Hydrogenation catalyst

Abstract

The present invention relates, in part, to an alpha-alumina support for a hydrogenation catalyst useful in hydrogenating fluoroolefins. In certain aspects, it relates to a method for hydrogenating a compound by contacting an olefin reactant having at least one carbon-fluorine bond, with a supported hydrogenation catalyst. The reaction results in a product that includes a hydrogenated derivative of the olefin. In certain embodiments, the supported hydrogenation catalyst includes a zero-valent metal disposed on an alpha-alumina support.

Claims

1. A method for hydrogenating a compound comprising: contacting a reactant comprising pentafluoropropene and/or hexafluoropropene, with a supported hydrogenation catalyst under reaction conditions effective to form a reaction product comprising a hydrogenated derivative of said pentafluoropropene and/or hexafluoropropene, wherein said supported hydrogenation catalyst comprises from 0.5 to about 10 weight percent of zero-valent palladium disposed on a support comprising about 90 percent by weight to about 99.5 percent by weight of alpha-alumina.

2. The method of claim 1 wherein said support consists essentially of alpha-alumina.

3. The method of claim 1 wherein said contacting comprises feeding said pentafluoropropene and/or hexafluoropropene into a first stage of a hydrogenation reactor at a rate resulting in a conversion of the feed pentafluoropropene and/or hexafluoropropene of from about 10% to about 60%.

4. The method of claim 3 wherein said reaction product further comprises at least a portion of said pentafluoropropene and/or hexafluoropropene from said reactant that remains unreacted subsequent to said contacting; and wherein said method further comprises converting, in one or more subsequent stages of said hydrogenation reactor, about 20 to about 100 percent of said pentafluoropropene and/or hexafluoropropene in said reaction product into said hydrogenated derivative of said pentafluoropropene and/or hexafluoropropene.

5. The method of claim 4 wherein said support consists essentially of alpha-alumina.

6. The method of claim 1 wherein said hydrogenation catalyst comprises about 0.5 weight percent of said zero-valent Pd.

7. The method of claim 1 wherein said olefin is selected from the group consisting of 1,1,2,3,3,3-hexafluoropropene; 1,2,3,3,3-pentafluoropropene; and 1,1,3,3,3-pentafluoropropene.

8. The method of claim 1 wherein said hydrogenated derivative of said olefin is selected from the group consisting of 1,1,1,2,3,3-hexafluoropropane; 1,1,1,2,3-pentafluoropropane; and 1,1,1,3,3-pentafluoropropane.

9. The method of claim 1 wherein said olefin comprises 1,1,2,3,3,3-hexafluoropropene and said hydrogenated derivative of said olefin comprises 1,1,1,2,3,3-hexafluoropropane.

10. The method of claim 1 wherein said olefin comprises 1,2,3,3,3-pentafluoropropene and said hydrogenated derivative of said olefin comprises 1,1,1,2,3-pentafluoropropane.

Description

BRIEF DESCRIPTION OF THE DRAWING

(1) FIG. 1 shows 1,1,1,2,3,3-hexafluoropropene (HFP) conversion versus time on stream during HFP hydrogenation over 0.5 wt % Pd/gamma-alumina and 0.5 wt % Pd/alpha-alumina catalysts.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS OF THE INVENTION

(2) According to a preferred embodiment of the invention, alpha-alumina supported metal catalysts are employed in the hydrogenation of fluoroolefins to hydrofluorocarbons. Non-limiting examples of metal components include Pd, Ru, Pt, Rh, Ir, Fe, Co, Ni, Cu, Ag, Re, Os, Au, and any combinations thereof. The metal loading can vary within a large range, e.g., from 0.1-10 wt %. However, for noble metals such as Ru, Ph, Pd, Pt, Ir, etc., the metal loading is preferably about 0.1 to about 5 wt %, and more preferably about 0.1 to about 1 wt %. It has been discovered that supported catalyst having metal concentrations below about 0.1 wt. % are not highly effective at hydrogenating fluoroolefins or hydrofluoroolefins.

(3) In one embodiment, the salt of a metal component (e.g., Pd(NO.sub.3).sub.2 or PdCl.sub.2 for Pd) is added to an amount of solvent sufficient to substantially dissolve or solubilize the metal salt. The preferred solvent is one in which the metal salt is readily soluble. The choice of solvent may vary depending on the particular metal salts. Examples of solvents that can be used for the preparation of the catalyst compositions of the present invention include water, alcohols, ethers, and mixtures thereof. Useful alcohols include monohydric and polyhydric alcohols. Most preferred alcohols are those that are monohydric and have 1 to 5 carbon atoms. A most preferred solvent is water.

