Abstract:
A method for obtaining a petroleum distillate product is provided, the method includes subjecting an untreated light Fischer-Tropsch liquid to a two-step hydrogenation process, each step to be carried in the presence of a catalyst comprising an amorphous substrate having a metallic composition embedded therein. After the first step of hydrogenation, an intermediate hydrotreated light Fischer-Tropsch liquid is obtained, followed by the second step of hydrogenation thereof, obtaining the petroleum distillate product as a result. An apparatus for carrying out the method is also provided.

Description:
TECHNICAL FIELD 
       [0001]    This disclosure relates generally to the processes of fabricating various petroleum-based fuels, and more specifically, to hydrogenation processes for obtaining petroleum distillate from light Fischer-Tropsch liquids. 
       BACKGROUND INFORMATION 
       [0002]    Fischer-Tropsch synthesis is known to yield a broad mixture of products including primarily paraffins, and some olefins. The individual compounds of such mixture can contain up to about 200 carbons, the number of carbons between about 20 and about 150, with average number about 60 being typical. Certain quantities of oxygenated products and trace amounts of sulfur- or nitrogen containing products or aromatic compounds can be also present. 
         [0003]    Some Fischer-Tropsch processes yield mixtures enriched with C 5 -C 30  alkanes and also containing a significant quantity of olefins and oxygenated compounds such as alcohols or acids. Such mixtures are known as “light Fischer-Tropsch liquids” or “LFTL.” Light Fischer-Tropsch liquids are frequently used as a raw material for obtaining various petrochemical products, such as, e.g., petroleum distillates, or diesel fuels, among others. 
         [0004]    To make LFTL useful and suitable as blending stock for diesel fuel, olefins and oxygenated compounds contained therein are removed, typically by the saturation of olefins and by conversion of oxygenated compounds into water via hydrogenation also known as hydrotreating, which involves the processes of hydrogenation of LFTL in the presence of hydrogen and a catalyst. 
         [0005]    Despite its many advantages, hydrotreating of LFTL is characterized by a number of drawbacks and deficiencies. For example, the process usually requires using very high pressures and temperatures. In addition, while traditional hydrotreating does allow for removal of olefins and oxygenated compounds, the final product often has a cloud point that is too high, limiting the amount of the product that can be blended into diesel fuels. 
         [0006]    To avoid or lessen the effects of the above-mentioned deficiencies, as well as for the purposes of improvement of the overall process efficiency, better processes are needed to be used with light Fischer-Tropsch liquids. 
       SUMMARY 
       [0007]    We provide methods for obtaining a petroleum distillate product. One method comprises subjecting an untreated light Fischer-Tropsch liquid to a first hydrogenation in the presence of a first catalyst to obtain a hydrotreated light Fischer-Tropsch liquid composite and subjecting the hydrotreated light Fischer-Tropsch liquid composite to a second hydrogenation in the presence of a second catalyst to obtain and recover the petroleum distillate product. 
         [0008]    The light Fischer-Tropsch liquid subject to hydrogenation may be an untreated light Fischer-Tropsch liquid having the degree of unsaturation characterized by the bromine number of about 200 or below. The light Fischer-Tropsch liquid subject to hydrogenation may be also an untreated light Fischer-Tropsch liquid containing between about 1 mass % and about 20 mass % of oxygen. 
         [0009]    The first catalyst, i.e., the catalyst used in the first step of hydrogenation process, may be a metallic composition embedded within an inorganic oxide or a zeolitic substrate, the composition comprising a base metal, e.g., a nickel-molybdenum composition or a cobalt-molybdenum composition. The metallic composition comprising the first catalyst may also include at least one noble metal, such as platinum or palladium. 
         [0010]    The second catalyst, i.e., the catalyst used in the first step of hydrogenation process, may be a metallic composition embedded within an inorganic oxide or a zeolitic substrate, the composition comprising a base metal, e.g., a nickel-molybdenum composition or a cobalt-molybdenum composition. The metallic composition comprising the second catalyst may also include at least one noble metal, such as platinum or palladium. The first and the second catalysts may be the same or different. 
         [0011]    We also provide a system for obtaining a petroleum distillate that subjects an untreated light Fischer-Tropsch liquid to a first hydrogenation and yields a hydrotreated light Fischer-Tropsch liquid composite, and a second hydrogenating unit that subjects the hydrotreated light Fischer-Tropsch liquid composite to a second hydrogenation and yields the petroleum distillate product. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0012]      FIG. 1  illustrates schematically a system for hydrogenating of light Fischer-Tropsch liquids according to one embodiment of the present invention. 
           [0013]      FIG. 2  illustrates schematically a system for hydrogenating of light Fischer-Tropsch liquids according to another embodiment of the present invention. 
       
