Abstract:
A process for producing alkyl aromatic middle distillate fuels is described. The process includes (a) catalytically converting paraffinic naphtha to a composition containing benzene and olefins; (b) processing the olefin/benzene composition in an aromatic alkylation reactor to produce alkyl-benzene components (c) separating the alkyl aromatics from the unconverted naphtha; and (d) optionally recycling the unconverted paraffinic naphtha to the dehydrogenation/amortization reactor of step a.

Description:
CROSS REFERENCE TO RELATED APPLICATIONS  
       [0001]     This Application claims priority to U.S. Provisional Application No. 60/828,373, filed on Oct. 5, 2006. 
     
    
     FEDERALLY SPONSORED RESEARCH  
       [0002]     Not applicable.  
       REFERENCE TO MICROFICHE APPENDIX  
       [0003]     Not applicable.  
       FIELD OF INVENTION  
       [0004]     The invention relates to a process for the production of middle distillates from synthetic naphtha.  
       BACKGROUND OF THE INVENTION  
       [0005]     Iso-paraffinic synthetic fuels (or “synfuels” for short) generally lack one or more desirable fuel attributes. For gasoline, this includes low octane values. In the case of jet fuel, these include lower density and lack of seal-swelling properties. Lack of seal-swelling properties means that a fuel tank equipped with nitrile rubber closure gasket used for conventional petroleum fuels (“petro-fuels”) will leak if filled with an iso-paraffinic synfuel. These differences with petro-fuels can limit use of iso-paraffinic synfuels. One solution has been to blend these synfuels with petro-fuels. However, blending with petro-fuels generally downgrades the synfuel&#39;s low emission qualities. Particulate emissions are attributed to naphthalene-type molecules in crude oil.  
         [0006]     Since aromatic hydrocarbons have higher density and can impart seal swelling properties, alkyl benzenes of jet fuel boiling range may be used as blend stocks for corresponding iso-paraffinic synfuels to solve the seal-swell and density issues without affecting their desirable low particulate emission qualities. In the case of gasoline, the alkyl-benzenes are known to increase synfuel octane value.  
         [0007]     Synthesis of alkyl aromatics via olefins and benzene has industrially important applications, such as manufacture of cumene and detergent-range linear alkyl benzenes. Alkyl benzenes having alkyl groups with from about 4 to about 9 carbon atoms may also be used as chemical intermediates or as fuel blend stocks.  
         [0008]     Traditional processes for manufacturing alkyl aromatic components employ different catalysts and reactors for the benzene and olefin components used to make the alkyl benzene products. For example catalytic reforming may be used to convert paraffinic feedstock to benzene by dehydrocyclization. Olefin production is typically achieved by dehydrogenation of the paraffins. Thus, the combination of two processes to make these components is capital-intensive.  
         [0009]     Consequently, a simpler process for the preparation of alkyl benzenes and synthetic fuels would be useful.  
       SUMMARY OF THE INVENTION  
       [0010]     A process for producing one or more middle distillate fuels is described. An embodiment of the described process includes (a) dehydrogenating/aromatizing a paraffinic naphtha stream into a composition containing olefins and aromatic hydrocarbons (b) subjecting the olefins and aromatic components to aromatic alkylation, and (c) separating the alkyl aromatics of middle distillate range.  
         [0011]     In some embodiments the synthetic naphtha is a product of the Fischer-Tropsch process. Selected Fischer-Tropsch processes employ synthesis gas derived from coal, petroleum coke, natural gas, petroleum residue and biomass. In other embodiments, the synthetic naphtha may be the co-product of hydroprocessing glycerides (mono-, di-, and tri-), and fatty acids present in vegetable oils, animal fats, and restaurant greases.  
         [0012]     Embodiments of the invention also include products produced by one or more of the methods described herein, particularly wherein the products include chemical intermediates, gasoline, kerosene, jet fuel and diesel fuel. Products further comprising petroleum- or bio-based fuels in any desirable amount are also contemplated.  
     
