PROCESS FOR ISOMERIZING 1,1,2-TRICHLOROTRIFLUOROETHANE

Abstract: A process is disclosed for producing CCl3CF3 by catalytic isomerization. The process comprises (1) activating a micropulverized anhydrous aluminum trichloride which has a surface area of greater than 0.8 m2/g by treating it with at least about 10 g per g of aluminum trichloride of CCl2FCClF2 with agitation; and (2) isomerizing an additional amount of CCl2FCClF2 by (i) mixing said additional amount of CCl2FCClF2 with said activated catalyst with agitation to provide an initial degree of isomerization, and (ii) cooling the mixture of chlorofluorocarbons and catalyst to a temperature of about 20 C with agitation, to provide a product containing CCl3CF3 and less than about 400 ppm of CCl2FCClF2.

Description: TITLE PROCESS FOR ISOMERIZING 1,1,2-TRICHLOROTRIFLUOROETHANE FIELD OF THE INVENTION This invention relates to processes using activated aluminum trichloride catalysts and more particularly to chlorofluorocarbon isomerizations in the presence of such catalysts. BACKGROUND OF THE INVENTION Chlorofluorocarbons have been widely used as refrigerants and aerosols. Concerns have developed over the release of various chlorofluorocarbons into the atmosphere. Efforts have already begun to eliminate any widespread emission of CCI2F 2 (CFC-12) and CCI 3 F (CFC-11) due to their ability to reach the stratosphere intact. In recent years, increased attention has focused on use of perfluorocarbons, hydrofluorocarbons and hydrochloro- fluorocarbons which are considered to have significantly lower potential for contributing to ozone depletion. Of particular interest to the refrigerant industry is the hydrofluorocarbon 1,1,1,2-tetrafluoroethane (HFC-134a) . HFC-134a can be derived from the intermediates 1,1,1- trichlorotrifluoroethane (CFC-113a) and 1,1,1,2-tetra- fluorodichloroethane CFC-114a) . These intermediates are, in turn, t e iso ers of the readily available and chemically more symmetric chlorofluoroethanes, 1,1,2- trichlorotrifluoroethane (CFC-113) and 1,1,2,2-tetra- fluorodichloroethane (CFC-114) , respectively. The isomerization of these more symmetric chlorofluoroethanes by treatment with aluminum trichloride is well documented in the art. For example, U.S. Pat. No. 4,925,993 discloses a process for isomerizing CFC-112 (i.e., CCI 2 FCCI 2 F) to CFC-112a ( i.e., CCI3CCIF2) or CFC-113 to CFC-113a by contacting the CFC-112 or CFC-113 with an activated aluminum trichloride catalyst. The catalyst is prepared by contacting the chlorofluorocarbon with anhydrous aluminum trichloride in the presence of selected metals. Reportedly, the amount of non-isomerized chlorofluoro- ethane in the product mixture can be held to less than 450 ppm, and the catalyst can be used for eighteen cycles. High purity CFC-113a is an advantageous starting material for the preparation of high purity 1,1,1,2- tetrafluoroethane (HFC-134a) . More particularly, CFC-113a may be reacted with HF to afford CFC-114a which in turn may be hydrodechlorinated to HFC-134a. Unless an isomer separation process is employed, the presence of substantial amounts CFC-113 in the starting material •would eventually lead to the production of a HFC-134a product containing significant amounts of 1,1,2,2- tetrafluoroethane (HFC-134) . It has been found that for many applications, the presence of significant amounts of HFC-134 in an HFC-134a product can alter the physical and chemical properties of the product. Thus, there is interest in developing more efficient isomerization methods for obtaining CFC-113a products with negligible amounts (i.e., less than about 500 ppm) of non- isomerized starting material. SUMMARY OF THE INVENTION The invention provides an isomerization process for producing a desirable chlorofluoroethane intermediate of 1,1, 1,2-tetrafluoroethane. The process comprises (1) activating a micropulverized anhydrous aluminum trichloride which has a surface area of greater than about 0.8 m 2 /g by treating it with at least about 10 g per g of aluminum trichloride of CCI 2 FCCIF 2 with agitation; and (2) isomerizing an additional amount of CCI2FCCIF 2 by (i) mixing said additional amount of CCI 2 FCCIF 2 with said activated catalyst with agitation to provide an initial degree of isomerization, and (ii) cooling the mixture of chlorofluorocarbons and catalyst to a temperature of about 20°C with agitation, to provide a product containing CCI 3 CF 3 . The amount of non-isomerized CCI 2 FCCIF 2 in the product is generally less than about 400 ppm. