Hydro-dealkylation process to generate high quality fuels, base stocks and waxes
Provided are methods of hydro-dealkylation of hydrocarbon feedstock to produce an intermediate hydrocarbon product having a boiling point at T10 of greater than about 500° F.+ by distillation method ASTM D7169 and a viscosity index greater than about 120 in accordance with ASTM D2270 where at least about 50 percent of the hydrocarbon feedstock is a SIMDIS of 400° F. The intermediate hydrocarbon product can be used to produce a base stock, a wax and/or paraffinic diesel.
1 . A method of hydro-dealkylation of a hydrocarbon feedstock to provide an intermediate hydrocarbon product comprising:
providing a hydrocarbon feedstock comprising crude oil or a fractionated hydrocarbon stream or blend thereof having a paraffin to ring compound ratio in a VGO boiling range of between about T10 of 650° F. (340° C.) to about T90 of 1050° F. (565° C.) in accordance with ASTM D2887 greater than or equal 0.2 and at least about T50 percent of the hydrocarbon feedstock is a SIMDIS of 400° F. (204° C.); and
reacting the hydrocarbon feedstock and hydrogen in the presence of a hydrotreating catalyst at a temperature between about 500° F. (260° C.) to about 1200° F. (650° C.) and at pressure between about 400 psig to about 2400 psig to produce an intermediate hydrocarbon product having a boiling point at T10 of greater than about 500° F.+ (260° C.+) to 650 CF (340°F.) by distillation method ASTM D7169 and a viscosity index greater than about 120 in accordance with ASTM D2270.
2 . The method of claim 1 , wherein the intermediate hydrocarbon product is used to produce a base stock.
3 . The method of claim 2 , further comprising hydrotreating the base stock.
4 . A method of producing a base stock and/or wax comprising:
providing a hydrocarbon feedstock comprising crude oil or a fractionated hydrocarbon stream or blend thereof having a paraffin to ring compound ratio in a VGO boiling range of between about 650° F. (340° C.) to about 1050° F. (565° C.) greater than or equal 0.2 and at least about 50 percent of the hydrocarbon feedstock is a SIMDIS of 400° F. (204° C.);
reacting the hydrocarbon feedstock and hydrogen in the presence of a hydrotreating catalyst at a temperature between about 500° F. (260° C.) to about 1200° F. (650° C.) and at pressure between about 400 psig to about 2400 psig to produce an intermediate hydrocarbon product; and fractionating the intermediate hydrocarbon product to produce a base stock and/or a wax, wherein the base stock and the wax each have a boiling point at T10 of greater than about 650° F.+ (340° C.+) by distillation method ASTM D7169 and a viscosity index greater than about 120 in accordance with ASTM D2270.
5 . The method of claim 4 , further comprising separating the base stock from a wax with a solvent dewaxing unit.
6 . The method of claim 5 , further comprising de-oiling the wax to generate a raffinate.
7 . The method of claim 6 , wherein the raffinate is hydrotreated to produce semi-refined or fully refined wax product and a de-oiling extract, wherein the de-oiling extract comprises a foots oil or soft wax.
8 . The method of claim 5 , wherein the intermediate hydrocarbon product is fractionated to produce a LVGO, a MVGO, an HVGO and/or a VTB.
9 . The method of claim 5 , wherein the intermediate hydrocarbon product is used to produce slack wax, semi-refined wax, fully refined wax and/or scale.
10 . The method of claim 5 , wherein the hydrocarbon product has a viscosity index between about 130 and about 140.
11 . The method of claim 5 , wherein an aromatic content of the intermediate hydrocarbon product is reduced by a solvent extraction unit.
12 . A method of producing at a paraffinic diesel comprising:
providing a hydrocarbon feedstock comprising crude oil or a fractionated hydrocarbon stream or blend thereof having a paraffin to ring compound ratio in a VGO boiling range of between about 650° F. (340° C.) to about 1050° F. (565° C.) greater than or equal 0.2;
reacting the hydrocarbon feedstock and hydrogen in the presence of a hydrotreating catalyst at a temperature between about 500° F. (260° C.) to about 1200 20 F. (650° C.) and at pressure between about 400 psig to about 2400 psig to produce an intermediate hydrocarbon product; and
fractionating the intermediate hydrocarbon product to produce a paraffinic diesel, wherein the paraffinic diesel having a boiling point of at T10 of greater than about 500° F.+ (260° C.+) by distillation method ASTM D7169 and Cetane number greater than or equal to 60 in accordance with ASTM 6870.
13 . The method of claim 12 , wherein the paraffinic diesel comprising less than or equal to about 5.0 ppm sulfur and less than or equal to 1.1 wt. % aromatics.
14 . The method of claim 12 , wherein the intermediate hydrocarbon product is selected from an atmospheric tower bottom, a vacuum tower bottom and a vacuum gas oil.
15 . The method of claim 12 , wherein the paraffin to ring compound ratio is between about 0.4 to about 1.2.
16 . The method of claim 12 wherein the hydrocarbon feedstock has an API gravity between about 35 and about 55.
17 . The method of claim 12 wherein the hydrocarbon feedstock comprising less than 0.5 wt. % sulfur.
18 . The method of claim 12 , wherein the hydrocarbon feedstock is reacted at a pressure between about 400 psig to about 2400 psig.
19 . The method of claim 12 , wherein the hydrocarbon feedstock comprises less than 2000 ppm, 50 to 1500 ppm or 50 to 400 ppm of nitrogen at 650° F. (340° C.).
20 . The method of claim 12 , wherein the catalyst is NiMo, CoMo, NiW or a hydrotreating catalyst.
21 . The method of claim 12 , wherein the hydrocarbon feedstock is about 0.2 to about 4.0 LHSV per hour.
22 . The method of claim 12 , wherein the hydrogen is provided between about 200 to about 6000 SCF/BBL.
23 . The method of claim 12 , wherein the hydrocarbon feedstock is at least 80 wt. % petroleum hydrocarbon.
24 . The method of claim 12 , wherein the hydrocarbon product is further processed by aromatic saturation, dewaxing, or hydrofinishing.
25 . The method of claim 12 , wherein the liquid hourly space velocity of the hydrocarbon feedstock is between about 0.2 to about 0.4 per hour and the hydrotreating catalystis not acidic.