| BE685511A | 1967-02-01 | |||
| US3754043A | 1973-08-21 |
| 1. | A process for enriching the amount of CCIF2CCIF2 relative to the amount of CCI2FCF3 from an initial mixture containing CCIF2CCIF2 and CCI2FCF3 comprising the steps of: contacting said initial mixture with hydrogen chloride in the vapor phase at an elevated temperature in the presence of a catalyst to produce a product mixture containing C2CI2F3 and chlorination products of CCI2FCF3 wherein the weight ratio of CCIF2CCIF2 to the total C2CI2F4 is higher than the weight ratio of CCIF2CCIF2 to the total C2CI2F4 in the initial mixture; and separating chlorinated products of CCI2FCF3 in the product mixture from the C2CI2F4 therein. |
| 2. | The process of Claim 1 wherein the catalyst is selected from the group consisting of alumina, fluorided alumina, aluminum fluoride, metals supported on alumina, metals supported on aluminum fluoride, magnesium fluoride supported on aluminum fluoride, metals supported on fluorided alumina, alumina on carbon, aluminum fluoride on carbon, fluorided alumina on carbon, metals supported on carbon, chromium catalysts, mixtures including metal halides with aluminum fluoride and graphite, and chromiummagnesium optionally supported on graphite; said metals being selected from the group consisting of chromium. Group VIII metals. Group VIIB metals. Group IIIB metals, and zinc. |
| 3. | The process of Claim 2 wherein the catalyst comprises aluminum fluoride. |
| 4. | The process of Claim 2 wherein the initial mixture is contacted with HCl at a temperature from about 200°C to 325°C, and wherein the molar ratio of HCl to C2CI2F4 in the initial mixture is from about 2:1 to 100:1. |
| 5. | The process of Claim 2 wherein the CCI2FCF3 content of the initial mixture is equal to or greater than the CCIF2CCIF2 content. |
| 6. | The process of Claim 5 wherein the fraction of total C2CI2F4 which is CCI2FCF3 is reduced by at least about 25%. |
| 7. | The process of Claim 1, Claim 2, or Claim 6 wherein the initial mixture consists essentially of CCI2FCF3 and CC1F2CC1F2. |
| 8. | The process of Claim 1, Claim 2, or Claim 6 wherein the CCIF2CCIF2 in the product mixture is at least 95% of the total C2CI2F4 content. |
| 9. | The process of Claim 1, Claim 2, or Claim 6 wherein CCI3CF3 is the major chlorination product of CCI2FCF3. |
| 10. | The process of Claim 9 wherein CCI3CF3 is separated from the C2CI2F4 in the product mixture by distillation. |
PROCESS FOR ENRICHING
1,2-DICHLORO-l,1,2,2-TETRAFLUOROETHANE
FROM A MIXTURE OF DICHLOROTETRAFLUOROETHANE ISOMERS FIELD OF THE INVENTION
This invention relates to halocarbon isomer enrichment, and more particularly, to a process for enriching compositions containing CCIF 2 CCIF 2 (i.e., CFC-114) relative to their CCI 2 FCF 3 (i.e., CFC-114a) content.
BACKGROUND Products containing isomers of C 2 CI 2 F 4 are produced in various degrees of isomer purity. For example, C 2 CI 2 F 4 can be produced by the chlorofluorination of perchloroethylene, and the product typically consists of a mixture of the isomers, CCIF 2 CCIF 2 and CCI 2 FCF 3 (see e.g., U.S. Patent No. 4,605,798). If the C 2 CI 2 F 4 isomer mixture is then used to produce CHCIFCF 3 (HCFC-124) , CHF2CCIF 2 (HCFC-124a), CHF 2 CHF 2 (HFC-134) and/or CH2FCF3 (HFC-134a) by hydrodehalogenation, the products often consist of a mixture of C 2 HCIF 4 isomers and C 2 H 2 F 4 isomers. GB 1,578,933 illustrates that mixtures of C 2 CI 2 F 4 isomers in ratios of CFC-114 to CFC-114a of about 28:1 to 1:1 can be hydrogenolyzed over a palladium on carbon catalyst to mixtures of C 2 H 2 F isomers in ratios of HFC-134 to HFC-134a of from less than 0.01:1 to about 4:1, depending on reaction conditions. Over a palladium on alumina catalyst mixtures having CFC-114 to CFC-114a ratios of about 3:1 to 1:1 are essentially completely hydrogenolyzed to HFC-134a. PCT
International Application No. 9218446 discloses that mixtures of C 2 CI 2 F 4 isomers can be converted to mixtures of C 2 H 2 F isomers with the product containing essentially the same distribution of fluorine atoms as the starting materials.
