COMPOSITIONS OF HFO-1234ZE AND HFO-1234YF AND PROCESSES FOR PRODUCING AND USING THE COMPOSITIONS

Abstract

A fluoropropene composition comprising Z-1,3,3,3-tetrafluoropropene, E-1,3,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene, and optionally 1,1,1,3,3-pentafluoropropane wherein the 2,3,3,3-tetrafluoropropene is present in an amount of 0.001 to 1.0%. A method for producing the fluoropropene, methods for using the fluoropropene, and the resulting composition are also described.

Description

FIELD OF INVENTION The present invention relates to tetrafluoropropene compositions and methods for manufacturing and using the compositions and, in particular, to a method for producing and using a product comprising 1,3,3,3-tetrafluoropropene (HFO-1234ze) and 2,3,3,3-tetrafluoropropene (HFO-1234yf) prepared from 1,1,1,3,3-pentafluoropropane (HFC245fa). BACKGROUND OF THE INVENTION The fluorocarbon industry has been working for decades to find replacement refrigerants to phase out ozone-depleting chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs), as a result of the Montreal Protocol. The solution for many applications has been the commercialization of hydrofluorocarbon (HFC) compounds for use as refrigerants, solvents, fire extinguishing agents, blowing agents, and propellants. These newer compounds, such as the HFC refrigerants HFC-134a and HFC-125, which are the most widely used at present, have zero ozone depletion potential and are therefore not Ref. 316179 affected by the current regulatory progressive reduction as a result of the Montreal Protocol. In addition to ozone depletion concerns, global warming is another environmental concern in many of these applications. Therefore, there is a need for compositions that meet low ozone depletion standards and have a low global warming potential. Certain hydrofluoroolefin compositions are believed to meet both objectives. Consequently, there is also a need for cost-effective manufacturing processes that yield these compositions. HFO-1234ze (CF3CH=CHF) and HFO-1234yf (CF3CF=CH2), which are non-ozone-depleting and have a low global warming potential, have been identified as potential refrigerants. U.S. Patent No. 7,862,742 describes compositions comprising HFO-1234ze and HFO-1234yf. U.S. Patent No. 9,302,962 describes methods for manufacturing HFO-1234ze. The descriptions in U.S. Patent No. 7,862,742 and U.S. Patent No. 9,302,962 are incorporated herein by reference. The catalytic dehydrofluorination of HFC-245fa generally produces a mixture of the E and Z isomers of HFC-1234ze. Depending on the specific catalyst chosen, the amount of the Z isomer can vary from 15% to 23%. Liquid-phase dehydrofluorination using aqueous solutions of caustics or other strong bases also produces a mixture of both isomers. Although the ratio of the two isomers can shift slightly with temperature, approximately 13% to 15% of the Z isomer is typically formed. Since the E isomer is the most useful for refrigeration applications, after separating the E isomer from the Z isomer, the Z isomer is typically isomerized to the E isomer in a separate step, or it is converted back to 245fa by the addition of hydrogen fluoride. Both alternatives require additional steps that add to the cost. There is a need in this technique for a process capable of producing near-azeotropic compositions of HFO-1234ze and HFO-1234yf that minimizes or eliminates the need for purification or separation steps to remove excessive amounts of HFO-1234yf. Specifically, there is a need in this technique for an economical process that produces near-azeotropic compositions comprising HFO-1234ze and more than zero and less than approximately 1 percent by weight of HFO-1234yf. BRIEF DESCRIPTION OF THE INVENTION A fluoropropene composition is described comprising Z1,3,3,3-tetrafluoropropene, El,3,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene, and optionally 1,1,1,3,3-pentafluoropropane. The 2,3,3,3-tetrafluoropropene is present in an amount of 0.001 to 1.0 mol%. Furthermore, the present description includes a method for producing a mixture of a fluoropropene of formula CF3CH=CHF and a fluoropropene of formula CF3CF=CH2, comprising contacting a gas-phase mixture of 1,1,1,3,3-pentafluoropropane and Z1,3,3,3-tetrafluoropropene with a catalyst comprising at least one catalyst selected from the group consisting of fluorinated Cr2O3 or Cr / Ni on fluorinated alumina, in the presence of an oxygen-containing gas, to form a mixture comprising Z-1,3,3,3-tetrafluoropropane, El,3,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene, and optionally unreacted 1,1,1,3,3-pentafluoropropane. One embodiment of the method of the invention produces a useful composition without the need for purification or separation steps that include steps to remove excessive amounts of 2,3,3,3-tetrafluoropropene (HFO-1234yf). Furthermore, the present description includes fluoropropene compositions formed from the method of contacting a gas-phase mixture of 1,1,1,3,3-pentafluoropropane and Z1,3,3,3-tetrafluoropropene with a catalyst comprising at least one catalyst selected from the group consisting of fluorinated Cr2O3 or Cr / Ni in fluorinated alumina, optionally in the presence of an oxygen-containing gas. In one embodiment, the process of the invention produces a near-azeotropic composition comprising HFO-1234ze (E) and HFO1234yf, and the azeotropic composition is useful as a refrigerant. One modality relates to any combination of the above, where 2,3,3,3-tetrafluoropropene is present in an amount of 0.01 to 1.0 molar %. One modality relates to any combination of the above, where 2,3,3,3-tetrafluoropropene is present in an amount of 0.1 to 0.9 molar %. One modality relates to any combination of the above, where 2,3,3,3-tetrafluoropropene is present in an amount of 0.2 to 0.4 molar percent. One modality relates to any combination of the above, where 2,3,3,3-tetrafluoropropene is present in an amount of 0.3 to 0.4 molar. One modality relates to any combination of the above, wherein the fluoropropene composition optionally comprises one or more of R-143a, R-152a, TFP (trifluoropropyne), R-1233xf, R-1233zd(E) or R-1233zd(Z). One modality relates to any combination of the above, wherein the sum total of the amounts of R143a, R-152a, TFP, R-1233xf, R-1233zd(E) and R-1233zd(Z) is between 0.001 mol% and 2 mol%, based on the total fluoropropene composition. One modality relates to any combination of the above, wherein the fluoropropene composition includes R-1233zd(E) in an amount of 0.7 mol% to 1.15 mol%, based on the total fluoropropene composition. One modality relates to any combination of the above, wherein the fluoropropene composition includes R-1233zd(Z) in an amount of 0.05 mol% to 0.25 mol%, based on the total fluoropropene composition. One modality relates to any combination of the above, wherein the fluoropropene composition includes R-143a in an amount of 0.05 mol% to 0.25 mol%, based on the total fluoropropene composition. One modality relates to any combination of the above, wherein the fluoropropene composition optionally comprises one or more of 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa and HFC-245cb. One modality relates to any combination of the above, wherein the sum total of the amounts of 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa and HFC-245cb is between 0.001 molar percent and 2 molar percent, based on the total fluoropropene composition. One modality relates to any combination of the above, where the composition