Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/23—Preparation of halogenated hydrocarbons by dehalogenation
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C17/00—Preparation of halogenated hydrocarbons
  • C07C17/26—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton
  • C07C17/272—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions
  • C07C17/278—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions of only halogenated hydrocarbons
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C21/00—Acyclic unsaturated compounds containing halogen atoms
  • C07C21/02—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds
  • C07C21/18—Acyclic unsaturated compounds containing halogen atoms containing carbon-to-carbon double bonds containing fluorine

Definitions

• This invention relates to novel methods for preparing fluorinated organic compounds, and more particularly to methods of producing fluorinated olefins.
• Hydrofluorocarbons in particular hydrofluoroalkenes such tetrafluoropropenes (including 2,3,3,3-tetrafluoro-l-propene (HFO-1234yf) and 1,3,3,3-tetrafluoro-l-propene (HFO-1234ze)) (HFO is hydrofluorolefm) have been disclosed to be effective refrigerants, fire extinguishants, heat transfer media, propellants, foaming agents, blowing agents, gaseous dielectrics, sterilant carriers, polymerization media, particulate removal fluids, carrier fluids, buffing abrasive agents, displacement drying agents and power cycle working fluids.
• HFC's hydrofluoroalkenes
• tetrafluoropropenes including 2,3,3,3-tetrafluoro-l-propene (HFO-1234yf) and 1,3,3,3-tetrafluoro-l-propene (HFO-1234ze)
• HFCs Unlike chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs), both of which potentially damage the Earth's ozone layer, HFCs do not contain chlorine and thus pose no threat to the ozone layer.
• CFCs chlorofluorocarbons
• HCFCs hydrochlorofluorocarbons
• Several methods of preparing hydrofluoroalkanes are known.
• U.S. Pat. No. 4,900,874 (Ihara et al) describes a method of making fluorine containing olefins by contacting hydrogen gas with fluorinated alcohols. Although this appears to be a relatively high-yield process, for commercial scale production the handling of hydrogen gas at high temperature raises difficult safety related questions. Also, the cost of producing hydrogen gas, such as building an on-site hydrogen plant, can be in many situations prohibitive.
• U.S. Pat. No. 2,931,840 (Marquis) describes a method of making fluorine containing olefins by pyrolysis of methyl chloride and tetrafluoroethylene or chlorodifluoromethane. This process is a relatively low yield process and a very large percentage of the organic starting material is converted in this process to unwanted and/or unimportant byproducts, including a sizeable amount of carbon black. The carbon black is not only unwanted, it tends to deactivate the catalyst used in the process.
• the preparation of HFO- 1234yf from trifluoroacetylacetone and sulfur tetrafluoride has been described. See Banks, et al., Journal of Fluorine Chemistry, Vol. 82, Iss.
• U.S. Pat. No. 5,162,594 discloses a process wherein tetrafluoroethylene is reacted with another f ⁇ uorinated ethylene in the liquid phase to produce a polyfluoroolefm product. Catalyzed hydrogen reduction reactions have been disclosed for the preparation of fluorinated C3 hydrocarbons in U.S. Patent No. 5,545,777. The patent describes the reaction as being one in which a compound of formula (1)
• CF 3 CZ CHZ (H).
• each X is independently Cl, I or Br; each Z is independently H or F; n is 1 or 2; m is 1, 2 or 3, provided that when n is 1, m is 1 or 2; a is 2 or 3, and a-m > 0.
• each Z is different.
• Formula II is intended to include all possible isomers.
• the preferred converting step of the present invention comprises catalytic reduction of the compound of formula (I).
• the catalytic reduction step comprises in preferred embodiments introducing said compound of formula (I) to a reaction system under conditions effective to convert, and preferably convert at least about 50%, more preferably at least about 70%, and even more preferably at least about 90%, of said compound of formula (I). It is also generally preferred that said converting step produces a reaction product having at least about 20% selectivity, more preferably at least about 40% selectivity and even more preferably at least about 70% selectivity, to compounds of formula (II), preferably tetrafluoropropene, and even more preferably HFO-1234yf.
