Preparation of tetrahydrogeraniol

Details Preparation of tetrahydrogeraniol Preparation of tetrahydrogeraniol

2002-12-04

2004-07-06

Richter, Johann (Department: 1621)

Organic compounds -- part of the class 532-570 series

Organic compounds

Oxygen containing

C568S875000, C568S876000, C568S878000, C568S880000, C568S884000

Reexamination Certificate

active

06759561

ABSTRACT:

The present invention relates to a process for the preparation of tetrahydrogeraniol, where the product mixtures and distillation residues from linalool, citronellal, citronellol or geraniol
erol synthesis are fed directly to catalytic hydrogenation.
Tetrahydrogeraniol (3,7-dimethyloctanol) is an important intermediate in industrial organic synthesis and is used as a scent in its own right or as an additive in soaps and detergents.
The preparation of tetrahydrogeraniol by hydrogenation of unsaturated precursors such as citral, citronellol or citronellal, or nerol/geraniol has been known for a long time. As long ago as 1912, the hydrogenation of citral over palladium was described (Ipatjew, Chem. Ber., 45, 1912, 3222). The hydrogenation of citral over metals on potassium-graphite supports is described in Savoia, Tagliavini, Trombini, Umani-Ronchi J. Org.Chem., 1981, 46, 5344-5348. Tetrahydrogeraniol is obtained in a yield of 95% over Ni/graphite catalysts. In 1993, the hydrogenation of citronellol to give tetrahydrogeraniol over a Pd/C catalyst succeeded in yields of 93%. The hydrogenation of 3,7-dimethyloctanal over a homogeneous (NiCl
2
(PPh
3
)
2
) catalyst was documented in J. Chem. Soc. Chem. Com. 1995 (Iyer, Varghese (4), 465-466). It succeeds in a yield of 57%.
The hydrogenation of precursors that are already expensive to prepare and are present in pure form, such as citral, nerol or geraniol, does not make commercial sense. Total hydrogenation, eg. in the preparation of nerol/geraniol is inadvisable due to the poor separability of tetrahydrogeraniol from the unsaturated products.
It is an object of the present invention to provide an economical process for the preparation of tetrahydrogeraniol by the reaction or the use of residues that are obtained during the preparation of linalool, citronellal, citronellol or geraniol
erol.
There is a need for a process whereby the hydrogenation of the residues from the abovementioned partial hydrogenations or rearrangements, particularly from linalool synthesis, can be conducted at high conversion and with good yields, selectivity and catalyst lifetime.
We have found that this object is achieved, surprisingly, by a process for the preparation of tetrahydrogeraniol, wherein the product mixtures and distillation residues resulting from linalool, citronellal, citronellol or geraniol
erol synthesis are fed directly to catalytic hydrogenation.
Suitable starting materials include all product mixtures or distillation residues comprising more than one compound of the following basic structure of the general formula I
where
R
1
is OH, H, CH
3
R
2
, R
3
are H, OH, CH
3
R
4
is H, CH
3
,
and one to four double bonds can be present at any site in the molecule.
The product mixtures or distillation residues preferably comprise more than one compound selected from the group consisting of nerol, geraniol, isonerol 2, citral, citronellol, 3,7-dimethyloctanal, isonerol 1, citronellal, linalool (from top to bottom in the formula scheme, linalool is not shown).
If, for example, the residues obtained from linalool synthesis (Table 1) are used, the total liquid phase concentration of linalool and geraniol
erol of the residue or product mixture used is less than 30% by weight, preferably less than 20% by weight, particularly preferably less than 10% by weight. The total quantity of citronellol and isonerol is more than 50% by weight, preferably more than 80% by weight.
TABLE 1
Typical residue from a linalool synthesis in % by weight:
Low boilers
0.10
Tetrahydrolinalool
0.00
Linalool
6.58
Citronellol
31.99
Nerol
0.57
Citrate (cis/trans)
1.04
Tetrahydrogeraniol
0.03
Isonerol (I + II)
54.60
Others
5.05
If, for example, the residues obtained from nerol/geraniol synthesis (Table 2) are used, the liquid phase content of usable products (geraniol and isonerols) is just under 60%.
TABLE 2
