Patent Description:
HFO-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene, also known as HFO-1336mzz, or 1336mzz has performance properties suitable for use as a refrigerant or working fluid in applications such as air conditioning, chillers, heat pumps and organic Rankine cycles, as well as for use in foam applications. HFO-1336mzz has an ozone depletion potential of zero and low global warming potential which are desirable attributes for use as or in refrigerants and foam expansion agents.

HFO-1336mzz may exist as one of two configurational isomers, that is, the cis- or Z-isomer and the trans- or E-isomer. Processes to prepare HFO-1336mzz are known and produce a mixture of the two isomers. Each isomer has different properties, therefore, one isomer or the other may be preferred, depending on the use or application.

Because processes to produce HFO-1336mzz provide mixtures of isomers, there may be times when only one of the isomers is desired. In particular, there may be desire for only the E-isomer. Alternatively, there may be desire for only the Z-isomer.

<CIT> discloses a process to isomerize Z-1336mzz to E-1336mzz using a low sodium (less than <NUM> ppm) alumina based catalyst.

<CIT> and <CIT> disclose processes to prepare HFO-1336mzz starting from carbon tetrachloride and ethylene with addition of more carbon tetrachloride and HF. <CIT> discloses a process to prepare HFO-1336mzz starting from carbon tetrachloride and <NUM>,<NUM>,<NUM>-trifluoropropene with addition of HF. A mixture of 1336mzz isomers is produced. Therein, it is disclosed a preference for the cis- or Z-isomer. These patents disclose isomerizing E-1336mzz to Z-1336mzz in a vapor phase reactor using a catalyst selected from halogenated metal oxide, Lewis acid metal halides and zero valent metals.

<CIT> discloses the isomerization of Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene to E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene using a variety of different isomerization catalysts.

There continues to be value to produce E-HFO-1336mzz.

Disclosed herein is a process to produce the trans-isomer of HFO-1336mzz (E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene) by isomerization of the cis-isomer of HFO-1336mzz (Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene).

Z-HFO-1336mzz is isomerized to E-HFO-1336mzz by contacting with a suitable catalyst which comprises chromium oxyfluoride and contains less than <NUM>% by weight alumina. The isomerization is performed in the gas phase, and the temperature in the reaction zone is in the range from <NUM>° to <NUM>. The isomerization process can be performed as a batch process or as a continuous process. The process may be supplemented by the step of recovering the E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene (E-1336mzz).

Also disclosed herein is a process as described in claims <NUM> to <NUM>.

The foregoing the following description are exemplary and explanatory only and are not restrictive of the invention as defined in the appended claims.

Before addressing details of embodiments described below, some terms are defined or clarified.

Also, use of "a" or "an" are employed to describe elements and components described herein. This description should be read to include one or at least one and the singular also includes the plural unless it is obvious that it is meant otherwise.

Although methods and materials similar or equivalent to those described herein can be used in the practice or testing of embodiments of the present invention, suitable methods and materials are described below. In addition, the materials, methods, and examples are illustrative only and not intended to be limiting.

When an amount, concentration, or other value or parameter is given as either a range, preferred range or a list of upper preferable values and/or lower preferable values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. Where a range of numerical values is recited herein, unless otherwise stated, the range is intended to include the endpoints thereof, and all integers and fractions within the range. If, alternatively, relative terms, such as "less than", "greater than" and the like are used to define an amount, concentration, or other value or parameter, the value recited is excluded.

<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene or HFO-1336mzz (each of which may be used herein interchangeably and are synonymous) may exist as one of two configurational isomers, E or Z, wherein E is the trans-isomer and Z is the cis isomer. HFO-1336mzz or 1336mzz as used herein refers to the isomers, E-HFO-1336mzz or Z-HFO-1336mzz, as well as any combinations or mixtures of such isomers.

E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene or E-HFO-1336mzz or E-1336mzz are used interchangeably and are synonymous herein and all refer to the cis isomer of <NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene.

Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene or Z-HFO-1336mzz or Z-1336mzz are used interchangeably and are synonymous herein and all refer to the trans isomer of <NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene.

The present disclosure provides a process to isomerize Z-1336mzz to form E-1336mzz. The process comprises contacting Z-1336mzz with a suitable catalyst in a reaction zone to produce a product comprising E-1336mzz. This isomerization process is carried out in the gas phase using well-known chemical engineering practices, which include continuous, semi-continuous or batch operations.

HFO-1336mzz may be prepared by contacting CF<NUM>-CCl=CCl-CF<NUM> with hydrogen in the presence of a catalyst, for example, as disclosed in <CIT> and <CIT>.

HFO-1336mzz may be prepared by contacting CF<NUM>-CHCl<NUM> with copper in the presence of an amide solvent and <NUM>,<NUM>'-bipyridine, as disclosed in <CIT>.

HFO-1336mzz may be prepared by (<NUM>) contacting CCl<NUM>-CF<NUM> with hydrogen in the presence of a catalyst comprising ruthenium, to produce 1316mxx (<NUM>,<NUM>-dichloro-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene); (<NUM>) contacting 1316mxx with hydrogen in the presence of a catalyst containing copper, nickel, copper-nickel, or copper-palladium to provide E- or Z-1326mxz (<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-chloro-<NUM>-butene); and (<NUM>) contacting 1326mxz with an aqueous solution of an alkali metal hydroxide in the presence of a quaternary alkylammonium salt to provide a mixture comprising hexafluoro-<NUM>-butyne; and (<NUM>) contacting hexafluoro-<NUM>-butyne with hydrogen and a catalyst, as disclosed in <CIT>.

HFO-1336mzz may be prepared by (<NUM>) contacting <NUM>,<NUM>,<NUM>-trifluoro-<NUM>-propene with carbon tetrachloride to provide <NUM>,<NUM>,<NUM>,<NUM>-tetrachloro-<NUM>,<NUM>,<NUM>-trifluorobutane; and (<NUM>) contacting <NUM>,<NUM>,<NUM>,<NUM>-tetrachloro-<NUM>,<NUM>,<NUM>-trifluorobutane as disclosed in <CIT>.

In any process to prepare HFO-1336mzz, a mixture of the Z- and E-isomers may be produced. Z-1336mzz may be separated from the mixture, for example, by distillation. Z-1336mzz produced in any method may serve as starting material for the process disclosed herein. A mixture E-1336mzz and Z-1336mzz may alternatively be used.

The catalyst suitable for the gas-phase isomerization comprises chromium oxyfluoride. In one embodiment, chromium oxyfluoride is represented by the formula Cr<NUM>OxFy wherein x + y/<NUM> = <NUM>. In another embodiment, chromium oxyfluoride is represented by the formula CrOF.

The suitable catalyst comprising chromium oxyfluoride may further comprise other metals, such as, but not limited to cobalt, manganese, nickel, iron in the form of the metal, oxide, halide, oxyhalide or as other inorganic salts. Supports may be present such as AlF<NUM> or carbon. The suitable catalyst contains less than <NUM>% by weight alumina.

Carbon used in the embodiments of this invention may come from any of the following sources: wood, peat, coal, coconut shells, bones, lignite, petroleum-based residues and sugar. Commercially available carbons which may be used include those sold under the following trademarks: Barneby & Sutcliffe™, Darco™, Nucharm™, Columbia JXN™, Columbia LCK™, Calgon™ PCB, Calgon™ BPL, Westvaco™, Norit™, Takeda™ and Barnaby Cheny NB™.

Embodiments of carbon include both non-acid washed and acid-washed carbons. In some embodiments of this invention, carbon may be prepared by treating the carbon with acids such as HNOs, HCl, HF, H<NUM>SO<NUM>, HClO<NUM>, CH<NUM>COOH, and combinations thereof. Acid treatment is typically sufficient to provide carbon that contains less than <NUM> ppm of ash. Some suitable acid treatments of carbon are described in <CIT>.

