Patent Grant
RE49849
The present invention relates to processes for the production of 1,1,1,2,2-pentafluoropropane, 2,3,3,3-tetrafluoro-1-propene, 1,1,1,3,3-pentafluoropropane, 1,3,3,3-tetrafluoro-1-propene, 2-chloro-3,3,3-trifluoro-1-propene and/or 1-chloro-3,3,3-trifluoro-1-propene.
As a result of the Montreal Protocol phasing out ozone depleting chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs), industry has been working for the past few decades to find replacement refrigerants. The solution for most refrigerant producers has been the commercialization of hydrofluorocarbon (HFC) refrigerants. The new hydrofluorocarbon refrigerants, HFC-134a being the most widely used at this time, have zero ozone depletion potential and thus are not affected by the current regulatory phase out as a result of the Montreal Protocol. The production of other hydrofluorocarbons for use in applications such as solvents, blowing agents, cleaning agents, aerosol propellants, heat transfer media, dielectrics, fire extinguishants and power cycle working fluids has also been the subject of considerable interest.
There is also considerable interest in developing new refrigerants with reduced global warming potential for the mobile air-conditioning market.
1,1,1,3,3-Pentafluoropropane (CF3CH2CHF2 or HFC-245fa), a refrigerant and blowing agent, may be prepared by fluorination of 1,1,1,3,3-pentachloropropane (CCl3CH2CHCl2 or HCC-240fa) in the liquid phase (see for example, U.S. Pat. No. 6,291,730).
1,1,1,2,2-Pentapropane (CF3CF2CH3 or HFC-245cb), useful as a refrigerant and blowing agent has been prepared by the addition of methyl fluoride to tetrafluoroethylene in the presence of antimony pentafluoride as disclosed in U.S. Pat. No. 6,184,426.
2,3,3,3-Tetrafluoro-1-propene (CF3CF═CH2 or HFC-1234yf), useful as a refrigerant and as a polymer intermediate has been prepared by fluorination of CH3CF2CCl3 over chromium oxide as disclosed by Rausch in U.S. Pat. No. 2,996,555.
1-Chloro-3,3,3-trifluoro-1-propene (CF3CH═CHCl or HCFC-1233zd) is useful as a chemical intermediate and may be prepared by fluorination of HCC-240fa as disclosed in U.S. Pat. No. 6,013,846.
1,3,3,3-Tetrafluoro-1-propene (CF3CH═CHF or HFC-1234ze) useful as a refrigerant has been prepared by dehydrofluorination of HFC-245fa using a strong base in aqueous or alcoholic solution or by means of chromium-containing catalyst in the presence of oxygen at elevated temperature as disclosed in U.S. Pat. No. 6,124,510, and from HCFC-1233zd as disclosed in U.S. Pat. No. 5,895,825. HFC-1234ze has also been prepared from HCC-240fa as disclosed in U.S. Pat. No. 6,111,150.
2-Chloro-3,3,3-trifluoro-1-propene (CF3CCl═CH2 or HCFC-1233xf) is useful as an intermediate and as a monomer for polymers. HCFC-1233xf has been prepared by dehydrochlorination of 1,2-dichloro-3,3,3-trifluoropropane using potassium hydroxide as described by Haszeldine in Journal of the Chemical Society (1951) pages 2495 to 2504.
There is a need for processes for the manufacture of a compound from the group HCFC-1233xf, HFC-245fa, HFC-245cb, HFC-1234ze, HCFC-1233zd, and HFC-1234yf, where other compounds of the group are also produced from common halogenated hydrocarbon starting materials and those other compounds can, if desired, also be recovered.
The present invention provides a process for making at least one product compound selected from the group consisting of CF3CF2CH3, CF3CF═CH2 and CF3CCl═CH2. The process comprises reacting at least one starting material selected from the group consisting of halopropanes of the formula CX3CH2CH2X, halopropenes of the formula CX3CH═CH2, and halopropenes of the formula CX2═CHCH2X wherein each X is independently selected from the group consisting of F and Cl, with HF and Cl2 in a reaction zone, optionally in the presence of a chlorofluorination catalyst, to produce a product mixture comprising HF, HCl, CF3CF2CH3, CF3CF═CH2 and CF3CCl═CH2, wherein the molar ratio of HF to total amount of starting material fed to the reaction zone is at least stoichiometric and wherein the molar ratio of Cl2 to total amount of starting material fed to the reaction zone is 2:1 or less; and recovering said at least one product compound from the product mixture.
