Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/0234—Nitrogen-, phosphorus-, arsenic- or antimony-containing compounds
  • B01J31/0235—Nitrogen containing compounds
  • B01J31/0237—Amines
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/72—Copper
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/22—Organic complexes
  • B01J31/2204—Organic complexes the ligands containing oxygen or sulfur as complexing atoms
  • B01J31/2208—Oxygen, e.g. acetylacetonates
  • B01J31/2226—Anionic ligands, i.e. the overall ligand carries at least one formal negative charge
  • B01J31/223—At least two oxygen atoms present in one at least bidentate or bridging ligand
  • B01J31/2234—Beta-dicarbonyl ligands, e.g. acetylacetonates
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/26—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24
  • B01J31/28—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24 of the platinum group metals, iron group metals or copper
  • B01J31/30—Halides
• • 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
  • C07C17/275—Preparation of halogenated hydrocarbons by reactions involving an increase in the number of carbon atoms in the skeleton by addition reactions of hydrocarbons and 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
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
  • B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
  • B01J2231/32—Addition reactions to C=C or C-C triple bonds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/10—Complexes comprising metals of Group I (IA or IB) as the central metal
  • B01J2531/16—Copper

Definitions

• the present invention relates to a process for the preparation of halogenated hydrocarbons comprising at least 3 carbon atoms by catalytic reaction between a haloalkane and an olefin.
• Patent application WO 97/07083 describes a process for the preparation of halogenated hydrocarbons under the catalytic action of cuprous chloride in the presence of t.butylamine as cocatalyst.
• Patent application EP-A-787 707 describes a process for the preparation of 1,1,1,3,3-pentachlorobutane under the catalytic action of cuprous chloride in the presence of cocatalysts of the amino type.
• the various constituents of the reaction medium are first introduced into a reactor, then the latter is brought to the reaction temperature.
• the yield and selectivity of the telomerization product are however not satisfactory.
• the invention therefore aims to provide a process which allows access with excellent yields and selectivities with halogenated hydrocarbons comprising at least 3 carbon atoms, in a single step from readily available reactants and in which the losses are minimized in cocatalyst, allowing maximum reuse.
• the present invention relates to a batch process for the preparation of halogenated hydrocarbons comprising at least 3 carbon atoms according to which a haloalkane and an olefin are reacted in a reaction medium in the presence of a catalyst and a cocatalyst , process in which (a) in a first step, a progressive addition is carried out to the reaction medium during the reaction of at least part of the cocatalyst; (b) in a subsequent step, at least part of the cocatalyst is recovered with a view to its reuse.
• the initial reaction medium generally comprises the catalyst, the haloalkane, the olefin and optionally a solvent.
• the initial reaction medium also comprises a fraction of the cocatalyst.
• the fraction of the cocatalyst included in the initial reaction medium is generally at least 1% of the total amount of cocatalyst used. Often this fraction is at least 5%. More often, it is at least 10%. Preferably, it is at least 15%. It is generally at most 80% of the total amount of cocatalyst. Often it is at most 70%. Preferably it is at most 60%.
• the progressive addition can be carried out in the liquid phase or in the gas phase.
• the addition in the liquid phase can be carried out, for example, by means of a tube immersed in the reaction medium.
• the gas phase addition can be carried out, for example, by introducing the cocatalyst in the vapor state into the headspace of the reactor.
• the progressive addition of the cocatalyst can be, for example, an addition carried out in several portions, identical or not.
• This mode of addition of the cocatalyst corresponds to what is called, for bioreactors, a “fed-batch” type reaction (Ullmann's Encyclopedia of Industrial Chemistry, 5. Ed. Vol B4 p.387-388).
• a portion of cocatalyst is introduced into the initial reaction medium, then at least one other portion is added later, during the reaction.
• the number of portions to be used is theoretically not limited, approaching another mode of addition of the cocatalyst according to which the progressive addition is carried out continuously. However, a number of portions of at most 100 is generally used. Often the number is at most 50. Most often the number is at most 20. A number of at most 10 gives good results. A maximum number of 5 is advantageous. A number of at most 4 is preferred. Excellent results are obtained with a number of 2 or 3.
• the time intervals between the addition of the portions are generally at least 1 min. Often the intervals are at least 5 min. More often the intervals are at least 30 min. Preferably the intervals are at least 1 hour. Intervals of about 2, 3, 4, 5 or 6 hr give good results.
• R is the ratio between the molar flow rate of cocatalyst added continuously and the molar quantity of catalyst used defined by the following equation:
• the ratio R [Quantity of cocatalyst / time] (mol / h) / Quantity of catalyst per batch (mol).
