Paraffinic jet and diesel fuels and base oils from vegetable oils via a combination of hydrotreating, paraffin disproportionation and hydroisomerization

Abstract

The present invention relates to a new process which comprises the steps of hydrotreating, paraffin disproportionation and hydroisomerization to convert biological hydrocarbonaceous oxygenated oils comprising triglycerides into biologically-derived paraffinic jet/diesel fuels, solvents and base oils. A combination of conventional hydrogenation/dehydrogenation catalysts, such as Pt/Al 2 O 3 , and conventional olefin metathesis catalysts, such as WO 3 /SiO 2 , or inexpensive variations thereof, is generally employed in the paraffin disproportionation step.

What is claimed is: 
     
         1 . A process for the manufacture of biologically-derived paraffinic jet and diesel fuels, solvents and base oils from a biological hydrocarbonaceous oxygenated oil, comprising triglycerides, comprising:
 (a) hydrotreating the biological hydrocarbonaceous oxygenated oil to form a first effluent mixture comprising propane, carbon monoxide, carbon dioxide, water and a n-paraffinic product;   (b) recovering the n-paraffinic product from the first effluent mixture; and   (c) converting the n-paraffinic product of step (b) over a paraffin disproportionation catalyst to form a second effluent mixture comprising a light n-paraffinic biologically derived product and a heavy n-paraffinic biologically derived product.   
     
     
         2 . The process of  claim 1 , further comprising:
 (d) recovering the light n-paraffinic biologically derived product from step (c); and   (e) recovering the heavy n-paraffinic biologically derived product from step (c).   
     
     
         4 . The process of  claim 1 , further comprising an isomerization step of the n-paraffinic product from step (b). 
     
     
         5 . The process of  claim 1 , further comprising an isomerization step of the second effluent mixture from step (c). 
     
     
         6 . The process of  claim 2 , further comprising an isomerization step of the light n-paraffinic biologically derived product, heavy n-paraffinic biologically derived product, or both the light and heavy paraffinic biologically derived products. 
     
     
         7 . The process of  claim 1 , wherein the triglyceride is a mixture of triglycerides. 
     
     
         8 . The process of  claim 1 , wherein the biological hydrocarbonaceous oxygenated oil is selected from the group consisting of rapeseed oil, colza oil, canola oil, tall oil, sunflower oil, soybean oil, hempseed oil, olive oil, linseed oil, mustard oil, palm oil, peanut oil, castor oil, coconut oil, lard, tallow and train oil. 
     
     
         9 . The process of  claim 1 , wherein step (c) further comprises: treatment of the n-paraffinic product of step (b) with a hydrogenation/dehydrogenation catalyst and an olefin metathesis catalyst under conditions which dehydrogenate the paraffins to olefins, metathesize the olefins, and hydrogenate the olefins to paraffins to provide a third effluent mixture comprising a light n-paraffinic biologically derived product and a heavy n-paraffinic biologically derived product. 
     
     
         10 . The process of  claim 9 , wherein the hydrogenation/dehydrogenation catalyst includes at least one metal or a corresponding metal compound selected from the group consisting of iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum. 
     
     
         11 . The process of  claim 10 , wherein the hydrogenation/dehydrogenation catalyst comprises a metal or corresponding metal compound selected from the group consisting of: rhenium, tin, germanium, gallium, indium, lead, tin and mixtures thereof. 
     
     
         12 . The process of  claim 9 , wherein the olefin metathesis catalyst comprises a metal or corresponding metal compound is selected from the group consisting of tungsten, molybdenum, tin and rhenium. 
     
     
         13 . The process of  claim 12 , wherein the olefin metathesis catalyst comprises tungsten. 
     
     
         14 . The process of  claim 9 , wherein the hydrogenation/dehydrogenation catalyst comprises platinum or a platinum compound and the olefin metathesis catalyst comprises tungsten. 
     
     
         15 . The process of  claim 14 , wherein the hydrogenation/dehydrogenation catalyst is platinum-on-alumina and the olefin metathesis catalyst is tungsten-on-silica and the volumetric ratio of the platinum component to the tungsten component is greater than 1:50 and less than 50:1, and wherein the amount of platinum on the alumina is within the range of from about 0.01 weight percent to about 10 weight percent on an elemental basis and the amount of tungsten on the silica is within the range of from about 0.01 weight percent to about 50 weight percent on an elemental basis. 
     
     
         16 . The process of  claim 15 , wherein the volumetric ratio of the platinum component to the tungsten component is between 1:10 and 10:1 and wherein the amount of platinum on the alumina is within the range of from about 0.1 weight percent to about 5.0 weight percent on an elemental basis and the amount of tungsten on the silica is within the range of from about 0.1 weight percent to about 20 weight percent on an elemental basis. 
     
     
         17 . The process of  claim 9 , wherein step (c) further comprises a temperature between about 400° F. to 1000° F. 
     
     
         18 . The process of  claim 9 , wherein step (c) further comprises a pressure between about 50 psig to 3000 psig. 
     
     
         19 . The process of  claim 9 , wherein step (c) further comprises a liquid hourly space velocity between about 0.1 to 5 h −1 . 
     
     
         20 . The process of  claim 1 , wherein step (a) further comprises a temperature for hydrotreating between about 300° F. to 750° F. 
     
     
         21 . The process of  claim 1 , wherein step (a) further comprises a total reaction pressure for hydrotreating between about 50 to 3000 psig. 
     
     
         22 . The process of  claim 1 , wherein step (a) further comprises a liquid hourly space velocity for hydrotreating between about 0.1 to 5 h −1 . 
     
     
         23 . The process of  claim 1 , wherein step (a) further comprises a hydrogen feed rate for hydrotreating between about 0.1 to 20 MSCF/bbl.