A process for producing a liquid transportation fuel component

Abstract

A process for producing at least one liquid transportation fuel component is provided. In the process, a paraffinic hydrocarbon feed is subjected as part of a first reaction section feed to hydrocracking in a first reaction section to obtain a hydrocracking effluent, which hydrocracking effluent is subjected as part of a second reaction section feed to hydroisomerisation in a second reaction section to obtain a hydroisomerisation effluent, the hydroisomerisation effluent being fed to a fractionation, from which fractionation at least one liquid transportation fuel components is recovered.

1 .- 25 . (canceled) 
     
     
         26 . A process for producing at least one liquid transportation fuel component, the process comprising:
 providing a paraffinic hydrocarbon feed including at least 60 wt-% paraffins of a total weight of the paraffinic hydrocarbon feed, of which paraffins at least 5 wt-% are isoparaffins;   subjecting a first reaction section feed including the paraffinic hydrocarbon feed and optionally a recycle stream and/or a side cut, to hydrocracking in a first reaction section in a presence of a hydrocracking catalyst to obtain a hydrocracking effluent;   subjecting a second reaction section feed including the hydrocracking effluent to hydroisomerisation in a second reaction section in a presence of a hydroisomerisation catalyst to obtain a hydroisomerisation effluent; and   feeding the hydroisomerisation effluent to a fractionation and recovering from the fractionation at least one or more liquid transportation fuel components, and optionally the recycle stream and/or the side cut.   
     
     
         27 . The process according to  claim 26 , wherein the paraffinic hydrocarbon feed comprises:
 at least 70 wt-%, and/or at least 80 wt-%, and/or at least 90 wt-%, and/or at least 95 wt-% paraffins of a total weight of the paraffinic hydrocarbon feed; and/or at least 70 wt-%, and/or at least 80 wt-%, and/or at least 90 wt-%, and/or at least 95 wt-% C12-C30 hydrocarbons of the total weight of the paraffinic hydrocarbon feed.   
     
     
         28 . The process according to  claim 26 , wherein the paraffinic hydrocarbon feed comprises:
 at least 8 wt-%, or at least 10 wt-%, and/or at least 20 wt-%, and/or at least 30 wt-%, and/or at least 40 wt-%, and/or at least 50 wt-%, and/or at least 60 wt-%, and/or at least 70 wt-%, and/or at least 80 wt-% isoparaffins of the total weight of paraffins in the paraffinic hydrocarbon feed.   
     
     
         29 . The process according to  claim 26 , wherein the paraffinic hydrocarbon feed comprises:
 at least 3 wt-%, and/or at least 5 wt-%, and/or at least 10 wt-%, and/or at least 15 wt-% multiple-branched isoparaffins of the total weight of paraffins in the paraffinic hydrocarbon feed.   
     
     
         30 . The process according to  claim 26 , wherein the first reaction section feed comprises:
 at least 30 wt-%, and/or at least 40 wt-%, and/or at least 50 wt-%, and/or at least 60 wt-%, and/or at least 70 wt-%, and/or at least 80 wt-% isoparaffins of a total weight of paraffins in the first reaction section feed; and/or at least 5 wt-%, and/or at least 10 wt-%, and/or at least 15 wt-%, and/or at least 20 wt-% multiple-branched isoparaffins of the total weight of paraffins in the first reaction section feed.   
     
     
         31 . The process according to  claim 26 , comprising:
 recovering from the fractionation the recycle stream; and feeding the recycle stream to the first reaction section as part of the first reaction section feed, and/or   recovering from the fractionation the side cut and feeding the side cut to the first reaction section as part of the first reaction section feed, and/or   feeding a portion of the paraffinic hydrocarbon feed to the second reaction section as part of the second reaction section feed, which portion of the paraffinic hydrocarbon feed is obtained by splitting the paraffinic hydrocarbon feed between the first reaction section and the second reaction section; and/or   wherein the recycle stream and/or the side cut includes:   at least 50 wt-%, and/or at least 60 wt-%, and/or at least 70 wt-%, and/or at least 80 wt-% isoparaffins of the total weight of paraffins in the recycle stream or side cut, respectively; and/or at least at least 10 wt-%, and/or at least 15 wt-%, and/or at least 20 wt-%, and/or at least 30 wt-% multiple-branched isoparaffins of the total weight of paraffins in the recycle stream or side cut, respectively.   
     
     
         32 . The process according to  claim 26 , wherein the second reaction section feed comprises:
 a portion of the paraffinic hydrocarbon feed, and   wherein the paraffinic hydrocarbon feed is split between the first reaction section feed and the second reaction section feed in a weight ratio within a range from 1:99 to 99:1, and/or from 10:90 to 95:5, and/or from 20:80 to 90:10, and/or from 30:70 to 80:20 first reaction section feed to second reaction section feed.   
     
