Granted Patent B2

US 12,522,771 · App. 17/776,902 · Granted Jan 13, 2026

Inventors: Teemu Rantasalo (Espoo, FI); Olli Tuomala (Espoo, FI); Arto Neuvonen (Espoo, FI); Jesse Vilja (Espoo, FI)

Assignee: NESTE OYJ

C10G45/58C10G3/46C10G3/50C10G3/60C10G7/00C10G67/02C10L1/08C10M109/02C10G2300/1011C10G2300/1014C10G2300/1018C10G2300/202C10G2300/205C10G2300/207C10G2300/208C10G2300/302C10G2300/304C10G2300/307C10G2300/308C10G2300/4006C10G2300/4012C10G2300/4081C10G2300/80C10G2400/04C10G2400/08C10G2400/10C10L2200/0469C10L2270/026C10L2270/04C10M2203/003

Abstract

Claims (28)

1 . A method for combined production of aviation fuel and base oil both of biological origin, the method comprising:

providing feedstock of biological origin containing fatty acids and/or esters of fatty acids;

subjecting the feedstock to hydrotreatment and isomerization to obtain a paraffinic hydrocarbon intermediate;

fractionating said paraffinic hydrocarbon intermediate into at least two fractions,

a lighter fraction fulfilling a specification ASTM D7566-20 Annex A2 for aviation fuel, and

a heavier fraction fulfilling the following specifications for a base oil component, containing:

saturates (ASTM D2007) more than 90 wt-%;

sulfur content (ASTM D 1552/D2622/D3120/D4294/D4927) 0.03 wt-% or less;

kinematic viscosity 100° C. (EN ISO 3104/ASTMD445) between 1.3-3.5 mm 2 /s;

kinematic viscosity 40° C. (EN ISO 3104/ASTMD445) between 3.4-13 mm2/s;

pour point (ASTM D 97) less than −24° C.;

flash point (ENISO2719/ASTMD93) more than 120° C.; and

adjusting a production capacity of the lighter fraction and a production capacity of the heavier fraction by selection of process conditions, and/or isomerization process conditions, to produce a yield of the lighter fraction of 60-90 wt-% of a total weight of the formed fractions, and to produce yield of the heavier fraction of 10-40 wt-% of the total weight of the formed fractions;

wherein a combined yield of the two fractions is at least 98 wt-% of the paraffinic hydrocarbon intermediate of biological origin.

2 . The method according to claim 1 , comprising:

performing the hydrotreatment, and/or a hydrodeoxygenation, under a hydrogen pressure from 10 to 150 bar, and/or 20-120 bar, and/or 30-100 bar, and at a temperature from 200 to 400° C., and/or 250-380° C., and/or 280-360° C.

3 . The method according to claim 1 , comprising:

performing the hydrotreatment in a presence of one or more catalyst(s) selected from hydrogenation metal on a support, and/or a catalyst selected from a group containing of Pd, Pt, Ni, Co, Mo, Ru, Rh, W and/or any combination thereof, and/or a catalyst containing one or more catalyst(s) selected from CoMo, NiMo, NiW, CoNiMo on a support, and/or an alumina support.

4 . The method according to claim 1 , comprising:

performing the isomerization at a temperature of 200-500° C., and/or 280-370° C., and at a pressure of 10-150 bar, and/or 20-50 bar.

5 . The method according to claim 1 , comprising:

performing the isomerization in a presence of one or more catalyst(s) containing a Group VIII metal on a support, where the support is selected from silica, alumina, clays, titanium oxide, boron oxide, zirconia, used alone or as a mixture, and/or as silica and/or alumina.

6 . The method according to claim 1 , comprising:

subjecting the feedstock, after hydrotreatment and isomerization, to stabilization at a pressure lower than the isomerization pressure.

7 . The method according to claim 6 , comprising:

forming during stabilization, an overhead fraction containing hydrocarbons in a naphtha range (C4-C8); and

recycling an amount of 60 wt-% or more, and/or 90 wt-% or more, and/or from 90 to 95 wt-%, of the formed hydrocarbons in the naphtha range at the stabilization column overhead, back to the stabilization.

8 . The base oil component of biological origin produced by the method according to claim 1 .

Assignments (1)

Continuity (1)

References Cited (112)