Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/32—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions without formation of -OH groups
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
  • C07C29/172—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds with the obtention of a fully saturated alcohol
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/36—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal
  • C07C29/38—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal by reaction with aldehydes or ketones

Definitions

• the invention relates to a process for the preparation of 1,6-hexanediols by reacting formaldehyde with propenes to give homoallyl alcohols, converting the homoallyl alcohols in a metathesis reaction to 3-hexen-1,6-diols and subsequent hydrogenation to 1,6-hexanediols.
• 1,6-hexanediol is an important intermediate for the production of
• Polyesters and polyurethanes On an industrial scale, it is produced from adipic acid or from the by-products obtained in the production of adipic acid.
• 1,6-hexanediol can be prepared by hydrogenating adipic acid or adipic acid derivatives at temperatures from 170 ° C. to 240 ° C. and pressures from 150 to 300 bar (Ullmann's Encyclopedia of Industrial Chemistry, Nol. AI, p. 310 ; Weissermel, Arpe, Industrial Organic Chemistry, 3.
• Adipic acid esters are hydrogenated to 1,6-hexanediol in the gas phase at pressures of 10 to 70 bar.
• the disadvantage of these ner drives lies in the use of acidic and thus corrosive material flows. Furthermore, their versatility makes them technically complex.
• WO 97/31 882 describes a process for the preparation of 1,6-hexanediol from by-products which are obtained in the oxidation of cyclohexane to cyclohexanone / cyclohexanol which is carried out for the production of adipic acid.
• a carboxylic acid mixture is obtained by water extraction of the reaction mixture.
• the carboxylic acid mixture is then mixed with low molecular weight alcohols to give the corresponding carbon implemented acid esters, which are freed from excess alcohol and low boilers in a two-stage distillation.
• the ester fraction obtained in this way is catalytically hydrogenated, and 1,6-hexanediol is then obtained from the hydrogenation discharge in a pure distillation stage.
• This six-stage ner driving is a technically complex ner driving.
• Another disadvantage is the use of acidic and thus corrosive material flows, which require special materials in relation to the system design.
• the hydrogenation is carried out in a high-pressure process, so that high investment costs are incurred for corresponding reactors.
• the process according to the invention allows 1,6-hexanediol to be prepared in a way which is independent of the production of adipic acid or of the use of adipic acid as a starting material.
• the starting materials used are inexpensive and readily available compounds, which is particularly advantageous when the process according to the invention is implemented on an industrial scale.
• 1,6-hexanediol is particularly preferred by reacting formaldehyde with propene to give 3-buten-1-ol, converting 3-buten-1-ol in a metathesis reaction to 3-hexen-1, 6-diol and subsequent Hydrogenation to 1,6-hexanediol produced.
• step a) of the process according to the invention propenes which carry a substituent from the hydrogen, alkyl or aryl series at the 2-position are reacted with formaldehyde to give the corresponding homoallyl alcohols.
• propenes which at 2-position have a substituent selected from hydrogen, alkyl or aryl are used, said substituent for aryl in turn one or more substituents from the group linear and branched C j -CG alkyl and C ⁇ - C 8 alkoxy, halogenated linear and branched C j -Cg alkyl and Cj Cg alkoxy, linear and branched C - * - C 8 alkyloxycarbonyl and aryloxycarbonyl, Cj Cg dialkylamino, diarylamino, cyano and halogens such as F, Cl, Br and I can carry, and said substituent is alkyl in turn one or more substituents from the group linear and branched C j -CG alkyl, linear and branched C ⁇ -C 8 alkyloxycarbonyl and
• Aryloxycarbonyl, -CC 8 -dialkylamino and diarylamino can wear.