The present invention also provides a process for making at least one product compound selected from the group consisting of CF3CH2CHF2, CF3CH═CHF and CF3CH═CHCl. The process comprises reacting at least one starting material selected from the group consisting of halopropenes of the formula CX3CH═CH2 and halopropenes of the formula CX2═CHCH2X wherein each X is independently selected from the group consisting of F and Cl, with HF and Cl2 in a reaction zone, optionally in the presence of a chlorofluorination catalyst, to produce a product mixture comprising HF, HCl, CF3CH2CHF2, CF3CH═CHF and CF3CH═CHCl, wherein the molar ratio of HF to total amount of starting material fed to the reaction zone is at least stoichiometric and wherein the molar ratio of Cl2 to total amount of starting material fed to the reaction zone is 2:1 or less; and recovering said at least one product compound from the product mixture.
The term “starting material”, as used herein, means halopropanes or halopropenes which react with hydrogen fluoride (HF) and chlorine (Cl2) in a reaction zone in the embodiments of this invention. As indicated above, for certain processes of this invention the starting material is selected from the group consisting of halopropanes of the formula CX3CH2CH2X, halopropenes of the formula CX3CH═CH2 and halopropenes of the formula CX2═CHCH2X, wherein each X is independently selected from the group consisting of F and Cl; and for certain other processes of this invention the starting material is selected from the group consisting of halopropenes of the formula CX3CH═CH2 and halopropenes of the formula CX2═CHCH2X, wherein each X is independently selected from the group consisting of F and Cl.
The processes of this invention use a molar ratio of HF to the total amount of starting material that is at least stoichiometric. The stoichiometric ratio is determined by subtracting the weighted average of the number of fluorine substituents in the starting material(s) from the weighted average of the number of fluorine substituents in the desired product(s). For example, for producing a C3H3F5 isomer from C3H4Cl4, the stoichiometric ratio of HF to C3H4Cl4 is 5:1. As another example, for producing a 1:1 mixture of HFC-245cb to HFC-1234yf from CF3CH═CH2, the stoichiometric ratio of HF to CF3CH═CH2 is 1.5:1.
Certain compounds produced by the processes of this invention may exist as one of two configurational isomers. For example, HFC-1234ze and HCFC-1233zd may each exist as E- or Z-isomers. As used herein HFC-1234ze refers to the isomers, E-HFC-1234ze or Z-HFC-1234ze, as well as any combinations or mixtures of such isomers; and HCFC-1233zd as used herein refers to the isomers, E-HCFC-1233zd or Z-HCFC-1233zd, as well as any combinations or mixtures of such isomers.
As indicated above, the present invention provides a process that involves producing a product mixture comprising at least one product compound selected from the group consisting of HFC-245cb, HFC-1234yf and HCFC-1233xf using at least one starting material selected from the group consisting of halopropanes of the formula CX3CH2CH2X, halopropenes of the formula CX3CH═CH2 and halopropenes of the formula CX2═CHCH2X. Of note are embodiments of this process wherein HFC-1234yf is recovered. Additional HFC-1234yf may be obtained by dehydrofluorination of HFC-245cb from the product mixture. Also of note are embodiments of this process wherein HCFC-1233xf from the product mixture is fluorinated to produce at least one of HFC-1234yf and HFC-245cb.
The product mixture may also comprise HFC-1234ze. The HFC-1234ze may be recovered. The product mixture may further comprise HCFC-1233zd. HFC-1234ze and HFC-245fa may also be obtained by fluorination of HCFC-1233zd from the product mixture.
The product mixture may also comprise HFC-245fa. The HFC-245fa may be recovered. The HFC-245fa may also be dehydrofluorinated to produce HFC-1234ze.
The product mixture may further comprise HFC-1234ze. A mixture of HFC-245cb and HFC-1234ze may be recovered and further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising HFC-245fa and HFC-245cb. Alternatively, a mixture of HFC-245cb and HFC-1234ze may be recovered and further reacted under dehydrofluorination conditions in the presence of a dehydrofluorination catalyst to produce a mixture comprising HFC-1234ze and HFC-1234yf.
HFC-245fa, HFC-1234ze and/or HCFC-1233zd may also be present in the product mixture. HFC-245cb, HFC-1234yf, and HCFC-1233xf from the product mixture together with HFC-245fa (if present), HFC-1234ze (if present) and HCFC-1233zd (if present) may be further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising HFC-245fa and HFC-245cb. The HFC-245fa and HFC-245cb from the mixture may be dehydrofluorinated (individually or as a mixture) to produce both HFC-1234ze and HFC-1234yf which may be recovered. See for example, U.S. Patent Application Publication US2006/0106263(A1), which is hereby incorporated herein by reference.