• the ratio R is generally at least 0.1 h "1. More often the ratio is at least 0.5 h " 1 . Preferably the ratio is at least 1 hr. 1. In a particularly preferred manner, the ratio is at least 2. Most preferably, the ratio is at least 3. Generally, the ratio is at most 1000 h "1 . Often the ratio is at most 500 h "1. More often the ratio is at most 100 h " 1 . Preferably the ratio is at most 50 h "1. In a particularly preferred manner, the ratio is at most 10. Most preferably, the ratio is at most 9.
• the duration during which the the continuous addition is generally at least 10 minutes, more often the duration is at least 30 minutes, preferably the duration is at least 1 hour, durations of approximately 2, 3, 4, 5 or 6 hrs give good results.
• a particularly advantageous embodiment of the process consists in regulating the addition of the cocatalyst as a function of the temperature of the reaction medium.
• the initial reaction medium comprises generally the catalyst, the haloalkane and optionally the solvent.
• the initial reaction medium also comprises cocatalyst and / or olefin. It has been found, surprisingly, that when a gradual addition of at least part of the cocatalyst and at least part of the olefin is carried out, there is observed, in addition to the advantages mentioned above, an increase selectivity to halogenated hydrocarbons from the addition of a haloalkane molecule to an olefin molecule.
• the gradual addition of the olefin can be carried out separately from the gradual addition of the cocatalyst. It is also possible to gradually add a mixture of olefin and cocatalyst.
• the initial reaction medium generally comprises the catalyst, and optionally solvent.
• the initial reaction medium also comprises cocatalyst and / or haloalkane.
• the initial reaction medium can also comprise olefin.
• the progressive addition of the haloalkane can be carried out separately from the progressive addition of the cocatalyst and optionally the olefin.
• a gradual addition of a mixture of haloalkane and cocatalyst is carried out of a mixture comprising cocatalyst, haloalkane and olefin. It is also possible to carry out a gradual addition to the reaction medium of other compounds to be used in the reaction such as, for example, the catalyst and the solvent.
• the specific modes and conditions of gradual addition described above with respect to the cocatalyst also apply, where appropriate, to the gradual addition of the olefin, of the haloalkane and / or of any other compound for which a progressive addition.
• reaction medium is left to react after the gradual addition for a sufficient time to obtain an optimum between the conversion of the olefin and the observed degradation of the cocatalyst.
• the catalyst can be chosen from the metal derivatives known to catalyze the reaction of a haloalkane with an olefin. Copper salts and organic copper compounds are particularly preferred as catalyst. Such catalysts are described, for example, in patent applications WO-A-98/50329 and WO-A-98/50330, the content of which in this connection is incorporated by reference. Copper (I) chloride, copper (II) chloride, anhydrous or dihydrate, or copper (II) acetylacetonate give good results. Anhydrous copper (II) chloride is particularly preferred
• the reaction is carried out in the presence of a cocatalyst selected, for example, from the group consisting of amines and trialkylphosphine oxides. It is preferred to use an amine as cocatalyst, preferably isopropylamine, t.butylamine and tert-alkyl amines
• PRIMENE® 81 -R and JM-T sold by Rohm and Haas Company. T.butylamine, the amines PRIMENE® 81-R and PRIMENE® JM-T are very particularly preferred.
• the PRIMENE® 81-R amine is a mixture of tert.-alkyl primary amines with a number of carbon atoms from 12 to 14.
• the PRIMENE® JM-T amine is a mixture of tert primary amines. -alkyl whose number of carbon atoms is from 18 to 22.
• trialkylphosphine oxides which can be used as cocatalyst, there may be mentioned in particular the compounds of formula (RlR2R3) PO, in which RI, R2 and R3 represent identical or different, preferably linear, C3-C10 alkyl groups.
• RI, R2 and R3 represent identical or different, preferably linear, C3-C10 alkyl groups.
• a preferred catalyst-cocatalyst system in the process according to the invention tion is the system consisting of a copper compound and an amine. Particularly preferred are the catalyst-cocatalyst systems formed by copper (II) acetylacetonate or copper (II) chloride with t.butylamine. Another particularly preferred catalyst-cocatalyst system is the system formed by copper (II) acetylacetonate and PRIMENE®JM-T.
• the haloalkanes used in the process according to the present invention preferably have from one to three carbon atoms and preferably contain at least 2 chlorine atoms.
• haloalkanes By way of examples of haloalkanes according to the present invention, mention may be made of dichloromethane, chloroform, carbon tetrachloride, 1,1,1-trichloroethane. Carbon tetrachloride is very particularly preferred.