• propenes are used which carry a substituent from the hydrogen, C 1 -C 4 -alkyl or phenyl group at the 2-position, the phenyl substituent mentioned in turn being one or more linear and branched substituents from the series C - * - C 8 alkyl and Cj-C - alkoxy, halogenated linear and branched Cj-C 8 alkyl and Cj-Cg-alkoxy, linear and branched Ci-Cg-alkyloxycarbonyl and aryloxycarbonyl, Cj-Cg-dialkylamino, diarylamino , Cyano and halogens such as F, Cl, Br and I can carry and the substituent C 1 -C 4 - alkyl in turn one or more substituents from the series linear and branched C 1 -C 4
• the formaldehyde used in the process according to the invention can be used in gaseous form, in polymeric form or in the form of an aqueous solution. If formaldehyde is used in the form of an aqueous solution in the process according to the invention, then a 35 to 55% solution, particularly preferably a 35% solution, is preferably used. If formaldehyde is used in polymeric form in the process according to the invention, 1,3,5-trioxane,
• 1,3,5,7-tetroxane or paraformaldehyde which has a degree of polymerization of 8 to 100, is used.
• Paraformaldehyde or gaseous formaldehyde is very particularly preferably used in the process according to the invention.
• stage a) of the process according to the invention formaldehyde and the propenes to be used according to the invention can be reacted in stoichiometric amounts, but the propenes are preferably used in excess.
• 1.5 to 100 mol of the propenes to be used according to the invention are preferably used per mol of formaldehyde, in particular 2 to 60 mol, particularly preferably 3 to 30 mol.
• the reaction of formaldehyde with the propenes to be used according to the invention is preferably carried out in the presence of acidic compounds such as, for example, phenols or zeolites, basic compounds such as, for example, amines, Group V metal carbonyls, isopoly- or heteropolyacids and their salts, halogens or metal salts.
• acidic compounds such as, for example, phenols or zeolites
• basic compounds such as, for example, amines, Group V metal carbonyls, isopoly- or heteropolyacids and their salts, halogens or metal salts.
• metal salts such as, for example, halides, carbonates, phosphates, carboxylates or sulfites of the metals of the first to fourth main groups of the periodic table and of the first to seventh subgroups of the periodic table or metals from the group of the lanthanides.
• the reaction is particularly preferably carried out in the presence of phosphates; preferred phosphates are alkali metal and alkaline earth metal orthophosphates, pyrophosphates, metaphosphates and polyposphates.
• the reaction is very particularly preferably carried out in the presence of mixtures of alkali metal and / or alkaline earth metal hydrogen phosphates and alkali metal and / or alkaline earth metal dihydrogen phosphates, since an increased selectivity of the formation of the desired homoallyl alcohols is observed.
• Mixtures of dialkali metal hydrogen phosphates and alkali metal dihydrogen phosphates are particularly preferably used, very particularly preferably mixtures of disodium and or dipotassium hydrogen phosphates and sodium and / or
• Kaliumdihydrogenphosphaten Mixtures of alkali metal and / or alkaline earth metal hydrogen phosphates and alkali metal and / or alkaline earth metal dihydrogen phosphates in a molar ratio of 5: 1 to 1: 2, particularly preferably from 3: 1 to 1: 1.5, are preferably used.
• Alkali metal and or alkaline earth metal dihydrogen phosphates are preferably used in an amount of 0.1 to 30 mol%, preferably 0.5 to 25 mol% and particularly preferably 0.5 to 15 mol%, based on formaldehyde.
• Propenes can be carried out in the presence of a solvent or in bulk become. It is preferably carried out in the presence of a solvent.
• Preferred solvents are saturated aliphatic hydrocarbons, alicyclic hydrocarbons, aromatic hydrocarbons, alcohols, esters or ethers.
• Ethers such as diisopropyl ether or diethylene glycol dimethyl ether or substituted aromatic hydrocarbons such as toluene, xylenes, ethylbenzene or mesitylene are particularly preferably used. Toluene and xylenes are very particularly preferably used.
• the reaction of formaldehyde with the propenes to be used according to the invention is preferably carried out at temperatures from -20 ° to 320 ° C, particularly preferably at 50 ° C to 300 ° C and very particularly preferably at 180 ° C to 280 ° C.