     
         33 . The process according to  claim 26 , wherein
 the side cut is recovered from the fractionation, and has T5 and T95 temperatures, as determined according to EN ISO 3405-2019, within a range from 250° C. to 320° C., and/or within a range from 260° C. to 310° C., and/or within a range from 270° C. to 305° C.; and/or difference between T95 and T5 temperatures (95 vol-% and 5 vol-% recovered, EN ISO 3405-2019) of 40° C. or less, and/or 30° C. or less, and/or 20° C. or less; and/or   wherein the recycle stream is recovered from the fractionation, and has a T5 temperature (5 vol-% recovered, EN ISO 3405-2019) of 270° C. or higher; and/or a T5 temperature within a range from 270° C. to less than 300° C., and/or within a range from 270° C. to less than 295° C., and/or within a range from 270° C. to less than 290° C.; and/or an initial boiling point (IBP) less than 290° C., and/or less than 288° C., and/or less than 285° C.; and/or   wherein the first reaction section feed includes:   the paraffinic hydrocarbon feed and a recycle stream and/or side cut, and the weight ratio of the paraffinic hydrocarbon feed to a sum amount of the recycle stream and/or the side cut is within a range from 10:90 to 90:10, and/or from 20:80 to 80:20.   
     
     
         34 . The process according to  claim 26 , wherein the hydrocracking in the first reaction section is conducted at a temperature within a range from 200° C. to 500° C., and/or from 220° C. to 430° C., and/or from 280° C. to 400° C., a pressure within a range from 0.5 MPa to 20 MPa, and/or from 1 MPa to 20 MPa, and/or from 3 MPa to 15 MPa, a H 2  partial pressure at an inlet of the first reaction section within a range from 0.5 MPa to 20 MPa, and/or from 1 MPa to 20 MPa, and/or from 3 MPa to 15 MPa, a weight hourly space velocity within a range from 0.1 to 10, and/or from 0.2 to 10, and/or from 0.4 to 8 and/or from 0.5 to 5 kg first reaction section per kg catalyst per hour, and a H 2  to first reaction section feed ratio within a range from 10 to 2000, and/or from 50 to 1000 normal liters H 2  per liter first reaction section feed. 
     
     
         35 . The process according to  claim 26 , wherein the hydroisomerisation in the second reaction section is conducted at a temperature within a range from 200° C. to 500° C., and/or from 230° C. to 500° C., and/or from 250° C. to 450° C., and/or from 280° C. to 400° C., a pressure within a range from 1 MPa to 20 MPa, and/or from 2 MPa to 15 MPa or from 3 MPa to 10 MPa, a H2 partial pressure at an inlet of the second reaction section within a range from 1 MPa to 20 MPa, and/or from 2 MPa to 15 MPa or from 3 MPa to 10 MPa, a weight hourly space velocity within a range from 0.1 to 10, and/or from 0.2 to 8, and/or from 0.4 to 6 kg second reaction section feed per kg catalyst per hour, and a H 2  to paraffinic hydrocarbon feed ratio within a range from 10 to 2000, and/or from 50 to 1000 normal liters H 2  per liter second reaction section feed. 
     
     
         36 . The process according to  claim 26 , wherein the first reaction section is operated at a lower temperature than the second reaction section. 
     
     
         37 . The process according to  claim 26 , wherein the hydrocracking catalyst is arranged in one or more catalyst beds in the first reaction section and the hydroisomerisation catalyst is arranged in one or more catalyst beds in the second reaction section, and the first reaction section and the second reaction section are arranged in the same reactor or in separate reactors; and/or
 wherein a weight ratio of the hydrocracking catalyst in the first reaction section to the hydroisomerisation catalyst in the second reaction section is within a range from 5:95 to 70:30, and/or from 10:90 to 65:35, and/or from 20:80 to 60:40.   
     
     
         38 . The process according to  claim 26 , wherein the hydroisomerisation catalyst is a non-sulphided bifunctional hydroisomerisation catalyst and the hydrocracking catalyst is a non-sulphided bifunctional hydrocracking catalyst, and the non-sulphided bifunctional catalysts comprise:
 at least one or more metals selected from noble metals of Group VIII of the Periodic Table, and/or from Pt and/or Pd, and at least one or more acidic porous materials, and   optionally each of the first reaction section feed and the second reaction section feed includes:   less than 50 wt-ppm, and/or less than 30 wt-ppm, and/or less than 10 wt-ppm sulphur (ppm by weight, calculated as elemental S), as determined according to ISO 20846-2019, of a total respective reaction section feed.   
     