HCFC-1233zd and HFC-245fa may also be present in the product mixture; and HCFC-1233xf, HCFC-1233zd, and HFC-245fa from the product mixture may be further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising CF3CH2CHF2 and CF3CF2CH3.
As indicated above, the present invention also provides a process that involves producing a product mixture comprising HFC-245fa, HFC-1234ze, and HCFC-1233zd using at least one starting material selected from the group consisting of halopropenes of the formula CX3CH═CH2 and halopropenes of the formula CX2═CHCH2X. Of note are embodiments of the process wherein HFC-1234ze is recovered. Additional HFC-1234ze may be obtained by dehydrofluorination of HFC-245fa from the product mixture. Also of note are embodiments of this process wherein HCFC-1233zd from the product mixture is fluorinated to produce at least one of HFC-1234ze and HFC-245fa.
Also of note are processes wherein HFC-245fa is recovered.
Also of note are processes wherein the product mixture further comprises HFC-1234yf and wherein HFC-1234yf from the product mixture is recovered.
The product mixture may further comprise HFC-245cb. A mixture of HFC-245cb and HFC-1234ze may be recovered and further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising HFC-245fa and HFC-245cb. Alternatively, a mixture of HFC-245cb and HFC-1234ze may be recovered and further reacted under dehydrofluorination conditions in the presence of a dehydrofluorination catalyst to produce a mixture comprising HFC-1234ze and HFC-1234yf.
HFC-245cb, HFC-1234yf and/or HCFC-1233xf may also be present in the product mixture. HFC-245fa, HFC-1234ze and HCFC-1233zd from the product mixture together with HFC-245cb (if present), HFC-1234yf (if present) and HCFC-1233xf (if present) may be further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising HFC-245fa and HFC-245cb. The HFC-245fa and HFC-245cb from the mixture may be dehydrofluorinated (individually or as a mixture) to produce both HFC-1234ze and HFC-1234yf which may be recovered. See for example, U. S. Patent Application Publication US200610106263(A1).
HCFC-1233xf may also be present in the product mixture; and HCFC-1233xf, HCFC-1233zd, and HFC-245fa from the product mixture may be further reacted with HF in the liquid phase under fluorination conditions in the presence of a fluorination catalyst to produce a mixture comprising CF3CH2CHF2 and CF3CF2CH3.
Suitable halopropane starting materials of the formula CX3CH2CH2X include CF3CH2CH2F (HFC-254fb), CF3CH2CH2Cl (HCFC-253fb), CClF2CH2CH2Cl (HCFC-252fc), CCl2FCH2CH2Cl(HCFC-251fb) and CCl3CH2CH2Cl (HCC-250fb). Preferred is HCC-250fb.
Suitable halopropene starting materials of the formula CX3CH═CH2 include CF3CH═CH2 (HFC-1243zf), CClF2CH═CH2 (HCFC-1242zf), CCl2FCH═CH2 (HCFC-1241zf), and CCl3CH═CH2 (HCC-1240zf). Preferred is HFC-1243zf.
Suitable halopropene starting materials of the formula CX2═CHCH2X include CCl2═CHCH2Cl (HCC-1240za).
HCC-250fb is a readily available starting material that can be prepared by the reaction of ethylene with carbon tetrachloride as disclosed in International Patent Application No. WO 97/05089, which is incorporated herein by reference. HCC-250fb may be converted to HFC-1243zf by reaction with HF in vapor phase as disclosed in U.S. Pat. No. 6,329,559, which is incorporated herein by reference. HCC-1240za may be prepared by reaction of 1,1,1,3-tetrachloropropane with ferric chloride as disclosed by Fujimori, et. al. in Japanese Kokai 49066613.
The reaction may be carried out in the liquid or vapor phase. For liquid phase embodiments of the invention, the reaction of starting materials with HF and Cl2 may be conducted in a liquid-phase reactor operating in batch, semi-batch, semi-continuous, or continuous modes. In the batch mode, starting materials, Cl2, and HF are combined in an autoclave or other suitable reaction vessel and heated to the desired temperature.
Preferably, this reaction is carried out in semi-batch mode by feeding Cl2 to a liquid-phase reactor containing HF and starting materials or by feeding starting materials and Cl2 to a liquid-phase reactor containing HF, or by feeding Cl2 to a mixture containing HF and reaction products formed by initially heating starting materials and HF. Alternatively, HF and Cl2 may be fed to a liquid-phase reactor containing a mixture of starting materials and reaction products formed by reacting HF, Cl2, and starting materials. In another embodiment of the liquid-phase process, HF, Cl2, and starting materials may be fed concurrently in the desired stoichiometric ratio to the reactor containing a mixture of HF and reaction products formed by reacting HF, Cl2, and starting materials.