• the converting step comprises reacting a compound of formula (I) in the gas phase, in the liquid phase, or a combination of these, with gas phase reactions preferably occurring in the presence of catalyst.
• One beneficial aspect of the present invention is that it enables the production of desirable fluroolefms, preferably C3 fluoroolefms, using relatively high conversion and high selectivity reactions.
• the methods of the present invention provided reactions with relatively high yield and which are capable of obtaining relatively long catalyst life.
• the present methods permit the products of the desirable fluoroolefms from relatively attractive starting materials.
• Ethylene and is halogentated derivates such as tertrafluorethylene
• the present methods include the step of reacting fluorinated C2 olefin, such as tetrafluoroethylene, with a Cl addition agent under conditions effective to produce a compound of formula (I)
• the fluorinated olefin reactant is a compound of formula (III)
• CY 2 CY 2 (III) where each Y is independently F, Cl, I or Br, provided that at least one F on each carbon atom, and the Cl addition agent comprises a compound of formula (IV) CH m Y a-m (IV)
• the compound of formula (III) comprises a compound of formula (IIIA)
• CF 2 CY 2 (IIIA) where each Y is independently F or Cl, and the compound of formula (IV) comprises a compound of formula (IVA) CH 2 FCl (IVA).
• reaction by which the compound of formula (III) is converted to a compound of formula (I) is sometimes referred to herein for convenience, but not necessarily by way of limitation, as an addition reaction.
• the formula (I) compound which in certain embodiments is preferably formed by a process comprising a catalyzed Cl addition reaction, is then exposed to reaction conditions effective to produce a reaction product containing one or more of the desired fiuorolefms, preferably one or more compounds of formula (II).
• the conversion step comprises a reaction that is sometimes referred to herein for convenience, but not necessarily by way of limitation, as a reduction reaction and in other aspects as a fluorination dehydrohalogenation reaction. Preferred aspects of each of the preferred steps is described below, with the titles used as headings for these steps being used for convenience but not necessarily by way of limitation.
• CF 2 CF 2
• CFCl sometimes referred to herein as "CTFE”
• one or more fluorinated ethylene compounds are reacted with one or more of CH 2 FCl.
• the addition step comprises contacting, (preferably by introducing into a reactor) the compounds in an CH m Y a-m :formula III mole ratio of from about 1 : 1 to about 200: 1 , more preferably from about 1 : 1 to about 100:1 and even more preferably of from about 2:lto about 3:1.
• the CH 2 FC1:TFE mole ratio of the feeds to the reactor are from about 1:1 to about 200:1, more preferably from about 1 : 1 to about 100:1 and even more preferably from about 1.5:1 to about 2:1.
• this reaction step can be carried out in the liquid phase or in the gas phase, or a combination of liquid/gas phases, and it is further contemplated that the reaction can be carried out batch wise, continuous, or a combination of these.
• the addition step when it is used, may be preformed using a wide variety of process parameters and process conditions in view of the overall teachings contained herein.
• this reaction step comprise a gas phase reaction, preferably in the presence of catalyst, supported on carbon or unsupported, preferably a metal- based catalyst, such as antimony-based catalysts (such as SbF 3 , SbF 5 , and partially flourinated SbCl 3 or SbCl 5 ) aluminum-based catalyst (such as AlCl 3 ), iron-based catalyst such FeCl 3 including such catalysts on a carbon or other appropriate support.
• a metal- based catalyst such as antimony-based catalysts (such as SbF 3 , SbF 5 , and partially flourinated SbCl 3 or SbCl 5 ) aluminum-based catalyst (such as AlCl 3 ), iron-based catalyst such FeCl 3 including such catalysts on a carbon or other appropriate support.
• a metal- based catalyst such as antimony-based catalysts (such as SbF 3 , SbF 5 , and partially flourinated SbCl 3 or SbCl 5 ) aluminum-based catalyst (such as Al
• the gas phase addition reaction may be conducted, for example, by introducing a gaseous form of a compound of formula (III) and formula (IV) into a suitable reaction vessel or reactor.
• the vessel is comprised of materials which are resistant to corrosion, such as Hastelloy, Inconel, Monel and/or fluoropolymers linings.