• the haloalkanes may also include other substituents such as other halogen atoms, alkyl groups or halo. However, haloalkanes containing only chlorine as the halogen are preferred.
• the olefin used in the process according to the present invention is generally an ethylene, a propylene or a butene, optionally substituted with a substituent.
• Halogenated olefins are particularly suitable. Among the halogenated olefins, chlorinated olefins give good results. Chlorinated olefins which can be used in the process according to the invention generally correspond to the general formula
• R1C1C CR2R3 (I) in which RI, R2, R3 and R4 independently represent an H or Cl atom, an alkyl or alkenyl group, linear, cyclic or branched, optionally substituted, or an aryl or heteroaryl group, optionally substituted.
• chlorinated olefins mention may be made of vinyl chloride, vinylidene chloride, trichlorethylene, the various isomers of chloropropenes such as 1-chloroprop-1-ene, 2-chloroprop-1-ene and 3-chloroprop-1-ene. Excellent results can be obtained with vinyl chloride and 2-chloroprop-1-ene.
• the overall molar ratio, that is to say between the total quantities used per batch, between the catalyst and the olefin is usually greater than or equal to 0.0001.
• it is greater than or equal to 0.0005.
• it is greater than or equal to 0.001.
• the molar ratio between the catalyst and the olefin is usually less than or equal to 1.
• it is less than or equal to 0.5.
• it is less than or equal to 0.1.
• the amount of cocatalyst used per batch is generally at least 10 times the amount of catalyst used per batch.
• the amount of cocatalyst used is at least 20 times the amount of catalyst.
• the amount is at most 100 times the amount of catalyst.
• the amount is at most 75 times the amount of catalyst.
• the recovery of the cocatalyst in step (b) of the process according to the invention can be carried out by well-known separation techniques. It is also advantageously possible to use a method of recovering a cocatalyst from an aqueous phase comprising a step of treating an aqueous phase with at least one base and a step in which the cocatalyst of the aqueous phase treated with washing.
• the aqueous phase can be obtained, for example, by contacting the reaction mixture containing cocatalyst, obtained after step (a) of the process according to the invention with an aqueous medium, preferably with a hydrochloric acid solution.
• the reaction medium is maintained at a temperature and a pressure sufficient to allow the catalytic reaction of the haloalkane with the olefin.
• the preferred reaction conditions in the process according to the invention with regard to temperature, pressure and duration are described in patent application WO-A-98/50330, the content of which in this connection is incorporated by reference. The same applies to the molar ratios between the haloalkane and the olefin, between the cocatalyst and the olefin and, where appropriate, between the solvent and the olefin, it being understood that these are the relationships between the overall quantities used.
• the presence of a cocatalyst generally makes it possible to carry out the reaction in the absence of solvent.
• the reaction can also be carried out in the presence of a solvent. Any solvent in which the reactants form the desired product with a satisfactory yield can be used.
• halogenated hydrocarbons obtained according to the process of the present invention generally belong to the family of chlorinated alkanes comprising at least three carbon atoms. Often halogenated hydrocarbons contain only chlorine as the halogen.
• the halogenated hydrocarbons obtained according to the process of the present invention correspond to the general formula C n H ( "2n + 2) -pClp in which n is an integer and has the values 3 or 4, p is an integer which has the values 3 to 7.
• Examples of compounds obtained according to the process of the present invention are 1,1,1,3,3-pentachloropropane, 1,1,2,3,3-pentachloropropane, 1, 1,1,3,3-pentachlorobutane, 1,1,1,3- tetrachloropropane, 1,1,3,3-tetrachlorobutane, 1,1,1,3,3,3- hexachlororopropane and l, Among these compounds, 1,1,3,3,3 -pentachl oropropane, 1,1,1,3,3-pentachlorobutane and 1,1,3,3,3, 1-dichloro-2-trichloromethylpropane. 3-hexachlororopropane are preferred, 1,1,1,3,3-pentachlorobutane and 1,1,1,3,3-pentachloropropane are most particularly preferred.
• halogenated hydrocarbons obtained according to the process of the invention are precursors of the corresponding fluorinated analogs, which can be easily obtained by treatment with hydrogen fluoride, preferably anhydrous, optionally in the presence of a fluorination catalyst such as by example an antimony salt, a titanium salt, a tantalum salt or a tin salt. Halides are preferred as the salt of said metals.
• fluorination catalysts which can be used are chosen from compounds, preferably oxides, of chromium, of alumina and of zirconium.
