Patent Application
20230150900
The present invention relates to a process for making 2-chloro-1,1,1,2-tetrafluoropropane. The present invention further relates to a process for making 2-chloro-1,1,1,2-tetrafluoropropane via hydrofluorination of 2-chloro-3,3,3-trifluoropropene with high single-pass conversion.
The refrigerant and blowing agent 2,3,3,3-tetrafluoropropene (1234yf) is produced from the dehydrochlorination of 2-chloro-1,1,1,2-tetrafluoropropane (244bb). 244bb may be manufactured from 2-chloro-3,3,3-trifluoropropene (1233xf).
When conversion of 2-chloro-1,1,1,2-tetrafluoropropane from 2-chloro-3,3,3-trifluoropropene is low, 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene are present in admixture in product streams. 2-chloro-1,1,1,2-tetrafluoropropane and 2-chloro-3,3,3-trifluoropropene exhibit similar boiling points and azeotrope-like properties that make them difficult to separate via standard techniques such as conventional distillation.
One method of addressing the problem of low conversion is to increase recycle of product streams to the reactor so that additional conversion is obtained. The increased recycle would require process equipment to be increased in size and scale to maintain a desired level or product output, and, thus significantly increase manufacturing cost. In addition, the separation of components in the product stream is difficult.
It would be desirable to have a process for making 2-chloro-1,1,1,2-tetrafluoropropane from 2-chloro-3,3,3-trifluoropropene at higher single-pass conversion levels.
Provided is a process for making 2-chloro-1,1,1,2-tetrafluoropropane. The process has the step of hydrofluorinating 2-chloro-3,3,3-trifluoropropene in the presence of a catalyst selected from the group consisting of SbCl3, SbCl5, SbF5, TiCl4, SnCl4, Cr2O3, and fluorinated Cr2O3. Preferably, the process is performed as a continuous process.
In the process of the present invention, selected catalysts are employed to enhance the single-pass conversion of 2-chloro-3,3,3-trifluoropropene to 2-chloro-1,1,1,2-tetrafluoropropane via HF addition across the double bond of 2-chloro-3,3,3-trifluoropropene. The catalysts are the following: SbCl3, SbCl5, SbF5, TiCl4, SnCl4, Cr2O3, and fluorinated Cr2O3.
The catalyst may be supported or in bulk form (unsupported). Useful catalyst supports include carbon, alumina, fluorinated alumina, aluminum fluoride, alkaline earth metal oxides, fluorinated alkaline earth metals, zinc oxide, zinc fluoride, tin oxide, and tin fluoride.
The catalyst optionally may be activated prior to and during use. Useful activating agents include anhydrous hydrogen fluoride and chlorine. The catalyst is kept activated by the continuous or batch addition of an oxidizing agent such as Cl2.
The hydrofluorination process may be carried out in a vapor phase or a liquid phase.
In vapor-phase hydrofluorination, HF (hydrogen fluoride gas) is fed continuously through the catalyst bed. After a short time with only the HF feed stream, 2-chloro-3,3,3-trifluoropropene is fed continuously through the catalyst bed at a ratio of about 1:1 to about 1:30 and preferably from about 1:2 to about 1:15 (2-chloro-3,3,3-trifluoropropene/HF mole ratio). The reaction between HF and 2-chloro-3,3,3-trifluoropropene is carried out at a temperature from about 30° C. to about 200° C. (preferably from about 50° C. to about 120° C.) and at a pressure of about 5 psia to about 200 psia (pounds per square inch absolute) (preferably from about 30 psia to about 175 psia). The catalyst may be supported on a substrate, such as on activated carbon, or may be unsupported or free-standing. The catalyst may (or may not) have to be activated with anhydrous hydrogen fluoride HF (hydrogen fluoride gas) and/or Cl2 (chlorine gas) before use depending on the state of the catalyst. If necessary, the catalyst can be kept activated by the continuous or batch addition of Cl2 or a similar oxidizing agent.