C 2 HCIF 4 isomers and C 2 H 2 F 4 isomers are used as refrigeration fluids for a number of applications.
C2HCIF 4 isomers, like C 2 CI2 4 isomers, are also valuable raw material feeds for a number of other commercial processes. It has been found that for many of these applications, the presence of the unwanted isomer of an isomer pair can alter the physical properties of the desired product. As a result, there have been continually increasing market and process demands for high isomer purity materials. Identification of methods for enriching a composition's content of one isomer over another represents a significant aspect of preparing products for specific applications.
Purification of fluorocarbon products has been the subject of considerable research. Of particular interest are the challenges presented in separating fluorocarbon products from materials such as impurities in the starting materials used to produce the fluorocarbon products; and in separating excess reactants, and reaction co-products and by-products which are difficult to remove by standard separation methods such as distillation. Enrichment of CFC-114 in the presence of its isomer, CFC-114a, by distillation is not considered practical since their boiling points are close; the boiling point of CFC-114 is 3.6°C, and the boiling point of CFC-114a is 3.3°C.
SUMMARY OF THE INVENTION
This invention provides a process for enriching the amount of 1,2-dichloro-l, 1,2,2-tetrafluoroethane relative to the amount its isomer, 1, 1-dichloro-l, 2,2,2- tetrafluoroethane, from an initial mixture containing them. The process comprises contacting the initial mixture with hydrogen chloride in the vapor phase at an elevated temperature in the presence of a catalyst to produce a product mixture containing dichlorotetra-
fluoroethane (C 2 CI 2 F 4 ) and chlorination products of
CCI 2 FCF 3 wherein the weight ratio of CCIF 2 CCIF 2 to the total C 2 CI 2 F 4 is higher than the weight ratio of
CCIF 2 CCIF 2 to the total C 2 CI 2 F 4 in the initial mixture. The chlorination products of CCI 2 FCF 3 in the product mixture may then be separated from the C 2 CI 2 F 4 therein
(e.g., by distillation).
DETAILED DESCRIPTION
The present invention involves selectively reacting 1,l-dichloro-l,2,2,2-tetrafluoroethane (CCI 2 FCF 3 ) with
HCl in the presence of its isomer, 1,2-dichloro-l,1,2,2- tetrafluoroethane (CCIF 2 CCIF 2 ) in the vapor phase in the presence of a catalyst. The process is especially useful for enriching CCIF 2 CCIF 2 from initial mixtures wherein the CCI 2 FCF 3 content is equal to or greater than the CCIF 2 CCIF 2 content. Preferably, the fraction of total C 2 CI 2 F 4 which is CCI 2 FCF 3 is reduced by at least about 25%. The initial mixture may consist essentially of C 2 CI 2 F 4 isomers, or may contain other compounds which do not interfere with the selective reaction of
CCI 2 FCF 3 . Typically, the reaction is controlled to provide CCI 3 CF 3 as the major chlorination product of CCI 2 FCF 3 .
Oxygen may be present in some process embodiments. However, the mole ratio of oxygen to total C 2 CI 2 F 4 during the contacting step is generally less than 1:1. Indeed, oxygen may be absent. Where oxygen is added, it may be fed to the reactor as such, or it may be diluted with an inert gas such as nitrogen, helium or argon. The source of the oxygen may also be air containing molecular oxygen. Chlorine may be present in some process embodiments, either as an initial reactant or as an in-situ formed product.
Suitable catalysts which can be used for selectively reacting CFC-114a with HCl in the presence
of CFC-114 include vapor phase fluorination catalysts.