• fluorinated hydrocarbons correspond to the formula C n H (2n-i-2) -pFp in which n is an integer and has the values 3 or 4 and p is an integer which has the values 3 to 7
• Preferred fluorinated hydrocarbons are chosen from 1, 1,1,3,3-pentafluorpropane, 1,1,1,3,3,3-hexafluorpropane and 1,1,1,3,3, - pentafluorbutane.
• the invention therefore also relates to a method for obtaining a fluorinated hydrocarbon comprising (a) the synthesis of a halogenated hydrocarbon according to the process according to the invention and (b) a treatment of the halogenated hydrocarbon derived from (a ) with hydrogen fluoride as described above.
• 1,1,1,3,3-pentachlorobutane (HCC-360) was prepared by reaction between 2-chloroprop-1-ene (2-CPe) and carbon tetrachloride in the presence of Cu (II acetylacetonate) ) and Prim imperative® JM-T.
• 2-CPe 2-chloroprop-1-ene
• carbon tetrachloride in the presence of Cu (II acetylacetonate)
• Prim imperative® JM-T 0.15 g of copper salt, 0.9 g of Primene® JM-T and 48 g of CC14 were introduced into a 300 ml autoclave in hastelloy C276.
• the apparatus was then sealed and placed in a vertical oven.
• the stirring was carried out by a magnetic bar placed at the bottom of the autoclave.
• the temperature was gradually increased.
• Example 1 was repeated by introducing all of the reagents (2-CPe and CC14) and of the cocatalyst (Primène® JM-T) at the start of the test. After 5 a.m. reaction, the conversion of 2-CPe was 45%, with a selectivity to HCC-360 of 81%.
• Example 3
• 1,1,1,3,3-Pentachlorobutane was prepared by reaction between 2-chloroprop-1-ene (2-CPe) and carbon tetrachloride in the presence of cupric chloride and t.butylamine. To do this, 0.094 g of CuC12, 27.1 g of 2-CPe and 108.5 g of CC14 were introduced into a 300 ml autoclave in hastelloy C276. The apparatus was then sealed and placed in a vertical oven. The stirring was carried out by a magnetic bar placed at the bottom of the autoclave. The temperature was gradually increased.
• 1,1,1,3,3-Pentachlorobutane was prepared by reaction between 2-chloroprop-1-ene (2-CPe) and carbon tetrachloride in the presence of cupric chloride and t.butylamine.
• 2-CPe 2-chloroprop-1-ene
• carbon tetrachloride in the presence of cupric chloride and t.butylamine.
• 0.093 g of CuCl 2 8.8 g of 2-CPe, 106.9 g of CC14 and 0.7 g of t.butylamine were introduced into a 300 ml autoclave in hastelloy C276.
• the apparatus was then sealed and placed in a vertical oven.
• the stirring was carried out by a magnetic bar placed at the bottom of the autoclave.
• the temperature is gradually increased to 70 ° C.
• Examples 3 and 4 were repeated, introducing all of the reagents (2-CPe and CC14) and of the cocatalyst (t.butylamine) at the start of the test. After 10 h of reaction at 70 ° C, the conversion of 2-CPe is complete (100%) but the selectivity for HCC-360 is only 95.1%. 93% of t.butylamine was consumed.
• Example 6 (recovery of t.butylamine) A manufacturing reaction of 1,1,1,3,3-pentachlorobutane was carried out according to the process according to the invention using CuCl 2 .2H O as catalyst and t.butylamine as cocatalyst.
• reaction mixture resulting from this reaction was subjected to washing with an aqueous HCl solution containing 1.112 moles of HCl per kg, in an amount of 0.35 kg of aqueous HCl solution per kg of reaction mixture.
• an organic phase was recovered, consisting essentially of 1,1,1,3,3-pentachlorobutane and unconsumed reagents, having a copper content of 0.03 mg / kg and a t.butylamine content of 1.34 mmol / kg and an aqueous phase containing 644 mg Cu / kg and 694 mmol t.butylamine / kg.
• a fraction of the recovered aqueous phase was heated to boiling in a distillation apparatus, while bringing the pH to a value of 10.5 by adding to the boiling aqueous phase an aqueous solution having an NaOH content. 50% by weight.
• the water recovered after filtration contained only 3.8 mg / kg of Cu and 2.9 mmol / kg of t.butylamine.

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• 2000
  • 2000-09-26 WO PCT/EP2000/009493 patent/WO2001025175A1/fr not_active Ceased
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  • 2000-09-26 AU AU79089/00A patent/AU7908900A/en not_active Abandoned
  • 2000-09-26 EP EP00969329A patent/EP1222153B2/fr not_active Expired - Lifetime
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