is almost azeotropic. Another embodiment of the invention relates to a method for producing a fluoropropene mixture of formula CF3CH=CHF and a fluoropropene of formula CF3CF=CH2, comprising: Contacting a gas-phase mixture of 1,1,1,3,3-pentafluoropropane and Z1,3,3,3-tetrafluoropropene with a catalyst comprising at least one catalyst selected from the group consisting of fluorinated Cr2O3 or Cr / Ni on fluorinated alumina, in the presence of an oxygen-containing gas, to form a mixture comprising Z1,3,3,3-tetrafluoropropene, Z1,3,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene, hydrogen fluoride, and optionally unreacted 1,1,1,3,3-pentafluoropropane wherein the mixture includes 0.01% to 1.00% of 2,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing wherein the mixture of 1,1,1,3,3-pentafluoropropane and Z1,3,3,3-tetrafluoropropene comprises at least 7% by weight of Z-1,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination thereof, wherein the mixture of 1,1,1,3,3-pentafluoropropane and Z1,3,3,3-tetrafluoropropene comprises at least 10% by weight of Z1,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing wherein at least 94% by weight of 1,1,1,3,3-pentafluoropropane is converted to the E isomer of 1,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing, wherein at least 98% by weight of 1,1,1,3,3-pentafluoropropane is converted to the E isomer of 1,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing and further comprises recovering Z1,3,3,3-tetrafluoropropene, or a mixture of Z1,3,3,3-tetrafluoropropene and 1,1,1,3,3-pentafluoropropane, and recycling Z1,3,3,3-tetrafluoropropene, or a mixture of Z1,3,3,3-tetrafluoropropene and 1,1,1,3,3-pentafluoropropane back to step (a). One embodiment of the invention relates to any combination of the foregoing wherein the hydrogen fluoride produced in step (a) is separated and recovered. One embodiment of the invention relates to any combination of the foregoing, wherein the oxygen-containing gas is either oxygen or air. One embodiment of the invention relates to any combination of the foregoing wherein the mixture includes 0.1 to 0.5 mol% of 2,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing wherein the mixture includes 0.2 to 0.4 mol% of 2,3,3,3-tetrafluoropropene. One embodiment of the invention relates to any combination of the foregoing wherein the mixture includes 0.3 to 0.4 mol % 2,3,3,3-tetrafluoropropene. Another embodiment of the invention relates to any combination of the above methods and to a fluoropropene composition produced by these methods. One embodiment of the invention relates to a process for transferring heat, comprising: provide an article; to put the item in contact with a heat transfer medium; wherein the heat transfer medium comprises the fluoropropene composition of any combination of the above embodiments and includes a near-azeotropic composition produced by the method of the invention. Another embodiment of the invention relates to a process for treating a surface, comprising: provide a surface; to put the surface in contact with a treatment composition; characterized in that the surface includes a treatable material deposited thereon; and wherein the treatment composition comprises the fluoropropene composition of any combination of the above modalities. One embodiment of the invention relates to any combination of the foregoing, wherein the treatment composition substantially dissolves the treatable material. / UU One embodiment of the invention relates to a process for forming a composition comprising: provide a solute; bring the solute into contact with a solvent; wherein the solvent comprises the fluoropropene composition of any of the above forms. One embodiment of the invention relates to a refrigeration system, comprising: an evaporator; a condenser; a compressor; an expansion device; and a heat transfer medium; wherein the heat transfer medium comprises the fluoropropene composition of any combination of the above embodiments and includes a near-azeotropic composition produced by the method of the invention. The foregoing general description and the following detailed description are illustrative and explanatory only and do not limit the invention as defined in the appended claims. The various embodiments of the invention may be used alone or in combination with each other. Other features and advantages of the present invention will become apparent from the following detailed description of the preferred embodiment, which illustrates, by way of example, the principles of the invention. / UU DETAILED DESCRIPTION OF THE INVENTION A method is described for producing a mixture of a fluoropropene of formula CF3CH=CHF and a fluoropropene of formula CF3CF=CH2, comprising contacting a gas-phase mixture of 1,1,1,3,3-pentafluoropropane and Z-,1,3,3,3-tetrafluoropropene with a catalyst comprising at least one catalyst selected from the group consisting of fluorinated Cr2O3 or Cr / Ni on fluorinated alumina, optionally in the presence of an oxygen-containing gas, to form a mixture comprising Z1,3,3,3-tetrafluoropropene, 11,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene and, optionally, unreacted 1,1,1,3,3-pentafluoropropane. Certain dehydrofluorination reactions are well known in the art. The dehydrofluorination of HFC-245fa has been particularly studied. Both gas-phase and liquid-phase processes are known. 1,3,3,3-tetrafluoropropene (HFO-1234ze) exists as a Z isomer and an E isomer around the double bond. Both gas-phase and liquid-phase processes are known to produce a mixture of both the Z and E isomers, with the E isomer predominating. The selectivity for the production of the Z isomer can vary from approximately 10% to approximately 23%, depending on the temperature and the choice of catalyst. The boiling point of the E isomer at 1 atm is approximately -19 °C, while the boiling point of the Z isomer is approximately 9 °C. For many applications, the E isomer is preferred.To minimize performance losses in the form of the generally undesirable Z isomer, it becomes necessary to add an isomerization step to isomerize the Z isomer to the E isomer, or to add a fluorination step to convert HFO1234ze(Z) back to HFC-245fa. The dehydrofluorination reaction according to the modalities described herein can result in azeotropic and, in most cases, near-azeotropic compositions of HFO-1234ze(E) and HFO-1234yf, minimizing or eliminating the need for purification or separation steps to remove excessive amounts of HFO-1234yf. An azeotropic composition is a constant-boiling mixture of two or more substances that behave as a single substance. One way to characterize an azeotropic composition is that the vapor produced by partial evaporation or distillation of the liquid has the same composition as the liquid from which it is evaporated or distilled (i.e., the mixture is distilled / refluxed without any change in composition).Constant-boiling compositions are defined as azeotropic because they exhibit a maximum or minimum boiling point compared to the boiling point of the non-azeotropic mixture of the same compounds. An azeotropic composition will not fractionate within an operating refrigeration or air conditioning system. Furthermore, an azeotropic composition will not fractionate when filtered from a refrigeration or air conditioning system. When a component of a mixture is flammable, fractionation during filtration could render the composition flammable either inside or outside the system. A near-azeotropic composition