Suitable temperatures for the reaction of HF and Cl2 with starting materials in the liquid-phase reactor are from about 80° C. to about 180° C., preferably from about 100° C. to about 150° C. Higher temperatures typically result in greater conversion of the starting materials.
A suitable molar ratio of HF to total amount of starting materials fed to the liquid-phase reactor is at least stoichiometric and is typically from about 5:1 to about 100:1. Of note are embodiments wherein the molar ratio of HF to starting material is from about 8:1 to about 50:1. A suitable molar ratio of Cl2 to total amount of starting materials fed to the liquid-phase reactor is from about 1:1 to about 2:1.
The reactor pressure in the liquid-phase process is not critical and in batch reactions is usually the autogenous pressure of the system at the reaction temperature. The pressure of the system increases as hydrogen chloride is formed by replacement of hydrogen substituents by chlorine, and by replacement of chlorine substituents by fluorine in the starting materials and intermediate reaction products. In a continuous process it is possible to set the pressure of the reactor in such a way that the lower boiling products of the reaction, such as HCl, CF3CF═CH2, E/Z-CF3CH═CHF, and CF3CF2CH3, are vented from the reactor, optionally through a packed column or condenser. In this manner, higher boiling intermediates remain in the reactor and the volatile products are removed. Typical reactor pressures are from about 20 psig (239 kPa) to about 1,000 psig (6,994 kPa).
In embodiments of the invention in which the reaction is conducted using a liquid-phase process, catalysts which may be used include carbon, AlF3, BF3, FeCl3-aFa (where a=0 to 3), FeX3 supported on carbon, SbCl3-aFa, AsF3, MCl5-bFb (where b=0 to 5 and M=Sb, Nb, Ta, or Mo), and M′Cl4-cFc (where c=0 to 4, and M′=Sn, Ti, Zr, or Hf). Preferred catalysts for the liquid phase process are MCl5-bFb (where b=0 to 5 and M=Sb, Nb, or Ta).
Preferably, the reaction of HF and Cl2 with starting materials is carried out in the vapor phase. Typically a heated reactor is used. A number of reactor configurations are possible including horizontal or vertical orientation of the reactor as well as the sequence of reaction of the starting materials with HF and Cl2. In one embodiment of the invention, the starting materials may be initially vaporized and fed to the reactor as gases.
In another embodiment of the invention, starting materials may be contacted with HF, optionally in the presence of Cl2, in a pre-reactor prior to reaction in the vapor-phase reactor. The pre-reactor may be empty, but is preferably filled with a suitable packing such as Monel™ or Hastelloy™ nickel alloy turnings or wool, or other material inert to HCl and HF which allows efficient mixing of starting materials and HF vapor.
Suitable temperatures for the pre-reactor for this embodiment of the invention are from about 80° C. to about 250° C., preferably from about 100° C. to about 200° C. Temperatures greater than about 100° C. result in some conversion of the starting materials to compounds having a higher degree of fluorination. Higher temperatures result in greater conversion of the starting materials entering the reactor and a greater degree of fluorination in the converted compounds. Under these conditions, for example, a mixture of HF, Cl2, and HCC-250fb is converted to a mixture containing predominantly HFC-1243zf and HCFC-243db (CF3CHClCH2Cl) and a mixture of HF, Cl2, and HFC-1243zf is converted to a mixture containing predominantly HCFC-243db and HCFC-244db (CF3CHClCH2F).
The degree of fluorination reflects the number of fluorine substituents that replace chlorine substituents in the starting materials and their chlorinated products. For example, HCFC-253fb represents a higher degree of fluorination than HCC-250fb and HFC-1243zf represents a higher degree of fluorination than HCC-1240zf.
The molar ratio of HF to the total amount of starting material(s) in the pre-reactor is typically from about the stoichiometric ratio of HF to the total amount of starting material to about 50:1. Preferably, the molar ratio of HF to the total amount of starting material in the pre-reactor is from about twice the stoichiometric ratio of HF to the total amount of starting material to about 30:1. In one embodiment of the invention, the preferred molar ratio of HF to the total amount of starting materials is present in the pre-reactor, and no additional amount of HF is added to the vapor-phase reaction zone.
In another embodiment of the invention, the starting materials may be contacted with Cl2 in a pre-reactor, optionally in the presence of HF, prior to reaction in the vapor-phase reactor.
