced and, thereafter, separating the 1,1,1-trifluorodichloroethane and/or 1,1,1,2-tetrafluorochloroethane from the product stream. The process of claim 1 wherein the tetrahaloethylene is tetrachloroethylene. The process of claim 1 wherein the HF is contacted with the tetrahaloethylene and/or pentahaloethane at a mol ratio of 3/1 to 10/1, at a temperature of 225°C to 250°C., and a contact time of 10 seconds to 90 seconds. The process of claim 3 wherein the HF is contacted with the tetrahaloethylene and/or pentahaloethane at a mol ratio of 4/1 to 6/1, at a temperature of 225°C. to 250°C., and a contact time of 15 seconds to 90 seconds. The process of claim 1 wherein conversion of the tetrahaloethylene and/or pentahaloethane to fluorinated products is between 30% and 100%. The process of claim 1 wherein the amount of pentafluoroethane in the product stream is less than 10 area percent by gas chromatography. The process of claim 1 further comprising the step of recycling at least a portion of starting materials and underfluorinated products. The process of claim 1 wherein before the contacting step, the Cr₂O₃ is given a pretreatment by passing hydrogen fluoride gas over it. The process of claim 8 wherein the pretreatment is carried out for 15 to 300 minutes at 200°C. to 450°C.

Inventors: GUMPRECHT WILLIAM HENRY, MANZER LEO ERNEST, RAO VELLIYUR NOTT MALLIKARJUNA, GUMPRECHT, WILLIAM HENRY, MANZER, LEO ERNEST, RAO, VELLIYUR NOTT MALLIKARJUNA
Applicants: DU PONT, E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1988
Main classification: C07C19
IPC codes: C07B61, C07C67, C07C19, B01J23, C07C17