(4) Desired amount of alpha-alumina powder is added to the solution of said metal salt to form a slurry. After formation of the slurry, substantially all of the solvent is removed to form a solid mass of a mixture of said metal salt and said alpha-alumina. Although the solvent can be removed in one step, a preferred method is to drive off a portion of the solvent from the slurry to form a paste and then followed by drying the paste to form the solid mass. Any conventional technique can be used to drive off the solvent. Examples of such techniques include vigorous stirring at room or elevated temperatures, evaporation, settling and decanting, centrifugation, and filtration. It is preferred to evaporate off a desired amount of solvent to form the paste. The paste is then dried by any suitable method to form a free-flowing, substantially solvent-free powder. Preferred methods for drying include oven drying, most preferably at temperatures from about 110° C. to about 120° C., and spray drying. As used herein, the term “solvent free” means that less than 1 wt. %, preferably about 0.5 wt % or less, more preferably about 0.1 wt % or less, and most preferably no solvent will remain with the powder after solvent removal/drying. Upon removal of solvent, the powder will take the form of a solid mass (or powder) of a mixture of particles of said metal salt and said alpha-alumina.

(5) Optionally, the solid mass of the mixture of said metal salt and said alpha-alumina powder is then calcined. Calcination is preferably carried out at a temperature of about 100° C. to about 750° C., more preferably at a temperature of about 200° C. to about 600° C., and most preferably at a temperature of about 300° C. to about 500° C. Calcination may further optionally be carried out in the presence of an inert gas, such as nitrogen or argon.

(6) After calcination, the powder is optionally further grinded such that it becomes more finely-divided. The powder is further optionally pelletized in order to form pellets.

(7) The catalyst pellets are then loaded into a reactor and prior to use are reduced in hydrogen or diluted hydrogen flow for 2-4 hours at a temperature of about 50 to about 500° C., more preferably at a temperature of about 100 to about 300° C., and most preferably at a temperature of about 150 to about 250° C.

(8) Although it is contemplated that the hydrogenation of fluoroolefins may be conducted in batch operation, it is preferred that the hydrogenation reaction is carried out as a substantially continuous operation. Furthermore, while it is possible that the hydrogenation reaction may involve in certain embodiments a liquid phase reaction, it is contemplated that in preferred embodiments the hydrogenation reaction comprises, and even more preferably consists of, at least two vapor phase reaction stages.

(9) With respect to the number of reaction stages, applicants have found surprisingly and unexpectedly that overall reaction conversion and selectivity can be achieved at relatively high levels by the use of at least two reaction stages wherein the first stage of reaction is conducted under conditions effective to achieve a first, relatively low rate of conversion to produce a first stage reaction effluent, and at least a second stage of reaction which is fed by at least a portion of said first stage effluent and which is conducted under conditions effective to achieve a second rate of conversion higher than said first rate. Preferably, reaction conditions are controlled in each of the first and second stages in order to achieve the desired conversion in accordance with the present invention. As used herein, the term “reaction conditions” is intended to include the singular and means control of any one or more processing parameters which can be modified by the operator of the reaction to produce the conversion of the feed material in accordance with the teachings contained herein. By way of example, but not by way of limitation, conversion of the feed material may be controlled or regulated by controlling or regulating any one or more of the following: the temperature of the reaction, the flow rate of the reactants, the presence of diluent, the amount of catalyst present in the reaction vessel, the shape and size of the reaction vessel, the pressure of the reaction, and any combinations of these and other process parameters which will be available and known to those skilled in the art in view of the disclosure contained herein.

(10) Applicants have found that in preferred embodiments the step of controlling the conversion in the first stage of the hydrogenation reaction is achieved by judicious selection and control of the amount of catalyst present in the first stage of reaction relative to the feed rate of one or more of the reactants and/or by judicious selection and control of the reaction temperature, and preferably by judicious selection and control of both of these process parameters. The step of judiciously selecting the amount of catalyst to be used in the first stage of reaction includes the step of estimating the amount of catalyst theoretically needed to convert 100% of the feed material. Such an estimate can be obtained by any and all known methods for making such an estimate, which should be apparent to those skilled in the art in view of the teachings contained herein. In addition, the step of judiciously selecting the amount of catalyst may also involve conducting bench, pilot or similar studies to determine the amount of the particular catalyst being used which is needed to convert 100% of the feed material under the feed rate in other process parameters which have otherwise been chosen. Based upon this estimate, the preferred embodiments of the present invention then include the step of providing in the first stage of reaction an amount of catalyst that is substantially below the amount required for 100% conversion, and even more preferably is sufficiently low so as to result in a conversion of the feed olefin of from about 10% to about 60%, more preferably from about 10% to about 40%, and even more preferably from about 10% to 25%. Once again, those skilled in the art will appreciate that the step of judiciously choosing the amount of catalyst may further include running additional bench, pilot or other studies with the reduced amount of catalyst and adjusting the amount of catalyst accordingly. It is contemplated that all such studies and estimates can be achieved without undue experimentation in view of the teachings contained herein.