is a substantially constant boiling-point mixture of two or more compounds that behave essentially as a single substance. One way to characterize a near-azeotropic composition is that the vapor produced by partial evaporation or distillation of the liquid has substantially the same composition as the liquid from which it is evaporated or distilled; that is, the mixture is distilled / refluxed without a substantial change in composition. Another way to characterize a near-azeotropic composition is that the bubble-point vapor pressure and the dew-point vapor pressure of the composition at a particular temperature are substantially equal.In particular, a composition of the invention is nearly azeotropic if, after removing 50 percent (50%) of the composition, such as by evaporation or boiling, the difference in vapor pressure between the original composition and the composition remaining after 50 percent of the original composition has been removed is less than approximately 10 percent (10%). IVIA / a / ¿U¿ I / UUJDU¿ According to one embodiment of the present invention, the near-azeotropic compositions of the invention have a flammability classification of A2L as determined by ASHRAE 34 and ASTM E681-09 standards. The various aspects and embodiments described above are merely illustrative and not limiting. After reading this description, those skilled in the art will understand that other aspects and embodiments are possible without departing from the scope of the invention. Other features and benefits of any modality or modalities will be better understood with the following detailed description and with the claims. Certain dehydrofluorination reactions are known in the art and are preferably carried out in the vapor phase. The dehydrofluorination reaction can be performed in any suitable reaction vessel or reactor, but it should preferably be constructed from materials resistant to the corrosive effects of hydrogen fluoride, such as nickel and its alloys, including Hastelloy, Monel, and Inconel, or vessels lined with fluoropolymers. These can be single-tube or multi-tube vessels filled with a dehydrofluorination catalyst. Useful catalysts for the process include chromium-based catalysts, such as fluorinated chromium oxide. This catalyst may be unsupported or supported on a support, such as activated carbon, graphite, graphite fluoride, or aluminum fluoride. The chromium catalyst may be used alone or in the presence of a cocatalyst selected from a nickel, cobalt, manganese, or zinc salt. In one embodiment, a chromium catalyst is large surface area chromium oxide or chromium / nickel on aluminum fluoride (Cr / Ni / AlFa), the preparation of which is reported in European Patent No. EP486,333. In another embodiment, the catalyst is a fluorinated Guignet green catalyst. Other suitable catalysts include, but are not limited to, JM 62-2 (chromium catalyst available from Johnson Matthey), LV (chromium catalyst available from Chemours), JM-62-3 (chromium catalyst available from Johnson Matthey) and Newport Chrome (chromium catalyst available from Chemours).Preferably, chromium catalysts are activated prior to use, typically by a procedure whereby the catalyst is heated to 350°C to 400°C under a flow of nitrogen for a period of time, after which the catalyst is heated under a flow of HE and nitrogen or air for a further period of time. In one embodiment, the Guignet green of the fluoride-activated Guignet green catalyst used in the present invention is prepared by reacting (melting) boric acid with an alkali metal dichromate between 500°C and 800°C, followed by hydrolysis of the reaction product, whereby Guignet green contains boron, an alkali metal, and water of hydration. The usual alkali metal dichromates are sodium and / or potassium dichromates. The reaction is typically followed by the steps of cooling the reaction product in air, grinding this solid to produce a powder, followed by hydrolysis, filtration, drying, milling, and sieving. Guignet green is blue-green, but it is primarily known as a green pigment, hence the pigment is commonly called Guignet green. When used as a catalyst, it is also called Guignet green, as described in U.S. Patent No. 3,413,363. In U.S. patent no.6,034,289, the Cr2O3 catalysts are preferably described in the alpha form, and Guignet green is also described as a commercially available green pigment having the composition: Cr2Os 79-83%, H2O 16-18%, B2O5 1.5 to 2.7% (bridging phrases in columns 2 and 3) that can be converted to the alpha form (column 3, I. 3). U.S. Patent No. 7,985,884 recognizes the presence of alkali metal in Guignet green in the Guignet green composition described in Example 1: 54.5% Cr, 1.43% B, 3400 ppm Na, and 120 ppm K. The physical form of the catalyst is not critical and may include, for example, pellets, extruded products, powders, or granules. Preferably, fluoride activation of the catalyst is carried out in its final form. In one embodiment, the present invention relates to feeding a mixture of HFC-245fa and at least approximately 10 wt% of the Z isomer of HFO-1234ze to a dehydrofluorination reactor in the presence of an oxygen-containing gas to suppress the formation of additional Z isomer, such that the HFC-245fa converted by dehydrofluorination produces substantially only E-HFO-1234ze and HFO-1234yf. A feed of less than approximately 10 wt% will produce some suppression of the formation of additional Z-1234ze. A feed of more than approximately 10 wt% Z-1234ze simply results in the presence of additional material that must be separated and recycled. The amount of Z-1234ze required to suppress the additional formation of the Z isomer product depends to some extent on the conversion. At a 70% conversion of 245fa, approximately 1011% Z isomer is required in the feed.At a conversion of 80%, approximately 13% of the Z isomer is required in the feed. In one embodiment, the reaction vessel can be maintained at a temperature between 200 °C and 375 °C. In another embodiment, the reaction vessel can be maintained at a temperature between 250 °C and 350 °C. In yet another embodiment, the reaction vessel can be maintained at a temperature between 275 °C and 325 °C. znornn / Lznz / Bm The reaction pressure can be subatmospheric, atmospheric, or superatmospheric. In one configuration, the reaction takes place at a pressure of approximately 14 psig (0.98 kg / cm²) to approximately 100 psig (7.03 kg / cm²). In another configuration, the reaction takes place at a pressure of 14 psig (0.98 kg / cm²) to approximately 60 psig (4.21 kg / cm²). In yet another configuration, the reaction takes place at a pressure of 40 psig (2.81 kg / cm²) to approximately 85 psig (5.97 kg / cm²). In yet another configuration, the reaction takes place at a pressure of 50 psig (3.51 kg / cm²) to 75 psig (5.27 kg / cm²). Generally, increasing the pressure in the reactor above atmospheric pressure will increase the contact time of the reactants in the process. Longer contact times will necessarily increase the degree of conversion in a process, without having to increase the temperature. Depending on the reactor temperature and contact time, the reactor product mixture will contain varying amounts of unreacted HFC-245fa. In one embodiment, 1,3,3,3-tetrafluoropropene and HFO-1234yf can be separated from the unreacted 1,3,3,3-tetrafluoropropene, hydrogen fluoride, and HFC-245fa, which are then recycled back to the reactor with additional HFC-245fa. The hydrogen fluoride can be removed by scrubbing, by passing the reactor effluent through an aqueous caustic solution, or by distillation. In particularly suitable embodiments, the composition formed from the process described herein includes 1,3,3,3-tetrafluoropropene (HFO-1234ze(E)) and 2,3,3,3-tetrafluoropropene (HFO-1234yf), which are not separated. In one embodiment, the reactor feed is preheated in a vaporizer to a temperature of approximately 30 °C to approximately 100 °C. In another embodiment, the reactor feed is preheated in a vaporizer to a temperature of approximately 30 °C to approximately 80 °C. In some embodiments, an inert diluent gas is used as the carrier gas for the hydrochlorofluoropropane. In one embodiment, the carrier gas is selected from nitrogen, argon, helium, or carbon dioxide. In one modality the product mix includes (in a molar base) s mtre 0. . 