In liquid phase hydrofluorination, the catalyst is charged in a liquid form to a reactor and optionally activated with HF. The activated catalyst is then heated to the desired reaction temperature of about 30° C. to about 200° C. (preferably from about 50° C. to about 120° C.) and the pressure is kept between about 15 psia to about 200 psia (preferably from about 50 psia to about 175 psia). After a short time with only HF feed, a 2-chloro-3,3,3-trifluoropropene feed stream is fed continuously through the catalyst bed at a ratio of about 1:1 to about 1:30 and preferably about 1:2 to about 1:15 (2-chloro-3,3,3-trifluoropropene/HF mole ratio). If necessary, the catalyst can be kept activated by the continuous or batch addition of Cl2 or a similar oxidizing agent.
Enhanced or improved single-pass conversion of 2-chloro-3,3,3-trifluoropropene to 2-chloro-1,1,1,2-tetrafluoropropane is an important feature of the present invention. The hydrofluorination reaction is preferably carried out to attain a conversion of about 70% or more, preferably about 90% or more, and most preferably about 93% or more. Conversion is calculated by the number of moles of reactant (2-chloro-3,3,3-trifluoropropene) consumed divided by number of moles of reactant (2-chloro-3,3,3-trifluoropropene) fed to the reactor multiplied by 100. The selectivity for 2-chloro-1,1,1,2-tetrafluoropropane attained is preferably about 60% or more and most preferably about 80% or more. Selectivity is calculated by number of moles of product (2-chloro-1,1,1,2-tetrafluoropropane) formed divided by number of moles of reactant consumed.
Hydrofluorination is preferably carried out in a corrosion-resistant reaction vessel. Examples of corrosion-resistant materials are Hastelloy, Nickel, Incoloy, Inconel, Monel and fluoropolymer linings. The vessel may have a fixed or a fluidized catalyst bed. If desired, inert gases such as nitrogen or argon may be employed in the reactor during operation.
The following are examples of the present invention and are not to be construed as limiting. Unless otherwise indicated, all percentages and parts are by weight.
The vapor phase fluorination of the 2-chloro-3,3,3-trifluoropropene (1233xf)+HF→2-chloro-1,1,1,2-tetrafluoropropane (244bb) was carried out. The fluorination catalyst for the experiment was 50 wt % SbCl5 impregnated on 50 wt % Calgon PCB activated carbon.
Several kilograms of 50 weight % SbCl5 on activated carbon were produced in the lab. The catalyst was first passed through a 10-mesh sieve to remove fines. A total of 2272.6 grams (or about 2800 cc) was charged to two 2-inch vapor-phase pipe reactors in series and installed in a sand bath for controlled heating.
The catalyst was activated by adding a minimum of a 5:1 mole ratio of HF to SbCl5, followed by a Cl2 addition of a minimum of a 3:1 mole ratio of Cl2 to SbCl5. Finally, a large excess of HF was passed through the catalyst bed for 2 hours.
The reaction was run using 2-chloro-3,3,3-trifluoropropene crude raw material with various compositions as organic feed to produce 2-chloro-1,1,1,2-tetrafluoropropane. The reactor effluent was collected in a distillation column before removal of excess HF. During the experiment, a 93.5% conversion of 2-chloro-3,3,3-trifluoropropene was achieved. The maximum selectivity of 2-chloro-1,1,1,2-tetrafluoropropane achieved was 98.4% on a molar basis. The reaction ran continuously for 76.5 hrs without attempting catalyst regeneration with Cl2. The catalyst began showing signs of deactivation after about 65 hours on-stream time. The experimental data and reaction conditions are shown below in Tables 1A to 1D.
The liquid phase fluorination reaction of 2-chloro-3,3,3-trifluoropropene (1233xf)+HF→2-chloro-1,1,1,2-tetrafluoropropane (244bb) was carried out. The fluorination catalyst for the experiment was SbCl3.
