Process for the production of hydrocarbon fluids having a low aromatic content
View Patent ↗The invention provides a process to prepare very low sulphur, very low aromatic hydrocarbon fluids having a boiling range in the range of from 100 to 400° C. and a boiling range of not more than 80° C., comprising at least the two successive steps of —deep hydrodesulphurating of middle distillate down to less than 10 ppm sulphur, and —catalytic hydrogenating the desulphurized middle distillates of preceding step at a temperature from 80 to 180° C. and at a pressure from 60 to 160 bars.
1. Process to prepare very low sulphur, very low aromatic hydrocarbon fluids containing less than 5 ppm sulphur and having a content in aromatics below 100 ppm, boiling in the range of from 100 to 400° C. and having a boiling range of not more than 80° C., comprising at least the two successive steps of
deep hydrodesulphurating of middle distillate down to less than 10 ppm sulphur, wherein the deep hydrodesulphurization of middle distillate is operated at a reaction temperature higher than 320° C. under a pressure higher than 70 bars and
catalytic hydrogenating the desulphurized middle distillates of the preceding step at a temperature from 80 to 180° C. and at a pressure from 60 to 160 bars, with a supported nickel-containing catalyst, a hydrogen treat rate ranging from 100 to 300 Nm 3 /ton of feed, the catalytic hydrogenation being performed in at least two stages, wherein the first stage operates sulphur trapping on the supported nickel-containing catalyst, hydrogenation of substantially all unsaturated hydrocarbons and up to 90% hydrogenation of aromatics,
wherein the middle distillate is issued from atmospheric distillation unit effluents or from atmospheric distillation unit and catalytic cracking effluents, such distillates boiling in the range of from 200° C. to 380° C.
2. Process of claim 1 wherein the middle distillate contains more than 20% aromatics.
3. Process of claim 1 wherein the middle distillate contains less than 100% aromatics.
4. Process of claim 1 wherein the hydrogenated hydrodesulphurized fluids contain less than 3 ppm sulphur.
5. Process of claim 1 , wherein the hydrogenated desulphurized fluids contain less than 50 ppm aromatics.
6. Process of claim 1 , wherein deep hydrodesulphurization of distillates is operated at a reaction temperature varying between 330 and 370° C., under a pressure higher than 80 bars, in the presence of a hydrodesulphurization catalyst with a liquid hourly space velocity (LHSV) varying between 0.5 and 3 h −1 .
7. Process of claim 1 , wherein the hydrodesulphurization catalyst comprises an alumina support with at least a couple of metals from Group VIII.
8. Process of claim 1 , wherein in the hydrogenation step, the liquid hourly space velocity (LSHV) is from 0.2 to 5 hr −1 .
9. Process of claim 1 , wherein in the hydrogenation step, the catalyst comprising nickel is a supported catalyst on an alumina carrier having a specific surface area varying between 100 and 250 m 2 /g of catalyst.
10. Process of claim 1 , wherein in the hydrogenation step, the temperature is 120 to 160° C.
11. Process of claim 1 , wherein in the hydrogenation step, the pressure is from 100 to 150 bars.
12. Process of claim 1 , wherein in the hydrogenation step, the temperature is from 80 to 160° C. and the pressure is from 100 to 160 bars.
13. Process of claim 1 wherein the hydrogenation of desulphurized distillates is performed within three hydrogenation stages, followed by a separating step to evaporate remaining gaseous products and a fractionation step.
14. Process of claim 13 , wherein the weight amount (wt. %) of catalyst in the three hydrogenation stages is 5-50 wt. %, 10-70 wt. % and 25-85 wt. %, respectively.
15. Process of claim 14 , wherein the weight amount (wt. %) of catalyst in the three hydrogenation stages is 7-25 wt. %, 15-35 wt. % and 40-78 wt. %, respectively.
16. Process of claim 1 , wherein the hydrogenation of desulphurized distillates is performed within two hydrogenation stages, followed by a separating step to evaporate remaining gaseous products and a fractionation step.
17. Process of claim 16 , wherein the amount of catalyst in the two stages, according to weight amounts (wt. %) is 5-50 wt. % and 50-95 wt. %, respectively.
18. Process of claim 17 , wherein the amount of catalyst in the two stages according to weight amounts (wt. %) is 7-40 wt. % and 60-93 wt. %, respectively.
19. Process of claim 1 , wherein the hydrodesulphurized middle distillate contains less than 8 ppm sulphur.
20. Process of claim 1 , further comprising a separation stage, whereby unreacted hydrogen is recovered and a stream of hydrogenated desulphurized middle distillate is recovered.
21. Process of claim 20 , wherein the unreacted hydrogen is recycled at least in part to the inlet of the process or to the hydrogenation stage.
22. Process of claim 1 , wherein a stream of hydrogenated desulphurized middle distillate is partly recycled, at least in part, to the inlet or to the hydrogenation stage.
23. Process of claim 20 , wherein the separation stage comprises at least two flash separators staged according to decreasing pressure.
24. Process of claim 23 , wherein the pressure in the last flash separator is about atmospheric pressure.
25. Process of claim 1 , further comprising a step of prefractionation of the desulphurized middle distillates prior to hydrogenation, into low-sulphur feed fractions having a boiling range of less than 90° C. then subjected to hydrogenation.
26. Process of claim 1 , further comprising a step of fractionation of the hydrogenated products into fluids of defined boiling ranges.
27. Process of claim 25 , wherein the prefractionation step is carried out at a vacuum pressure from 10 to 50 mbars absolute.
28. Process of claim 15 , wherein the weight amount (wt. %) of catalyst in the three hydrogenation stages is 10-20 wt. %, 20-32 wt. % and 48-70 wt. %, respectively.
29. Process of claim 2 , wherein the middle distillate contains more than 30% aromatics.
30. Process of claim 3 , wherein the middle distillate contains less than 70% aromatics.
31. Process of claim 4 , wherein the hydrogenated hydrodesulphurized fluids contain less than 0.5 ppm sulphur.
32. Process of claim 5 , wherein the hydrogenated desulphurized fluids contain less than 30 ppm aromatics.
33. Process of claim 6 , wherein deep hydrodesulphurization of distillates is operated under a pressure varying between 80 and 90 bars.
34. Process of claim 7 , wherein the couple of metals from group VIII are nickel/molybdenum.
35. Process of claim 8 , wherein in the hydrogenation step, the liquid hourly space velocity (LSHV) is from 0.5 to 3 hr −1 .
36. Process of claim 8 , wherein in the hydrogenation step, the liquid hourly space velocity (LSHV) is from 0.8 to 1.5 hr −1 .
37. Process of claim 1 , wherein in the hydrogenation step, the treat rate is from 150 to 250 Nm 3 /ton of feed.
38. Process of claim 1 , wherein in the hydrogenation step, the treat rate is from 160 to 200 Nm 3 /ton of feed.
39. Process of claim 9 , wherein in the hydrogenation step, the catalyst has a specific surface area varying between 150 and 200 m 2 /g of catalyst.
40. Process of claim 12 , wherein in the hydrogenation step, the treat rate is above 150 Nm 3 /ton of feed.
41. Process of claim 18 , wherein the amount of catalyst in the two stages according to weight amounts (wt. %) is 10-20 wt. % and 80-90 wt. %, respectively.
42. Process of claim 19 , wherein the hydrodesulphurized middle distillate contains less than 5 ppm sulphur.
43. Process of claim 1 , further comprising a step of prefractionation of the desulphurized middle distillates prior to hydrogenation, into low-sulphur feed fractions having a boiling range of less than 80° C., then subjected to hydrogenation.