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a plot of non-isomerized CFC-113 in CFC-113a product as a function of isomerization cycle for catalyst prepared from AICI 3 having a surface area of about 0.27 m 2 /g. Figure 2 is a plot of non-isomerized CFC-113 in CFC-113a product as a function of isomerization cycle for catalyst prepared from AICI 3 having a surface area of about 0.39 m 2 /g. Figure 3 is a plot of non-isomerized CFC-113 in CFC-113a product as a function of isomerization cycle for catalyst prepared from AICI 3 having a surface area of about 0.85 m 2 /g. Figure 4 is a plot of non-isomerized CFC-113 in CFC-113a product as a function of isomerization cycle for catalyst prepared from micropulverized AICI 3 having a surface area of about 0.95 m 2 /g. DETAILED DESCRIPTION This invention provides catalytic isomerization of CCI2FCCIF2 starting materials. The process uses advantageous activated AICI 3 catalysts. The isomerization catalyst may be activated in situ (i.e., in the same reactor used for isomerization) by treating micropulverized anhydrous aluminum trichloride with CCI2FCCIF2. Agitation (e.g., stirring) should be provided during treatment. Micropulverization involves mechanical comminution and may be practiced using a conventional operation such as crushing, ball milling. rod milling or grinding. Typically, the micropulverized anhydrous aluminum trichloride has the following properties: a particle size such that greater than 80% of the material passes through a 100 mesh screen (sieve opening of 0.149 mm); less than 30 ppm iron; less than 0.3% non-volatile material; less than 25 ppm free aluminum; less than 200 ppm water insolubles; and an aluminum chloride purity of greater than 99.6%. In any case, after micropulverization the AICI 3 should have a surface area greater than about 0.8 m 2 /g (as measured by the well known single-point BET method using nitrogen, for example, a gas mixture of 30% nitrogen and 70% helium) . Preferably, the AICI 3 is sufficiently micropulverized to provide a first order rate constant, after activation, of at least 0.10 minute -1 at boiling •under reflux conditions. The weight ratio of chloro- fluorocarbon used during activation to micropulverized anhydrous aluminum trichloride is typically from about 10:1 to about 300:1, is preferably from about 20:1 to 70:1, and is most preferably about 50:1. The aluminum trichloride is preferably activated at a temperature within the range of from about 7°C to about 52°C when CFC-113 is used. For example, a mixture of micropulverized AICI 3 and CCI 2 FCCIF 2 may be heated to boil under reflux (about 48°C) for four hours with stirring. Overheating due to rapid reaction of CFC-113 can be controlled during activation by using CFC-113a (e.g., a ratio of CFC-113a to CFC-113 of about 1.5:1) as a heat sink and diluent to limit the reaction rate. The mixture may then be cooled with stirring to 20°C, at which point the stirring is stopped. After the catalyst has settled to the bottom of the reaction vessel, the supernatant liquid may be decanted from the reaction vessel. A small amount of chlorofluorocarbons (typically between about 10 to about 20 weight percent) is generally retained as a slurry with the activated catalyst. The activated aluminum trihalide derivative is contacted with additional CCI 2 FCCIF 2 for isomerization. Typically, stirring is employed during catalyst contact. A catalyst slurry containing the activated catalyst may be transferred to a new reaction vessel for the isomerization, or the additional CCI 2 FCCIF2 to be isomerized may be added directly to the vessel containing the freshly activated catalyst. The reaction vessel(s) used for catalyst activation and isomerization may be any chemically resistant material such as glass (e.g., glass-lined reactors) or carbon steel. Reactor materials which leach contaminants such as undesirable metals into the • reaction mixture are preferably avoided. To achieve a desirable reaction rate, the isomerization is initially conducted with stirring at a temperature of at least about 47°C. Preferably, the initial temperature is from about 47°C to 52°C (i.e., at or near the boiling temperature for CCI 2 FCCIF 2 ) . After achieving an initial degree of isomerization, the reaction mixture is cooled to about 