0.1% to 1.00% of HFO-1234yf, alternatively between 0.05% and 0.95% of HFO-1234yf, alternatively between 0.10% and 0.90% of HFO-1234yf, alternatively between 0.20% and 0.80% of HFO-1234yf, alternatively between 0.01% and 0.20% of HFO-1234yf, alternatively between 0.10% and 0.30% of HFO-1234yf, alternatively between 0.20% and 0.40% of HFO-1234yf, alternatively between 0.30% and 0.50% of HFO-1234yf, alternatively between 0.30% and 0.40% of HFO-1234yf, alternatively between 0.40% to 0.60% of HFC-1234yf, alternatively between 0.50% to 0.70% of HFO-1234yf, alternatively between 0.60% to 0.80% of HFO-1234yf, alternatively between 0.70% to 0.70% of HFO-1234yf, alternatively between 0.80% to 1.00% of HFO-1234yf. In some embodiments, the fluoropropene composition optionally also comprises one or more of R-143a, R-152a, TFP, R-1233xf, R-1233zd(E), or R-1233zd(Z). In some embodiments, the sum total of the amounts of R-143a, R-152a, TFP, R-1233xf, R-1233zd(E), and R-1233zd(Z) is between 0.01 mol% and 2 mol%, based on the total fluoropropene composition. In one embodiment, the fluoropropene composition includes R-1233zd(E) in an amount of 0.7 mol% to 1.15 mol%, based on the total heat transfer medium. In one embodiment, the fluoropropene composition includes R-1233zd(Z) in an amount of 0.05 mol% to 0.25 mol%, based on the total heat transfer medium. In one embodiment, the fluoropropene composition includes R-143a in an amount of 0.05 mol% to 0.25 mol%, based on the total fluoropropene composition. In other embodiments, the fluoropropene composition optionally comprises one or more of 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa and HFC-245cb. / UU In one particular form, the sum total of the amounts of 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa and HFC-245cb is between 0.001 molar percent and 2 molar percent, based on the total fluoropropene composition. Fluoropropene compositions can be useful in several applications. In one embodiment, fluoropropene compositions can be used as refrigerants. In some embodiments, fluoropropene compositions can be used as replacements for older generation refrigerants (e.g., R404A, R502) to provide a more environmentally compatible composition. In some embodiments, fluoropropene compositions can be hydrofluoroolefin compositions. In one embodiment, the fluoropropene composition includes 99 mol% to 99.99 mol% of 1,3,3,3-tetrafluoropropene (HFO-1234ze)(E) and 0.01 mol% to 1.0 mol% of 2,3,3,3-tetrafluoropropene (HFO-1234yf). In another embodiment, the fluoropropene composition is a near-azeotropic composition that is substantially free of HFO-1234ze(Z).Substantially free means that the fluoropropene composition contains less than approximately 1000 ppm, less than approximately 500 ppm, and typically less than approximately 100 ppm of HFO-1234ze(Z). In one embodiment, the fluoropropene compositions of the invention can be mixed with other fluorochemicals. This embodiment of the present invention relates to a refrigerant composition comprising the almost azeotropic composition of the invention (e.g., HFO-1234ze(E) and HFO1234yf) and at least one compound selected from the group consisting of: HFC-1234ye, HFC-1243zf, HFC-32, HFC-125, HFC-134, HFC-134a, HFC-143a, HFC-152a, HFC-161, HFC-227ea, HFC-236ea, HFC-236fa, HFC-245fa, HFC-365mfc, propane, n-butane, isobutane, 2-methylbutane, n-pentane, cyclopentane, dimethyl ether, CF3SCF3, CO2, CF3I and combinations thereof. In some embodiments, the fluoropropene composition may be used in a refrigeration system. One embodiment of a refrigeration system includes an evaporator, a condenser, a compressor, an expansion device, and a heat transfer medium. The heat transfer medium includes the fluoropropene composition. The heat transfer medium may further comprise at least one lubricant, including those suitable for use with refrigeration or air conditioning equipment. These lubricants include those conventionally used in compression refrigeration equipment that uses chlorofluorocarbon refrigerants. These lubricants and their properties are discussed in the 1990 ASHRAE Handbook, Refrigeration Systems and Applications, Chapter 8, entitled "Lubricants in Refrigeration Systems," pages 8.1 to 8.21, incorporated herein by reference.The lubricants of the present invention may include what are commonly referred to as mineral oils in the field of compression refrigeration lubrication. Mineral oils comprise paraffins (i.e., saturated hydrocarbons with straight and branched carbon chains), naphthenes (i.e., saturated hydrocarbons with cyclic or ring structures, which may be paraffins), and aromatics (i.e., unsaturated cyclic hydrocarbons containing one or more rings characterized by alternating double bonds). The lubricants of the present invention further include what are commonly referred to as synthetic oils in the field of compression refrigeration lubrication. Synthetic oils comprise alkylaryls (i.e., linear or branched alkylbenzenes), synthetic paraffins and naphthenes, silicones, and poly-alpha-olefins.Representative conventional lubricants of the present invention are commercially available BVM 100 N (paraffinic mineral oil sold by BVA Oils), commercially available naphthenic mineral oil under the trademarks Suniso® 3GS and Suniso® 5GS from Crompton Co., commercially available naphthenic mineral oil from Pennzoil under the trademark Sontex® 372LT, commercially available naphthenic mineral oil from Calument Lubricants under the trademark Calumet® RO-30, commercially available linear alkylbenzenes from Shrieve Chemicals under the trademarks Zerol® 75, Zerol® 150 and Zerol® 500, and branched alkylbenzene sold by Nippon Oil as HAB 22. In one embodiment, the lubricating component may comprise those that have been designed for use with refrigerants and are miscible with the fluoropropene compositions (e.g., near-azeotropic compositions) of the present invention under the operating conditions of refrigeration and air-compression equipment. Such lubricants and their properties are described in Synthetic Lubricants and High-Performance Fluids, R.L. Shubkin, editor, Marcel Dekker, 1993. Such lubricants include, but are not limited to, polyol esters (POE), such as Castrol® 100 (Castrol, UK), polyalkylene glycols (PAG), such as RL-488A from Dow (Dow Chemical, Midland, Michigan), and polyvinyl ethers (PVE). The lubricants of the present invention are selected considering the requirements of a given compressor and the environment to which the lubricant will be exposed. The amount of lubricant can vary from approximately 1 to approximately 50, from approximately 1 to approximately 20, and in some cases from approximately 1 to approximately 3 percent by weight