    
     BRIEF DESCRIPTION OF THE DRAWING  
       [0013]      FIG. 1  depicts a process for selectively converting paraffinic components according to one embodiment of the invention. 
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0014]     The terms “middle distillate product(s)” and “middle distillate” refer to hydrocarbon mixtures with a boiling point range that corresponds substantially with that of kerosene and gas oil fractions obtained in a conventional atmospheric distillation of crude oil material. The middle distillate boiling point range may include temperatures between about 150° C. and about 600° C., with a fraction boiling point between about 200° C. and about 360° C.  
         [0015]     The term “middle distillate fuel” means jet fuel, kerosene, diesel fuel, gasoline, and combinations thereof.  
         [0016]     The term “BTX” means Benzene, Toluene, Xylene, or a mixture of any of Benzene, Toluene, and Xylene.  
         [0017]     The term “C x ”, where x is a number greater than zero, refers to a hydrocarbon compound having predominantly a carbon number of x. As used herein, the term C x  may be modified by reference to a particular species of hydrocarbons, such as, for example, C 5  olefins. In such instance, the term means an olefin stream comprised predominantly of pentenes but which may have impurity amounts, i.e. less than about 10%, of olefins having other carbon numbers such as hexene, heptene, propene, or butene.  
         [0018]     The term “light fraction” generally indicates a hydrocarbon comprised primarily of C 2  to C 24  hydrocarbons; preferably C 2 -C 9  in some cases.  
         [0019]     The term “light fraction” generally indicates a hydrocarbon comprised primarily of hydrocarbons having a carbon number greater than about C 24 , but in some cases the heavy fraction contains C 1 + fractions.  
         [0020]     Naphtha fractions described herein generally have a boiling range of 30 to 250 degrees F. and contains alkanes in the C 5  to C 9  range.  
         [0021]     LPG fractions generally refer to hydrocarbons having from 2 to 5 carbon atoms, but in most cases  3  and  4 .  
         [0022]     It has surprisingly been found that using certain noble metal catalyst systems naphtha range paraffins that do not cyclize to an aromatic will dehydrogenate to form olefins which will react in the alkylation step to form alkylated aromatics in the middle distillate boiling range. In particular, commercially available tin/platinum-on-alumina catalysts convert n-hexane to benzene and convert C 7  paraffins to linear internal olefins with high selectivity. Thus, the conversion of naptha-range n-paraffin feed to a composition suitable for aromatic alkylation.  
         [0023]     One such process is schematically represented in  FIG. 1 . In  FIG. 1 , an n-paraffin naphtha feed  201  is provided to a dehydrogenation unit  202  equipped with a tin/platinum-on-alumina catalyst. The product of the dehydrogenation unit  202  is fed to aromatic alkylation unit  203 . Homogeneous Lewis acid catalysts such as aluminum trichloride or boron trifluoride, and heterogeneous zeolite catalysts, may be employed to carryout the aromatic alkylation reaction. Alkylated-benzenes and unconverted C 6 -C 9  products are provided to a separator  204  configured to separate C 10 + products from lower carbon products, including the unconverted C 6 -C 9  fraction. Conventional distillation is well suited for this application. The separated unconverted fraction may be recycled to the dehydrogenation unit  202 .  
         [0024]     When the paraffinic naphtha is the byproduct of a middle distillate synfuel process, this method can be employed to maximize C 10 + product yield and modify the product properties such as density and seal swell.  
       EXAMPLE 1  
       [0025]     Commercial Sn/Pt-on-alumina dehydrogenation catalyst from Englehard Corporation comprising 0.65-0.85 wt. percent Sn, 0.40-0.58 wt. percent Li, 0.30-0.45 wt. percent Pt is used. The catalyst has a particle size of 1.58-2.54 mm and a surface area of 140-180 m 2 /g according to BET-N 2  surface area measurements. Tube-in-tube glassware is used in a reactor with about 0.1 g of catalyst in the inside tube. Slits in the bottom tube allow for bottom-up feed flow. The reactor is placed in a furnace and heated to about 450° C. under a flow of hydrogen suitable for catalyst activation. After 30 minutes of activation, hydrocarbon recirculation is started. Results from n-hexane, n-heptane, and n-octane are presented in Tables I-III respectively.  
                                                                     TABLE I                       Reactor Conditions                                    Catalyst   0.1171   g           Reactor temp   450°   C.           n-C 6     10   torr           H 2     200   torr           He   790   torr                                Batch Cycle Time (min)                Products (wt. percent)   10 min   30 min   50 min                       Ethane/Ethylene   0.883   1.397   1.561           Propane/propylene   0.785   1.271   1.437           1-butene   0.28   0.398   0.252           1-hexene   1.247   0.522   1.736           n-hexane   44.448   15.307   5.9           trans-2-hexene   2.197   0.88   2.695           cis-2-hexene   1.225   0.495   2.216           Benzene   38.542   69.323   80.66                      
 