Typical residue from a nerol/geraniol synthesis in % by weight %:
Low boilers
1
Geraniol
45
Isonerol (I + II)
13
High boilers
41
If, for example, the residues obtained from a citronellal synthesis (Table 3) are used, the liquid phase content of usable products is just below 90%.
TABLE 3
Typical residue from a citronellal synthesis in % by weight:
Citral
44
Citronellal
30
Citronellol
13
High boilers
11
If, for example, the residues obtained from a citronellol synthesis (Table 4) are used, the liquid phase content of usable products (geraniol and isonerol) is 95%.
TABLE 4
Typical residue from a citronellol synthesis in % by weight:
Geraniol
10
Nerol
5
Citronellol
75
Dimethyloctanol
5
High boilers
5
Suitable hydrogenation catalysts include in principle all hydrogenation catalysts that can be used for the hydrogenation of olefinic double bonds (eg. Houben Weyl, Methoden der organischen Chemie, Volume 4/1c).
Particularly suitable hydrogenation catalysts are catalysts that contain, as active components, elements selected from the group consisting of copper, silver, gold, iron, cobalt, nickel, rhenium, ruthenium, rhodium, palladium, osmium, iridium, platinum, chromium, molybdenum and tungsten, in each case in metallic form (eg. as Ra catalyst, oxidation state 0) or in the form of compounds, such as oxides, which are reduced to the corresponding metal under the process conditions.
The catalytically active components copper, silver, gold, iron, cobalt, nickel, rhenium, ruthenium, rhodium, palladium, osmium, iridium, platinum, chromium, molybdenum and/or tungsten are generally present in the catalytically active mass of the catalyst in quantities in the range from 0.1 to 80% by weight, preferably from 0.1 to 70% by weight, particularly preferably from 0.1 to 60% by weight, calculated as the metal in the oxidation state 0.
Preferred catalysts comprise elements as catalytically active components that are selected from the group consisting of copper, silver, cobalt, nickel, ruthenium, rhodium, palladium, platinum, chromium and molybdenum, in particular selected from the group consisting of copper, cobalt, nickel and palladium, in each case in metallic form (oxidation state 0) or in the form of compounds, such as oxides, which are reduced to the corresponding metal under the process conditions.
Particularly preferred catalysts are those with Co, Ni, Cu, Ru, Pd and/or Pt as active components. These can be used as unsupported catalysts, as supported catalysts or as activated metal catalysts (Raney catalysts).
The catalytically active mass of these preferred catalysts further comprises the support materials aluminum oxide (Al
2
O
3
), zirconium dioxide (ZrO
2
), titanium dioxide (TiO
2
), carbon and/or oxygen-containing compounds of silicon, in general in total quantities in the range from 20 to 99.9% by weight, preferably from 30 to 99.9% by weight, particularly preferably from 40 to 99.9% by weight, based on SiO
2
.
Of the Raney catalysts, catalysts such as Ra—Ni are preferably used. Ra—Co, Ra—Co—Ni—Fe, Ra—Ni—Co—Fe—Cr or Ra—Ni and Ra—Co with doping of other transition metals are used in water-free form, or else in water-moist or solvent-free form.
The hydrogenation catalysts used in the process of the invention can be prepared by processes described in the prior art and can sometimes also be obtained commercially.
The hydrogenation can be carried out batchwise or continuously. To make comparatively large quantities (>500 t/a), a continuously operated hydrogenation is advisable.
The reaction can be carried out in a suspension or in a fixed bed. A continuously operated fixed bed variant can be operated by trickle or liquid-phase methods. Gas phase hydrogenation can also be considered.
Suspension hydrogenation can be carried out batchwise, generally in liquid phase.
For all variants, temperatures are chosen in the range from 20 to 250° C., preferably from 30 to 200° C., particularly preferably from 50 to 180° C.
The pressure is generally selected in the range from 1 to 250 bar, preferably from 5 to 200 bar, particularly preferably from 10 to 100 bar.
The hydrogenation by the process of the invention can be carried out either with or without a solvent, for example alcohols

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