    
    
     DETAILED DESCRIPTION 
       [0014]    The following definitions and abbreviations are used below, unless otherwise described: 
         [0015]    The term “a light Fischer-Tropsch liquid” or the abbreviation “LFTL” is defined as a mixture comprised of n-paraffins having the number of carbons between about 5 and about 50, the mixture containing a substantial portion of C 5 -C 30  alkanes and also containing olefins and oxygenated compounds. 
         [0016]    The term “a hydrocarbon” is defined as an organic compound, the molecule of which consists only of carbon and hydrogen. 
         [0017]    The terms “a paraffin” and “alkane” are used interchangeably and refer to a hydrocarbon identified by saturated carbon chains, which can be normal (straight), branched, or cyclic (“cycloparaffin”), and described by a general formula C n H 2n+2 , where n is an integer. Paraffins or alkanes are substantially free of carbon-carbon double bonds (C═C). 
         [0018]    The term “an olefin,” also known as “alkene” is defined as a hydrocarbon containing at least one carbon-carbon double bond, and described by a general formula C n H 2n , where n is an integer. 
         [0019]    The terms “hydrogenation” and “hydrotreating” are used interchangeably and refer to a process of addition of hydrogen to unsaturated organic compounds, such as olefins (alkenes), typically, in a presence of a suitable catalyst, to obtain saturated organic compounds, such as alkanes, as a result. 
         [0020]    The term “a catalyst” is defined as substance that changes the speed or yield of a chemical reaction without being itself substantially consumed or otherwise chemically changed in the process. 
         [0021]    The term “a noble metal” refers to a metal that is highly resistant to corrosion or oxidation, and does not easily dissolve, as opposed to most base metals. Examples include, but are not limited to, platinum, palladium, gold, silver, tantalum, or the like. 
         [0022]    The team “a base metal” refers to any non-precious metal that is capable of being readily oxidized. Examples include, but are not limited to, nickel, molybdenum, tungsten, cobalt, or the like. 
         [0023]    The term “a bromine index” or “bromine number” indicates the degree of aliphatic unsaturation and is defined as the amount of bromine in grams absorbed by 100 grams of a sample containing an unsaturated compound, such as an olefin. 
         [0024]    The term “a cloud point” refers to a temperature at which fuel starts congealing and starts becoming cloudy due to the appearance of wax crystals, when the fuel is tested in accordance with the American Society for Testing and Materials (ASTM) Specification D2500. The cloudiness increases as the temperature is lowered further. 
         [0025]    The term “diesel fuel” is defined in accordance with the specifications described in the ASTM Specification D975 and refers to a petroleum fraction having containing primarily C 10 -C 24  hydrocarbons and having distillation temperatures of about 160° C. at the 10% recovery point and about 340° C. at the 90% recovery point. 
         [0026]    The term “API gravity” refers to American Petroleum Institute&#39;s measure of the density of a petroleum product relative to the density of water. 
         [0027]    The abbreviation “WABT” means “weighted bed average temperature” and refers to an average temperature on the bed of catalyst. 
         [0028]    The abbreviation “LHSV” means “liquid hourly space velocity” and refers to a ratio between the hourly volume of feedstock used in the process of hydrogenation and the volume of catalyst used. 
         [0029]    The abbreviations “IBP” and “EBP” refer to the temperatures that are the initial boiling point of a product and the ending boiling point, respectively. 
         [0030]    A petroleum distillate product,may be obtained by using a two-stage process of hydrogenation. At the first stage, where most of the hydrotreating occurs, an untreated light Fischer-Tropsch liquid may be subjected to hydrogenation, which includes reacting the untreated LFTL with gaseous hydrogen, at an elevated temperature and elevated pressure, in the presence of a catalyst. During hydrogenation, the olefins that are present in the untreated LFTL react with hydrogen and become saturated by forming alkanes. If the original LFTL contained some quantity of cycloolefins, in addition cycloalkanes may be also formed. As a result, a hydrotreated light Fischer-Tropsch liquid composite is formed and water is released as a by-product. 
         [0031]    The hydrotreated light Fischer-Tropsch liquid composite obtained as described above is then further hydrogenated to complete the process. Again, the second stage of hydrogenation includes reacting the hydrotreated LFTL, at an elevated temperature and elevated pressure, in the presence of a catalyst. Upon the completion of the process of hydrogenation, the final petroleum distillate product may be recovered. The final product is a diesel range material that may be substantially devoid of olefins and oxygenated products and may be suitable for blending with diesel fuels. 
         [0032]    Both stages of hydrogenation may be carried out in a hydrotreating unit, or in two separate hydrogenating units, as desired. The temperature at which hydrogenation is carried out may be between about 200° C. and about 370° C., such as about 315° C. The pressure at which hydrogenation is carried out may be between about 1 MPa and about 15 MPa, for example, about 4 MPa. A desired rate of supply of hydrogen gas can be selected. For example, hydrogen gas can be supplied at a rate between about 170 and about 840 m 3  per 1 m 3  of the untreated LFTL at the first stage of hydrogenation or per 1 m 3  of the hydrotreated LFTL at the second stage. 
         [0033]    Each stage of hydrogenation can be carried out under the same conditions, such as temperature, pressure, and the rate of hydrogen supply, or under the different conditions so long as the temperature and pressure are within the respective ranges disclosed above. 
         [0034]    The process of hydrogenation can be described by the exemplary reaction schemes (1) (for straight-chained olefins such as methylbutene) and (2) (for cycloolefins such as cyclopentene): 
         [0000]    
       