20°C, and the isomerization is terminated when the amount of CCI2FCCIF2 in the reaction vessel is less than 400 ppm, preferably, especially for commercial production, about 350 ppm or less (e.g., about 320 ppm). The catalyst activity, the reaction temperature and the catalyst concentration are preferably controlled so that the desired degree of isomerization is acheived in from about 0.25 to about 4 hours, most preferably about 0.5 hours. After isomerization, the stirring is stopped, and the catalyst is separated from the product mixture (e.g., by allowing the catalyst to settle to the bottom of the reactor and drawing off or decanting the liquid product) . Separation of the isomerization products from other compounds in the organic phase (e.g., disproportionation products and other reaction byproducts) then proceeds by techniques well known to those skilled in the art, such as distillation. Usually 10 to 20 weight percent of the product mixture is retained as a slurry with the catalyst. The catalyst may be reused until its activity becomes undesirably low. The catalyst may be reused by adding to the slurried catalyst an amount of fresh chlorofluorocarbon approximately equal in weight to the product mixture removed. The weight ratio of chlorofluorocarbon to the original aluminum trichloride catalyst used in each batch is typically between about •30:1 to about 70:1. Separation of the products from the organic phase can be done collectively using a pool of organic phases recovered from a series of isomerizations, or singularly upon the removal of product mixture from the settled catalyst. Catalyst life can be as important commercially as the rate of the reaction. Surprisingly, the lifetime of catalysts, as indicated by the number of batch runs that a catalyst can be used to produce product within specification (e.g., less than about 400 ppm CFC-113 at 20°C) , increases with the surf ce area of the micro¬ pulverized catalyst precursor. Typically, the catalyst of this invention can be used to isomerize at least about 500 kg of CFC-113 per kg of AICI 3 . The isomerization rate prior to cooling (e.g., prior to cooling from an initial isomerization temperature of about 47°C or more) is typically at least about 10 kg of CFC-113 per kg of AICI 3 per hour. When used during isomerization in a weight ratio up to about 50 g CFC-113 per g AICI 3 (e.g., 20 to 40 g CFC-113/g AICI 3 ) the catalyst is preferably used for at least about 30 isomerization cycles (i.e., isomerization of 30 batches of fresh CCI 2 FCCIF 2 ) ; most preferably, especially for commercial production, at least about 70 isomerization cycles (e.g., about 140 cycles, or even more) . Preferably, the catalyst is used to isomerize at least about 1000 kg CCI 2 FCCIF2 per kg of AICI3, most preferably, especially for commercial production, at least about 4000 kg CCI 2 FCCIF 2 per kg AICI 3 (e.g., about 5000 kg CCI 2 FCCIF 2 per kg AICI 3 , or more) . Preferably, the isomerization rate of CCI 2 FCCIF 2 prior to cooling is at least about 25 kg of said chlorofluorocarbon per kg AICI 3 per hour. The isomerization normally proceeds at atmospheric pressure. However, since the autocatalytic reaction between anhydrous aluminum trichloride and certain chlorofluorocarbons, such as CCI 2 FCCIF 2 , can be highly exothermic and can present thermal control problems, especially at high temperatures under adiabatic conditions, the process may be performed in a suitable pressure vessel. Adequate heat removal to prevent overheating of the catalyst is desirable to achieve the most active, long-lived catalyst. The product produced by isomerization of CCI2FCCIF 2 starting material is a high purity composition of CCI 3 CF 3 (i.e., the product produced consists essentially of CCI 3 CF 3 containing less than about 400 ppm CCI2FCCIF2) . Practice of the invention is further illustrated by the following non-limiting examples. Reaction Rate Study CCI 2 FCCIF 2 (CFC-113) Isomerization A. Catalyst Activation A 250 mil Erlenmeyer flask was equipped with a hot plate/stirrer. Teflon® (polytetrafluoroethylene) stirring bar. Teflon® sleeves, an inlet port capped with a Teflon®-coated septum, a condenser with a nitrogen inlet tube and a 250 mL addition funnel fitted with a Teflon® stopcock and connected to a Krytox® (perfluorinated polyether) oil bubbler. All the glassware was oven-dried prior to use. The Erlenmeyer flask was flushed