Sugar alcohol split injection conversion
View Patent ↗A method of hydrotreating liquefied biomass feedstock with diesel feedstock to produce alkanes is demonstrated that prevents damage to the reactor catalyst, reduces coke production, and converts nearly all of the polyols to alkanes. In order to mitigate the potential coking issue and to moderate the temperature of the catalyst bed while maintaining high conversion for sugar alcohol to hydrocarbon via a hydrotreating process, a diesel feedstock is fed over the reactor catalyst with multiple injections of polyol feedstock along the reactor.
1. A method of hydrotreating polyol feedstock that reduces coking, the method comprising:
a) contacting a hydrotreating catalyst with a diesel feedstock at the beginning of the reactor catalyst,
b) contacting the hydrotreating catalyst with a polyol feedstock at the beginning of the reactor catalyst,
c) contacting the hydrotreating catalyst with one or more additional polyol feedstocks at intervals along the reactor catalyst,
wherein said polyol feedstock is reacted on said catalyst to generate alkanes.
2. The method of claim 1 , wherein said fuel oil feedstock is heated to reaction temperature prior to contacting the hydrotreating catalyst.
3. The method of claim 1 , wherein said polyol feedstock comprises Glycol, Glycerol, Erythritol, Threitol, Arabitol, Ribitol, Xylitol, Allitol, Dulcitol, Galactitol, Iditol, Mannitol, Sorbitol, Isomalt, Lactitol, Maltitol, Trehalose, and combinations thereof.
4. The process of claim 1 , wherein said fuel oil feedstock is selected from the group consisting of gasoline, jet fuel, kerosene, heating oil, fuel oils, diesel fuel, petro-diesel, bio-diesel, synthetic diesel, blended diesel, and combinations thereof.
5. The process of claim 1 ,wherein said hydrotreating catalyst is selected from the group consisting of cobalt (Co), molybdenum (Mo), nickel (Ni), titanium (Ti), tungsten (W), zinc (Zn), antimony (Sb), bismuth (Bi), cerium (Ce), vanadium (V), niobium (Nb), tantalum (Ta), chromium (Cr), manganese (Mn), rhenium (Re), iron (Fe), platinum (Pt), iridium (Ir), palladium (Pd), osmium (Os), rhodium (Rh), ruthenium (Ru), and combinations thereof.
6. The process of claim 1 , wherein said hydrotreating catalyst is a bimetallic catalyst selected from the group consisting of Co/Mo, Co/W, Ni/Mo, Ni/W, Ti/Mo, Ti/W and combinations thereof.
7. The process of claim 1 , wherein said reaction occurs at an approximate temperature of 400° F., 425° F., 450° F., 475° F., 500° F., 525° F., 550° F., 575° F., 600° F., 625° F., 650° F., 675° F., 700° F., 725° F., 750° F., 775° F., 800° F., 825° F., 850° F., 875° F., or 900° F.
8. The process of claim 1 , wherein said reaction occurs at an approximate pressure of 500, 550, 600, 650, 700, 750, 800, 850, 900, 950, 1000, 1050, 1100, 1150, 1200, 1250, 1500, 1750, 2000, 2250, 2500, 2750, and 3000 psig.
9. The process of claim 1 , wherein said hydrotreating catalyst is an unsupported catalyst selected from the group consisting of Co/Mo, Co/W, Ni/Mo, Ni/W, Ti/Mo, Ti/W, Co/Mo/W, Ni/Mo/W, Ti/Mo/W and combinations thereof.
10. A method of hydrotreating liquefied biomass feedstock that reduces coking, the method comprising:
a) liquifying biomass to generate a polyol feedstock,
b) contacting a hydrotreating catalyst with a fuel oil feedstock at the beginning of the reactor catalyst,
c) contacting the hydrotreating catalyst with the polyol feedstock at the beginning of the reactor catalyst,
d) contacting the hydrotreating catalyst with one or more additional polyol feedstocks at intervals along the reactor catalyst,
wherein said polyol feedstock is reacted on said catalyst to generate alkanes.
11. The method of claim 10 , wherein said fuel oil feedstock is heated to reaction temperature prior to contacting the hydrotreating catalyst.
12. The method of claim 10 , wherein said polyol feedstock comprises Glycol, Glycerol, Erythritol, Threitol, Arabitol, Ribitol, Xylitol, Allitol, Dulcitol, Galactitol, Iditol, Mannitol, Sorbitol, Isomalt, Lactitol, Maltitol, Trehalose, and combinations thereof.
13. The process of claim 10 , wherein said fuel oil feedstock is selected from the group consisting of gasoline, jet fuel, kerosene, heating oil, fuel oils, diesel fuel, petro-diesel, bio-diesel, synthetic diesel, blended diesel, and combinations thereof.
14. The process of claim 10 , wherein said hydrotreating catalyst is selected from the group consisting of cobalt (Co), molybdenum (Mo), nickel (Ni), titanium (Ti), tungsten (W), zinc (Zn), antimony (Sb), bismuth (Bi), cerium (Ce), vanadium (V), niobium (Nb), tantalum (Ta), chromium (Cr), manganese (Mn), rhenium (Re), iron (Fe), platinum (Pt), iridium (Ir), palladium (Pd), osmium (Os), rhodium (Rh), ruthenium (Ru), and combinations thereof.
15. The process of claim 10 , wherein said hydrotreating catalyst is a bimetallic catalyst selected from the group consisting of Co/Mo, Co/W, Ni/Mo, Ni/W, Ti/Mo, Ti/W and combinations thereof.
16. The process of claim 10 , wherein said reaction occurs at an approximate temperature of 400° F., 425° F., 450° F., 475° F., 500° F., 525° F., 550° F., 575° F., 600° F., 625° F., 650° F., 675° F., 700° F., 725° F., 750° F., 775° F., 800° F., 825° F., 850° F., 875° F., or 900° F.
17. The process of claim 10 , wherein said reaction occurs at an approximate pressure of 500, 550, 600, 650, 700, 750, 800, 850, 900, 950, 1000, 1050, 1100, 1150, 1200, 1250, 1500, 1750, 2000, 2250, 2500, 2750, and 3000 psig.
18. The process of claim 10 , wherein said hydrotreating catalyst is an unsupported catalyst selected from the group consisting of Co/Mo, Co/W, Ni/Mo, Ni/W, Ti/Mo, Ti/W, Co/Mo/W, Ni/Mo/W, Ti/Mo/W and combinations thereof.