Suitable temperatures for the pre-reactor for this embodiment of the invention are from about 80° C. to about 250° C., preferably from about 100° C. to about 200° C. Under these conditions, at least a portion of CX3CH2CH2X is converted to CX3CHClCH2X, at least a portion of CX3CH═CH2 is converted to CX3CHClCH2Cl, and at least a portion of CX2═CHCH2X is converted to CX2ClCHClCH2X. Higher temperatures typically result in a higher degree of halogenation of the starting material.
The degree of halogenation reflects the total number of halogen substituents (chlorine plus fluorine) in a halopropane and/or halopropene product. For example, HFC-245cb has a higher degree of halogenation (i.e., 5) than does HCC-250fb (i.e., 4); and HFC-1234yf has a higher degree of halogenation (i.e., 4) than does HFC-1243zf (i.e., 3). The preferred degree of halogenation in the halopropane products in the process of this invention is five. The preferred degree of halogenation of halopropene products in the process of this invention is four.
The molar ratio of Cl2 to the total amount of the starting materials is typically from about 0.5:1 to about 2:1. Preferably the molar ratio of Cl2 to the total amount of the starting materials is from about 1.1:1 to about 1:1.
In a preferred embodiment of the invention, the starting materials are vaporized, optionally in the presence of HF, and fed to a pre-reactor or to a vapor-phase reactor along with HF and Cl2.
Suitable temperatures for the vapor-phase reaction of this invention are from about 120° C. to about 500° C. Temperatures of from about 250° C. to about 350° C. favor the formation of HFC-1234yf and HFC-245cb. Temperatures of from about 350° C. to about 450° C. favor the formation of HFC-1234ze, HFC-245fa, and HCFC-1233zd. At temperatures of from about 250° C. to about 450° C., some HCFC-1233xf is also produced. Higher temperatures result in greater conversion of starting materials and higher degrees of fluorination and halogenation in the converted compounds.
Suitable reactor pressures for the vapor-phase reactor may be from about 1 to about 30 atmospheres. A pressure of about 15 to about 25 atmospheres may be advantageously employed to facilitate separation of HCl from other reaction products, and the suitable reaction time may vary from about 1 to about 120 seconds, preferably from about 5 to about 60 seconds.
The molar ratio of HF to the total amount of starting material(s) for the vapor-phase reaction is typically from about the stoichiometric ratio of HF to the total amount of starting material to about 50:1 and preferably from about 10:1 to about 30:1.
Preferably a catalyst is used in the reaction zone for the vapor-phase reaction of HF and Cl2 with starting materials. Chlorofluorination catalysts which may be used in the vapor phase reaction of the invention include carbon; graphite; alumina; fluorided alumina; aluminum fluoride; alumina supported on carbon; aluminum fluoride supported on carbon; fluorided alumina supported on carbon; magnesium fluoride supported on aluminum fluoride; metals (including elemental metals, metal oxides, metal halides, and/or other metal salts); metals supported on aluminum fluoride; metals supported on fluorided alumina; metals supported on alumina; and metals supported on carbon; mixtures of metals.
Suitable metals for use as catalysts (optionally supported on alumina, aluminum fluoride, fluorided alumina, or carbon) include chromium, iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, manganese, rhenium, scandium, yttrium, lanthanum, titanium, zirconium, and hafnium, copper, silver, gold, zinc, and/or metals having an atomic number of 58 through 71 (i.e., the lanthanide metals). Preferably when used on a support, the total metal content of the catalyst will be from about 0.1 to about 20 percent by weight based on the total weight of the catalyst; typically from about 0.1 to about 10 percent by weight based on the total weight of the catalyst.
Suitable chlorofluorination catalysts for the vapor-phase reactions in this invention include chromium-containing catalysts including chromium(III) oxide (Cr2O3); Cr2O3 with other metals such as magnesium halides or zinc halides supported on Cr2O3; chromium(III) halides supported on carbon; mixtures of chromium and magnesium (including elemental metals, metal oxides, metal halides, and/or other metal salts) optionally supported on graphite; and mixtures of chromium and other metals (including elemental metals, metal oxides, metal halides, and/or other metal salts) optionally supported on graphite, alumina, or aluminum halides such as aluminum fluoride.
Chromium-containing catalysts are well known in the art. They may be prepared by either precipitation methods or impregnation methods as generally described by Satterfield on pages 87-112 in Heterogeneous Catalysis in Industrial Practice, 2nd edition (McGraw-Hill, New York, 1991).