• the vessel contains catalyst, for example a fixed or fluid catalyst bed, packed with a suitable addition catalyst, with suitable means to heat the reaction mixture to the desired reaction temperature.
• reaction temperatures and pressures may be used, depending on relevant factors such as the catalyst being used and the most desired reaction product, it is generally preferred that at least a portion of the addition step is carried out at a reaction temperature of from about
• the compound of formula (III) and the compound of formula (IV) are introduced into an appropriate reaction vessel in the form of a gas and the reactor is preferably maintained at a temperature of about 50 0 C and the reactor is preferably maintained at a pressure of about 30 psig.
• the conversion of the formula (III) compound, particularly formula (IIIA) compound(s), is preferably at least about 15%, more preferably at least about 20%, and selectivity to compounds of formula I is preferably at least about 50%, more preferably at least about 70%, and even more preferably at least about 75%.
• the methods of the present invention preferably comprise converting a compound of formula (I) to a fluorolef ⁇ n, prefereably a C3 fluorolefm, more preferably a compound of formula (II), and even more preferably tetrafluoropropene.
• the present converting step is carried out under conditions effective to provide a formula (I) conversion of at least about
• the conversion of the compound of formula I to produce a compound of formula II is conducted under conditions effective to provide a formula II selectivity of at least about 25%, more preferably at least about 40%, more preferably at least about 70%, and even more preferably at least about 90%.
• This reaction step can be carried out in the liquid phase or in the gas phase, or in a combination of gas and liquid phases, and it is contemplated that the reaction can be carried out batch wise, continuous, or a combination of these.
• one preferred compound of formula (IA) is 1,1,1,2,2-pentafluoro- 3chloropropane (CF 3 C F 2 CH 2 Cl).
• CF 3 C F 2 CH 2 Cl 1,1,1,2,2-pentafluoro- 3chloropropane
• the above noted reaction proceeds by the formation of another compound in accordance with formula (IA), namely, CF 3 C F 2 CH 3 , which is generated as an intermediate or byproduct of the reaction with hydrogen, methane or other dehydrogenating agent.
• the intermediate formula (IA) compound is then converted to the desired compound of formula (II), preferably HFO- 1234yf, under the existing reaction conditions, and preferably on the surface of the catalyst.
• the stream containing the compound of formula (I), and preferably (IA) is preheated, primarily to avoid condensation, to a temperature of from about 50 0 C to about 90 0 C, preferably about 6O 0 C to about 70 0 C, and introduced into a reaction vessel.
• the appropriate amount of the reducing agent which is preferably from about 0.1 % to about 500% of the stoichometric amount, is then added to the reaction vessel.
• the vessel is comprised of materials which are resistant to corrosion as Hastelloy, Inconel, Monel and/or fluoropolymers linings.
• the vessel contains catalyst, for example a fixed or fluid catalyst bed, packed with a suitable dehydrohalogenation catalyst, with suitable means to heat the reaction mixture to the desired reaction temperature.
• the dehydrohalogenation reaction step may be preformed using a wide variety of process parameters and process conditions in view of the overall teachings contained herein.
• this reaction step comprise a gas phase reaction, preferably in the presence of catalyst, and even more preferably a carbon- and/or metal-based catalyst, such as activated carbon, palladium on carbon, palladium- based catalyst (including palladium on carbon and palladium on aluminum oxides), and ruthenium-based catalysts (including ruthenium on aluminum oxides). It is expected that many other catalysts may be used depending on the requirements of particular embodiments in view of the teachings contained herein.
• the catalysts are fluorinated, preferably for a period of from about several hours (eg, 6 hours).
• fluorination of the catalysts comprises exposing the catalyst to a stream of HF at about reaction temperature and under slight pressure, for example about 5-150 psia.
• the gas phase dehydrohalogenation reaction may be conducted, for example, by introducing a gaseous form of a compound of formula (I), and preferably (IA) and a gaseous form of the reducing agent (and/or dehydrohalogenation agent), into a suitable reaction vessel or reactor.