                 
         
             
             
         
       
     
         [0035]    As can be seen from the reaction schemes (1) and (2), the process of hydrogenation is carried out in the presence of a catalyst. An appropriate catalyst can be selected from a variety of available options known in the art. For example, the catalyst that can be used is a base metal composition, such as a nickel-molybdenum composition, a cobalt-molybdenum composition, or the like. Alternatively, or a noble metal composition comprising, for example, platinum, palladium, or the like can be employed. The same catalyst or different catalysts can be utilized at the first and second stages of hydrogenation as discussed above. 
         [0036]    Any LFTL can be used as feedstock as the starting product in the hydrogenation processes described above, including a variety of commercially available light Fischer-Tropsch liquids. The starting untreated LFTL may have distillation temperatures of about 90° C. at the 10% recovery point and about 370° C. at the 90% recovery point. 
         [0037]    An acceptable LFTL that can be used may include a substantial quantity of paraffins, which may include one or more straight-chained paraffin(s) and may in addition include at least one branched paraffin. Such straight-chained and branched paraffin(s) are the principal components of the untreated starting LFTL. In addition to straight-chained paraffin and branched paraffin(s) the paraffin composition can further comprise at least some quantity of cycloparaffin(s). 
         [0038]    Furthermore, the starting LFTL may have the contents of olefins that is characterized by the bromine number greater than about 10. In addition, the starting LFTL may include a quantity of oxygenated products that is characterized by the total oxygen contents between about 1 mass % and about 20 mass %. Not more than just trace amounts of any aromatic compounds, including alkyl aromatic compounds and polyalkyl aromatic compounds, may be present in the original LFTL. 
         [0039]    The final product of the entire process of hydrogenation can be for blended with diesel fuels and with jet oil, may have the cetane number of at least about 50, and may have a cloud point of about 5° C. or less. 
         [0040]    Various systems and apparatuses can be used for conducting our processes. One embodiment of such a system that can be used is shown by  FIG. 1  and can be described as follows.  FIG. 1  illustrates the system  100  comprising three hydrotreament reactors  4 ,  11 , and  19 . All three reactors may be the same or different. In the exemplary system  100  shown by  FIG. 1 , the reactors  4  and  11  may use a nickel/molybdenum catalysts such as KF-647 or KF-846, and the reactor  19  may utilize a platinum/palladium catalyst. The catalysts are described in more detail in the “Examples” portion of the application, below. 
         [0041]    The LFTL feed  1  can be mixed with the hydrogen gas  2  that can be supplied at a rate between about 170 and about 840 m 3  per 1 m 3  of the LFTL. The LFTL/H 2  mixture can be then pre-heated to the desired temperature (e.g., 200° C. and about 370° C., such as about 315° C.) and can be then directed to the first hydrotreatment reactor  4 . The process of hydrogenation then occurs inside the reactor  4  and includes the reaction of the LFTL with hydrogen gas on a bed, such as a fixed bed, of a catalyst (not shown). As hydrogen is consumed during this process, hydrogen may be replenished from a make-up source of hydrogen  3 , and hydrogen provided from this source may contain some amount of H 2 S. The process may be carried out at a pressure between about 1 MPa and about 15 MPa, for example, about 4 MPa. The required pressure can be generated and maintained using the compressor  7 . 
         [0042]    The exothermic reactions occurring in reactor  4  may lead to a temperature increase. In order to control the temperature in the reactor the reacting fluid may be cooled (quenched). Such quenching can be achieved by supplying cool hydrogen via the by-pass line  5 . Upon completion of this stage of hydrogenation, the partially hydrogenated product then may exit the reactor  4  and be directed into the separator  6 , where water is separated as the stream  13 . The product may exit the separator  6  via the line  8 , and may then be directed to the second hydrotreatment reactor  11 , using the pump  9 . 
         [0043]    In the second reactor  11 , the process of hydrogenation may be continued using additional hydrogen that may be supplied via the line  10 . The conditions for the second stage hydrogenation may be the same as those used for the hydrogenation in the reactor  4 , as described above. 
         [0044]    The hydrogenated product then may exit the reactor  11  and be directed into the separator  12 , where water is separated as the stream  13 , and the product may exit the separator  12  via the line  14 , and may then be directed to the stripper  15 , where the H 2 S gas is removed as the stream  16 , and the product may exit the stripper  15  via the line  17 , and may then be directed to the third hydrotreatment reactor  19 , using the pump  18 . 