(11) Applicants have found that the step of maintaining a relatively low conversion of reactant in accordance with the present invention in a first stage of reaction has an advantageous affect on the selectivity of the reaction to the desired hydrofluorocarbon. In other words, although the amount of conversion which occurs in the first stage of reaction is controlled to be well below that which is desired for the overall hydrogenation step, applicants have found that an improved, higher percentage of the feed material is converted to the desired hydrofluorocarbon in the first reaction stage (that is, improved selectivity is achieved) by controlling the conversion as described herein. More specifically, it is preferred in many embodiments that the selectivity to the desired hydrofluorocarbon in the first reaction stage is at least about 80%, more preferably at least about 90%, and even more preferably at least about 95%, and in many preferred embodiments about 97% or greater.

(12) In certain preferred embodiments the step of controlling the conversion in the first reaction stage further includes removing heat from the reaction by cooling at least a portion of the reaction mixture. It is contemplated that those skilled in the art will be able to devise without undue experimentation and many means and mechanisms for attaining such cooling in view of the teachings contained herein and all such means and mechanisms are with the scope of the present invention.

(13) In preferred embodiments, at least a portion of the effluent from the first reaction stage is fed directly, or optionally after some further processing, to a second reaction stage in which the unreacted fluoroolefin remaining in the effluent after the first reaction stage is converted to the hydrofluorocarbon in accordance with the present invention. More specifically is preferred that the second reaction stage or subsequent reaction stages if present, is operated under conditions effective to convert the fluoroolefin contained in the feed stream to the second reactor stage at a conversion rate that is greater than, and preferably substantially greater than, the conversion percentage in the first reaction stage. In certain preferred embodiments, for example, the conversion percentage in the second reaction stage is from about 20% to about 99%, depending in large part upon the total number of reactant stages used to affect the overall conversion step. For example, in embodiments consisting of a two-stage reaction system, it is contemplated that the conversion in the second reaction stage is preferably greater than 95%, and even more preferably about 100%. However, as those skilled in the art will appreciate from the teachings contained herein, such a two-stage reaction may not be sufficient to produce the desired selectivity to the hydrofluorocarbon. In such cases, it is within the scope of the present invention that the conversion step may comprise greater than two reaction stages, including in some embodiments as many 10 or more reaction stages.

(14) The size and shape, and other characteristics of the reaction vessel itself may vary widely with the scope of the present invention, and it is contemplated that the vessel associated with each stage may be different than or the same as the vessel associated with the upstream and downstream reaction stages. Furthermore, it is contemplated that all reaction stages can occur inside a single vessel, provided that means and mechanisms necessary to control conversion are provided. For example, it may be desirable in certain embodiments to utilize a single tubular reactor for each reaction stage, providing conversion control by judicious selection of the amount and/or distribution of catalyst throughout the tubular reactor. In such a case, it is possible to further control the conversion in different sections of the same tubular reactor by controlling the amount of heat removed from or added to different sections of the tubular reactor.

(15) The catalyst compositions disclosed in the present invention are useful in converting fluoroolefins to hydrofluorocarbons. The catalysts are stable because of their resistance to HF attack and can be re-used after regeneration. One or more of the hydrogenation catalyst disclosed in the present invention may be used for one or more of the reaction stages in accordance with the present invention.

(16) Thus, certain embodiments of the present methods comprise bringing a fluoroolefin and a hydrogenation agent, such as H.sub.2, into contact with a first amount of catalyst in a first reaction stage to produce a reaction stream comprising hydrofluorocarbon(s), unreacted fluoroolefin and hydrogen; contacting at least a portion of this first effluent stream with a second amount of catalyst in a second stage of reaction to produce a hydrofluorocarbon, wherein the second amount of catalyst is greater than the first amount of catalyst and wherein conversion to the fluoroolefin is higher in the second stage of reaction.

(17) Table 1 sets forth examples of hydrofluorocarbons and fluoroolefins from which they can be obtained (fluoroolefin in left column and corresponding hydrofluorocarbon in the right column).