         [0026]    
       
         
               
             
               
               
               
               
             
               
               
               
             
               
               
               
               
               
             
           
               
                 TABLE II 
               
               
                   
               
               
                   
               
               
                 Reactor Conditions 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Catalyst 
                 0.1147 
                 g 
               
               
                   
                 Reactor temp 
                 450° 
                 C. 
               
               
                   
                 n-C 7   
                 10 
                 torr 
               
               
                   
                 H 2   
                 200 
                 torr 
               
               
                   
                 He 
                 790 
                 torr 
               
               
                   
                   
               
             
          
           
               
                   
                   
                 Batch Cycle Time (min) 
               
             
          
           
               
                   
                 Products (wt. percent) 
                 10 min 
                 30 min 
                 50 min 
               
               
                   
                   
               
               
                   
                 1-heptene 
                 1.2066 
                 1.215 
                 1.187 
               
               
                   
                 trans-3-heptene 
                 4.552 
                 4.523 
                 4.561 
               
               
                   
                 n-heptane 
                 83.844 
                 79.715 
                 76.456 
               
               
                   
                 trans-2-heptene 
                 4.159 
                 4.165 
                 4.123 
               
               
                   
                 cis-2-heptene 
                 2.252 
                 2.28 
                 2.26 
               
               
                   
                 Toluene 
                 0.24 
                 0.247 
                 0.257 
               
               
                   
                 Total n-heptenes 
                 12.1696 
                 12.183 
                 12.131 
               
               
                   
                   
               
             
          
         
       
     
         [0027]    
       
         
               
             
               
               
               
               
             
               
               
               
             
               
               
               
               
             
           
               
                 TABLE III 
               
               
                   
               
               
                   
               
               
                 Reactor Conditions 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Catalyst 
                 0.1192 
                 g 
               
               
                   
                 Reactor temp 
                 450° 
                 C. 
               
               
                   
                 n-C 8   
                 10 
                 torr 
               
               
                   
                 H 2   
                 200 
                 torr 
               
               
                   
                 He 
                 790 
                 torr 
               
               
                   
                   
               
             
          
           
               
                   
                   
                 Batch Cycle Time (min) 
               
             
          
           
               
                   
                 Products (wt. percent) 
                 30 min 
                 50 min 
               
               
                   
                   
               
               
                   
                 n-butane 
                 0.737 
                 1.147 
               
               
                   
                 2-methyl-1,3-butadiene 
                 0.771 
                 1.216 
               
               
                   
                 1-octene 
                 1.568 
                 1.855 
               
               
                   
                 trans-3-octene 
                 2.461 
                 2.273 
               
               
                   
                 cis-3-heptene 
                 5.127 
                 5.404 
               
               
                   
                 1,2,3 trimethylcyclopentane 
                 1.568 
                 1.653 
               
               
                   
                 n-octane 
                 71.468 
                 71.237 
               
               
                   
                 trans-2-octene 
                 3.516 
                 3.683 
               
               
                   
                 cis-2-heptene 
                 2.004 
                 2.121 
               
               
                   
                 Ethylbenzenes 
                 1.44 
                 1.814 
               
               
                   
                 Total n-octenes 
                 14.676 
                 15.336 
               
               
                   
                   
               
             
          
         
       
     
         [0028]     Variations, modifications and additions to this invention will be readily apparent to one skilled in the art and such modifications and additions would be fully within the scope of the invention, which is not limited by the claims.