with dry nitrogen and capped with a glass stopper. The flask was charged with AICI 3 (1.0 g) in a nitrogen-blanketed dry box. The flask was capped with a glass stopper, removed from the dry box and quickly attached to the reflux condenser purged with N 2 , and the addition funnel. A thin wire (1/32", 0.79 mm) thermocouple was inserted through the septum so that it was located in the vapor space of the reaction (in some experiments, a thermocouple was inserted in a thermowell) . A continuous and generous 2 purge was maintained through the nitrogen inlet. Water maintained at 10°C in a low temperature bath was circulated through the condenser. The addition funnel was charged with 270 g (about 170 mL) of high-purity CFC-113. The stirring rate was set at 500 rpm, and the N 2 purge reduced to a slow bubbling rate exiting the system. After the addition (10 20 minutes), the heating was set at 85°C, and the time and temperature noted. The mixture was heated to boil under reflux (time is variable depending on the activity of the catalyst) . The vapor was sampled through the septum when the reflux was a steady stream coming off the condenser tip. This was noted as the starting point of the activation. The reaction was sampled at appropriate intervals to yield a conversion curve; for each point the time was recorded to the nearest tenth of a minute. The reaction was shut down when the reaction composition did not change significantly as determined by vapor-phase GC analyses. B. Isomerization Procedure Most of the liquid was removed from the reactor with an 18 gauge needle and a 50 mL syringe, an additional change of 270 g CFC-113 was added to the reactor, and the above process was repeated. C. Reaction Rate The activation and isomerization reactions described above were carried out using a series of AICI3 samples including both standard, commercially available AICI 3 and micropulverized AICI 3 . All the •micropulverized AICI 3 samples possessed a particle size such that 80% of the material passed through 100 mesh screen (sieve opening of 0.149 mm) . Surface areas for each of the AICI 3 samples were measured using the standard BET nitrogen sorption method by degassing about one gram (g) of the sample at room temperature using helium flow in a Micromeritics Desorb 2300B system, measuring adsorption and desorption on a Micromeritics Flowsorb II 2300 system with a mixed gas of 30% nitrogen and 70% helium, and calculating the surface area. The first-order rate constant for the conversion of CC1 2 FCC1F 2 (CFC-113) to CCI 3 CF 3 (CFC-113a) was measured for the first isomerization for each sample, and the results are shown in Table 1. The data show that the rates of isomerization are faster for catalyst precursors with higher surface areas. Moreover, the micropulverized AICI 3 , always performed better (i.e., faster) than standard AICI 3 . Surface Area (m 2 /g) prior to activation 0.24 0.26 0.32 0.35 0.39 0.66 0, 68 0, 83 0, 83 0, 91 0, 98 1, 05 1, 06 1, 08 Catalyst Life Study CCI 2 FCCIF 2 (CFC-113) Isomerization A. Catalyst Act . a ion The modified Erlenmeyer flask described above was flushed (septum attached) with dry nitrogen. While flushing, it was quickly stoppered and placed in a dry box with a glass vial, a wide-bore glass funnel and a scoupula. A small amount of AICI 3 was placed in the vial to coat the internal walls. Some AICI 3 was also used to coat the walls of the funnel. AICI 3 was weighed in the coated glass- vial, and then about 5.4 g was transferred to the reaction flask through the funnel. The flask was quickly stoppered and removed from the dry box. While the equipment was swept with 2 at a moderate rate, the flask was quickly unstoppered and attached to the bottom of the condenser described above. The N2 flow was then reduced to a slow rate. CFC-113 (about 270 g CCI 2 FCCIF 2 ) was added to the addition funnel. The condenser cooling water was started at a medium-high rate, and the magnetic stirrer was turned on at 300 rpm; without turning on the hot plate. The CCI 2 FCCIF2 was added over about 10 minutes with stirring. There was no significant exotherm for this catalyst activation procedure. After addition, the mixture was heated to boil under reflux at 8-52°C with continued stirring. The mixture was stirred at gentle boil for 4 hours, and then allowed to cool while stirring to 25°C, at which point the stirring was stopped. B. Isomerizatign