         [0045]    The final stage of the process of hydrogenation then occurs inside the reactor  19  and includes the reaction of the partially treated LFTL with hydrogen gas on a bed, such as a fixed bed, of a catalyst (not shown). As hydrogen is consumed during this process, hydrogen may be replenished from a make up source of hydrogen  20 , where hydrogen may be typically free of H 2 S. The process may be carried out at a pressure between about 1 MPa and about 15 MPa, for example, about 4 MPa. The required pressure can be generated and maintained using the compressor  23 . 
         [0046]    The exothermic reactions occurring in reactor  19  may lead to a temperature increase. In order to control the temperature in the reactor the reacting fluid may be cooled (quenched). Such quenching can be achieved by supplying cool hydrogen via line  21 . Upon completion of this stage of hydrogenation, the partially hydrogenated product then may exit the reactor  19  via the line  22 , then may be directed to the separator  24 . After the process of separation, the final product can exit the system  100  as the stream  25  and then may be directed to fractionation. 
         [0047]    Another embodiment of a system that can be used is shown by  FIG. 2  illustrating the system  200  comprising two hydrotreament reactors  29  and  40 . These reactors may be the same or different. In the exemplary system  200  shown by  FIG. 2 , the reactor  29  may use a nickel/molybdenum catalysts such as KF-647 or KF-846, and the reactor  40  may utilize a platinum/palladium catalyst. 
         [0048]    The LFTL feed  26  can be mixed with the hydrogen gas  27  that can be supplied at a rate between about 170 and about 840 m 3  per 1 m 3  of the LFTL. The LFTL/H 2  mixture can be then pre-heated to the desired temperature (e.g., 200° C. and about 370° C., such as about 315° C.) and can be then directed to the first hydrotreatment reactor  29 . 
         [0049]    The process of hydrogenation then occurs inside the reactor  29  and includes the reaction of the LFTL with hydrogen gas on a bed of a catalyst (not shown). Hydrogen may be replenished from a make-up source of hydrogen  28 , and hydrogen supplied from this source may contain some amount of H 2 S. The process may be carried out at a pressure between about 1 MPa and about 15 MPa, for example, about 4 MPa. The required pressure can be generated and maintained using the compressor  33 . 
         [0050]    The exothermic reactions occurring in reactor  29  may lead to a temperature increase. In order to control the temperature in the reactor the reacting fluid may be cooled (quenched), which can be achieved by supplying cool hydrogen via line  30 . The partially hydrogenated product then may exit the reactor  29  and be directed via the line  31  into the separator  32 , where water is separated as the stream  37 . The product may exit the separator  32  via the line  34 , and may then be directed to stripper  35 , where the H 2 S gas is removed as the stream  36 . The product may then exit the stripper  35  via the line  38 , and may then be directed to the second hydrotreatment reactor  40 , using the pump  39 . 
         [0051]    A later stage of the process of hydrogenation then occurs inside the reactor  40  and includes the reaction of the partially treated LFTL with hydrogen gas on a bed of a catalyst (not shown). As hydrogen is consumed during this process, hydrogen may be replenished from a make up source of hydrogen  41 , where hydrogen may be typically free of H 2 S. The process may be carried out at a pressure between about 1 MPa and about 15 MPa, for example, about 4 MPa. The required pressure can be generated and maintained using the compressor  42 . 
         [0052]    The exothermic reactions occurring in reactor  40  may lead to a temperature increase. In order to control the temperature in the reactor the reacting fluid may be cooled (quenched) by supplying cool hydrogen via the by-pass line  44 . Upon completion of this stage of hydrogenation, the partially hydrogenated product then may exit the reactor  40  via the line  43 , then may be directed to the separator  45 . After the process of separation, the final product can exit the system  200  as the stream  46  and then may be directed to fractionation. 
       EXAMPLES 
       [0053]    The following examples are provided to further illustrate the advantages and features of our processes and systems, but are not intended to limit the scope of this disclosure. 
       Example 1  
     Starting Material 
       [0054]    The starting material that was used as a feed in hydrogenation was a commercially available light Fischer-Tropsch liquid and had the properties and characteristics shown in Table 1. In Table 1, the data for distillation temperatures show the boiling temperature at the beginning and the end of the recovery (by mass %) range. For example, the entry “10/20” in the property column and “100/142” in the value column signifies the boiling temperature of about 100° C. at the 10% mass recovery point and about 142° C. at the 20% mass recovery point. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
             