Of note are chlorofluorination catalysts that comprise at least one chromium-containing component selected from the group consisting of crystalline alpha-chromium oxide where from about 0.05 atom % to about 6 atom % of the chromium atoms in the alpha-chromium oxide lattice are replaced by trivalent cobalt atoms, and crystalline alpha-chromium oxide where from about 0.05 atom % to about 6 atom % of the chromium atoms in the alpha-chromium oxide lattice are replaced by trivalent cobalt atoms which has been treated with a fluorinating agent. These catalysts, including their preparation, have been disclosed in U. S. Patent Application Publication US2005/0228202 which is incorporated herein by reference in its entirety.
Optionally, the metal-containing catalysts described above can be pretreated with HF. This pretreatment can be accomplished, for example, by placing the metal-containing catalyst in a suitable container, and thereafter, passing HF over the metal-containing catalyst. In one embodiment of this invention, such container can be the reactor used to perform the chlorofluorination reaction in this invention. Typically, the pretreatment time is from about 15 to about 300 minutes, and the pretreatment temperature is from about 200° C. to about 450° C.
In one embodiment of this invention, the product mixture comprises HFC-245cb, HFC-245fa, HFC-1234yf, HFC-1234ze, HCFC-1233zd and HCFC-1233xf.
Halopropane by-products that may be formed in the chlorofluorination reactions of this invention having higher degrees of halogenation and/or fluorination than pentafluoropropanes include CF3CCl2CF3 (CFC-216aa), CF3CClFCClF2 (CFC-216ba), CF3CClFCF3 (CFC-217ba), CF3CF2CClF2 (CFC-217ca), CF3CHFCF3 (HFC-227ea), CF3CF2CHF2 (HFC-227ca), CF3CClFCHF2 (HCFC-226ba), CF3CF2CHClF (HCFC-226ca), CF3CHClCF3 (HCFC-226da), CF3CCl2CHF2 (HCFC-225aa), CF3CClFCHClF (HCFC-225ba), CF3CF2CHCl2 (HCFC-225ca), CF3CCl2CClF2 (CFC-215aa), CF3CClFCCl2F (CFC-215bb), CF3CCl2CCl2F (HCFC-214ab), CF3CCl2CHClF (HCFC-224aa), and CF3CClFCHCl2 (HCFC-224ba).
Halopropene by-products that may be formed in the chlorofluorination reactions of this invention having a higher degree of halogenation than tetrafluoropropenes include CF3CCl═CHCl (HCFC-1223xd).
In cases where the product mixture produced by the processes of this invention comprises (i) product compounds HFC-245cb, HFC-245fa, HFC-1234yf, HFC-1234ze, HCFC-1233zd and HCFC-1233xf, (ii) HF, HCl, and Cl2, (iii) higher boiling by-products such as CF3CHClCH2Cl, CF3CHClCH2F and (iv) chlorinated by-products such as C3HCl3F4, C3HCl2F5, C3HClF6, C3Cl3F5, and C3Cl2F6, the separation steps (a) through (e) may be employed to recover the product compounds from such a product mixture.
In separation step (a), the product mixture may be delivered to a distillation column to separate HCl and Cl2 from the product mixture.
In separation step (b), the product mixture from separation step (a) may be delivered to one or more distillation columns to separate the azeotropic composition of HFC-1234yf and HF from the rest of the product mixture. The recovered azeotropic composition of HFC-1234yf and HF may be further separated into individual components by using procedures similar to those described in U. S. Patent Application Publication US2006/0106263(A1).
In separation step (c), the product mixture from separation step (b) may be delivered to one or more distillation columns in which HF, HFC-245cb, HFC-1234ze, HCFC-1233xf, HCFC-1233zd, and HFC-245fa are recovered from the top of the distillation column, and the higher boiling by-products such as CF3CHClCH2Cl, CF3CHClCH2F and the chlorinated by-products such as C3HCl3F4, C3HCl2F5, C3HClF6, C3Cl3F5, and C3Cl2F6 are removed from the bottom of the distillation column. The higher boiling by-products such as CF3CHClCH2Cl and CF3CHClCH2F may be further separated from the chlorinated by-products, e.g. by distillation, and may be recycled back to the vapor-phase chlorofluorination reactor.
In separation step (d), the product mixture comprising HF, HFC-245cb, HFC-1234ze, HCFC-1233xf, HCFC-1233zd and HFC-245fa, which is recovered from the top of the distillation column in separation step (c), may be delivered to one or more distillation columns to recover the azeotropic composition of HFC-245cb/HF and the azeotropic composition of HFC-1234ze/HF from the top of the distillation column. The recovered HFC-245cb/HF and HFC-1234ze/HF azeotropic compositions may then be further separated into individual components by using procedures similar to those described in U.S. Patent Application Publication US2006/0106263(A1).