of the refrigerant composition. In one particular embodiment, the above refrigerant compositions are combined with a PAG lubricant for use in an automotive air conditioning system having an internal combustion engine. In another particular embodiment, the above refrigerant compositions are combined with a POE lubricant for use in an automotive air conditioning system having an electric or hybrid drivetrain. In one embodiment, a refrigerant composition comprising the near-azeotropic composition of the invention, at least one lubricant, and at least one additive that can improve the service life of the refrigeration and air conditioning system and the durability of the compressor is preferred. In one aspect of the invention, the above refrigerant compositions comprise at least one member selected from the group consisting of acid scrubbers, performance enhancers, and flame suppressants. In another embodiment, the fluoropropene composition can be used in a process to transfer heat. The process may include providing an article and bringing the article into contact with a heat transfer medium that includes the fluoropropene composition. In some embodiments, the article may include electrical equipment (e.g., circuit board, computer, visor, semiconductor chip, or transformer), a heat transfer surface (e.g., heat sink), or an article of clothing (e.g., a leotard). In another embodiment, the fluoropropene composition can be used in a process to treat a surface. The process may involve providing a surface with a treatable material deposited on it and contacting the surface with a treatment composition that includes the fluoropropene composition. In some embodiments, the treatment composition can substantially dissolve the treatable material. In another embodiment, the fluoropropene composition can be used in a process to form a composition. The process includes providing a solute and contacting the solute with a solvent that includes the fluoropropene composition. In some embodiments, the fluoropropene composition can substantially dissolve the solute. In another embodiment, the present invention relates to blowing agent compositions comprising fluoroolefin-containing compositions (e.g., compositions containing near-azeotropes), as described herein, for use in the preparation of foams. In other embodiments, the invention provides foaming compositions and, preferably, polyurethane and polyisocyanate foam compositions, and a method for preparing foams. In the foam embodiments, one or more fluoroolefin-containing compositions of the present description are included as blowing agents in foaming compositions, and the composition preferably includes one or more additional components that can react and foam under suitable conditions to form a foam or cellular structure.Any of the methods known in the art, such as those described in Polyurethanes Chemistry and Technology, Volumes I and II, Saunders and Frisch, 1962, John Wiley and Sons, New York, NY, which are incorporated herein by reference, may be used or adapted for use in accordance with the foaming modalities of the present invention. The present invention further relates to a method for forming a foam comprising: (a) adding to a foamable composition a fluoroolefin-containing composition of the present invention; and (b) reacting the foamable composition under conditions effective to form a foam. Another embodiment of the present invention relates to the use of the fluoroolefin-containing compositions as described herein (e.g., nearly azeotropic compositions of HFO-1234ze(E) and HFO-1234yf) as propellants in sprayable compositions. Furthermore, the present invention relates to a sprayable composition comprising the fluoroolefin-containing compositions as described herein. A sprayable composition may also include the active ingredient to be sprayed together with inert ingredients, solvents, and other materials. Preferably, the sprayable composition is in aerosol form. / UU Suitable active materials to be atomized include, but are not limited to, cosmetic materials such as deodorants, perfumes, hairsprays, cleansers and polishing agents in addition to medicinal materials, for example, asthma medications and halitosis remedies. The present invention also relates to a process for producing aerosol products comprising the step of adding a fluoroolefin-containing composition as described herein to active ingredients in an aerosol container, wherein the composition acts as a propellant. As used herein, the terms comprise, which comprises, include, which includes, has, which has, or any variant thereof are intended to encompass a non-exclusive inclusion. For example, a process, method, article, or apparatus comprising a list of elements is not necessarily limited to those elements alone, but may include other elements not expressly listed or inherent in that process, method, article, or apparatus. Furthermore, unless expressly stated otherwise, the disjunction "or" refers to an inclusive "or" and not an exclusive "or." For example, a condition A or B is met by any of the following criteria: A is true (or present) and B is false (or not present), A is false (or not present) and B is true (or present), and both A and B are true (or present). The transition phrase "consists of" excludes any unspecified element, stage, or ingredient. If it appears in the claim, it would close the claim to include materials other than those mentioned, except for impurities normally associated with them. When the phrase "consists of" appears in a clause within the body of a claim, rather than immediately following the preamble, it limits only the element described in that clause; other elements are not excluded in accordance with the claim as a whole.The transitional phrase "essentially consisting of" is used to define a composition or method that includes materials, steps, features, components, or elements, in addition to those literally described, provided that these additional materials, steps, features, components, or elements do not materially affect the basic or novel feature(s) of the claimed invention, especially the mode of action for achieving the desired result of any of the processes of the present invention. The term "essentially consisting of" occupies an intermediate position between "comprising" and "consisting of." In the above combinations of the embodiments of the invention, the quasi-azeotropic compositions may comprise, consist essentially of, or consist of HFO1234ze(E) and HFO-1234yf. Furthermore, "one" or "an" are used to describe elements and components included in this description. This is done solely for convenience and to give a general sense of the scope of the present invention. This description should be interpreted as including one or at least one, and the singular should also include the plural, unless it is obvious that it is intended to denote otherwise. Unless otherwise defined, all scientific and technical terms used herein have the same meaning as commonly understood by a person skilled in the art to which this invention pertains. While methods and materials similar to or equivalent to those described herein may be used in the practice or testing of embodiments of the present invention, suitable methods and materials are described below. All publications, patent applications, patents, and other references mentioned herein are fully incorporated by reference, unless a specific passage is cited. In case of conflict, this description, including the definitions, shall