Process for hydrogenation of esters of aromatic carboxylic acids to yield saturated homologues thereof
A process for the hydrogenation of substituted aromatic compounds, with particular reference to esters of aromatic carboxylic acids, for example of aromatic esters used commonly as plasticizers in polymers having wide commercial application (see, in particular, esters of phthalic acid and trimellitic acid).
1. A process for the semi-continuous catalytic liquid phase hydrogenation of esters of aromatic carboxylic diacids and triacids, wherein the esters, loaded in a reactor without adding diluent/solvent, are hydrogenated at an internal temperature of the reactor comprised in the range from 100° C. to 200° C., by continuously feeding a hydrogenation gas into the reactor, controlling the hydrogenation gas pressure inside the reactor to values in the range from at least 7 bar gauge (barg) to below 18 barg and in the presence of 0.1-3% by weight relative to the quantity of esters of aromatic carboxylic acids loaded into the reactor, of a supported catalyst comprising between 0.1 and 10% by weight, relative to the total weight of the catalyst, of an active metal of the group consisting of ruthenium, rhodium, palladium, osmium, iridium, platinum, gold or mixtures thereof, and optionally of at least one additional metal selected from groups I-III of the periodic system, also present at most as 10% by weight, relative to the total quantity of catalyst, and present in a quantity that does not exceed that of the active metal.
2. The process according to claim 1 for the semi-continuous catalytic liquid phase hydrogenation of esters of aromatic carboxylic diacids and triacids, selected from diesters of phthalic acid and triesters of 1,2,4-benzene tricarboxylic acid, wherein the esters, loaded in a reactor without adding diluent/solvent, are hydrogenated at an internal temperature of the reactor comprised in the range from 130° C. to 170° C., by continuously feeding a hydrogenation gas into the reactor, controlling the hydrogenation gas pressure inside the reactor to values in the range from at least 7 barg to below 18 barg and in the presence of 0.3-1.5% by weight, relative to the quantity of esters of aromatic carboxylic acids loaded into the reactor, of a supported catalyst comprising between 0.1 and 10% by weight, relative to the total weight of the catalyst, of an active metal of the group consisting of ruthenium, rhodium, palladium, osmium, iridium, platinum, gold or mixtures thereof, and optionally of at least one additional metal selected from groups I-III of the periodic system, also present at most as 10% by weight, relative to the total quantity of catalyst, and present in a quantity that does not exceed that of the active metal.
3. The process according to claim 1 , wherein aromatic carboxylic diacid esters are used which are selected from phthalic acid diesters with non-cyclic monofunctional alkanols comprising 1 to 16 carbon atoms or mixtures thereof.
4. The process according to claim 1 , wherein aromatic carboxylic triacid esters are used which are selected from triesters of 1,2,4-benzene tricarboxylic acid with non-cyclic monofunctional alkanols comprising 1 to 16 carbon atoms or mixtures thereof.
5. The process according to claim 4 , wherein the non-cyclic monofunctional alkanol is selected from the group consisting of methanol, ethanol, n-butanol, sec-butanol, iso-butanol, tert-butanol, n-hexanol, 2-ethyl hexanol, n-heptanol, n-octanol, n-nonanol, i-nonanol, n-decanol, i-decanol, n-undecanol, n-dodecanol or mixtures thereof.
6. The process according to claim 4 , wherein the non-cyclic monofunctional alkanol comprises 7-12 carbon atoms.
7. The process according to claim 1 , wherein the catalyst comprises an active metal selected from Ru, Rh or Pd or mixtures thereof on a coal or alumina support.
8. The process according to claim 7 , wherein the catalyst is selected from Pd on alumina, Pd on coal, Ru on coal or Rh on coal or mixtures thereof.
9. The process according to claim 1 , wherein the hydrogenation gas comprises an inerting gas which contributes to the pressure in the reactor with a partial pressure that corresponds to a contribution of up to 20% of the total pressure detected in the reactor.
10. The process according to claim 6 , wherein the feeding of hydrogenation gas is controlled during the hydrogenation reaction so as to increase the pressure inside the reactor with increasing conversion, and wherein the feeding of hydrogenation gas is interrupted when the internal pressure of the reactor reaches a value comprised in the range from 9 to 15 barg at an internal temperature comprised in the range from 150° C. to 170° C., without consumption of hydrogen for about 0.25-1.0 hours, after which the reaction mix is subjected to the separation of the hydrogenated esters that have formed.
11. The process according to claim 1 , wherein the esters of aromatic carboxylic diacids and triacids are selected from diesters of phthalic acid and triesters of 1,2,4-benzene tricarboxylic acid.
12. The process according to claim 1 , wherein the esters are hydrogenated at an internal temperature of the reactor comprised in the range from 120° C. to 190° C.
13. The process according to claim 1 , wherein the esters are hydrogenated at an internal temperature of the reactor comprised in the range from 130° C. to 180° C.
14. The process according to claim 1 , wherein the esters are hydrogenated at an internal temperature of the reactor comprised in the range from 140° C. to 170° C.
15. The process according to claim 1 , wherein the hydrogenation gas pressure inside the reactor is equal to or lower than 15 barg.
16. The process according to claim 1 , wherein the hydrogenation gas pressure inside the reactor is comprised in the range from 9 to 15 barg.
17. The process according to claim 1 , wherein the supported catalyst is present in an amount from 0.3 to 1.5% by weight, relative to the quantity of esters of aromatic carboxylic acids loaded into the reactor.
18. The process according to claim 2 , wherein the hydrogenation gas pressure inside the reactor is comprised in the range from 9 to 15 barg.
19. The process according to claim 5 , wherein the non-cyclic monofunctional alkanol is selected from the group consisting of 2-ethyl hexanol, n-heptanol, n-octanol, n-nonanol, i-nonanol, n-decanol, i-decanol, n-undecanol, n-dodecanol- or mixtures thereof.
20. The process according to claim 5 , wherein the non-cyclic monofunctional alkanol is 2-ethyl hexanol.
21. The process according to claim 6 , wherein the non-cyclic monofunctional alkanol comprises 8-11 carbon atoms.
22. The process according to claim 6 , wherein the non-cyclic monofunctional alkanol comprises 8-10 carbon atoms.
23. The process according to claim 8 , wherein the active metal is present between 1.5 and 7.0% by weight, relative to the total weight of the catalyst.