               
             
               
               
               
             
               
             
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Properties of Starting Untreated LFTL 
               
             
          
           
               
                   
                 Property 
                 Value 
               
               
                   
                   
               
             
          
           
               
                   
                 Specific gravity, g/cm 3   
                 0.7884 
               
               
                   
                 API Gravity 
                 47.98 
               
               
                   
                 Sulfur Contents, ppm* ) , mass 
                 Less than 1 
               
               
                   
                 Nitrogen Contents, ppm* ) , mass 
                 10 
               
               
                   
                 Oxygen Contents, mass % 
                 5.9 
               
               
                   
                 Bromine Index 
                 56 
               
               
                   
                 Acid Number 
                 25.9 
               
             
          
           
               
                 Distillation Temperature** ) , ° C. 
               
             
          
           
               
                   
                 IBP/5 
                 21/86 
               
               
                   
                 10/20 
                 100/142 
               
               
                   
                 30/40 
                 167/190 
               
               
                   
                 50/60 
                 418/454 
               
               
                   
                 70/80 
                 266/296 
               
               
                   
                 90/95 
                 336/373 
               
               
                   
                 EBP 
                 469 
               
             
          
           
               
                 Contents of Aromatic Compounds, mass % 
               
             
          
           
               
                   
                 One Ring 
                 0.8 
               
               
                   
                 Two Rings 
                 0.2 
               
               
                   
                 Three or More Rings 
                 1.5 
               
               
                   
                   
               
               
                   
                 * ) parts per million 
               
               
                   
                 ** ) determined in accordance with ASTM Specification D2887 
               
               
                   
                 *** ) determined in accordance with Institute of Petroleum Test IP-391 
               
             
          
         
       
     
       Example 2  
     Hydrogenation of the Starting LFTL 
       [0055]    The starting untreated LFTL described in Example 1 was subjected to hydrogenation. The process was carried out in a two reactor (R- 1  and R- 2 ) configuration, with the removal of water between reactors. Nickel/molybdenum catalysts KF-647 and KF-846 were used in reactors R- 1  and R- 2 , respectively. The catalysts were obtained from Albemarle Corp. of Baton Rouge, La. 
         [0056]    The process yielded hydrotreated LFTL composite. The conditions of the process of hydrogenation are shown in Table 2, and the properties of the product are shown in Table 3. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
             
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 Operating Conditions Used for Hydrogenating LFTL 
               
             
          
           
               
                 Operating Condition 
                 Reactor 1 (R-1) 
                 Reactor 2 (R-2) 
               
               
                   
               
             
          
           
               
                 Pressure, MPa 
                 4.14 
                 4.14 
               
               
                 WABT* ) , ° C. 
                 316 
                 316 
               
               
                 LHSV** ) , hr −1   
                 2.5 
                 1.67 
               
             
          
           
               
                 Overall LHSV** ) , hr −1   
                 1.00 
               
               
                 Recycle Gas to Reactor 1, m 3  per 
                 337 
               
               
                 1 m 3  of LFTL 
               
               
                   
               
               
                 * ) weighted bed average temperature 
               
               
                 ** ) liquid hourly space velocity 
               
             
          
         
       
     
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                 TABLE 3 
               
             
             
               
                   
               
               
                 Properties of Hydrotreated LFTL Composite 
               
             
          
           
               
                   
                 Property 
                 Value 
               
               
                   
                   
               
             
          
           
               
                   
                 Specific Gravity, g/cm 3   
                 0.7387 
               
               
                   
                 API Gravity 
                 60.04 
               
               
                   
                 Hydrogen Contents, mass % 
                 15.39 
               
               
                   
                 Bromine Index 
                 Less than 10 
               
               
                   
                 Oxygen Contents, mass % 
                 Less than 0.02 
               
               
                   
                 Acid Number 
                 0.005 
               
             
          
           
               
                 Distillation Temperature* ) , ° C. 
               
             
          
           
               
                   
                 IBP/5 
                 −9/66 
               
               
                   
                 10/20 
                  88/126 
               
               
                   
                 30/40 
                 152/175 
               
               
                   
                 50/60 
                 197/218 
               
               
                   
                 70/80 
                 255/287 
               
               
                   
                 90/95 
                 331/369 
               
               
                   
                 EBP 
                 510 
               
             
          
           
               
                 Distillation Temperature** ) , ° C. 
               
             
          
           
               
                   
                 IBP/5 
                 48/85 
               
               
                   
                 10/20 
                 103/128 
               
               
                   
                 30/40 
                 148/167 
               
               
                   
                 50/60 
                 189/214 
               
               
                   
                 70/80 
                 239/Solidified 
               
               
                   
                 90/95 
                 N/A (Solidified) 
               
               
                   
                 EBP 
                 N/A (Solidified) 
               
               
                   
                   
               
               
                   
                 * ) determined in accordance with ASTM Specification D2887 
               
               
                   
                 ** ) determined in accordance with ASTM Specification D86, fractions are in volume % 
               
             
          
         
       
     
         [0057]    The product obtained as described above and having properties shown in table 3 was then fractionated into two fractions to separate naphtha from diesel fuel. The first fraction (i.e., the naphtha fraction) had the IBP of about 149° C., and the second fraction (i.e., the diesel fraction) had the IBP above 149° C. The properties of the diesel fraction are provided in Table 4. 
         [0000]    
       
         
               
             
               
               
               
             
               
             
               
               
               
             
           
               
                 TABLE 4 
               
             
             
               
                   
               
               
                 Properties of the Diesel Fraction (IBP &gt;149° C.) 
               
