CA2077007C - Process for the preparation of alcohols - Google Patents

Abstract

The invention relates to a process for the preparation of an alcohol by hydrogenation of a carbonyl compound at elevated temperature and superatmospheric pressure in the presence of a homogeneous catalytic system comprising a source of a Group VIII
metal compound and a bidentate phosphine. Conveniently, an aldehyde which has been prepared by hydroformylation of an olefinically unsaturated compound is used as starting material.

Description

~~°~pl ~~~1 PROCESS FOR THE PREPARATION OF ALCOHOLS
This invention relates to a process for the preparation of an alcohol by hydrogenation of a carbonyl compound at elevated temperature and superatmospheric pressure in the presence of a homogeneous catalytic system.
Catalyst systems which have been proposed for this process, include catalysts based on soluble Group VIII metal compounds, for example of cobalt or rhodium.
Precursors for use in this process, such as aldehydes or ketones may, for instance, be obtained by hydroformylation or hydro-acylation of an olefinically unsaturated compound in the presence of a Group VIII metal catalyst. The hydroformylation process has attained industrial application and is also known as the oxo process. Frequently, the aldehyde produced by hydroformylation of an olefin is separated from the reaction mixture obtained by the hydroformylation to eliminate the catalyst and by-products and is subsequently used in the hydrogenation.
US-A-4 263 449 discloses a process for the preparation of alcohols, wherein the aldehyde-containing reaction product of a hydroformylation reaction is used as such in a subsequent hydrogenation reaction catalysed by a heterogeneous Raney nickel or cobalt catalyst. Water is added far generating a biphasic reaction product facilitating separation of the catalysts used. Apart from the inherent complications of the use of a plurality of catalysts, the use of active Raney catalysts will concurrently hydrogenate any olefin values remaining in the hydroformylation product.
According to GB-A-1 270 985, cobalt carbonyls modified by tertiary phosphines, known to be active as hydroformylation catalyst, can be used in the hydrogenation of aldehydes to alcohols under an atmosphere comprising both hydrogen and carbon monoxide.

~~'~'~~~~1 However, high reaction temperatures and pressures are required for this process.
US-A-3 876 672 discloses a process for the hydroformylation of olefins to form aldehydes and alcohols using a catalyst comprising a cationic hydride of Ni, Pd or Pt complexed with 2-4 monophosphine ligands. Rather low conversions With low selectivities to alcohols were observed.
Other known hydrogenation processes require a pure hydrogenation atmosphere, so that carbon monoxide should be removed, if an aldehyde-containing hydroformylation product is to be directly used.
Therefore, there remains a continued need for improved and more versatile catalysts for the hydrogenation of carbonyl compounds.
It has now been found that the hydrogenation of aldehydes or ketones to alcohols is advantageously effected in the presence of a homogeneous catalytic system comprising a source of a Group VIII
metal compound and a bidentate phosphine.
The catalyst system used according to the invention offers the advantages of high activity at mild conditions of temperature and/or pressure, applicability in the presence or absence of carbon monoxide in the hydrogenation atmosphere, and a remarkable selectivity in that olefinically unsaturated compounds remain substantially unaffected under conditions where the carbonyl compounds are readily hydrogenated to alcohols.
It is also remarkable that the present invention allows for hydrogenation of hindered ketones, i.e. ketones having at least one secondary or tertiary alkyl group linked to the ketogroup, at high rates.
It is remarked, that a catalytic system comprising a compound of palladium and a bidentate phosphine is described by Y. Ben-David et al., in J.Am.Chem.Soc., 1989, 111, 8742-4, but only for use in the carbonylation of aryl chlorides.
Carbonyl compounds used as percursor in the present process include aldehydes and ketones.