About 6100 grams of SbCl5 were contained in a Teflon™-lined liquid phase reactor (Teflon is a trademark of E.I. duPont de Nemours & Co) equipped with a 2-inch ID (inside diameter) packed column and a condenser. The reactor was 2.75-inch ID×36-inch L (length). Initially, a greater than 5:1 mole ratio of HF was added to the reactor to fluorinate the catalyst. A greater than 3:1 mole ratio of Cl2 was then added to the reactor to ensure that the catalyst was brought back to a pentavalent state. The reactor was heated to about 85° C.-87° C. HF feed was started first. When an additional 1.3 lbs of HF had been added the 2-chloro-3,3,3-trifluoropropene feed was started. The purity of the 2-chloro-3,3,3-trifluoropropene feed stock was about 98 GC area % (gas chromatograph). The experiment ran continuously for 71 hours. For this run, chlorine was fed batchwise about every 4 hours throughout the run to keep the catalyst active. The HF and 2-chloro-3,3,3-trifluoropropene feeds were varied during the run. The feeds averaged 0.495 lbs/hr HF, and 0.408 lbs/hr 2-chloro-3,3,3-trifluoropropene (chlorine was 5.4% by weight of organic) for a 7.9/1 ratio of HF/2-chloro-3,3,3-trifluoropropene, and 135 seconds residence time at the beginning of the run. In the middle of the run, the feeds averaged 0.843 lbs/hr HF (pounds/hour) and 0.66 lbs/hr 2-chloro-3,3,3-trifluoropropene (chlorine was 3.3% by weight of organic) for a 8.33/1 ratio of HF/2-chloro-3,3,3-trifluoropropene, and 80 seconds residence time. For the end of the run, the rate was increased. The feeds for this period averaged 1.42 lbs/hr HF and 1.24 lbs/hr 2-chloro-3,3,3-trifluoropropene (chlorine was 2% by weight of organic) for a 7.5/1 ratio of HF/2-chloro-3,3,3-trifluoropropene, and 47 seconds residence time. The level of unreacted 2-chloro-3,3,3-trifluoropropene appeared to increase late in the run, which could have been the result of lower Cl2 level or shorter residence time.
The reactor temperature range for the experiment was 78-91° C. and the pressure range was 85 psig-115 psig (pounds per square inch gauge).
The following Table 2 contains the 2-chloro-3,3,3-trifluoropropene conversion and product selectivity data:
Example 3 used the same equipment as Example 2.
About 5615 grams of SbCl5 were contained in the same reactor as that of Example 2. The reactor was heated to about 85° C.-87° C. HF feed was started first. After about 1.5 lbs of HF had been added, the 2-chloro-3,3,3-trifluoropropene feed was started. The purity of the 2-chloro-3,3,3-trifluoropropene feed stock was about 97.3 GC area %. The experiment ran continuously for 71 hours. For this run, Cl2 was fed batchwise about every 4 hours throughout the run to keep the catalyst active.
The Run # for this experiment was 36b. Conversion was immediately above 98%, and remained that way throughout the rest of the run (through Friday shut-down). The catalyst charge was left hot over the weekend, and operation resumed on Monday (now called Run #37), and similar high conversion was observed throughout the week. About 123 pounds of acid-free 2-chloro-1,1,1,2-tetrafluoropropane crude was collected between runs #36b and its continuation as Run #37 the following week.
The reactor temperature range for the experiment was 78° C.-86° C. and the pressure range was 70 psig-105 psig. The organic crude material collected from the run was run on a gas chromatograph and exhibited the following GC analysis.
The following Tables 3A and 3B set forth the 2-chloro-3,3,3-trifluoropropene (1233xf) conversion and product selectivity data.
About 327 grams of HF, about 50 grams 1233xf, and about 75 grams SbCl5 were charged into a 1-L autoclave. The reaction mixture was stirred at a temperature of about 80° C. for about 3 hours under about 620 psig of pressure. After the reaction, the reactor was cooled to about 0° C. and about 300 ml water was then added slowly into the autoclave over a period of about 45 min. After complete addition of water under stirring, the reactor was cooled to room temperature and then the overhead gases were transferred to another collecting cylinder. The yield of CF3CFClCH3 was about 90% at a 1233xf conversion level of about 98%. The other major by-products were CF3CF2CH3 (2%), and an unidentified isomer of a C4 compound of the general formula, C4H3Cl3F4 (8%).
