Synthetically Derived Illuminating and Heating Paraffin Oil

Abstract

The invention provides synthetically derived distillate kerosene produced by catalytic conversion of Fisher-Tropsch derived light olefins to distillates (COD) and hydrotreating thereof. The kerosene boils in the range of about 170 to 250° C. and includes less than 10% n-paraffins, more than 75% iso-paraffins and less than 1% aromatics.

1 - 27 . (canceled) 
     
     
         28 . A synthetically derived distillate kerosene produced by catalytic conversion of Fisher-Tropsch derived light olefins to distillates and hydrotreating thereof the kerosene having a boiling range of from about 180 to 215° C., and the kerosene comprising:
 less than 10% n-paraffins;   more than 75% iso-paraffins;   less than 1% aromatics; and   about 10% naphthenes.   
     
     
         29 . A synthetically derived distillate kerosene produced by catalytic conversion of Fisher-Tropsch derived light olefins to distillates and hydrotreating thereof, the kerosene having a boiling range of from about 180 to 215° C., the kerosene comprising:
 less than 10% n-paraffins;   more than 60% iso-paraffins;   less than 10% aromatics as mono aromatics only; and   about 10% naphthenes.   
     
     
         30 . The synthetically derived distillate kerosene of  claim 28 , having a flash point as measured by ASTM D93 of from 60° C. to 80° C., a kinematic viscosity at 40° C. as measured by ASTM D445 below about 1.5 cSt, a char value as measured by IP10 below 2 mg/Kg, a total sulfur content of below 0.3 ppm(m/m) as measured by ASTM 3120, an olefins content reflected by a bromine number of less than 1 mg/100 g as measured by IP 129, and a peroxide number of less than 1 mg/100 g as measured by ASTM D3703. 
     
     
         31 . The synthetically derived distillate kerosene of  claim 29 , having a flash point as measured by ASTM D93 of from 60° C. to 80° C., a kinematic viscosity at 40° C. as measured by ASTM D445 below about 1.5 cSt, a char value as measured by IP10 below 2 mg/Kg, a total sulfur content of below 0.3 ppm(m/m) as measured by ASTM 3120, an olefins content reflected by a bromine number of less than 1 mg/100 g as measured by IP 129, and a peroxide number of less than 1 mg/100 g as measured by ASTM D3703. 
     
     
         32 . The synthetically derived distillate kerosene of  claim 30 , which further comprising at least one additive selected from the group consisting of perfume and insect repellent. 
     
     
         33 . The synthetically derived distillate kerosene of  claim 31 , which further comprising at least one additive selected from the group consisting of perfume and insect repellent. 
     
     
         34 . A process for the production of kerosene, comprising the steps of:
 catalytic conversion of Fisher-Tropsch derived light olefins to distillates over a shape selective zeolite catalyst, whereby a COD product is obtained; and   hydrotreating the COD product; and   collecting a hydrotreated fraction boiling between about 170 to 250° C.   
     
     
         35 . The process of  claim 34 , wherein the hydrotreating step comprises distillate hydrotreating the COD product to produce an intermediate COD product, followed by deep hydrotreating the intermediate COD product to remove practically all aromatics. 
     
     
         36 . The process of  claim 35 , wherein a hydrotreated fraction boiling at from about 170 to 250° C. is collected during the distillate hydrotreating step before the deep hydrotreating step. 
     
     
         37 . The process of  claim 34 , wherein the hydrotreating step comprises a one step deep hydrotreating step of the COD product, and is followed by the step of collecting the hydrotreated fraction boiling between about 170 to 250° C. 
     
     
         38 . The process of  claim 37 , wherein the hydrotreating catalyst is a high nickel content catalyst. 
     
     
         39 . The process of  claim 38 , wherein the catalyst is bimetallic and comprises a noble metal. 
     
     
         40 . The process of  claim 39 , wherein the noble metal is platinum. 
     
     
         41 . The process of  claim 40 , wherein the catalyst is selected from selected from the group consisting of nickel supported on alumina and platinum supported on alumina. 
     
     
         42 . The process of  claim 34 , wherein a hydrogenation reaction pressure for the hydrotreating step is from 5000 kPa to about 8000 kPa, wherein a reaction temperatures is from 200° C. to 260° C., and wherein a liquid hourly space velocity for the hydrotreating step is from 0.3 to 2. 
     
     
         43 . The process of  claim 34 , wherein the COD product is hydrogenated over a catalyst selected from the group consisting of a nickel-molybdenum catalyst and a cobalt-molybdenum catalyst. 
     
     
         44 . The process of  claim 43 , wherein the reaction temperature is from about 240° C. to below 350° C., wherein a reaction pressure is from 5000 to 8000 kPa, wherein a hydrogen to hydrocarbon ratio is maintained at about 400 nm 3 /hr, and wherein a liquid hourly space velocity for the hydrotreating step is from 0.3 and 1. 
     
     
         45 . The process of  claim 34 , wherein a portion of the hydrotreated product is recycled to quench a hydrogenation reaction in the hydrotreating step. 
     
     
         46 . The process of  claim 34 , wherein the hydrotreatment catalyst bed comprises multiple zones with increased grades.