     
         39 . The process according to  claim 26 , wherein the hydroisomerisation catalyst is a bifunctional hydroisomerisation catalyst, and/or a non-sulphided bifunctional hydroisomerisation catalyst, comprising:
 at least one or more metals selected from Group VIII of the Periodic Table, from noble metals of Group VIII, and/or from Pt and/or Pd; and   at least one or more acidic porous materials selected from zeolites and/or zeolite-type materials, wherein the at least one or more of the zeolites and/or zeolite-type materials has a framework type selected from AEL, ATO, AFO, MRE, MTT, MTW, TON, MRT, MOR, FER, and/or MWW, and/or at least one or more acidic porous materials selected from SAPO-11, SAPO-31, SAPO-41, ZSM-22, ZSM-23, ZSM-48, NU-10, ZBM-30, IZM-2, EU-2, and/or mordenite, at least one or more acidic porous materials selected from SAPO-11, SAPO-41, ZSM-23, and/or ZSM-48; and/or   at least one or more of alumina, silica, amorphous silica-alumina, titanium alumina, titania, and/or zirconia.   
     
     
         40 . The process according to  claim 26 , wherein the hydrocracking catalyst is a bifunctional hydrocracking catalyst, and/or a non-sulphided bifunctional hydrocracking catalyst, comprising:
 at least one or more metals selected from Group VIII of the Periodic Table, Mo, Co, and/or W, and/or from Ni, Mo, Co, W, Pt, and/or Pd, and/or from Pt and/or Pd; and   at least one or more acidic porous materials selected from zeolites, zeolite-type materials, and/or amorphous silica-alumina, and/or wherein at least one or more of the zeolites or zeolite-type materials has a framework type selected from MFI, BEA, FAU, MOR, FER, AEL, AFI, ATO, AFO, MRE, MTT, MTW, TON, and/or MRT, and/or at least one or more acidic porous materials selected from SAPO-5, SAPO-11, SAPO-31, SAPO-41, ZSM-22, ZSM-23, ZSM-43, ZSM-48, IZM-2, mordenite, beta-zeolites, Y-type zeolites, and/or amorphous silica-alumina, and/or at least one or more acidic porous material selected from SAPO-5, SAPO-11, ZSM-23, beta-zeolites, Y-type zeolites, and/or amorphous silica-alumina; and/or   at least one or more of alumina, silica, titanium alumina, titania, and/or zirconia.   
     
     
         41 . The process according to  claim 38 , wherein the bifunctional hydrocracking catalyst in the first reaction section has a higher total number of acid sites compared to the bifunctional hydroisomerisation catalyst in the second reaction section, as determined by NH 3 -TPD. 
     
     
         42 . The process according to  claim 26 , wherein providing the paraffinic hydrocarbon feed comprises:
 subjecting a hydrotreatment feed to a hydrotreatment, and/or subjecting an oxygenated hydrocarbon feed to hydrodeoxygenation, optionally, followed by an initial hydroisomerisation to obtain a paraffinic hydrotreatment effluent, wherein the hydrotreatment feed includes:   at least one or more of vegetable oil(s), animal fat(s), microbial oil(s), thermally liquefied organic waste and residue(s), and/or enzymatically liquefied organic waste and residue(s), and/or the oxygenated hydrocarbon feed includes:   at least one or more of vegetable oil(s), animal fat(s), and/or microbial oil(s), and/or   subjecting a syngas to a Fischer-Tropsch (FT) conversion, optionally, followed by an initial dewaxing, to obtain a paraffinic FT effluent; and   subjecting the paraffinic hydrotreatment effluent and/or the paraffinic FT effluent to a gas-liquid separation, and optionally, to a paraffinic feed fractionation, to provide the paraffinic hydrocarbon feed.   
     
     
         43 . The process according to  claim 26 , wherein the biogenic carbon content (EN 16640 (2017)) of the paraffinic hydrocarbon feed is at least 50 wt-%, and/or at least 70 wt-%, and/or at least 90 wt-%, and/or at least 95 wt-%, or even about 100 wt-%, based on a total weight of carbon (TC) in the paraffinic hydrocarbon feed. 
     
     
         44 . The process according to  claim 26 , wherein at least one or more of an aviation fuel component, a diesel fuel component, a gasoline fuel component, and/or a marine fuel component are recovered from the fractionation, and/or at least an aviation fuel component, and/or at least an aviation fuel component and a diesel fuel component, and/or at least an aviation fuel component, a diesel fuel component and a gasoline fuel component; and/or
 wherein at least one of the liquid transportation fuel components recovered from the fractionation is an aviation fuel component having density at 15° C. within a range from 730 kg/m 3  to 772 kg/m 3  (EN ISO 12185-1996), T10 temperature at most 205° C. (EN ISO 3405-2019), final boiling point at most 300° C. (EN ISO 3405-2019), flash point at least 38° C. (IP 170-2013, Abel closed-cup method) and freezing point at most −40° C. (IP 529-2016).   
     
     
         45 . The process according to  claim 26 , comprising:
 recovering from the fractionation an aviation fuel component, in a yield of at least 30 wt-%, and/or at least 40 wt-%, and/or at least 50 wt-%, and/or within a range from 30 wt-% to 90 wt-%, of a total weight of the paraffinic hydrocarbon feed.