Y

Aldehydes which are used for the hydrogenation are preferably aliphatic aldehydes having 2-20 carbon atoms. They may contain one or more aldehyde groups, and also substituents which are inert under the reaction conditions, such as aryl groups, hydroxy groups, carboxy groups, C1-4 alkoxy groups, or ester groups having 1-7 carbon atoms. Aldehydes having 3-20 carbon atoms which have , been prepared by oxo synthesis are particularly suitable. Suitable examples include propanal, butanal, 2-methylpropanal, 4-hydroxybutanal, 6-oxohexanoic esters, octanal, nonyl aldehydes, tridecanals or 2-ethylhexanal.
Ketones which are used for the hydrogenation are preferably aliphatic ketones having 3-20 carbon atoms. They may contain one or more ketogroups, and also inert substituents such as mentioned above. Typical ketones include methyl iso-propylketone, ethyl iso-propylketone and dicyclohexyl ketone.
The hydrogenation is carried out in the presence of a catalytic system comprising a Group VIII metal which is preferably selected from palladium, platinum, and rhodium, and most preferably is palladium.
The Group VIII metal catalyst component may be provided in the form of a Group VIII metal salt such as salts of nitric acid;
sulphuric acid; sulphonic acids, for example trifluoromethane sulphonic acid or paratoluene sulphonic acid; and carboxylic acids, for example acetic acid or trifluoro acetic acid. The Group VIII
metal salt may be in the form of a complex, for example with a phosphine and/or other ligand. The Group VIII metal may also be provided in the form of the metallic element or a zero valent complex with a ligand such as a phosphine or carbon monoxide. If provided in metallic form, it should be used with a protonic acid for formation in situ of a soluble salt or complex.
The quantity of the Group VIII metal is not critical.
Preferably, it is in the range of 10'~ to 10-1 gram atom of Group VIII metal per mole of aldehyde substrate, more preferably from 10-6 to 10 2.

~'~~~'~OP~

The second essential component of the catalytic system to be used according to the invention is a bidentate phosphine. In the present context, a bidentate phosphine is intended to cover any organophosphorus compound having at least two phosphine groups and being free of steric hindrance preventing coordination of two phosphine F atoms to a single metal atom. The presence of further coordinating or non-coordinating phosphine groups is not excluded.
Preferred bidentate phosphines to be used according to the present invention have the formula, R1R2P-X-PR3R4 (I), wherein Rl, R2, R3 and R4 independently represent an optionally substituted hydrocarbyl group, or Rl and R2 together and/or R3 and R~' together represent an optionally substituted bivalent hydrocarbyl group, at least one of R1, R2, R3 and R4 being aliphatic, and X represents a bivalent bridging group having from 2 to 8 atoms in the bridge. More preferably, each of R1, R2, R3 and R4 independently represents an aliphatic group, such as a substituted or unsubstituted optionally branched or cyclic alkyl group, suitably having from 1 to 20 carbon atoms.
Preferred aliphatic groups are unsubstituted alkyl groups which may be branched or cyclic and have from 1 to 10 carbon atoms, more preferably from 1 to 5 carbon atoms. Examples of suitable alkyl groups are methyl, ethyl, n-propyl, iso-propyl, n-butyl, sec-butyl, iso-butyl, tert-butyl, cyclohexyl and n-hexyl. Preferred alkyl groups have one or two alpha-hydrogen atoms, in particular one alpha-hydrogen atom as in secondary alkyl groups. Most preferred alkyl group are ethyl, i-propyl, n-propyl, s-butyl and n-butyl. If together constituting a bivalent hydrocarbyl group, Rl and R2 or R3 and R4 preferably represent an aliphatic bivalent radical, such as an optionally substituted alkylene or cycloalkylene group, for example hexamethylene or cyclooctylene.
When the alkyl or alkylene group is said to be optionally substituted, it may be substituted by one or more substituents which do not annihilate the catalytic activity of the system.
Suitable substituents include halogen atoms, alkoxy groups, ~~~'~'~~~'~

