Preparation of high-quality oxo process alcohols from inconstant raw material sources

1. A process for continuously preparing an alcohol mixture, said process comprising:

oligomerizing an input mixture, which comprises an olefin and has a composition that changes over time, to obtain an oligomerizate comprising olefin oligomers;

hydroformylating at least a portion of the olefin oligomers present in the oligomerizate with carbon monoxide and hydrogen in the presence of a homogeneous catalyst system comprising rhodium and at least two different monophosphite ligands to give aldehydes; and

subsequently hydrogenating at least a portion of the aldehydes to obtain said alcohol mixture;

wherein

a composition of the oligomerizate and a composition of the aldehydes are determined during said process,

a temperature and/or a conversion in the oligomerization are controlled as a function of a current composition of the oligomerizate, and

a composition of the catalyst system during the hydroformylating is controlled by metered addition of one of the at least two monophosphite ligands into the hydroformylation as a function of a current composition of the aldehydes.

2. The process according to claim 1 , wherein the composition of the oligomerizate and the composition of the aldehydes are determined continuously, and the oligomerizing and/or the hydroformylating are controlled continuously.

3. The process according to claim 1 , wherein at least the hydroformylating is controlled in such a way that a first scalar controlled variable calculated from the composition of the aldehydes is kept constant.

4. The process according to claim 3 , wherein the oligomerizing is controlled in such a way that the first scalar controlled variable calculated from the composition of the aldehydes is kept constant.

5. The process according to claim 3 , wherein the first scalar controlled variable is an approximation of the viscosity of an ester mixture obtained by esterification of the alcohol mixture or by transesterification with the aid of the alcohol mixture.

6. The process according to claim 1 , wherein the oligomerizing is controlled in such a way that a second scalar controlled variable calculated from the composition of the olefin oligomers is kept constant.

7. The process according to claim 6 , wherein the second scalar controlled variable is an approximation of the iso index of the oligomerizate.

8. The process according to claim 1 , wherein the input mixture comprises an olefin having four carbon atoms which is oligomerized in the course of the oligomerization to give olefin oligomers having eight, twelve and sixteen carbon atoms, and the olefin oligomers having eight carbon atoms are removed from the oligomerizate and hydroformylated to aldehydes having nine carbon atoms.

9. The process according to claim 8 , wherein the input mixture comprises a combination of the following compound mass flow rates which vary within the specified compound mass flow rate ranges with a respective rate of variation within the specified range of rates of variation:

compound

compound mass flow rate

Rate of variation

isobutene:

0 kg/s to 1 kg/s

−0.05 g/s 2 to 0.05 g/s 2

1-butene:

0 kg/s to 6 kg/s

−0.30 g/s 2 to 0.30 g/s 2

2-butene (cis + trans):

1 kg/s to 13 kg/s

−0.30 g/s 2 to 0.30 g/s 2

isobutane:

0 kg/s to 3 kg/s

−0.15 g/s 2 to 0.15 g/s 2

n-butane:

1 kg/s to 7 kg/s

−0.30 g/s 2 to 0.30 g/s 2

other materials:

0 kg/s to 1 kg/s

−0.05 g/s 2 to 0.05 g/s 2 .

10. The process according to claim 1 , wherein the oligomerizing is effected in the presence of a heterogeneous nickel catalyst.

11. The process according to claim 1 , wherein the oligomerization is operated in circulation mode, in such a way that a proportion of the oligomerizate drawn off from the oligomerization is recycled into the oligomerization,

wherein

a conversion of said input mixture in the oligomerization is controlled by varying the proportion of an oligomerizate recycled.

12. The process according to claim 1 , wherein the one monophosphite ligand is metered in such a way that the molar ratio of the sum total of all the monophosphite ligands to rhodium remains constant, taking account of ligand losses.