• the reaction of formaldehyde with the propenes to be used according to the invention is preferably carried out at pressures from 100 to 250 bar, particularly preferably 100 to 230 bar and very particularly preferably 110 to 200 bar.
• Propene is preferably carried out in such a way that formaldehyde, preferably paraformaldehyde or gaseous formaldehyde, is initially introduced together with a mixture of dialkali metal hydrogen phosphates and alkali metal dihydrogen phosphates in a solvent and then the propenes to be used according to the invention, preferably propylene, are added.
• the reaction mixture can be reacted directly in stage b) of the process according to the invention or worked up beforehand without further workup.
• the reaction mixture is preferably worked up before carrying out stage b) of the process according to the invention.
• Stage a) is in the presence of predominantly insoluble in the reaction mixture
• the reaction mixture is preferably filtered after the reaction has ended.
• the filtrate can now be worked up, for example, by distillation or by extraction.
• the workup is preferably carried out in such a way that the homoallyl alcohol formed is separated off by distillation.
• stage b) of the process according to the invention the homoallyl alcohols obtained in stage a) are converted to 3-hexene-1,6-diols in a metathesis reaction in the presence of a metathesis catalyst.
• the metathesis catalysts used in stage b) of the process according to the invention are known, for example, from WO 00/43343. These are heterogeneous or homogeneous transition metal complexes, preferably those of transition metals of group IV and VI to X of the periodic table. Homogeneous transition metal complexes are preferably used.
• stage b) of the process according to the invention preference is given to using catalysts of the formula (I)
• X 1 and X 2 are the same or different and represent an anionic ligand, R 1 and R 2 are identical or different and represent hydrogen, cycloalkyl or aryl,
• L 1 represents an N-heterocyclic sheaf
• L 2 stands for a neutral electron donor, preferably for an N-heterocyclic carbene, a phosphine or a phosphite and
• M stands for Ru or Os.
• stage b) of the process according to the invention particular preference is given to using catalysts of the formula (I) in which
• X 1 and X 2 are the same and represent an anionic ligand from the halide or alcoholate series
• R 1 and R 2 are different and represent hydrogen and aryl
• R 3 to R 6 are the same or different and represent hydrogen or hydrocarbons
• L 2 stands for a phosphine PR 3 7 , where R 7 stands for alkyl and / or aryl and M stands for Ru.
• step b) of the process according to the invention very particular preference is given to using compounds of the formula (I) as catalysts in which
• X 1 and X 2 are the same and represent a halide, preferably chloride,
• R 1 and R 2 are different and represent hydrogen or aryl, preferably phenyl,
• L 1 represents an N-heterocyclic carbene of the formula (II), in which
• R 3 and R 4 are the same and stand for hydrogen and
• R 5 and R 6 are the same and represent an alkyl-substituted phenyl radical, preferably 2,4,6-trimethylphenyl,
• L 2 represents a phosphane, preferably tricyclohexylphosphine and
• the metathesis reaction b) of the process according to the invention can be carried out in the presence of a solvent or in bulk.
• Preferred solvents are ethers, such as tetrahydrofuran, diethylene glycol, Dimethyl ether, diethyl ether or methyl tert-butyl ether, hydrocarbons such as, for example, cyclohexane, benzene, toluene or cumene, halogenated hydrocarbons such as, for example, chloroform, dichloromethane, dichloroethane or chloropropane, and esters, for example methyl acetate or ethyl acetate, are used. If the metathesis reaction b) of the inventive method in
• halogenated hydrocarbons particularly preferably chloroform or dichloromethane, are preferably used.
• the reaction is very particularly preferably carried out in bulk.
• the process is preferably -40 ° C to 150 ° C, more preferably -10 ° C to 100 ° C, most preferably 10 ° C to 70 ° C.
• the pressure in the metathesis reaction b) of the process according to the invention is preferably 0.01 to 10 bar, particularly preferably 0.1 to 2.5 bar, very particularly preferably 0.25 to 0.75 bar.
• the metathesis reaction b) of the process according to the invention can be carried out continuously or batchwise, preferably in an inert gas atmosphere, such as, for example, in a nitrogen atmosphere.