(18) TABLE-US-00001 TABLE 1 Fluoroolefins Hydrofluorocarbons 1,1,2,3,3,3-hexafluoropropene 1,1,1,2,3,3-hexafluoropropane CF.sub.3CF═CF.sub.2 (1216) CF.sub.3CHFCHF.sub.2 (236ea) 1,2,3,3,3-pentafluoropropene 1,1,1,2,3-pentafluoropropane CF.sub.3CF═CHF (Z/E-1225ye) CF.sub.3CHFCH.sub.2F (245eb) 1,1,3,3,3-pentafluoropropene 1,1,1,3,3-pentafluoropropane CF.sub.3CH═CF.sub.2 (1225zc) CF.sub.3CH.sub.2CHF.sub.2 (245fa) 1,3,3,3-tetrafluoropropene 1,1,1,3-tetrafluoropropane CF.sub.3CH═CHF (trans/cis-1234ze) CF.sub.3CH.sub.2CH.sub.2F (254fb) 2,3,3,3-tetrafluoropropene 1,1,1,2-tetrafluoropropane CF.sub.3CF═CH.sub.2 (1234yf) CF.sub.3CHFCH.sub.3 (254eb)

EXAMPLES

(19) The following are examples of the invention and are not to be construed as limiting.

Example 1

Comparison of Gamma-Alumina and Alpha-Alumina Supported Pd Catalysts for 1,1,1,2,3,3-Hexafluoropropene Hydrogenation

(20) 0.5 wt % Pd/gamma-alumina and 0.5 wt % Pd/alpha-alumina, which have a specific surface area of 243 and 33 m.sup.2/g, respectively, were compared for 1,1,1,2,3,3-hexafluoropropene (HFP) hydrogenation. About 2 g of catalyst diluted with 20 ml of Monel packing was charged into a ¾″ Monel tube reactor and was in-situ reduced in 10% H.sub.2/N.sub.2 flow for 2 hours at 200° C. HFP was fed into reactor at a rate of 5 g/h, and H.sub.2 was co-fed according to a mole ratio of H.sub.2/HFP equal to 1.5. As shown in Table 2, both catalysts initially provided a near complete HFP conversion and a 236ea selectivity of above 99.5%. Nevertheless, as shown in FIG. 1, while no deactivation was noted over the 0.5 wt % Pd/alpha-alumina catalyst even after 1000 h on stream, rapid deactivation was observed over the 0.5 wt % Pd/gamma-alumina beginning around 600 h on stream. This indicates that the alpha-alumina supported Pd catalyst is much more stable than the gamma-alumina supported Pd catalyst.

(21) TABLE-US-00002 TABLE 2 HFP hydrogenation over alumina supported Pd catalysts* Temp. Conversion, % Selectivity, % Selectivity, % Catalyst (° C.) HFP 236ea others 0.5% Pd/γ- 100 99.9 99.6 0.4 alumina 0.5% Pd/α- 100 98.2 99.9 0.1 alumina *data obtained after 2 h on stream.

Example 2

Hydrogenation of 1,1,1,2,3,3-Hexafluoropropene Over Alpha-Alumina Supported Pd Catalyst

(22) 0.5 wt % Pd/alpha-alumina catalyst, which has a specific surface area of 33 m.sup.2/g, was used for 1,1,1,2,3,3-hexafluoropropene (HFP) hydrogenation. About 1 g of catalyst diluted with 10 ml of Monel packing was charged into a ¾″ Monel tube reactor and was in-situ reduced in 10% H.sub.2/N.sub.2 flow for 2 hours at 200° C. HFP was fed into reactor at a rate of 65 g/h, and H.sub.2 was co-fed according to a mole ratio of H.sub.2/HFP equal to 1.5. GC analysis of the product stream showed that the catalyst provided an HFP conversion of around 55% and a 245eb selectivity of about 99.5%. No deactivation was noted during the period of time of the test which lasted for 800 hours, indicating the alpha-alumina supported Pd catalyst can provide stable activity for HFP hydrogenation.

Example 3

Hydrogenation of 1,1,1,2,3-Pentafluoropropene Over Alpha-Alumina Supported Pd Catalyst

(23) 0.5 wt % Pd/alpha-alumina catalyst, which has a specific surface area of 33 m.sup.2/g, was used for 1,1,1,2,3-pentafluoropropene (1225ye) hydrogenation. About 0.5 g of catalyst diluted with 10 ml of Monel packing was charged into a ¾″ Monel tube reactor and was in-situ reduced in 10% H.sub.2/N.sub.2 flow for 2 hours at 200° C. 1225ye was fed into reactor at a rate of 30 g/h, and H.sub.2 was co-fed according to a mole ratio of H.sub.2/1225ye equal to 1.5. GC analysis of the product stream showed that the catalyst provided a 1225ye conversion of around 45% and a 245eb selectivity of about 98.5%. No deactivation was noted during the period of time of the test which lasted for 800 hours, indicating the alpha-alumina supported Pd catalyst can provide stable activity for 1225ye hydrogenation.

(24) 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 claim.