About 327 grams HF, about 50 grams 1233xf, and about 75 grams SbCl5 were charged into a 1-L autoclave. The reaction mixture was stirred at 80° C. for about 3 hours under about 625 psig of pressure. After the reaction, the reactor was cooled to about 45° C. and then the overhead gas mixture was passed through a well dried KF, NaF, or Al2O3 (350 g) packed column kept at about 80° C. to strip off HF from the gas stream. The gases coming out of the column are collected in a cylinder kept in dry ice (−70° C.) bath. The yield of CF3CFClCH3 was 87% at a 1233xf conversion level of 93%. The other major by-products were CF3CF2CH3 (1%), and an unidentified isomer of a C4 compound of the general formula, C4H3Cl3F4 (7%). The product, CF3CFClCH3 was isolated by distillation with 98% purity.
A 22-inch (½-inch diameter) Monel tube gas phase reactor was charged with about 120 cc of a catalyst. The reactor was mounted inside a heater with three zones (top, middle and bottom). The reactor temperature was read by a custom made 5-point thermocouple kept at the middle inside of the reactor. The inlet of the reactor was connected to a pre-heater, which was kept at about 300° C. by electrical heating. Organic (1233xf) was fed from a cylinder kept at 70° C. through a regulator, needle valve, and a gas mass-flow-meter. The organic line to the pre-heater was heat traced and kept at a constant temperature of about 73° C. by electrical heating to avoid condensation. N2 was used as a diluent in some cases and fed from a cylinder through a regulator and a mass flow controller into the pre-heater. All feed cylinders were mounted on scales to monitor their weight by difference. The reactions were run at a constant reactor pressure of from about 0 to about 100 psig by controlling the flow of reactor exit gases by another research control valve. The gas mixtures exiting reactor was analyzed by on-line GC and GUMS connected through a hotbox valve arrangements to prevent condensation. The conversion of 1233xf was from about 50% to about 65% and the selectivity to 244 isomer (CF3CFClCH3) was from about 90% to about 93% depending on the reaction conditions using 120 cc of 50 wt % SbCl5/C as the catalyst at about 65° C. to about −85° C. with a HF flow of about 50 g/h and organic flow of about 15 g/h. No CF3CF2CH3 was observed under the reaction conditions. The catalyst is pretreated at first with 50 g/h HF at about 65° C. for about 2 hours and then with about 50 g/h HF and about 200 sccm of Cl2 at about 65° C. for about 4 hours. After pre-treatment, about 50 sccm of N2 is flows over a period of about 40 minutes through the catalyst bed to sweep free chlorine from the catalyst surface prior to interacting with the organic feed (1233xf). Pretreatment is considered important to many embodiments of the invention. The products were collected by flowing the reactor exit gases through a 20-60 wt % aqueous KOH scrubber solution and then trapping the exit gases from the scrubber into a cylinder kept in dry ice or liquid N2. The products were then isolated by distillation. About 50 wt % SbCl5/C, about 3 to about 6 wt % FeCl3/C, 20 wt % SnCl4/C, and about 23 wt % TiCl4/C, using 4 different kind of activated carbon such as Shiro saga, Calgon, Norit, and Aldrich were used as the catalyst at from about 60 to about 150° C. Among all the catalysts used for this reaction, Cl2 and HF pre-treated SbCl5/C was found to be generally preferred in terms of activity. The results using SbCl5 as the catalyst are shown in Table 2.
Reaction conditions: 1233xf flow, 150 sccm; HF flow 50 g/h; pressure, 2.5-5.3 psig; in 1-5 reactions Calgon activated carbon is used as the catalyst support; catalyst, 120 cc. All catalysts are pre-treated with Cl2 and HF prior to contacting with 1233xf.