• a gaseous form of a compound of formula (I), and preferably (IA) and a gaseous form of the reducing agent (and/or dehydrohalogenation agent) into a suitable reaction vessel or reactor.
• the vessel is comprised of materials which are resistant to corrosion as Hastelloy,
• the vessel contains catalyst, for example a fixed or fluid catalyst bed, packed with a suitable reduction/dehydrohalogenation catalyst, with suitable means to heat the reaction mixture to the desired reaction temperature.
• catalyst for example a fixed or fluid catalyst bed, packed with a suitable reduction/dehydrohalogenation catalyst, with suitable means to heat the reaction mixture to the desired reaction temperature.
• reaction temperature for the dehydrohalogentation step particularly where the formula (I) compound comprises (and even more preferably consists essentially of compounds of formula (IA)) is from about 400 0 C to about 800 0 C, preferably about 400 0 C to about 700 0 C.
• the reaction temperature for the dehydrohalogentation step is preferably from about 45O 0 C to about 600 0 C, more preferably about from 450 0 C to about 55O 0 C.
• the reaction temperature for the dehydrohalogentation step is preferably from about 500 0 C to about 700 0 C, more preferably from about 600 0 C to about 700 0 C.
• reaction pressures may be used, depending again on relevant factors such as the specific catalyst being used and the most desired reaction product.
• the reaction pressure can be, for example, superatmospheric, atmospheric or under vacuum, and in certain preferred embodiments is from about 15 to about 120 psia.
• an inert diluent gas such as nitrogen, may be used in combination with the other reactor feeds.
• an inert diluent gas such as nitrogen
• the compound of formula (I) comprise from about 5% to greater than 99% by weight based on the combined weight of diluent and formula (I) compound.
• the amount of catalyst use will vary depending on the particular parameters present in each embodiment.
• the contact time is from about 0.1 seconds to about 1000 second, and preferably from about 2 seconds to about 50 seconds.
• the compound of formula (I) comprises or consists essentially of a compound of formula (IA) and the reducing agent comprises or consists essentially of hydrogen, and particularly where the desired product of formula (II) is HFO-1234yf
• a carbon-based catalyst such as activated carbon, or palladium-based catalyst, or a catalyst comprising palladium and carbon, such as a palladium on carbon catalyst.
• the compound of formula (I) comprises or consists essentially of a compound of formula (IA) and the reducing agent comprises or consists essentially of methane, and particularly where the desired product of formula (II) is HFO-1234yf
• a carbon-based catalyst such as activated carbon
• a catalyst based on a Period 6 metal particularly Cs and Ba
• a catalyst based on a Period 6 metal particularly Cs and Ba
• BaNO 3 or CsNO 3 including in combination with aluminum-based catalyst or catalyst support, such as Al 2 O 3
• Ni-based catalyst such as Ni mesh
• the conversion of the formula (I) compound is at least about 50%, more preferably at least about 65%, and even more preferably at least about 90%.
• the selectivity to HFO-1234yf is at least about 70%, more preferably at least about 80% and more preferably at least about 90%.
• CF 3 CF CHX (IB) where X is as previously defined.
• X is as previously defined.
• the reduction reaction step may be preformed using a wide variety of process parameters and process conditions in view of the overall teachings contained herein. However, it is preferred in certain embodiments that this reaction step comprise a liquid phase reaction, preferably in the presence of catalyst, and even more preferably in the presence of a catalyst contained in a liquid carrier, such as a solvent for at least one or more of the organic reactants. Although it is contemplated that many solvents and catalysts will be adaptable for use in connection with these preferred embodiments, it is generally preferred that the solvent comprises tetrahydrofuran, dioxane and the like, and any combinations of solvents including these. In such preferred embodiments, the catalysts preferably include palladium-based catalyst.
• the palladium based catalyst comprises, and in certain embodiments consists essentially of tetrakis(triphenylphosphine)palladium(0), [ Pd(PPh 3 ) 4 and/or tris(dibenzlideneacetone)dipalladium(0), Pd 2 (dba) 3 and combinations of these.