Catalysts which may be used in accordance with this invention include alumina; fluorided alumina; aluminum fluoride; metals supported on alumina; metals supported on aluminum fluoride; magnesium fluoride supported on aluminum fluoride; metals supported on fluorided alumina; alumina on carbon; aluminum fluoride on carbon; fluorided alumina on carbon; metals supported on carbon; chromium catalysts; mixtures of metal halides, aluminum fluoride, and graphite; and chromium-magnesium optionally supported on graphite. Suitable metals include chromium. Group VIII metals (e.g., iron, cobalt and/or nickel). Group VIIB metals (e.g., manganese). Group IIIB metals (e.g., lanthanum), and zinc. Preferably, when used on a support, the total metal content of the catalyst will be from about 0.1 to 20 percent by weight; typically from about 0.1 to 10 percent by weight . Preferred supports include aluminum fluoride, fluorided alumina, and mixtures thereof. Fluorided alumina and aluminum fluoride can be prepared as described in U.S. Pat. No. 4,902,838. Metals on aluminum fluoride and metals on fluorided alumina can be prepared by procedures described in U.S. Pat. No. 4,766,260. Catalysts comprising chromium are well known in the art, e.g. see U.S. Pat. No. 5,036,036. Chromium supported on alumina can be prepared as described in U.S. Pat. No. 3,541,165. Chromium supported on carbon can be prepared as described in U.S. Pat. No. 3,632,834. Catalysts comprising chromium and magnesium may be prepared as described in Canadian Pat. No. 2,025,145. Other metals and magnesium optionally on graphite can be prepared in a similar manner to the latter patent. Preferred catalysts include catalysts comprising aluminum fluoride.
The reaction of mixtures of CCIF 2 CCIF 2 and CCI 2 FCF3 with HCl in the presence of the catalysts of the instant invention is normally conducted at about 200°C to 325°C, preferably about 200°C to 275°C, with a contact time of about 1 to about 120 seconds, preferably about 5 to about 60 seconds.
The amount of HCl should be at least a stoichiometric amount. Typically, the molar ratio of
HCl to the C 2 CI 2 F 4 isomer mixtures is within the range of from about 2:1 to about 100:1, and is preferably from about 3:1 to 50:1, and more preferably from about 5:1 to 20:1.
In general, with a given catalyst composition, the higher the temperature and the longer the contact time, the greater is the conversion of the C 2 CI 2 F 4 isomer mixtures to polychlorinated products. The above variables can be balanced, one against the other, so that the reaction of CCI 2 FCF 3 in the presence of CCIF2CCIF2 is maximized. The reaction products are separated by conventional techniques, such as distillation. Some of the reaction products will have desired properties for commercial use. For example CCI 3 CF 3 (CFC-113a) can be used to prepare CFC-114a which can then be converted to CH 2 FCF 3 (HFC-134a) by hydrodechlorination. Others, such as CCl 2 =CCl 2 can be recycled back to reactors which are being used for the synthesis of halofluorocarbons.
The reaction of the C 2 CI 2 F 4 isomers with HCl 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 Inconel™ nickel alloy and Hastelloy™ nickel alloy.
Preferably, the CFC-114 in the product mixture is at least 95% of the total C 2 CI 2 F 4 content. If, after
separation, the relative amount of CFC-114 is lower than desired, the CFC-114 content can be further enriched by further reacting CFC-114a with HCl in accordance with this invention (e.g., by recycle or staging). Pressure is not critical. Atmospheric and superatmospheric pressures are the most convenient and are therefore preferred.
Practice of the invention will be come further apparent from the following non-limiting examples. EXAMPLE 1
Catalys Ac iva ion
A reactor (a 0.5 inch (1.3 cm) ID, 12 inch (30.5 cm) long Inconel™ nickel alloy pipe) was charged with 21.0 g (30 mL) of gamma-alumina (1/12" (2.1 mm) extrudates) and placed in a sand bath. The bath was gradually heated to 175°C while N 2 gas at a flow rate of 50 cc/min was passed through the reactor to remove traces of water. HF (50 cc/min) as well as nitrogen were then passed through the reactor for 4.3 hours at a 175°C bath temperature. The reactor temperature was gradually raised to 400°C over 4 hours while continuing to pass HF (80 cc/min) and nitrogen (20 cc/min) over the catalyst. At this point the temperature was reduced to 350°C, the HF stopped, and nitrogen flow continued until the catalyst was used.
A mixture containing CCIF 2 CCIF 2 (CFC-114, 44.1%) and CCI 2 FCF 3 (CFC-114a, 55.7%) and HCl was fed to the reactor. The HCl:C 2 Cl 2 F 4 molar ratio was 20:1, the reaction temperature varied between 250 and 350°C, and the contact time (CT.) was 15 seconds. The results of these runs, in mole % are shown in Table 1.