In separation step (e), the product mixture comprising HCFC-1233xf, HCFC-1233zd and HFC-245fa and any HF recovered from the bottom of the distillation column in separation step (d) may be delivered to a distillation column to separate the HCFC-1233xf, HCFC-1233zd and HFC-245fa. The HCFC-1233xf can be fluorinated to produce at least one of HFC-245cb and HFC-1234yf. The HCFC-1233zd can be fluorinated to produce at least one of HFC-245fa and HFC-1234ze.
As indicated above, in certain embodiments of this invention, the mixture of HF, HFC-245cb and HFC-1234ze, made according to the process of the invention is contacted with additional HF in a liquid-phase fluorination reactor, optionally in the presence of a liquid-phase fluorination catalyst to give a mixture of HF, HFC-245cb and HFC-245fa. The mixture of HF, HFC-245cb, and HFC-245fa is then separated into the individual components by using procedures similar to those described in U.S. Patent Application Publication US200610106263(A1). Suitable fluorination catalysts for these embodiments may be selected from those described for the liquid-phase embodiment of the chlorofluorination reactor described herein. The mole ratio of HF to HFC-245cb and HFC-1234ze in these embodiments is typically from about 5:1 to about 100:1, and is preferably from about 10:1 to about 40:1 based on the amount of HFC-1234ze in the mixture. Suitable temperatures for these embodiments of the invention are within the range of from about 30° C. to about 180° C., preferably from about 50° C. to about 150° C. Suitable reactor pressures for these embodiments are usually the autogenous pressures at the reactor temperatures. The pressure may be in the range of from about 1 to about 30 atmospheres.
As indicated above, in certain embodiments of this invention, a mixture of HF, HFC-245cb and HFC-1234ze, made according to the processes of this invention, may be delivered to a reaction zone containing a dehydrofluorination catalyst (optionally after removal of the HF). Conditions in the reaction zone are chosen to be suitable for conversion of HFC-245cb to HFC-1234yf. The products leaving the reactor, comprising HFC-1234ze and HFC-1234yf are separated by techniques known to the art. Catalysts suitable for these embodiments of the invention and suitable operating conditions are disclosed in U.S. Pat. No. 5,396,000 the teachings of which are herein incorporated by reference. Preferably, the dehydrofluorination catalyst comprises aluminum fluoride or fluorided alumina or trivalent chromium oxide. Reaction temperatures suitable for these embodiments are from about 150° C. to about 500° C. Contact times in the reaction zone for these embodiments are typically from about 1 second to about 500 seconds.
As indicated above, in certain embodiments of this invention, a mixture of HCFC-1233xf, HCFC-1233zd, and HFC-245fa made according to the process of the invention, is reacted with HF in a liquid-phase fluorination reactor in the presence of a liquid-phase fluorination catalyst to give a mixture of HF, HFC-245cb and HFC-245fa. The conditions of the fluorination are similar to those described for the mixture of HFC-1234ze and HFC-245cb above. The mixture of HF, HFC-245cb, and HFC-245fa is then optionally delivered to a distillation column to separate the two pentafluoropropanes and azeotropic HF by using procedures similar to those described in U.S. Patent Application Publication US2006/0106263(A1).
As noted above, HFC-245cb, made according to the processes of this invention, may be dehydrofluorinated to produce HFC-1234yf, and HFC-245fa, made according to the processes of this invention, may be dehydrofluorinated to produce HFC-1234ze. Typical dehydrofluorination reaction conditions and dehydrofluorination catalysts are disclosed in U.S. Pat. No. 5,396,000, which is herein incorporated by reference. Dehydrofluorination reaction temperatures suitable for this invention are from about 150° C. to about 500° C.; however, higher temperature are desirable for the dehydrofluorination of HFC-245cb. Suitable contact times for these dehydrofluorinations are from about 1 second to about 500 seconds. Preferably, the dehydrofluorination catalyst comprises at least one catalyst selected from the group consisting of aluminum fluoride, fluorided alumina, and trivalent chromium oxide.
As indicated above, in certain embodiments of this invention, a mixture of HFC-245cb, HFC-1234yf, HFC-1234ze, HCFC-1233xf, HCFC-1233zd, and HFC-245fa that are present in the product mixtures made according to the processes of the invention, is reacted with HF in a liquid-phase fluorination reactor in the presence of a liquid-phase fluorination catalyst. The conditions of the fluorination are similar to those described for the mixture of HFC-1234ze and HFC-245cb above. The fluorination catalysts for the above liquid-phase embodiments of the invention may be selected from those described for the liquid-phase embodiment the chlorofluorination reactor described herein.