prevail. Furthermore, the materials, methods, and examples are for illustrative purposes only and are not intended to be limiting. EXAMPLES The concepts described in this description will be described in more detail in the following examples, which do not limit the scope of the invention described in the claims. Example 1 Example 1 shows the dehydrofluorination of 245fa on Cr2Os in the presence of Z-HFC-1234ze. An Inconel tube (1 / 2 inch OD (1.27 cm)) was filled with 10 cc (8 g) of Cr₂U₃ catalyst (Johnson Mathey) prepared as follows: Chromium oxide in extruded form, which was crushed and sieved to 12 / 20 mesh. After loading the reactor tube, the catalyst bed temperature was raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow was then reduced to 60 cc / min, and HF was fed at 20 cc / min for 60 minutes. The temperature was then increased to 325 °C for 300 minutes. The nitrogen flow was reduced to 30 cc / min, and the HF flow was increased to 30 cc / min for 30 minutes. Next, the nitrogen flow rate was reduced to 12 cc / min and the HF flow rate was increased to 48 cc / min for 60 minutes. Then, the nitrogen flow rate was discontinued and the HF flow rate was increased to 48 cc / min for 30 minutes. The reactor temperature was decreased to 250 °C for 30 minutes.The HF flow was then shut off, and the reactor was purged with nitrogen at a rate of 30 mL / min. The reactor temperature was then stabilized at 300 °C, the nitrogen flow was shut off again, and CF3CH2CHF2, or CF3CH2CHF2 with varying amounts of Z-1234ze, was fed at a rate of 1.44 mL / h. The contact time in the reactor was 45 seconds. The CF3CH2CHF2 was vaporized at 50 °C. A portion of the reactor effluent was passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 245fa, and E-1234ze are expressed as molar percentages. The results are summarized in Table 1. Table 1 % of Z-ze added 0 7.5 10.9 Incoming compounds 100 / 0 92.5 / 7.5 89 / 11 245fa conversion (%) 71.2 69.3 72 Z-ze in product (%) 10.7 10.3 11.2 % of 245fa recovered 28.8 28.4 24.9 % of E-ze 60.5 60.3 63.9 % of E-ze yield 60.5 65.3 71.7 % of E-ze selectivity 85 94.2 99.7 Example 2 Example 2 shows the dehydrofluorination of 245fa on Cr2O3 in the presence of Z-HFC-1234ze. An Inconel tube (OD of h inch (1.27 cm)) was filled with 10 cc (8 g) of Cr₂O₃ catalyst (Guignet's green) prepared as follows: Chromium oxide in the form of an extruded product, which was crushed and sieved to 12 / 20 mesh. After loading the reactor tube, the catalyst bed temperature was raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow was then reduced to 60 cc / min, and HF was fed at 20 cc / min for 60 minutes. The temperature was then increased to 325 °C for 300 minutes. Finally, the nitrogen flow was reduced to 30 cc / min, and the HF flow was increased to 30 cc / min for 30 minutes. Next, the nitrogen flow rate was reduced to 12 cc / min and the HF flow rate was increased to 48 cc / min for 60 minutes. Then, the nitrogen flow rate was discontinued and the HF flow rate was increased to 48 cc / min for 30 minutes. The reactor temperature was decreased to 250 °C for 30 minutes.The HF flow was then shut off, and the reactor was purged with nitrogen at a rate of 30 mL / min. The reactor temperature was then stabilized at 300 °C, the nitrogen flow was shut off again, and CF3CH2CHF2, or CF3CH2CHF2 with varying amounts of Z-1234ze, was fed at a rate of 1.44 mL / h. The contact time in the reactor was 45 seconds. The CF3CH2CHF2 was vaporized at 50 °C. A portion of the reactor effluent was passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 245fa, and E-1234ze are expressed as molar percentages. The results are summarized in Table 2. Table 2 % of Z-ze added 0 10.9 Incoming compounds 100 / 0 89 / 11 245fa conversion (%) 69.9 71.8 Z-ze in product (%) 10.7 10.9 % of 245fa recovered 30.1 25.1 % of E-ze 59.2 64 % of E-ze yield 59.2 71.9 % of E-ze selectivity 84.7 100 Example 3 Example 3 demonstrates the dehydrofluorination of 245fa on Cr2O3 in the presence of Z-HFC-1234ze. An Inconel tube (1.27 cm (µin) OD) was filled with 10 cc (8 g) of Cr₂O₃ catalyst (Johnson Mathey) prepared as follows: Chromium oxide in extruded form, which was crushed and sieved to 12 / 20 mesh. After loading the reactor tube, the catalyst bed temperature was raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow was then reduced to 60 cc / min, and HF was fed at 20 cc / min for 60 minutes. The temperature was then increased to 325 °C for 300 minutes. The nitrogen flow was reduced to 30 cc / min, and the HF flow was increased to 30 cc / min for 30 minutes. Next, the nitrogen flow rate was reduced to 12 cc / min and the HF flow rate was increased to 48 cc / min for 60 minutes. Then, the nitrogen flow rate was discontinued and the HF flow rate was increased to 48 cc / min for 30 minutes. The reactor temperature was decreased to 250 °C for 30 minutes.The HF flow was then shut off, and the reactor was purged with nitrogen at a rate of 30 mL / min. The reactor temperature was then stabilized at 300 °C, the nitrogen flow was shut off again, and CF3CH2CHF2, or CF3CH2CHF2 with varying amounts of Z1234ze, was fed at a rate of 1.44 mL / h. The contact time in the reactor was 45 seconds. The CF3CH2CHF2 was vaporized at 50 °C. A portion of the reactor effluent was passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 245fa, and E1234ze are expressed as molar percentages. The results are summarized in Table 3. Table 3 % of Z-ze added 0 10.9 Incoming compounds 100 / 0 89 / 11 245fa conversion (%) 73 71.3 Z-ze in product (%) 11.4 11.0 % of 245fa recovered 27.0 25.5 % of E-ze 61.6 63.5 % of E-ze yield 61.6 72.5 % of E-ze selectivity 84 100 Example 4 Example 4 shows the dehydrofluorination of 245fa on Cr2O3 in the presence of Z-HFC-1234ze. An Inconel tube (1.27 cm OD) was filled with 10 cc (8 g) of Cr₂O₃ (Newport Cr) catalyst prepared as follows: chromium oxide in extruded form, which was crushed and sieved to 12 / 20 mesh. After loading the reactor tube, the catalyst bed temperature was raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow was then reduced to 60 cc / min, and HF was fed at 20 cc / min for 60 minutes. The temperature was then increased to 325 °C for 300 minutes. Finally, the nitrogen flow was reduced to 30 cc / min, and the HF flow was increased to 30 cc / min for 30 minutes. Next, the nitrogen flow rate was reduced to 12 cc / min and the HF flow rate was increased to 48 cc / min for 60 minutes. Then, the nitrogen flow rate was discontinued and the HF flow rate was increased to 48 cc / min for 30 minutes. The reactor temperature was decreased to 250 °C for 30 minutes.The HF flow was then shut off, and the reactor was purged with nitrogen at a rate of 30 mL / min. The reactor temperature was then stabilized at 300 °C, the nitrogen flow was shut off again, and CF3CH2CHF2, or CF3CH2CHF2 with varying amounts of Z-1234ze, was fed at a rate of 1.44 mL / h. The contact time in the reactor was 45 seconds. The CF3CH2CHF2 was vaporized at 50 °C. A portion of the reactor effluent was passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 245fa, and E-1234ze are expressed as molar percentages. The results are summarized in Table 4. / UU Table 4 % of Z-ze added 0 10.7 Incoming compounds 100 / 0 89.3 / 10.7 245fa conversion (%) 72.2 70.2 Z-ze in product (%) 10.4 10.5 % of 245fa recovered 27.8 26.6 % of E-ze 61.8 62.9 % of E-ze yield 61.8 70.4 % of E-ze selectivity 85.5 100 Example 5 Example 5 shows the dehydrofluorination of 245fa on fluorinated alumina in the presence