haloalkyl groups, haloalkoxy groups, acyl groups, acyloxy groups, amino groups, hydroxyl groups, nitrile groups, acylamino groups, and aryl groups.
The bridging group represented by X is preferably a hydro-carbon, an ether or a thioether residue. For example, the bridging group may be an optionally substituted alkylene chain which is optionally interrupted by one or more oxygen and/or sulphur atoms, as in:
-CH2CH2-; -GH2CH2CH2-; -CH2CH2CH2CH2-; or -CH2CH20CH2CH2-.
The bridging group preferably contains from 2 to 6 atoms in the bridge, more preferably from 3 to 5 atoms. For example, when the bridging group is a propane or neopeiitane residue, the bridge contains 3 atoms. Preferred bridging groups X include trimethylene, tetramethylene, and 3-oxapentamethylene.
Examples of phosphines of formula I which may be used in the process according to the invention are:
1,2-bis(di-n-butylphosphino)ethane, 1,3-bis(dimethylphosphino)propane, 1,3-bis(diethylphosphino)propane, 1,3-bis(di-i-propylphosphino)propane, 1,3-bis(di-n-propylphosphino)propane, 1,3-bis(di-i-butylphosphino)propane, 1,3-bis(di-n-butylphosphino)propane, 1,3-bis(di-s-butylphosphino)propane, 1,3-bis(di-t-butylphosphino)propane, 1,3-bis(di-n-hexylphosphino)propane, 1,2-bis(dicyclohexylphosphino)ethane, 1,3-bis(n-butylmethylphosphino)propane, 1,3-bis(n-butylethylphosphino)propane, 1,3-bis(cyclooctylenephosphino)propane, 1,4-bis(di-i-propylphosphino)butane, 1,S-bis(dimethylphosphino)-3-oxapentane, 1,8-bis(di-n-butylphosphino)-3,6-dioxaoctane, and 1,4-bis(di-n-butylphosphino)-2,2,.,3-tetramethylbutane.

~~~~~~~~~'l Chiral phosphine ligands may be used if it is aimed at obtaining chiral alcohols when hydrogenating asymmetric ketones, in particular hindered ketones.
The ratio of the number of moles of the phosphine of formula I
per gram atom of Group VIII metal is preferably in the range of from 0.5 to 10, more preferably from 0.9 to S, especially from 1 to 3.
It is preferred that the catalytic system to be used in the process of the invention comprises the Group VIII metal in cationic form, The required anion may be generated in situ, or, preferably, is provided as component of the catalyst system. The source of an anion is preferably a protonic acid. However, it may also be a salt of the Group VIII metal, e.g. of palladium. It may also be a salt of another metal, for example vanadium, chromium, nickel, copper or silver, or a salt obtained by addition of a base, such as an aromatic ~1-heterocycle, as in pyridinium salts.
Preferably the anion is a non- or weakly-coordinating anion:
that is to say an anion which does not or only weakly coordinates with the palladium cation. It is preferably derived from a strong acid having a pKa < 2, more preferably a pKa < - 1 (measured at 18 °C in aqueous solution). Since halide anions, in particular chloride anion, tend to coordinate fairly strong to palladium, the anion preferably is derived from strong acids except hydrohalogenic acids.
For example, the anion may be derived from nitric acid;
sulfuric acid; a sulphonic acid such as fluorosulphonic acid, chlorosulfonic acid, methanesulphonic acid, 2-hydroxypropane-sulphonic acid, t-butylsulphonic acid, p-toluenesulphonic acid, benzenesulphonic acid, trifluoromethanesulphonic acid, or a sulpho-nated ion exchange resin; a perhalic acid such as perchloric acid;
or an acid derived by the interaction of a Lewis acid, such as BF3, PFS, AsFS, SbFS, TaF~ or :lbFS, with a Broensted acid, such as HF
(e. g. fluorosilicic acid, HBF4, HPF6, HSbFS).
It will be appreciated that when using a palladium salt of a weak acid, such as acetic acid, the addition of a strong acid such '>
-,_ as a sulphonic acid will generate a salt of palladium with the stronger acid, and the weak acid.