In some embodiments of this invention, carbon is an activated carbon. In some embodiments of this invention, carbon is a non-acid washed activated carbon. In some embodiments of this invention, carbon is an acid washed activated carbon. The carbon can be in any form, such as, powder, granules, or pellets.

Chromium oxyfluoride may be prepared by any available method, such, for example, by treating chromium oxide (Cr<NUM>O<NUM>) with a fluorinating agent such as HF, CCl<NUM>F, COF<NUM> or hydrofluorocarbons. Other non-limiting methods to prepare chromium oxyfluoride are known and selected methods are disclosed, for example, in <CIT>, and references disclosed therein.

In some embodiments of this invention, the suitable catalyst comprises a metal-modified chromium oxide or a metal-modified chromium oxyfluoride. In some embodiments of this invention, such metal is selected from the group consisting of magnesium (e.g. magnesium fluoride), Group VIIB metals (e.g., manganese), Group IIIB metals (e.g., lanthanum), and zinc. In use, such metals are normally present as halides (e.g., fluorides), as oxides and/or as oxyhalides. In some embodiments of this invention, these metals are supported on chromium oxide or chromium oxyfluoride.

The process to isomerize Z-1336mzz comprises contacting Z-1336mzz with a suitable catalyst in a reaction zone to produce a product comprising E-1336mzz. The isomerization process is carried out in the gas phase.

A suitable catalyst for use in the gas phase may be, for example, in the form of pellets, powders or granules. The form of such catalysts is not critical. Suitable catalysts are described above.

The suitable catalyst for the gas phase isomerization process comprises or is chromium oxyfluoride and contains less than <NUM>% by weight alumina. In certain embodiments the catalyst comprises chromium oxyfluoride and alumina, wherein the catalyst comprises less than <NUM>% by weight alumina or less than <NUM>% by weight alumina or less than <NUM>% by weight alumina or less than <NUM>% by weight alumina or less than <NUM>% by weight alumina or less than <NUM>% by weight alumina. A suitable chromium oxyfluoride catalyst is alumina-free.

The temperature employed in the reaction zone of the gas phase isomerization process ranges from <NUM> to <NUM> or from <NUM> to <NUM>.

The reaction zone pressure for the gas phase isomerization process can be subatmospheric, atmospheric or superatmospheric. In some embodiments of the invention, the reaction zone pressure can be up to <NUM> psig (<NUM> MPa). In some embodiments of the invention, the reaction zone pressure is near atmospheric. In some embodiments of the invention, the pressure is from atmospheric (<NUM> kPa) to <NUM> psig (<NUM> MPa).

The contact time of the starting material which contains Z-HFO-1336mzz with the suitable catalyst for the gas phase isomerization process, which can be a batch or continuous process, can vary widely depending on the degree of conversion desired and generally will be from <NUM> second to <NUM> seconds.

In one embodiment of the gas phase isomerization process as disclosed herein, the process is a batch process with a contact time from <NUM> second to <NUM> seconds. In one embodiment of the gas phase isomerization process as disclosed herein, the process is a continuous process with a contact time from <NUM> second to <NUM> seconds.

It will be understood, that contact time in the reaction zone is reduced by increasing the flow rate of the starting material into the reaction zone.

In an embodiment, the process for isomerizing Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene to E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene, "the isomerization process", is conducted as a batch process in the gas phase.

In an embodiment, the isomerization process is conducted in a continuous process in the gas phase.

In certain embodiments of a continuous process, the starting material is Z-1336mzz or a mixture of Z-1336mzz and E-1336mzz. In one embodiment, the starting material is Z-1336mzz. In one embodiment, the starting material comprises Z-1336mzz. In one embodiment, the starting material comprises Z-1336mzz and E-1336mzz. The starting material is passed through a reaction vessel containing the catalyst. The reaction vessel can be any time of closed vessel such as, for example, a metal tube. In the gas phase process, the reaction vessel may be packed with the catalyst to form the reaction zone.