             
          
           
               
                   
                 Property 
                 Value 
               
               
                   
                   
               
               
                   
                 API Gravity 
                 53.9 
               
               
                   
                 Cloud Point, ° C. 
                 12.2 
               
               
                   
                 Flash Point, ° C. 
                 57.2 
               
             
          
           
               
                 Distillation Temperature* ) , ° C. 
               
             
          
           
               
                   
                 IBP/5 
                 168/181 
               
               
                   
                 10/20 
                 184/192 
               
               
                   
                 30/40 
                 203/216 
               
               
                   
                 50/60 
                 232/249 
               
               
                   
                 70/80 
                 268/293 
               
               
                   
                 90/95 
                 N/A//N/A (Solidified) 
               
               
                   
                 EBP 
                 N/A (Solidified) 
               
               
                   
                   
               
               
                   
                 * ) determined in accordance with ASTM Specification D86, fractions are in volume % 
               
             
          
         
       
     
         [0058]    As can be seen from Tables 3 and 4, in the process described above, it was not possible to complete the distillation according to ASTM Specification D86, and the diesel fraction had the cloud point which was quite high (about 12° C.), thus limiting the amount of the hydrotreated LFTL that can be used for blending into a diesel fuel. The following example demonstrates improvement of the process illustrated in Example 2. 
       Example 3  
     Further Processing of the Hydrotreated LFTL Composite 
       [0059]    The product described in Table 3, obtained as discussed in Example 2 above (prior to fractionating the hydrotreated LFTL composite into the naphtha and diesel fractions), was further processed by additional hydrogenation, as follows. 
         [0060]    The hydrotreated LFTL composite described in Table 3 was hydrogenated over a catalyst comprising about 0.45 mass % of platinum and about 0.45 mass % of palladium embedded on a support comprising a zeolite. The processing conditions for the process of hydrogenation are described in Table 5. 
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                 TABLE 5 
               
             
             
               
                   
               
               
                 Conditions for Processing the Hydrotreated LFTL Composite 
               
               
                 by Hydrogenation over a Platinum/Palladium Catalyst 
               
             
          
           
               
                   
                 Operating Condition 
                 Value 
               
               
                   
                   
               
             
          
           
               
                   
                 Pressure, MPa 
                 6.9 
               
               
                   
                 LHSV, hr −1   
                 1.0 
               
               
                   
                 Hydrogen Flow, m 3  per 1 m 3  of LFTL 
                 1,011 
               
               
                   
                 Temperature, ° C.* )   
                 265.6 
               
               
                   
                   
                 291.7 
               
               
                   
                   
               
               
                   
                 * ) two separate experiments 
               
             
          
         
       
     
         [0061]    As can be seen from Table 5, the process of hydrotreating was carried out at two different temperatures. Using the lower temperature, i.e., 265.6° C., may be suitable for improving the quality of the diesel fraction, while using the higher temperature, i.e., 291.7° C., may be beneficial if the product is to be used in the manufacturing of jet fuel with enhanced properties. 
         [0062]    The product obtained under conditions shown in Table 5 was then fractionated and the light and the heavy naphtha fractions were removed by distillation. The properties of the remaining fraction are provided in Tables 6 and 7. Table 6 shows the properties of the diesel fraction that remained, as obtained after the hydrogenation carried out at the lower hydrogenation temperature of about 265.6° C. 
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                 TABLE 6 
               
             
             
               
                   
               
               
                 Properties of the Diesel Fraction After Processing the Hydrotreated LFTL Composite 
               
               
                 by Hydrogenation over a Platinum/Palladium Catalyst at 265.6° C. 
               
             
          
           
               
                 Stream 
                 Liquid Product 
                 IBP/85° C. 
                 85° C./143° C. 
                 143° C./EBP 
               
               
                   
               
             
          
           
               
                 Yield, g 
                 9,357 
                 779 
                 1,865 
                 6,642 
               
               
                 Yield, mass % 
                 N/A 
                 8.4 
                 20.1 
                 71.5 
               
               
                 API Gravity 
                 59.8 
                 84.5 
                 69.6 
                 54.6 
               
               
                 Specific Gravity, g/cm 3   
                 0.7397 
                 0.6550 
                 0.7036 
                 0.7602 
               
               
                 Hydrogen Contents, mass % 
                 N/A 
                 N/A 
                 15.78 
                 15.33 
               
               
                 Flash Point, ° C. 
                 N/A 
                 N/A 
                 2.8 
                 53.9 
               
               
                 Cloud Point, ° C. 
                 N/A 
                 N/A 
                 N/A 
                 3.9 
               
               
                 Pour Point, ° C. 
                 N/A 
                 N/A 
                 N/A 
                 −6.1 
               
               
                 Viscosity at −20° C., cSt 
                 N/A 
                 N/A 
                 1.185 
                 N/A 
               
               
                 Iron Contents, mass % 
                 N/A 
                 N/A 
                 &lt;0.00002 
                 &lt;0.00002 
               
               
                 Reid Vapor Pressure, Pa 
                 N/A 
                 N/A 
                 9,928.5 
                 896.3 
               
               
                 Micro Research Octane 
                 N/A 
                 N/A 
                 &lt;40 
                 N/A 
               
               
                 Number 
               
               
                 Micro Motor Octane 
                 N/A 
                 N/A 
                 &lt;40 
                 N/A 
               
               
                 Number 
               
               
                 Cetane Number 
                 N/A 
                 N/A 
                 N/A 
                 73.7 
               
             
          
           
               
                 Distillation Temperatures* ) , ° C. 
               