The amount of HF required for the liquid-phase reaction is determined by the total amount of HFC-1234yf, HFC-1234ze, HCFC-1233xf, and HCFC-1233zd, present in the mixture. The mole ratio of HF to the sum of the moles of HFC-1234yf, HFC-1234ze, HCFC-1233xf, and E/Z-HCFC-1233zd is typically from about the stoichiometric amount (between 1:1 to 2:1) to about 100:1, and is preferably from about 8:1 to about 50:1. Suitable temperatures for these embodiments of the invention are typically within the range of from about 30° C. to about 180° C., preferably from about 50° C. to about 150° C. The resulting mixture of pentafluoropropanes (i.e, HFC-245cb and HFC-245fa) may be then be freed of HF and recovered as individual compounds by techniques known to the art.
The reactor, distillation columns, and their associated feed lines, effluent lines, and associated units used in applying the process of this invention should be constructed of materials resistant to hydrogen fluoride and hydrogen chloride. Typical materials of construction, well-known to the fluorination art, 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.
Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the present invention to its fullest extent. The following specific embodiments are, therefore, to be construed as merely illustrative, and do not constrain the remainder of the disclosure in any way whatsoever.
Preparation of 98% Chromium/2% Cobalt Catalyst
A solution of 784.30 g Cr(NO3)3[9(H2O)] (1.96 moles) and 11.64 g Co(NO3)2[6(H2O)] (0.040 mole) was prepared in 2000 mL of deionized water. The solution was treated dropwise with 950 mL of 7.4M aqueous ammonia until the pH reached about 8.5. The slurry was stirred overnight at room temperature and then evaporated to dryness in air at 110-120° C. The dried catalyst was then calcined in air at 400° C. for 24 hours prior to use.
General Procedure for Product Analysis
The following general procedure is illustrative of the method used for analyzing the products of fluorination reactions. Part of the total reactor effluent was sampled on-line for organic product analysis using a gas chromatograph equipped a mass selective detector (GC/MS). The gas chromatography utilized a 20 ft. (6.1 m) long×⅛ in. (0.32 cm) diameter tube containing Krytox® perfluorinated polyether on an inert carbon support. The helium flow was 30 mL/min (5.0×10−7 m3/sec). Gas chromatographic conditions were 60° C. for an initial hold period of three minutes followed by temperature programming to 200° C. at a rate of 6° C./minute.
The 98% chromium/2% cobalt catalyst prepared above (21.4 g, 15 mL, −12 to +20 mesh, (1.68 to 0.84 mm)) was placed in a ⅝″ (1.58 cm) diameter Inconel™ nickel alloy reactor tube heated in a fluidized sand bath. The catalyst was pre-fluorinated by treatment with HF as follows. The catalyst was heated from 45° C. to 175° C. in a flow of nitrogen (50 cc/min) over the course of about 1.5 h. HF was then admitted to the reactor at a flow rate of 50 cc/min for 1.3 h at a temperature of 175° C. The reactor nitrogen flow was decreased to 20 cc/min and the HF flow increased to 80 cc/min; this flow was maintained for 0.3 h. The reactor temperature was then gradually increased to 400° C. over 1 h. After this period, the HF and nitrogen flow was stopped and the reactor brought to the desired operating temperature. A flow of HF vapor, CF3CH═CH2, and Cl2 then started through the reactor. Part of the reactor effluent was analyzed by on line GC/MS.
The results of the chlorofluorination of CF3CH═CH2 over the 98/2 Cr/Co catalyst at various operating temperatures and indicated molar ratios of HF, CF3CH═CH2, and Cl2 are shown in Table 1; analytical data is given in units of GC area %. The nominal catalyst bed volume was 15 cc; the contact time (CT) was 15 seconds. Examples 1 and 2 were carried out in the absence of the catalyst.
a243db and 244db confirmed by 1H and 19F NMR.
b245cb and 1233xf confirmed by 1H and 19F NMR.
cAdditional major products were 215aa, 216aa, 216ba, 225aa, 225ba, 226ca, 226da
This application represents a national filing under 35 U.S.C. 371 of International Application No. PCT/US2007/022995 filed Oct. 31, 2007, and claims priority of U.S. Provisional Application No. 60/855,538 filed Oct. 31, 2006.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/US2007/022995 | 10/31/2007 | WO | 1/7/2010 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2008/054782 | 5/8/2008 | WO | A |
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| Number | Date | Country | |
|---|---|---|---|
| 60855538 | Oct 2006 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 12444462 | Oct 2007 | US |
| Child | 14552613 | US |