IΔBLE_ 1
Temp 1141
°C 114 a 114a b 113 c 113a d 112/a< lllf PCE9 Others* 1 14+114a
Feed 44.1 55.7 0.2 44.2
250 44.3 24.0 0.1 31.2 0.2 0.2 64.9
275 44.1 15.9 0.3 38.1 0.9 0.2 0.1 0.4 73.4
300 39.6 14.8 1.4 38.0 3.9 0.4 0.9 1.0 72.9
325 26.6 19.5 2.2 41.1 5.1 0.5 3.4 1.6 57.6
350 8.5 25.4 2.9 44.3 5.4 0.4 7.7 5.4 25.1 a 114 is CCIF2CCIF2 b 11 a is CCI2FCF3 c 113 is CCI2FCCIF2 d 113a is CCI3CF3 e 112/a is CCI2FCCI2F+CCI3CCIF2 f lll is CCI3CCI2F
9PCE is CCI2-CCI2
^Others includes CCIF3 and C2CIF5
Comparison of the data presented in Table 1 shows that for a given HCl/organic ratio and contact time, the 114/(114+114a) ratio increases with temperature up to a certain point and then decreases with increasing temperature.
A second series of runs was done with a commercially available mixture containing CCIF 2 CCIF 2 (CFC-114, 87.9%) and CCI 2 FCF 3 (CFC-114a, 12.1%) and HCl was fed to the reactor. The HCl:C 2 Cl2F 4 molar ratio was varied from 5:1 to 20:1, the reaction temperature varied between 200 and 275°C, and the contact time (CT.) was varied from 15 to 60 seconds. The results of these runs, in mole % are shown in Table 2.
TABLE 2
114
Temp HCl/ 114+114a ° C Orq . CT 114 114a 113 113a 112/a 111 PCE Others
FEED 87.9 12.1 87.9 200 20 45 87.3 1.4 10.9 0.3 0.1 98.4 225 20 30 86.3 1.5 0.1 10.6 0.8 0.3 0.3 0.1 98.3 225 10 30 87.2 2.1 0.1 9.8 0.6 0.1 0.1 97.7 225 5 30 88.0 3.1 0.1 8.4 0.3 0.1 96.6 250 20 30 81.8 2.4 0.5 11.7 2.3 0.7 0.6 97.2 250 10 30 83.9 2.8 0.4 10.7 1.6 0.4 0.2 96.8 250 5 30 86.0 3.4 0.4 9.1 0.9 0.1 0.1 96.2 275 20 60 61.6 7.0 1.1 23.3 3.6 1.0 2.2 0.2 89.8 275 20 30 68.7 4.8 0.9 18.6 3.6 1.0 2.1 0.3 93.4 275 20 15 77.4 3.2 0.7 13.7 2.8 0.9 1.3 96.1
Examination of the data in Table 2 shows that the reactions parameters can be adjusted to maximize CFC-114 and minimize CFC-114a .
EXAMPLE 2
The same reactor as used in Example 1 was charged with 28.3 g (30 mL) of 2% Co on fluorided alumina prepared as described in U.S. Patent No. 4,766,260. A mixture containing CCIF 2 CCIF 2 (CFC-114, 88.1%) and 0 CCI 2 FCF 3 (CFC-114a, 11.9%) and HCl was fed to the reactor. The HCl:C 2 Cl 2 F 4 molar ratio was 20:1. For runs at 31, 38, 89, 90, and 93 hours, oxygen was added to the feed with the following molar ratios; HCl:C2Cl2F4:θ 2 = 20:1:0.2. The reaction temperature 5 varied between 200 and 275°C, and the contact time was 30 seconds except for the 112 hour run where it was 15 seconds. The results of this run, in mole %, are shown in Table 3.
y TABLE 3
114/
Temp. 114+114a
Hrs. °C. 114 114a 113 113a 112/a 111 PCE
0 FEED 88.1 11.9 88.1
31 275 50.3 10.7 1.3 29.7 3.9 1.3 1.8 82.6
38 275 55.5 9.4 1.3 26.5 3.9 1.4 1.7 85.6
66 225 77.8 3.2 0.7 14.0 2.9 1.1 0.4 96.1
69 200 83.1 2.1 0.4 11.4 2.1 0.8 0.0 97.5
85 200 83.7 2.0 0.4 11.1 1.9 0.8 0.0 97.7
89 200 83.9 2.0 0.4 11.1 1.9 0.8 0.0 97.7
90 225 80.0 2.7 0.6 12.6 2.6 1.1 0.5 96.8
93 250 71.8 4.5 0.9 17.0 3.4 1.4 0.9 94.1
112 250 77.6 3.0 0.7 13.3 3.0 1.4 0.9 96.3
Particular embodiments of the invention are illustrated in the Examples. Other embodiments will become apparent to those skilled in the art from a consideration of the specification or practice of the invention. 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 forms thereof as come within the scope of the claims.