of Z-HFC-1234ze. An Inconel tube (OD of 1.27 cm) is filled with 10 cc (6.1 g) of Al₂O₃ catalyst (purchased from Sigma-Aldrich). The Al₂O₃ is in the form of an extruded product, which is crushed and sieved to 12 / 20 mesh. After loading the reactor tube, the catalyst bed temperature is raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow is then reduced to 60 cc / min, and HF is fed at 20 cc / min for 60 minutes. The temperature is then increased to 325 °C for 300 minutes. Finally, the nitrogen flow is reduced to 30 cc / min, and the HF flow is increased to 30 cc / min for 30 minutes. Afterwards, the nitrogen flow is reduced to 12 cc / min and the HF flow is increased to 48 cc / min for 60 minutes. / UU Next, the nitrogen flow is discontinued, and the HF flow is increased to 48 cc / min for 30 minutes. The reactor temperature is then decreased to 250 °C for 30 minutes. Afterward, the HF flow is stopped, and the reactor is purged with 30 cc / min of nitrogen. The reactor temperature is then stabilized at 300 °C, the nitrogen flow is stopped, and CF3CH2CHF2 or CF3CH2CHF2 is fed with varying amounts of Z1234ze at 1.44 ml / h. The contact time in the reactor is 45 seconds. CF3CH2CHF2 is evaporated at 50 °C. Part of the reactor effluent is passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 245fa, and E-1234ze are expressed as molar percent. The results are summarized in Table 5. Table 5 % of Z-ze added 0 10.9 Incoming compounds 100 / 0 89 / 11 245fa conversion (%) 70 71 Z-ze in product (%) 11 11 % of 245fa recovered 30 29 % of E-ze 59 58 % of E-ze yield 59 65 % of E-ze selectivity 84.3 100 Example 6 Table 6 describes the reaction products of the dehydrofluorination of 245fa over various catalysts in the presence of Z-HFC-1234ze (in molar %). Table 6 Unknown Catalyst 143a 152a TFP 1234yf 1233xf JM 62-2 0.15% 0.13% 0.0 0% 0.01% 0.35% 0.03% LV 0.28% 0.14% 0.03% 0.02% 0.04% 0.00% JM-62-3 0.2 8 % 0.14 % 0.02 % 0.02 % 0.24 % 0.04 % Newport- Chrome 0.12 % 0.13 % 0.00 % 0.00 % 0.92 % 0.00 % Catalytic converter E-1233zd Z- 1233zd z- 1234ze E- 1234ze E+Z- 1234ze JM 62-2 0.88 % 0.13 % 11.17 % 87.13 % 98.3 % LV 1.03 % 0.15 % 10.9 % 87.4 % 98.3 % JM-62-3 0.92 % 0.14 % 11 % 87.2 % 98.2 % Newport-Chrome 0.92 % 0.11% 10.5% 87.3% 97.8% An Inconel tube (0.27 in. OD) was filled with 10 cc (8 g) of catalyst (see Table 6). After loading the reactor tube, the catalyst bed temperature was raised to 300 °C and purged with nitrogen (30 cc / min) for 200 minutes. The nitrogen flow rate was then reduced to 60 cc / min, and HF was supplied at 20 cc / min for 60 minutes. The temperature was then raised to 325 °C for 300 minutes. The nitrogen flow rate was reduced to 30 cc / min, and the HF flow rate was increased to 30 cc / min for 30 minutes. Finally, the nitrogen flow rate was reduced to 12 cc / min, and the HF flow rate was increased to 48 cc / min for 60 minutes. Next, the nitrogen flow was discontinued and the HF flow was increased to 48 cc / min for 30 minutes. The reactor temperature was then decreased to 250 °C for 30 minutes. Afterward, the HF flow was stopped and the reactor was purged with 30 cc / min of nitrogen.The reactor temperature was then stabilized at 300 °C, the nitrogen flow was shut off, and CF3CH2CHF2, or CF3CH2CHF2 with 10.5–11% Z-1234ze, was fed at 1.44 mL / h. The contact time in the reactor was 45 seconds. The CF3CH2CHF2 was vaporized at 50 °C. Part of the reactor effluent was passed through a series of valves and analyzed by GC-MS. The amounts of Z-1234ze, 134a, 152b, TFP, 1234yf, 1233xf, E-1233zd, Z-1233zd, and E + Z-1234ze are expressed as molar percentages. The results are summarized in Table 6. Example 7. Table 7 shows the near-azeotropic characteristic of several compositions that can be produced by the method of the present invention when measuring the vapor pressure ΔP in terms of percentage change. The vapor pressure ΔP is the change in vapor pressure at -25 °C after a 50% vapor leakage, where 50% of the vapor is removed. Table 7 % by weight of 1234zeE / 1234yf % of Delta P 99 / 1 0.45 99.1 / 0.9 0.40 99.2 / 0.8 0.36 99.3 / 0.7 0.31 99.4 / 0.6 0.28 99.5 / 0.5 0.22 99.6 / 0.4 0.19 99.7 / 0.3 0.13 99.8 / 0.2 0.09 99.9 / 0.1 0.04 99.91 / 0.09 0.04 99.95 / 0.05 0.03 99.96 / 0.04 0.02 99.97 / 0.03 0.01 99.98 / 0.02 0.009 99.99 / 0.01 0.005 99.9987 / .0013 0.001 Example 8 Table 8 shows the cooling performance of several near-azeotropic compositions that can be produced by the method of the present invention by comparing the cooling capacity and energy efficiency (COP) with HFO-1234ze(E). The data are based on the following conditions. T_condenser = 47.0 degrees C / UU T_evaporator = 7.0 degrees C subcooling = 12.0 K superheating = 3.0 K compressor efficiency = 0.7 Average temperature set points of the heat exchanger Superheating is included in the cooling effect. Cooling load = 1.0 tonne, compressor displacement = 0.1 (mA3 / min) Table 8 Molar % Cooling capacity (kJ / m3) Capacity with respect to 1234ze (%) COP COP with respect to 1234ze (%) 1234ze 100 2111 100.0 % 4.402 100.0 % 1234ze / 1234yf. 99.9 / 0.1 2112 100.0 % 4.402 100.0 % 1234ze / 1234yf. 99.7 / 0.3 2114 100.1 % 4.402 100.0 % 1234ze / 1234yf. 99.5 / 0.5 2116 100.2 % 4.402 100.0 % 1234ze / 1234yf. 99.1 / 0.9 2120 100.4 % 4.401 100.0 % Example 8 illustrates azeotropic refrigerants of the invention and have equivalents to HFO-1234ze(E). that the compositions almost effective for use as refrigerants at least are properties Note that not all the activities described above in the overview or examples are necessary, that part of a specific activity may not be required, and that other activities may be performed in addition to those described. Furthermore, the order in which the activities are listed is not necessarily the order in which they are performed. The benefits, other advantages, and solutions to the problems have been described above with respect to specific modalities. However, the benefits, advantages, solutions to the problems, and any feature that may produce or enhance a benefit, advantage, or solution shall not be construed as a critical, necessary, or essential feature of any of the claims. It is understood that, for ease of understanding, certain characteristics described herein in the context of individual modalities may also be provided combined into a single modality. Conversely, several characteristics that, for the sake of brevity, are described in the context of a single modality may also be provided separately or in any subcombination. Furthermore, references to the values ​​indicated in the intervals include every value within that interval. Although the invention has been described with reference to a preferred embodiment, those skilled in the art will understand that various changes can be made and that equivalents can be substituted with elements thereof without departing from the scope of the invention. Furthermore, many modifications can be made to adapt a particular situation or material to the teachings of the invention without departing from its essential scope. Therefore, it is the objective that the invention not be limited to the particular embodiment described as the best contemplated way of carrying out this invention, but that the invention include all embodiments that fall within the scope of the appended claims. It is hereby stated that, as of this date, the best method known to the applicant for putting the aforementioned invention into practice is the one that is clear from the present description of the invention.