• step c) of the process according to the invention the reaction product of step b) is hydrogenated with hydrogen in the presence of a hydrogenation catalyst, 1,6-hexanediols being obtained as reaction products.
• the hydrogen pressure is preferably 1 to 100 bar, particularly preferably 1 to 70 bar, very particularly preferably 1 to 40 bar.
• the reaction temperature is preferably 0 ° C to 200 ° C ? particularly preferred
• the hydrogenation c) of the process according to the invention can be carried out in the presence of a solvent or in bulk. If the reaction is carried out in the presence of a solvent, ethers such as, for example, tetrahydrofuran, diethylene glycol dimethyl ether, diethyl ether, methyl tert-butyl ether or dioxane, alcohols, such as, for example, methanol, ethanol, propanol or 1,6-hexanediol, are preferably used or esters, such as, for example, methyl acetate, ethyl acetate, propyl acetate or tert-butyl acetate.
• ethers such as, for example, tetrahydrofuran, diethylene glycol dimethyl ether, diethyl ether, methyl tert-butyl ether or dioxane
• alcohols such as, for example, methanol, ethanol, propanol or 1,6-hex
• the hydrogenation c) of the process according to the invention is carried out in the presence of a solvent
• alcohols such as, for example, methanol, ethanol or propanol
• the hydrogenation is very particularly preferably carried out in bulk.
• the hydrogenation c) of the process according to the invention is carried out in the presence of a hydrogenation catalyst.
• a hydrogenation catalyst Known homogeneous or heterogeneous catalysts can be used as hydrogenation catalysts.
• Heterogeneous catalysts such as noble metal catalysts from the Pt, Pd and Rh series or transition metal catalysts from the Mo, W, Cr, Fe, Co and Ni series are preferably used.
• the noble metal and transition metal catalysts can be used in elemental form or in the form of their oxides or sulfides. Mixtures of the catalysts mentioned can also be used.
• the heterogeneous noble metal and transition metal catalysts can be applied to supports such as activated carbon, aluminum oxide or kieselguhr to increase the activity and stability.
• Catalysts which contain elements from groups VII to X of the periodic table, for example Pd, Pt, Re, Cu or Ni, are particularly preferred.
• Pt / activated carbon, Pd activated carbon, Re / activated carbon, Cu / activated carbon, Cu / SiO 2 , Ni / activated carbon or Raney nickel are particularly preferably used.
• the metathesis catalyst used in the metathesis reaction is used as the hydrogenation catalyst used, preferably in such a way that the reaction mixture present after the metathesis reaction b) is subjected directly to a hydrogenation c) without further working up.
• Both the metathesis reaction b) and the hydrogenation c) are preferably carried out in bulk.
• the possible implementation of stages b) and c) in a one-pot reaction represents a further advantage of the invention
• the hydrogenation c) of the process according to the invention is carried out using hydrogenation catalysts which are different from the metathesis catalysts used.
• Crude product from the metathesis reaction b) is preferably dissolved in a solvent, preferably in an alcohol, and the hydrogenation catalyst, preferably a heterogeneous catalyst, is added to the reaction mixture.
• a solvent preferably in an alcohol
• the hydrogenation catalyst preferably a heterogeneous catalyst
• the one used in the metathesis reaction is very particularly preferred
• Metathesis catalyst is used as the hydrogenation catalyst, the reaction mixture present after the metathesis reaction b) being subjected directly to a hydrogenation c) without further workup, and thus reaction steps b) and c) are carried out in a one-pot reaction.
• the 1,6-hexanediols obtained by the process according to the invention can be worked up by distillation or crystallization.
• the working up is preferably carried out in such a way that, after the catalyst used in reaction step c) has been separated off, the 1,6-hexanediols obtained are obtained by distillation.
• the reaction mixture obtained from Example 2 was metered in at 20 bar

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  • 2000-12-22 DE DE2000164750 patent/DE10064750A1/de not_active Withdrawn
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