• ligands for the catalyst are included in the reaction mixture, and although many ligands are believed to adaptable for use with the preferred catalyst systems of the present invention, in certain embodiments the ligands comprise tetraributyl phosphine, ammonium formate and combinations of these and/or other ligands. It is expected that other catalysts may be used depending on the requirements of particular embodiments in view of the teachings contained herein. Of course, two or more any of these catalysts, or other catalysts not named here, may be used in combination.
• the liquid phase reduction reaction may be conducted, for example, by introducing the solvent and catalyst into a suitable reaction vessel or reactor.
• the vessel is comprised of materials which are resistant to corrosion as
• Hastelloy, Inconel, Monel and/or fluoropolymers linings havetelloy, Inconel, Monel and/or fluoropolymers linings.
• the compound of formula (I), preferably including a compound of formula (IB), is preferably cooled to below its boiling point, and preferably to a temperature of from about -5 0 C to about 20 0 C and introduced into the solvent.
• the reaction mixture is then preferably brought to a temperature of from about -20 0 C to about -5O 0 C, and even more preferably to about -30 0 C to about -4O 0 C and then a partial vacuum is applied to pull residual air or O 2 from the reactor.
• the reaction mixture is then preferably heated, preferably with agitation (such as stirring) to a temperature of from about 10 0 C to about 200 0 C, more preferably from about 20 0 C to about 15O 0 C, and the reaction mixture is preferably maintained at this temperature for a time period of from about 1 hour to about 48 hours, more preferably from about 15 hours to about 30 hours.
• the pressure in the reactor may increase in certain embodiments to about 150 psig to about 250 psig, and even more preferably from about 150 psig to about 200 psig.
• the amount of catalyst use will vary depending on the particular parameters present in each embodiment.
• the weight ratio of the compound of formula (I) to catalyst is from about 50,000:1 to about 1:1, and even more preferably from about 100:1 to about 1 :1.
• the conversion of the formula (IB) compound is at least about 85%, more preferably at least about 95%, and even more preferably about 100%.
• the selectivity to HFO-1234yf is at least about 20%, more preferably at least about 30% and more preferably at least about 40%.
• the HFC-235cb is passed through gas-flow controllers into a preheater maintained a temperature of about 300 0 C.
• the gas stream coming out of the preheater is passed through the catalyst bed at the desired temperature over a specified period of time and at a pressure of from about 2.5 - 5.3 psig.
• An on-line GC and a GCMS are used to analyze samples taken at the reactor exit line at regular time intervals.
• the reactor effluent is introduced into a 20 - 60 % KOH scrubber solution, and the effluent from the scrubber solution is then condensed to collect the products.
• HFC-235cb The conversion of HFC-235cb is from about 50% to about 100% and the selectivity to HFO-1234yf is from about 60% to about 100%, depending on the reaction conditions.
• Catalysts ( 100 cc): H is activated carbon; 13wt%
• J is 3wt% BaNO3/A1203 with 0.5wt% CsNO3 used as a promoter
• K is a two zone reaction with two catalysts, specifically 50 cc CsNO3 promoted with
• BaNO3/A1203 is used at 650 0 C in the first zone and 50 cc Calgon activated carbon is used at
• L is Ni mesh.
• the reactor is sealed immediately, cooled to -30 to -40 0 C, and partially evacuated.
• the contents in the Parr reactor are brought to room temperature and gradually heated to 100 0 C with stirring.
• the reactants are maintained at this temperature for 24 hours.
• the pressure in the reactor is increased to approximately 180-200 psig.
• the reactor is then cooled to 25 0 C and the volatile materials are collected in an evacuated metal cylinder.
• CF 3 CF CH 2 (HFO- 1234yf) with Pd 2 (dba) 3 catalyst.
• the reactor is sealed immediately, cooled to the range of from about -30 0 C to about -40 0 C, and partially evacuated.
• the contents in the Parr reactor are brought to room temperature and then gradually heated to 100 0 C with stirring.
• the reactants are maintained at this temperature for 24 hours during which the internal pressure rises to approximately 200 psig.
• the reactor is then cooled to 25°C and the volatile materials are passed through a trap at about -7O 0 C to about -78°C and collected in a cold evacuated metal cylinder.