Claims

1. A fluoropropene composition characterized in that it comprises Z1,3,3,3-tetrafluoropropene, El,3,3,3-tetrafluoropropene, 2,3,3,3-tetrafluoropropene, and optionally 1,1,1,3,3-pentafluoropropane wherein the 2,3,3,3-tetrafluoropropene is present in an amount of 0.001 to 1.0 mol%.

2. The composition according to claim 1, characterized in that 2,3,3,3-tetrafluoropropene is present in an amount of 0.1 to 0.9 mol% 3. The composition according to claim 1, characterized in that 2,3,3,3-tetrafluoropropene is present in an amount of 0.2 to 0.4 molar %.

4. The composition according to claim 1, characterized in that 2,3,3,3-tetrafluoropropene is present in an amount of 0.3 to 0.4 molar %.

5. The composition according to claim 1, characterized in that the fluoropropene composition further comprises one or more of R-143a, R-152a, TFP, R-1233xf, R-1233zd(E), R-1233zd(Z), 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa, and HFC-245cb. / UU 6. The composition according to claim 5, characterized in that the sum total of the amounts of R143a, R-152a, TFP, R-1233xf, R-1233zd(E), R-1233zd(Z), 1224yd, 1224zc, 1326mxz, 113, 32, 23, trifluoropropyne, 356mff, 1326mxz, HFC-245fa and HFC-245cb is between 0.001 mol% and 2 mol%, based on the total fluoropropene composition.

7. The composition according to claim 1, characterized in that the fluoropropene composition includes R-1233zd(E) in an amount of 0.7 mol% to 1.15 mol%, based on the total fluoropropene composition.

8. The composition according to claim 1, characterized in that the fluoropropene composition includes R-1233zd(Z) in an amount of 0.05 mol% to 0.25 mol%, based on the total fluoropropene composition.

9. The composition according to claim 1, characterized in that the fluoropropene composition includes R-143a in an amount of 0.05 mol% to 0.25 mol%, based on the total fluoropropene composition.

10. The composition according to claim 1 characterized in that the composition is almost azeotropic.

11. The composition according to claim / UU 10, characterized in that it further comprises at least one member selected from the group consisting of HFC-1234ye, HFC-1243zf, HFC-32, HFC-125, HFC-134, HFC-134a, HFC-143a, HFC-152a, HFC161, HFC-227ea, HFC-236ea, HFC-236fa, HFC-245fa, HFC-365mfc, propane, n-butane, isobutane, 2-methylbutane, n-pentane, cyclopentane, dimethyl ether, CF3SCF3, CO2, and CF3I.

12. A process for transferring heat, characterized in that it comprises: providing an article; contacting the article with a heat transfer medium; wherein the heat transfer medium comprises the fluoropropene composition of any of claims 1 to 11.

13. A refrigeration system, characterized in that it comprises: an evaporator; a condenser; a compressor; an expansion device; and a heat transfer medium; wherein the heat transfer medium comprises the fluoropropene composition according to any one of claims 1 to 11.