Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources

Abstract

A process to prepare a kerosene and a gasoil product from a crude petroleum source having a Watson characterization factor K value of equal or below 12.0 by (a) isolation of a petroleum derived kerosene fraction and a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm or below 19 mm if naphthalenes content of the kerosene fraction is below 3% vol and the petroleum derived gas oil has a cetane number of below 50 or a density higher than 845 kg/m 3 , ( ) adding a Fischer-Tropsch derived kerosene fraction to the petroleum derived kerosene fraction in an amount sufficient to obtain a mixture having a smoke point value of above 25 mm or above 19 mm if the naphthalenes content of the mixture is below 3% vol and (c) adding a Fischer-Tropsch derived gas oil fraction to the petroleum derived gasoil fraction such that the resultant mixture has a cetane number value of above 51.

1 . A process to prepare a kersosene and a gasoil product from a crude petroleum source having a Watson characterization factor K value of equal to or below 12.0 comprising: 
 (a) isolating a petroleum derived kerosene fraction and a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm if the naphthalenes content of the petroleum derived kerosene fraction is at least 3% vol, or below 19 mm if the naphthalenes content of the petroleum derived kerosene fraction is below 3% vol, and the petroleum derived gasoil fraction has a cetane number of below 50 or a density higher than 845 kg/m3;    (b) adding a Fischer-Tropsch derived kerosene fraction to the petroleum derived kerosene fraction in an amount sufficient to obtain a mixture having a smoke point value of above 25 mm if the naphthalenes content of the mixture is at least 3% vol, or above 19 mm if the naphthalenes content of the mixture is below 3% vol; and,    (c) adding a Fischer-Tropsch derived gasoil fraction to the petroleum derived gasoil fraction such that the resultant mixture has a cetane number value of above 51, wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffins to normal paraffins weight ratio of greater than 0.3.    
     
     
         2 . The process of  claim 1 , wherein the petroleum derived kerosene fraction and the petroleum derived gasoil fraction are isolated from the crude petroleum source in a hydroskimming refinery.  
     
     
         3 . The process of  claim 1 , wherein the petroleum derived gasoil fraction and the petroleum derived kerosene fraction are each more than 50 wt % based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         4 . The process of  claim 1 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200 CC to 300° C.  
     
     
         5 . The process of  claim 1 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         6 . The process of  claim 1 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         7 . The process of  claim 2 , wherein the petroleum derived gasoil fraction and the petroleum derived kerosene fraction are each more than 50 wt % based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         8 . The process of  claim 2 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200° C. to 300° C.  
     
     
         9 . The process of  claim 2 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         10 . The process of  claim 2 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         11 . The process of  claim 3 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200° C. to 300° C.  
     
     
         12 . The process of  claim 3 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         13 . The process of  claim 3 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         14 . The process of  claim 4 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         15 . The process of  claim 4 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         16 . The process of  claim 5 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         17 . A process to prepare a kerosene product from a crude petroleum source having a Watson characterization factor K value of equal to or below 12.0 comprising: 
 (a) isolating a petroleum derived kerosene fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm if the naphthalenes content of the petroleum derived kerosene fraction is at least 3% vol, or below 19 mm if the naphthalenes content of the kerosene fraction is below 3% vol; and,    (b) adding a Fischer-Tropsch derived kerosene fraction to the petroleum derived kerosene fraction in an amount sufficient to obtain a mixture having a smoke point value of above 25 mm if the naphthalenes content of the mixture is at least 3% vol, or above 19 mm if the naphthalenes content of the mixture is below 3% vol, wherein the Fischer-Tropsch derived kerosene fraction has an iso-paraffin to normal paraffin weight ratio of greater than 0.3.    
     
     
         18 . The process of  claim 17 , wherein the petroleum derived kerosene fraction is isolated from the crude petroleum source in a hydroskimming refinery.  
     
     
         19 . The process of  claim 17 , wherein the petroleum derived kerosene fraction is more than 50 wt % based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         20 . The process of  claim 17 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200° C. to 300° C.  
     
     
         21 . The process of  claim 17 , wherein the Fischer-Tropsch derived kerosene fraction has an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         22 . A process to prepare a gasoil product from a crude petroleum source having a Watson characterization factor K value of equal to or below 12.0 comprising: 
 (a) isolating a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived gasoil fraction has a cetane number of below 50 and/or a density higher than 845 kg/m3; and    (b) adding a Fischer-Tropsch derived gasoil fraction to the petroleum derived gasoil fraction such that the resultant mixture has a cetane number value of above 51, wherein the Fischer-Tropsch derived gasoil fraction has an iso-paraffin to normal paraffin weight ratio of greater than 0.3.    
     
     
         23 . The process of  claim 22 , wherein the petroleum derived gasoil fraction is isolated from the crude petroleum source in a hydroskimming refinery.  
     
     
         24 . The process of  claim 22 , wherein the petroleum derived gasoil fraction is more than 50 wt % based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         25 . The process of  claim 22 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         26 . The process of  claim 22 , wherein the Fischer-Tropsch derived gasoil fraction has an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         27 . A process to prepare a hydrocarbon product from a crude petroleum source having a Watson characterization factor K value of equal to or below 12.0 comprising: 
 (a) isolating a petroleum derived kerosene fraction and a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm if the naphthalenes content of the petroleum derived kerosene fraction is at least 3% vol, or below 19 mm if the naphthalenes content of the petroleum derived kerosene fraction is below 3% vol, and the petroleum derived gasoil fraction has a cetane number of below 50 and/or a density higher than 845 kg/m3; and    (b) adding a Fischer-Tropsch derived kerosene fraction to the petroleum derived kerosene fraction in an amount sufficient to obtain a mixture having a smoke point value of above 25 mm if the naphthalenes content of the mixture is at least 3% vol, or above 19 mm if the naphthalenes content of the mixture is below 3% vol; and/or,    (c) adding a Fischer-Tropsch derived gasoil fraction to the petroleum derived gasoil fraction such that the resultant mixture has a cetane number value of above 51, wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of greater than 0.3.    
     
     
         28 . The process of  claim 27 , wherein the petroleum derived kerosene fraction and/or the petroleum derived gasoil fraction are isolated from the crude petroleum source in a hydroskimming refinery.  
     
     
         29 . The process of  claim 27 , wherein the petroleum derived gasoil fraction and the petroleum derived kerosene fraction are each more than 50 wt % based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         30 . The process of  claim 27 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200° C. to 300° C.  
     
     
         31 . The process of  claim 27 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         32 . The process of  claim 27 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.  
     
     
         33 . The process of  claim 28 , wherein the petroleum derived gasoil fraction and the petroleum derived kerosene fraction are each more than 50 Wt% based on a crude having a Watson characterization factor K value equal to or below 12.0.  
     
     
         34 . The process of  claim 28 , wherein the petroleum derived kerosene fraction has an ASTM D86 distillation initial boiling point of between 140° C. to 200° C. and a final boiling point of between 200° C. to 300° C.  
     
     
         35 . The process of  claim 28 , wherein the petroleum derived gasoil fraction has an ASTM D86 distillation initial boiling point of between 250° C. to 300° C. and a final boiling point of between 340° C. to 380° C.  
     
     
         36 . The process of  claim 28 , wherein the Fischer-Tropsch derived kerosene fraction and the Fischer-Tropsch derived gasoil fraction each have an iso-paraffin to normal paraffin weight ratio of between 2 and 6.