The conditions of the reacting step, including the choice of catalyst, are selected to obtain E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene at a selectivity of at least <NUM>%, or at least <NUM>%, or at least <NUM>%.

In some embodiments of this invention, isomerization yield of E-1336mzz is at least <NUM> mole %. In some embodiments of this invention, isomerization yield of E-1336mzz is at least <NUM> mole % or at least <NUM> mole %.

In one embodiment, upon completion of a batch-wise or continuous isomerization process, the E-1336mzz can be recovered through any conventional process, including for example, fractional distillation. In another embodiment, upon completion of a batch-wise or continuous hydrogenation process, the E-1336mzz is of sufficient purity to not require further purification steps.

In certain embodiments, there is unreacted Z-1336mzz in the product. In one such embodiment, unreacted Z-1336mzz can be separated from the product and recycled to the reaction zone for the production of additional E-1336mzz.

The reaction vessel (reactors), distillation columns, and their associated feed lines, effluent lines, and associated units used in applying the processes of embodiments of this invention should be constructed of materials resistant to corrosion. Typical materials of construction include stainless steels, in particular of the austenitic type, the well-known high nickel alloys, such as Monel™ nickel-copper alloys, Hastelloy™ nickel-based alloys and, Inconel™ nickel-chromium alloys, and copper-clad steel.

The various embodiments of each reaction and recovery described above can be used in any combination in the integrated process of the present invention.

Into an Inconel® (<NUM> inch OD) tube was added <NUM> cc of chromium oxide, formed by pressing hydrated chromic oxide powder at <NUM>,<NUM> lb (<NUM>,<NUM>). The resulting mass was crushed and sieved to <NUM>/<NUM> mesh.

The chromium oxide was converted to chromium oxyfluoride and activated as follows. The chromium oxide was heated at <NUM> under <NUM> cc/min of nitrogen flow for <NUM> minutes. Then nitrogen flow was increased to <NUM> cc/min and HF was introduced at <NUM> cc/min for <NUM> minutes. Then the temperature was increased to <NUM> for <NUM> minutes. Then the nitrogen and HF flow were each set to <NUM> cc/min for <NUM> minutes. Then nitrogen flow was lowered to <NUM> cc/min and HF flow was increased to <NUM> cc/min for <NUM> minutes. The nitrogen was then turned off and HF was allowed to flow at <NUM> cc/min. for an additional <NUM> minutes. The temperature of the reactor was then decreased to <NUM> for <NUM> minutes. After activation, the reactor was purged with nitrogen.

A stream of Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene (Z-HFO-1336mzz) preheated at <NUM> was fed into the tube reactor. Part of the reactor effluent was passed through a series of valves and analyzed by GCMS.

In Examples <NUM> and <NUM>, the catalyst was as described above. In Example <NUM>, the gas flow rate of Z-1336mzz fed to the reactor was <NUM> standard cubic centimeters per minute ("sccm"). In Example <NUM>, the gas flow rate of Z-1336mzz fed to the reactor was <NUM> sccm.

In Example <NUM> (Comparative), no catalyst was used. In Example <NUM>, the gas flow rate of Z-1336mzz fed to the reactor was <NUM> sccm.

Reaction temperatures, feed rates and results are listed in Tables <NUM>-<NUM> below.

Claim 1:
A process for isomerizing Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene to E-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene comprising:
(a) providing a starting material comprising Z-<NUM>,<NUM>,<NUM>,<NUM>,<NUM>,<NUM>-hexafluoro-<NUM>-butene;
(b) contacting the starting material with a suitable catalyst in a reaction zone to produce E-HFO-1336mzz; and optionally,
(c) recovering the E-HFO-1336mzz,
wherein the contacting step is performed in the gas phase, and
wherein the suitable catalyst comprises chromium oxyfluoride and contains less than <NUM>% by weight alumina, and
wherein the temperature in the reaction zone is in the range from <NUM> to <NUM>.