The phosphines of formula I as such are known compounds, and can be prepared by general methods described in the literature, for example Houben-Weyl, Vol. XII/I, p.21.
The catalyst system according to the invention may be constituted in a liquid phase. The catalyst system is preferably used in homogeneous mixture with the liquid phase of the reaction.
It is also possible to use the catalyst system in pseudo-hetero-genized ~orm, for example an adsorbed liquid on porous carrier surfaces. It is not necessary to use a separate solvent in the process according to the invention. The starting aldehyde or ketone and the alcohol product can often ~orm a suitable liquid phase. In some cases, however, it may be desirable to use a separate solvent.
Any inert solvent can be used for that purpose. Representative suitable solvents include hydrocarbons, suiphoxides, sulphones, ethers, esters, ketones, alcohols, and amides. The reaction may be conducted in the gaseous phase.
Conveniently, the aldehydas are hydrogenated in the reaction mixture in which they are obtained, for example in the hydroformylation.
Accordingly, the same catalyst can be used for both the preparation of an aldehyde by hydroformylation, and subsequent hydrogenation to the corresponding alcohol. Under reaction conditions of fast hydroformylation and slow hydrogenation, the aldehyde may be produced at high concentration in the reaction mixture, from which it could be isolated, if desired. By adapting the reaction conditions to fast hydrogenation, for example by raising the temperature or increasing the hydrogen partial pressure, the intermediate aldehyde is further reacted to the alcohol in the same liquid reaction phase.
By appropriate choice of reaction conditions of fast hydrogenation the alcohol may directly be prepared using the aldehyde precursor olefinically unsaturated compound as starting ~~'~'~~~~'l _8_ material. The aldehyde initially formed then is immediately consumed in the hydrogenation reaction to form the alcohol.
The process according to the invention is conveniently effected at a temperature in the range of from 20 °C to 200 °C, in particular from SO °C to 150 °C.
The process according to the invention is preferably effected at a total pressure of from 1 to 80 bar. Pressures higher than 100 bar may be used, but are generally economically unattractive on account of special apparatus requirements. A pure hydrogen atmosphere may be used for the hydrogenation, or the hydrogen atmosphere may comprise inert diluent gases. For example, an atmosphere comprising hydrogen and carbon monoxide may be used.
The process according to the invention may be carried out batchwise. Industrially, however, it is advantageous to carry it out continuously.
The alcohols produced by the process of the invention find application as chemical solvent or as precursor for various chemicals.
The invention will now be illustrated by the following Examples.
Example 1 A 250 ml magnetically-stirred autoclave was charged with 20 ml propanal, 40 ml diglyme (2,5,8-trioxanonane), 0.25 mmol of palladium acetate, 0.3 mmol of 1,3-bis(di-i-propylphosphino)propane and 1 mmol p-toluenesulphonic acid. After being flushed, the autoclave was pressurised with 60 bar of hydrogen. The autoclave was sealed, heated to a temperature of 90 °C, and maintained at that temperature for 15 minutes, whereupon a sample of the contents of the autoclave was analysed,by gas liquid chromatography (GLC).
From the results of the analysis it appeared that the propanal had been completely converted into 1-propanol with a selectivity close to 100. An average rate of conversion of 3900 mol of propanal per gram atom of palladium per hour was observed.