Procedure After the catalyst settled in the flask, the clear organic liquid was withdrawn with a hypodermic needle using a vacuum flask. The addition funnel was refilled with another portion of CCI2FCCIF2. The stirrer was turned on at 300 rpm, and the CCI2FCCIF 2 was added at a moderately fast rate, taking about 10 to 15 minutes. The mixture normally reached the boiling point during the addition. After the addition was complete, the mixture was allowed to cool to 20°C while stirring. The stirring was stopped, and the catalyst allowed to settle until the organic liquid was clear. An aliquot of organic liquid was analyzed by gas chromatography. c. Catalyst Life Three different samples of non-micropulverized aluminum chloride (surface areas of 0.27, 0.39 and 0.85 m /g, respectively) and one sample of micro¬ pulverized aluminum chloride (surface area of 0.95 m 2 /gm) were each employed for a series of consecutive isomerization cycles, and the concentration of CFC-113 (ppm) in the CFC-113a product was monitored. The concentration of CFC-113 in the product is shown as a function of the number of cycles, C, in Figures 1 through 4 for each of the respective samples. The surface area for each AICI3 sample was measured using the standard BET nitrogen sorption method described in Example 1 above. Examples 1 and 2 clearly show that catalysts of this invention are not only highly active (as shown by the rate of isomerization) , but also produce high quality product through numerous batch runs. The examples serve to illustrate particular embodiments of the invention. Other embodiments will become apparent to those skilled in the art from a consideration of the specification or practice of the invention disclosed herein. It is understood that modifications and variations may be practiced- without departing from the spirit and scope of the novel concepts of this invention. It is further understood that the invention is not confined to the particular formulations and examples herein illustrated, but it embraces such modified form thereof as come within the scope of the following claims.

Claims: What is claimed is: 1. A process for producing compounds of the formula CCI3CF3 comprising: (1) activating a micropulverized anhydrous aluminum trichloride which has a surface area of greater than about 0.8 m 2 /g by treating it with at least about 10 g per g of aluminum trichloride of CCI 2 FCCIF2 with agitation; and (2) isomerizing an additional amount of CCI2FCCIF2 by (i) mixing said additional amount of CCI2FCCIF2 with said activated catalyst with agitation to provide an initial degree of isomerization, and (ii) cooling the mixture of chlorofluorocarbons and catalyst to a temperature of about 20°C with agitation, to provide a product containing CCI3CF3 and less than about 400 ppm of CCI2FCCIF2. 2. The process of Claim 1 wherein the reactor used for activation is glass or carbon steel; and wherein the reactor used for isomerization is glass or carbon steel. 3. The process of Claim 1 wherein the isomerization catalyst is activated in the same reactor used for isomerization. 4. The process of Claim 3 wherein the reactor is a glass reactor. 5. The process of Claim 3 wherein the reactor is a carbon steel reactor. 6. The process of Claim 1 wherein the isomerization is initially conducted at a temperature of at least about 47°C and the isomerization rate prior to cooling is at least about 10 kg of CCI2FCCIF2 per kg of AICI3 per hour. 7. The process of Claim 1 wherein at least about 500 kg of CCI 2 FCCIF 2 is isomerized per kg of AICI 3 . 8. The process of Claim 1 wherein the catalyst is used during isomerization of CCI 2 FCCIF 2 in a weight ratio up to abut 50 g CCI 2 FCCIF 2 per g AICI 3 , and wherein the catalyst is used for at least about 30 isomerization cycles. 9. The process of Claim 1 wherein the AICI 3 is sufficiently micropulverized to provide a first order rate constant, after activation, of at least 0.10 minutes" 1 at boiling under reflux conditions. 10. The process of any one of Claim 1 through 9 wherein at least about 1000 kg CCI2FCCIF2 is isomerized per kg of AICI 3 .

Inventors: GUMPRECHT WILLIAM HENRY, HUEBNER WILLIAM JOEL, NAPPA MARIO JOSEPH, GUMPRECHT, WILLIAM, HENRY, HUEBNER, WILLIAM, JOEL, NAPPA, MARIO, JOSEPH
Applicants: DU PONT, E.I. DU PONT DE NEMOURS AND COMPANY
Application year: 1993
Main classification: C07C17
IPC codes: B01J27, C07B61, C07C17, C07C19