             
          
           
               
                 IBP 
                 −1.1 
                 −9.4 
                 63.9 
                 139.4 
               
               
                  5 
                 66.7 
                 17.8 
                 87.2 
                 149.4 
               
               
                 10 
                 96.7 
                 30.0 
                 96.7 
                 150.0 
               
               
                 20 
                 126.1 
                 33.3 
                 98.3 
                 173.9 
               
               
                 30 
                 151.1 
                 35.6 
                 99.4 
                 195.0 
               
               
                 40 
                 173.9 
                 56.7 
                 105.6 
                 207.2 
               
               
                 50 
                 196.1 
                 67.2 
                 118.9 
                 223.3 
               
               
                 60 
                 216.7 
                 69.4 
                 126.7 
                 243.9 
               
               
                 70 
                 246.7 
                 70.0 
                 127.8 
                 270.0 
               
               
                 80 
                 273.9 
                 70.6 
                 128.9 
                 288.3 
               
               
                 90 
                 316.1 
                 70.6 
                 129.4 
                 329.4 
               
               
                 95 
                 356.1 
                 87.2 
                 141.1 
                 366.7 
               
               
                 EBP 
                 500.6 
                 97.2 
                 149.4 
                 475.6 
               
             
          
           
               
                 Distillation Temperatures** ) , ° C. 
               
             
          
           
               
                 IBP 
                 N/A 
                 N/A 
                 103.9 
                 166.7 
               
               
                  5 
                 N/A 
                 N/A 
                 107.2 
                 178.3 
               
               
                 10 
                 N/A 
                 N/A 
                 108.3 
                 178.3 
               
               
                 20 
                 N/A 
                 N/A 
                 109.4 
                 186.7 
               
               
                 30 
                 N/A 
                 N/A 
                 111.1 
                 196.1 
               
               
                 40 
                 N/A 
                 N/A 
                 112.8 
                 208.3 
               
               
                 50 
                 N/A 
                 N/A 
                 115.0 
                 222.2 
               
               
                 60 
                 N/A 
                 N/A 
                 117.2 
                 238.3 
               
               
                 70 
                 N/A 
                 N/A 
                 120.0 
                 257.2 
               
               
                 80 
                 N/A 
                 N/A 
                 123.3 
                 279.4 
               
               
                 90 
                 N/A 
                 N/A 
                 127.2 
                 315.6 
               
               
                 95 
                 N/A 
                 N/A 
                 130.6 
                 N/A 
               
               
                 EBP 
                 N/A 
                 N/A 
                 143.9 
                 354.4 
               
               
                 Recovery, mass % 
                 N/A 
                 N/A 
                 98.7 
                 93.9 
               
               
                   
               
               
                 * ) simulated, determined in accordance with ASTM Specification D2887 
               
               
                 ** ) Engler distillation, determined in accordance with ASTM Specification D86 
               
             
          
         
       
     
         [0063]    As can be seen from the data presented in Table 6, the cloud point has been substantially improved compared with that of the diesel fraction recovered from the hydrotreated LFTL composite (see Table 4 for comparison of the respective cloud points), and the cetane number is quite high. Thus, the diesel fraction characterized in Table 6 may be used for blending with various diesel fuels. It may be also noticed that the difficulties previously experienced with the ASTM D86 distillation were eliminated. 
         [0064]    Table 7 shows the properties of the kerosene/jet fuel fraction that remained, as obtained after the hydrogenation carried out at the higher hydrogenation temperature of about 291.7° C., and demonstrates that the product can be used as a high quality jet fuel blending component. 
         [0000]    
       
         
               
             
               
               
               
               
               
             
               
               
               
               
               
             
               
             
               
               
               
               
               
             
               
             
               
               
               
               
               
             
           
               
                 TABLE 7 
               
             
             
               
                   
               
               
                 Properties of the Kerosene/Jet Fuel Fraction After Processing the Hydrotreated LFTL 
               
               
                 Composite by Hydrogenation over a Platinum/Palladium Catalyst at 291.7° C. 
               