~~~'~'~fl~~l Examples 2-4 Example 1 was repeated, except for using the phosphines and anion sources in the amounts and for the reaction times mentioned in Table 1 below. The observed conversions of propanal (8), rates of conversion (mol/gr.at.Pdjhr), and selectivities to 1-propanol ($) are reported in the Table.

z~~~~~~~

Table 1 Ex. Gr.VIIIligandl)anion2)time convey-cony. ~lec-No. metal source sion rate civity (mmol) (mmol) (mmol) (hr) 1 Pd0Ac2 iPrPC3 pTSA 0.25 100 3900 99 (0.25) (0.3) (1) 2 Pd0Ac2 iPrPC3 pTSA 0.25 98 3900 99 (0.25) (0.3) (1) TFAcOH

(1) 3 Pd0Ac2 iPrPC3 TFMSA 0.25 100 3400 99 (0.25) (0.6) (1) 4 Pd0Ac EtPC3 pTSA 1.5 100 900 99 (0.25) (0.3) (1) 1) iPrPC3: 1,3-bis(di-i-propylphosphino)propane;
EtPC3: 1,3-bis(diethylphosphino)propane;
2) pTSA: p-toluene sulphonic acid; TFAcOH: trifluoro acetic acid;
TFMSA: trifluoromethylsulphonic acid; PhPA: benzenephosphonic acid Example 5 A 250 ml magnetically-stirred autoclave was charged with 20 m1 a-octene, 40 ml diglyme (2,5,8-trioxanonane), 0.25 mmol of palladium acetate, 0.6 mmol of 1,3-bis(di-i-propylphosphino)propane and 1 mmol t-butylsulphonic acid. After being flushed, the autoclave was pressurised with carbon monoxide and hydrogen up to a partial pressure of 30 bar of each. The autoclave Was sealed, ~~~'l'~~~' heated to a temperature of 70 °C, and maintained at that temperature for 7 hours, whereupon GLC of a sample of the contents of the autoclave showed that 80~ of the ac-octene had been converted into nonyl aldehydes, of which 888 were linear and 123 were S branched.
After cooling the autoclave was flushed, and was then pressurised with 60 bar of hydrogen and heated at 90 °C for hours. GLC analysis showed a 100 conversion of nonyl aldehydes into the corresponding nonyl alcohols at an initial rate of conversion above 300 mol/gr at Pd/hr. The residual octenes remaining after the hydroformylation step, appeared to be substantially unchanged during the hydrogenation, with only 6~
being hydrogenated.
Example 6 a, A 250 ml magnetically-stirred autoclave was charged with 20 ml a-octene, 40 ml diglyme, 0.25 mmol of palladium acetate, 0.6 mmol of 1,3-bis(di-i-propylphosphino)propane and 1 mmol p-toluene-sulphonic acid. After being flushed, the autoclave was pressurised with carbon monoxide and hydrogen up to a partial pressure of 30 bar of each. The autoclave was sealed, heated to a temperature of 90 °C, and maintained at that temperature for 5 hours, whereupon GLC analysis of a sample of the contents of the autoclave showed that 67$ of the a-octene had been converted with a selectivity of 94$ into nonyl aldehydes and S$ into the corresponding nonyl alcohols.
b. The procedure under a. of this Example was repeated charging the autoclave with 15 ml of a-octene and the same solvent and catalytic system. The autoclave was pressurised with 20 bar of carbon monoxide and 40 bar of hydrogen, and heated at 12S °C for 5 hours. GLC analysis showed that 63$ of the a-octene had been converted with a selectivity of 888 into nonyl alcohols and 9$ into nonyl aldehydes.
It is seen that using the same catalytic system the aldehyde is formed as the predominant product under a., whereas at higher hydrogen pressure and higher temperature the alcohol is the predominant product under b.. Apparently, in both experiments the aldehyde is formed in a first reaction step and subsequently consumed as a starting material for the second hydrogenation step, under a. at relatively low rate and under b. at relatively high rate under conditions of temperature and hydrogen concentration favourable for hydrogenation.
Example 7 Following generally the procedure of Example 6b., a 250 ml magnetically-stirred autoclave was charged with 20 ml a-dodecene, 40 ml diglyme, 0.25 m.-nol of palladium acetate, 0.6 mmol of 1,3-bis(1,S-cyclooctylenephosphino)propane, 1 mrnol p-toluene-sulphonic acid and 1 mmol trifluoro acetic acid. The autoclave was pressurised with 20 bar of carbon monoxide and 40 bar of hydrogen, and heated at 12S °C for 5 hours. It was found that 62~ of the a-dodecene had been converted with a selectivity of 98$ into tridecyl alcohols and traces of the corresponding aldehydes.
Example 8 As in the previous Example, a 250 ml magnetically-stirred autoclave was charged with 30 ml of a mixture of internally unsaturated C14 olefins, 40 ml diglyme, 0.5 mmol of palladium acetate, 1.2 mmol of 1,3-bis(di-i-propylphosphino)propane, 2 mmol p-toluenesulphonic acid and 1 mmol trifluoro acetic acid. The autoclave was pressurised with 20 bar of carbon monoxide and 40 bar of hydrogen, and heated at 15S °C for 10 hours. It was found that 71$ of the C14 olefins had been converted with a selectivity of 98~
into pentadecyl alcohols.
Example 9 As in the previous Example, a 250 ml magnetically-stirred autoclave was charged with 20 ml cyclohexene, 50 ml diglyme, 0.25 mmol of palladium acetate, 0.6 mmol of 1,3-bis(dimethyl-phosphino)propane, 1 mmol trifluoro acetic acid and 1 mmol p-toluenesulphonic acid. The autoclave was pressurised with 20 bar of carbon monoxide and 40 bar of hydrogen, and heated at 130 °C for S hours. It was found that 6$ of the cyclohexene had been converted with a selectivity of 99$ into cyclohexylmethanol.