13. The process according to claim 1 , wherein the homogeneous catalyst system comprises exactly two different monophosphite ligands, the first monophosphite ligand being a compound of structural formula II, and

wherein the second monophosphite ligand is a compound of structural formula Ia, Ib or III:

wherein, in Ia,

R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , R 8 are each independently selected from the group consisting of:

—H, —(C 1 -C 12 alkyl), —O—(C 1 -C 12 alkyl), —O—(C 6 -C 20 aryl), —(C 6 -C 20 aryl), halogen, —COO—(C 1 -C 12 alkyl), —CONH—(C 1 -C 12 alkyl), —(C 6 -C 20 aryl)-CON[(C 1 -C 12 alkyl)] 2 , —CO—(C 1 -C 12 alkyl), —CO—(C 6 -C 20 aryl), —COOH, —OH, —SO 3 H, —SO 3 Na, —NO 2 , —CN, —NH 2 , and —N[(C 1 -C 12 alkyl)] 2 ; and

R 9 , R 10 , R 11 , R 12 , R 13 , R 14 , R 15 , R 16 are each independently selected from the group consisting of:

—H, —(C 1 -C 12 alkyl), —O—(C 1 -C 12 alkyl), —O—(C 6 -C 20 aryl), —(C 6 -C 20 aryl), halogen, —COO—(C 1 -C 12 alkyl), —CONH—(C 1 -C 12 alkyl), —(C 6 -C 20 aryl)-CON[(C 1 -C 12 alkyl)] 2 , —CO—(C 1 -C 12 alkyl), —CO—(C 6 -C 20 aryl), —COOH, —OH, —SO 3 H, —SO 3 Na, —NO 2 , —CN, —NH 2 , and —N[(C 1 -C 12 alkyl)] 2

wherein, in Ib,

R 9 , R 10 , R 11 , R 12 , R 13 , R 14 , R 15 , R 16 are each independently selected from the group consisting of:

—H, —(C 1 -C 12 alkyl), —O—(C 1 -C 12 alkyl), —O—(C 6 -C 20 aryl), —(C 6 -C 20 aryl), halogen, —COO—(C 1 -C 12 alkyl), —CONH—(C 1 -C 12 alkyl), —(C 6 -C 20 aryl)-CON[(C 1 -C 12 alkyl)] 2 , —CO—(C 1 -C 12 alkyl), —CO—(C 6 -C 20 aryl), —COOH, —OH, —SO 3 H, —SO 3 Na, —NO 2 , —CN, —NH 2 , and —N[(C 1 -C 12 alkyl)] 2

wherein, in II,

R 21 ″, R 22 ″, R 23 ″, R 24 ″, R 25 ″, R 31 ″, R 32 ″, R 33 ″, R 34 ″, R 35 ″, R 41 ″, R 42 ″, R 43 ″, R 44 ″, R 45 ″ are each independently selected from the group consisting of:

—H, —(C 1 -C 12 alkyl), —O—(C 1 -C 12 alkyl), —O—(C 6 -C 20 aryl), —(C 6 -C 20 aryl), halogen, —COO—(C 1 -C 12 alkyl), —CONH—(C 1 -C 12 alkyl), —(C 6 -C 20 aryl)-CON[(C 1 -C 12 alkyl)] 2 , —CO—(C 1 -C 12 alkyl), —CO—(C 6 -C 20 aryl), —COOH, —OH, —SO 3 H, —SO 3 Na, —NO 2 , —CN, —NH 2 , and —N[(C 1 -C 12 alkyl)] 2

wherein, in III,

R 1′ is selected from the group consisting of

—(C 1 -C 12 alkyl), and —(C 3 -C 12 cycloalkyl), and

R 21′ , R 22 ′, R 23′ , R 24′ , R 25′ , R 31′ , R 32 ′, R 33 ′, R 34 ′, R 35 ′ are each independently selected from the group consisting of:

—H, —(C 1 -C 12 alkyl), —O—(C 1 -C 12 alkyl), —O—(C 6 -C 20 aryl), —(C 6 -C 20 aryl), -halogen, —COO—(C 1 -C 12 alkyl), —CO—(C 1 -C 12 alkyl), —CO—(C 6 -C 20 aryl), —COOH, and —OH.

14. The process according to claim 13 , wherein the second monophosphite ligand is a compound of structural formula Ia or Ib.

15. The process according to claim 13 , wherein the second monophosphite ligand is a compound of structural formula Ia.

16. The process according to claim 13 , wherein the second monophosphite ligand is a compound of structural formula Ib.

17. The process according to claim 1 , wherein a pressure during the hydroformylating is controlled, in addition to the composition of the catalyst system, as a function of a current composition of the aldehydes.

18. The process according to claim 1 , further comprising:

esterifying said alcohol mixture with an acid, to obtain an ester mixture.

19. The process according to claim 18 , wherein said ester mixture is a plasticizer.