             
          
           
               
                 Stream 
                 Liquid Product 
                 IBP/85° C. 
                 85° C./135° C. 
                 135° C./EBP 
               
               
                   
               
             
          
           
               
                 Yield, g 
                 4,995 
                 649 
                 1,307 
                 2,965 
               
               
                 Yield, mass % 
                 N/A 
                 13.2 
                 26.6 
                 60.3 
               
               
                 API Gravity 
                 65.1 
                 85.2 
                 70.0 
                 58.3 
               
               
                 Specific Gravity, g/cm 3   
                 0.7197 
                 0.6530 
                 0.7022 
                 0.7456 
               
               
                 Hydrogen Contents, mass % 
                 N/A 
                 N/A 
                 15.78 
                 15.44 
               
               
                 Total Sulfur Contents, mass ppm 
                 N/A 
                 N/A 
                 &lt;0.05 
                 0.07 
               
               
                 Flash Point, ° C. 
                 N/A 
                 N/A 
                 1.0 
                 43.0 
               
               
                 Cloud Point, ° C. 
                 N/A 
                 N/A 
                 N/A 
                 −35.0 
               
               
                 Pour Point, ° C. 
                 N/A 
                 N/A 
                 N/A 
                 −57.0 
               
               
                 Smoke Point, mm 
                 N/A 
                 N/A 
                 N/A 
                 39 
               
               
                 Freeze Point, ° C. 
                 N/A 
                 N/A 
                 N/A 
                 −56.6 
               
               
                 Viscosity at −20° C., cSt 
                 N/A 
                 N/A 
                 1.137 
                 3.250 
               
               
                 Iron Contents, mass % 
                 N/A 
                 N/A 
                 &lt;0.00002 
                 &lt;0.00002 
               
               
                 Reid Vapor Pressure, Pa 
                 N/A 
                 N/A 
                 10,824.8 
                 1,930.5 
               
               
                 Micro RON 
                 N/A 
                 N/A 
                 &lt;40 
                 N/A 
               
               
                 Micro MON 
                 N/A 
                 N/A 
                 &lt;40 
                 N/A 
               
             
          
           
               
                 Distillation Temperatures* ) , ° C. 
               
             
          
           
               
                 IBP 
                 −22.2 
                 −12.2 
                 63.3 
                 123.3 
               
               
                  5 
                 33.9 
                 16.7 
                 85.0 
                 140.6 
               
               
                 10 
                 72.8 
                 18.3 
                 87.2 
                 142.3 
               
               
                 20 
                 97.8 
                 32.2 
                 97.2 
                 151.1 
               
               
                 30 
                 117.8 
                 34.4 
                 98.9 
                 165.0 
               
               
                 40 
                 131.7 
                 52.8 
                 100.0 
                 174.4 
               
               
                 50 
                 151.7 
                 57.2 
                 115.0 
                 186.7 
               
               
                 60 
                 167.8 
                 66.1 
                 117.8 
                 196.7 
               
               
                 70 
                 187.2 
                 68.3 
                 125.6 
                 208.3 
               
               
                 80 
                 205.0 
                 69.4 
                 127.2 
                 221.1 
               
               
                 90 
                 227.8 
                 70.0 
                 128.3 
                 238.9 
               
               
                 95 
                 245.0 
                 83.9 
                 131.1 
                 253.9 
               
               
                 EBP 
                 286.7 
                 95.6 
                 148.9 
                 286.1 
               
             
          
           
               
                 Distillation Temperatures** ) , ° C. 
               
             
          
           
               
                 IBP 
                 N/A 
                 N/A 
                 101.1 
                 156.1 
               
               
                  5 
                 N/A 
                 N/A 
                 103.9 
                 164.4 
               
               
                 10 
                 N/A 
                 N/A 
                 105.0 
                 163.9 
               
               
                 20 
                 N/A 
                 N/A 
                 106.7 
                 168.3 
               
               
                 30 
                 N/A 
                 N/A 
                 107.8 
                 172.2 
               
               
                 40 
                 N/A 
                 N/A 
                 109.4 
                 177.2 
               
               
                 50 
                 N/A 
                 N/A 
                 111.1 
                 184.4 
               
               
                 60 
                 N/A 
                 N/A 
                 113.3 
                 191.7 
               
               
                 70 
                 N/A 
                 N/A 
                 116.1 
                 201.1 
               
               
                 80 
                 N/A 
                 N/A 
                 119.4 
                 212.2 
               
               
                 90 
                 N/A 
                 N/A 
                 123.9 
                 229.4 
               
               
                 95 
                 N/A 
                 N/A 
                 128.3 
                 247.2 
               
               
                 EBP 
                 N/A 
                 N/A 
                 141.1 
                 248.3 
               
               
                 Recovery, mass % 
                 N/A 
                 N/A 
                 97.0 
                 95.8 
               
               
                   
               
               
                 * ) simulated, determined in accordance with ASTM Specification D2887 
               
               
                 ** ) Engler distillation, determined in accordance with ASTM Specification D86 
               
             
          
         
       
     
         [0065]    Although our methods and systems have been described with reference to the above-discussed reactions and structures, it will be understood that modifications and variations are encompassed within the spirit and scope of the disclosure as defined in the appended claims.