Example 10 As in the previous Example, a 250 ml magnetically-stirred autoclave was charged with 20 ml styrene, 50 ml diglyme, 0.25 mmol of palladium acetate, 0.6 mmol of 1,3-bis(di-i-propylphosphino)- , propane and 1 mmol p-toluenesulphonic acid. The autoclave was pressurised with 20 bar of carbon monoxide and 40 bar of hydrogen, and heated at 125 °C for 5 hours. It was found that 90$ of the styrene had been converted with a selectivity of 85$ 3-phenyl-1-propanol and 158 into 2-phenyl-1-propanol.
Example 11 As in the previous Examples, an autoclave was charged with 10 ml ethyl isopropyl ketone, 30 ml 2-butanol as solvent, 0.25 mmol palladium acetate, 0.3 mmol 1,3-bis(di-i-propylphosphino)propane and 2 mmol tri-fluoromethane sulphonic acid. The autoclave was pressurized with 50 bar of hydrogen and heated at 70 °C for 6 hours. It was found that 100$ of the ethyl isopropyl ketone had been converted with a selectivity of 98~ into 2-methylpentanol-3.
Example 12 Example 11 was exactly repeated except for charging 20 ml methyl ethyl ketone instead of ethyl isopropyl ketone, and 20 ml instead of 30 ml of 2-butanol solvent. After 2 hours of reaction at 70 °C, 90$ conversion of methyl ethyl ketone with a selectivity of about 98~ into 2-butanol was observed.
Example 13 As in the previous Example, an autoclave was charged with 10 ml methyl isopropyl ketone, 25 ml 2-butanol, 0.25 mmol palladium acetate, 0.3 mmol 1,3-bis(di-i-propylphosphino)propane and 2 mmol paratoluenesulphonic acid. The autoclave was pressurized with 50 bar of hydrogen and heated at 70 °C for 6 hours. It was found that 60$ of the methyl isopropyl ketone has been converted with a selectivity of 98$ into 3-methylbutanol-2.

Claims (10)

1. A process for the preparation of an alcohol by hydrogenation of a carbonyl compound at elevated temperature and superatmospheric pressure in the presence of a homogeneous catalytic system comprising a source of a Group VIII metal compound and a bidentate phosphine.

2. A process as claimed in claim 1, wherein the Group VIII metal is selected from palladium, platinum, and rhodium.

3. A process as claimed in claim 2, wherein the Group VIII metal is palladium.

4. A process as claimed in any one or more of claims 1-3, wherein the bidentate phosphine is a compound of general formula:
R1R2P-X-PR3R4 (I) wherein R1, R2, R3 and R4 independently represent an optionally substituted hydrocarbyl group, or R1 and R2 together and/or R3 and R4 together represent an optionally substituted bivalent hydrocarbyl group, at least one of R1, R2, R3 and R4 being aliphatic, and X represents a bivalent bridging group having from 2 to 8 atoms in the bridge.

5. A process as claimed in claim 4, wherein in formula I each of R1, R2, R3 and R4 independently represents a substituted or unsubstituted optionally branched or cyclic alkyl group having from 1 to 10 carbon atoms.

6. A process as claimed in any one or more of claims 1-5, wherein the catalytic system further comprises a source of anions derived from a strong acid.

7. A process as claimed in any one or more of claims 1-6, wherein the carbonyl compound is selected from aldehydes and ketones.

8. A process as claimed in claim 7, wherein an aldehyde which has been prepared by hydroformylation of an olefinically unsaturated compound is used as starting material.

9. A process as claimed in claim 8, wherein the aldehyde starting material is prepared in situ and without isolation is hydrogenated to the alcohol.

10. A process as claimed in claim 9, wherein the aldehyde starting material is prepared in the presence of the same catalyst as used for the hydrogenation.