• Example 17 is repeated except that dioxane is substituted for tetrahydrafuran as the solvent. The result is essentially the same as Example 17.
• the reaction is carried out as in Example 17 except that an equivalent amount of catalyst Pd 2 (dba) 3 is substituted by tris(dibenzlideneacetone)dipalladium (0) chloroform complex, Pd 2 (dba) 3 -CHCl 3 .
• CF 3 CF CH 2 (HFO- 1234yf) with Pd(PPh 3 ) 4 catalyst in tetrahydrofuran.
• the reactor is sealed immediately, cooled to -30 to -40 0 C, and partially evacuated.
• GC Gas chromatographic
• a flow of reducing agent comprising hydrogen gas is maintained at a rate as indicated in Table 3 below.
• the reactor temperature is brought to the temperature indicated in the table.
• the HFC-245cb is passed through gas-flow controllers into a preheater maintained a temperature of about 300 0 C.
• the gas stream coming out of the preheater is passed through the catalyst bed at the desired temperature over a specified period of time and at a pressure of from about 2.5 - 5.3 psig.
• An on-line GC and a GCMS are used to analyze samples taken at the reactor exit line at regular time intervals.
• the reactor effluent is introduced into a 20 - 60 % KOH scrubber solution, and the effluent from the scrubber solution is then condensed to collect the products.
• the conversion of HFC-245cb is from about 30% to about 70% and the selectivity to HFO-1234yf is from about 90% to aboutlOO%, depending on the reaction conditions.
• Catalysts (100 cc): M is NORIT RFC 3; N is Shiro-Saga activated carbon; O is Aldrich activated carbon; P is Calgon activated carbon; Q is 0.5 wt% Pd/C; R is 0.5 wt% PVC; S is Ni-mesh
• This example illustrates the addition formation of compounds of formula (I) by the reaction of TFE with CH 2 FCl in a gas phase reaction.
• a V% inch flow reactor (Monel) 50 grams of freshly prepared catalyst (as indicated below) are charged.
• the preheater was connected to the reactor and always kept 10 0 C below the reactor temperature.
• the reactor was uniformly heated to the desired temperature by an external heating element with an automatic control.
• the exit line from the reactor was connected to an on-line GC and GCMS for analysis.
• a 15 wt% KOH scrubber solution was used at 50 0 C to neutralize acids coming out from the reactor.
• the gas stream coming out of the scrubber solution was then condensed in a cylinder under liquid N2 and then finally fractionated (distilled) to isolate products.
• SbFs/C and AICI 3 /C are used as the catalyst.
• At 50 0 C and under 30 psig reactor pressure when 50 seem of TFE and 150 seem of R31 were passed over SbF5/C to achieve a 26% conversion of TFE and an 82% selectivity to CF 3 CF 2 CH 2 Cl.
• A1C13/C is used as the catalyst, a 35% conversion and 78% selectivity to CF 3 CF 2 CH 2 Cl was obtained.
• This example illustrates the formation of compounds of formula (I) by the reaction of TFE with CH 2 FCl in a gas phase reaction.
• a gas phase reaction Into a 300 ml autoclave, 0.1 mol C 2 F 4 was reacted with 0.2 mol CH 2 ClF in the presence of 0.05 mol of AlCl 3 at 20-30° for 3 hr to give 60% yield to CF 3 CF 2 CH 2 Cl which was then isolated and purified by distillation.
• This example illustrates the formation of compounds of formula (I) by the reaction of TFE with CH 2 FCl in a gas phase reaction.
• a gas phase reaction Into a 300 ml autoclave, 0.1 mol C 2 F 4 was reacted with 0.2 mol CH 2 ClF in the presence of 0.05 mol of
• This example illustrates the formation of compounds of formula (I) by the reaction of CTFE with CH 2 FCl in a gas phase reaction.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Priority Applications (6)

Applications Claiming Priority (2)

Publications (1)

Family

ID=37866036

Family Applications (1)

Country Status (8)

Cited By (13)

Families Citing this family (6)

Citations (7)

Family Cites Families (12)

• 2006
  • 2006-11-03 JP JP2008540087A patent/JP5592607B2/ja not_active Expired - Fee Related
  • 2006-11-03 CN CNA2006800498307A patent/CN101356143A/zh active Pending
  • 2006-11-03 CA CA2628446A patent/CA2628446C/en active Active
  • 2006-11-03 RU RU2008122214/04A patent/RU2425822C2/ru active
  • 2006-11-03 KR KR1020087012086A patent/KR101351802B1/ko active Active
  • 2006-11-03 EP EP11156860.6A patent/EP2348007B1/en not_active Ceased
  • 2006-11-03 ES ES06827435.6T patent/ES2611052T3/es active Active
  • 2006-11-03 WO PCT/US2006/042936 patent/WO2007056128A1/en not_active Ceased
  • 2006-11-03 EP EP06827435.6A patent/EP1954661B1/en active Active

Patent Citations (7)

Non-Patent Citations (8)

Also Published As

Similar Documents

Legal Events