It should be understood that the foregoing description is only illustrative of the present invention. Various alternatives and modifications can be devised by those skilled in the art without departing from the invention. Accordingly, the present invention is intended to embrace all such alternatives, modifications and variances that fall within the scope of the appended claims.
This application is a Continuation of U.S. application Ser. No. 16/983,949, filed Aug. 3, 2020, which is a Continuation of U.S. application Ser. No. 15/911,658, filed Mar. 5, 2018, now pending, which in turn is a Continuation of U.S. application Ser. No. 14/704,491, filed May 5, 2015 (now U.S. Pat. No. 9,914,680), which in turn is a Continuation of U.S. application Ser. No. 12/631,728, filed Dec. 4, 2009, (now U.S. Pat. No. 9,024,092, issued May 5, 2015), which in turn is: (1) a continuation of U.S. application Ser. No. 12/338,466 (now abandoned) and (2) a Continuation-in-Part of U.S. application Ser. No. 11/619,592, filed Jan. 3, 2007, (now U.S. Pat. No. 8,084,653, issued Dec. 27, 2011), which in turn is a Continuation-in-Part of each of: (a) U.S. application Ser. No. 11/118,530 (now U.S. Pat. No. 7,189,884); (b) U.S. Ser. No. 11/118,503 (now U.S. Pat. No. 7,345,209); and (c) U.S. application Ser. No. 11/118,504 (now U.S. Pat. No. 7,371,904). Each of the applications and patents mentioned in this paragraph are incorporated by reference in its entirety. U.S. application Ser. No. 11/118,503 (now U.S. Pat. No. 7,335,209) claims the priority benefit of U.S. Provisional Application No. 60/567,427, filed Apr. 29, 2004, which is incorporated herein by reference. U.S. application Ser. No. 11/118,504 (now U.S. Pat. No. 7,371,904) claims the priority benefit of each of U.S. Provisional Applications Nos. 60/567,429, 60/567,426, and 60/567,425, each filed Apr. 29, 2004 and each of which is incorporated herein by reference. U.S. Application No. of U.S. Ser. No. 11/118,530 (now U.S. Pat. No. 7,189,884) claims the priority benefit of U.S. Provisional Application No. 60/567,428, filed Apr. 29, 2004, which is incorporated herein by reference. U.S. application Ser. No. 11/619,592, filed Jan. 3, 2007, (now U.S. Pat. No. 8,084,653, issued Dec. 27, 2011), claims the priority benefit of U.S. Provisional Application No. 60/755,485, filed Jan. 3, 2006, which is incorporated herein by reference in its entirety. U.S. application Ser. No. 12/338,466, filed Dec. 18, 2008 (now abandoned), claims the priority benefit of U.S. Provisional Application No. 61/021,121, filed Jan. 15, 2008, which is incorporated herein by reference in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 60567427 | Apr 2004 | US | |
| 60567426 | Apr 2004 | US | |
| 60567425 | Apr 2004 | US | |
| 60567429 | Apr 2004 | US | |
| 60567428 | Apr 2004 | US | |
| 60775485 | Feb 2006 | US | |
| 61021121 | Jan 2008 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 16983949 | Aug 2020 | US |
| Child | 18100034 | US | |
| Parent | 15911658 | Mar 2018 | US |
| Child | 16983949 | US | |
| Parent | 14704491 | May 2015 | US |
| Child | 15911658 | US | |
| Parent | 12631728 | Dec 2009 | US |
| Child | 14704491 | US | |
| Parent | 12338466 | Dec 2008 | US |
| Child | 11619592 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 11619592 | Jan 2007 | US |
| Child | 12631728 | US | |
| Parent | 11118530 | Apr 2005 | US |
| Child | 11619592 | US | |
| Parent | 11118503 | Apr 2005 | US |
| Child | 11118530 | US | |
| Parent | 11118504 | Apr 2005 | US |
| Child | 11118503 | US |
