Patent Publication Number: US-5895830-A

Title: Process for oligomer production and saturation

Description:
CROSS REFERENCE TO RELATED APPLICATION 
     This application is a continuation in part of application Ser. No. 08/573,314, filed Dec. 15, 1995, now abandoned, the contents of which are hereby incorporated by reference. 
    
    
     FIELD OF THE INVENTION 
     This invention relates generally to the production of gasoline boiling range hydrocarbons by the oligomerization of light olefins. 
     BACKGROUND OF THE INVENTION 
     Prior Art 
     Processes for the oligomerization of light olefins to produce C 7  and higher carbon number oligomers are well known. Oligomerization processes have been long employed to produce good quality motor fuel components from propylene and butylene. Such oligomerization processes are also referred to as catalytic condensation and polymerization with the resulting motor fuel often referred to as polymer gasoline. Methods have always been sought to improve the octane number of the gasoline boiling range oligomerization products. In addition the oligomerization process is also susceptible to catalyst fouling from the condensation of heavy oligomers into coke that covers the catalyst. 
     Another process that has met the continuing demand for the conversion of light hydrocarbons into high octane motor fuels was the alkylation of isobutane with propylene, butenes and amylenes using a hydrofluoric acid (HF) catalyst, commonly referred to as HF alkylation. The HF process has provided a highly successful method for the production of high octane motor fuels. Despite a long history of safe operation, recent concerns over the possibility of a catastrophic release of HF acid from HF alkylation units has prompted the investigation of modification or alternatives to the HF alkylation process for the production of motor fuels. One existing alternative is a similar alkylation process that uses sulfuric acid as the catalyst. While the use of sulfuric acid may decrease the degree of the hazard that some associate with the use of HF acid, the sulfuric acid process is still perceived as possibly presenting the same hazard and is not as economically advantageous as the HF alkylation process. Therefore, processing methods have been sought to improve the operation of oligomerization processes as substitutes for acid catalyzed alkylation. 
     A number of arrangements are known for using oligomerization in combination with other processes such as saturation and dehydrogenation as substitutes for acid catalyzed isomerization alkylation. Patents disclosing the dehydrogenation of light paraffin stream with oligomerization of the dehydrogenation effluent include U.S. Pat. No. 4,393,259, U.S. Pat. No. 5,049,360, U.S. Pat. No. 4,749,820, U.S. Pat. No. 4,304,948 and U.S. Pat. No. 2,526,966. 
     It also known to hydrotreat the olefinic hydrocarbon streams produced by oligomerization to saturate olefins. Patent GB 2186287 discloses dehydrogenation of and oligomerization of a C4 fraction to produce a jet aircraft fuel that is optionally hydrogenated into premium gasoline. The hydrotreatment of jet fuels, diesel fuels and lubes produced by dehydrogenation and oligomerization of light paraffins is disclosed in U.S. Pat. No. 4,678,645. However, hydrotreating is not always beneficial for gasoline fractions produced by oligomerization and can lower octane ratings, but is known to be particularly beneficial when saturating isooctenes to isooctanes. 
     Some prior art process that use highly acidic halide type catalysts for polymerization have suggested the recycle of paraffins to the polymerization zone for purposes of cooling. Such references include U.S. Pat. No. 4,200,774 and U.S. Pat. No. 4,254,294. However, heavier paraffin streams in these references are disclosed exclusively for the purposes of controlling reaction zone temperature. 
     It is an object of this invention to improve the operation of an oligomerization reaction zone by extending the catalyst life. 
     It is a further object of this invention to increase the octane number of the saturated oligomerization products. 
     It is a yet further object of this invention to reduce the impact of catalyst fouling by coke accumulation in oligomerization processes. 
     BRIEF SUMMARY OF THE INVENTION 
     It has been surprisingly found that the introduction of heavy paraffins into an oligomerization zone for the oligomerization of light olefins will have the dual benefits of reducing catalyst fouling and significantly raising the octane number of the resulting oligomers upon saturation. The process introduces a stream of heavy paraffins into the oligomerization zone. The heavy paraffins keep the surface of the catalyst flushed of heavy isomers that can condense to foul the surface of the catalyst. In addition to the inhibition of fouling the recycling of the heavy paraffins to the oligomerization zone provides improvements in the selectivity of the oligomerization zone to higher octane C 8  isomers. 
     While not wishing to be bound to any theory it is believed that the flushing action of the heavy paraffins may be responsible for the improved selectivity of the oligomerization reaction zone for higher octane C 8  isomers. The reactions that produce the highest products are those that result in the initial products. Flushing of the catalyst with the heavy paraffin stream maintains a liquid phase flow across the catalyst. The liquid phase flow may be responsible for rapidly removing the initial products from the surface of the catalyst before further reaction can take place with resulting cracking and the formation of lower potential octane products. The oligomerization reaction is highly exothermic so it is believed that the presence of the heavy liquid paraffin also moderates any temperature rise in the reaction zone at large and locally within the catalyst. 
     A number specific operational steps can separately or collectively provide the oligomerization improvements of this invention. The flushing benefits of this invention are facilitated by the use of liquid phase conditions and heavier hydrocarbons. Passing heavier hydrocarbons, such as octanes and higher, enhances the improvements of this invention to the oligomerization zone. Furthermore the invention has been proven to raise octane number of gasoline streams substantially when used in conjunction with a mild acid catalyst in the oligomerization zone. Substantial liquid phase conditions in conjunction with the heavy paraffin addition of this invention will offer substantial improvements to the catalyst life, and the catalyst life may be further improved as oligomerization zone approaches 100% liquid phase conditions. 
     Accordingly in a broad embodiment this invention is an oligomerization process for the production of oligomers having a high octane numbers after saturation and for extending the life of catalyst. The process passes an oligomerization zone feed comprising C 3  and/or C 4  olefins to an oligomerization zone and into contact with an oligomerization catalyst. A heavy saturate stream comprising paraffins having a carbon number of at least 7 or 8 passes into contact with the feed and the catalyst. The process recovers an oligomerization effluent stream comprising the paraffins and C 8  alkenes as products. Useful embodiments may use a mild acid catalyst having a Hammett acidity function of less than 6. The heavy paraffin stream may comprise C 8  and heavier paraffins. The oligomerization zone may be operated to maintain substantial liquid phase conditions. 
     In a more specific embodiment this invention is a process for the production of high octane C 8  isomers by the oligomerization of an isobutene containing feed stream. The process passes an oligomerization zone feed comprising C 4  olefins and a paraffin recycle stream comprising paraffins having at least eight carbon atoms to an oligomerization zone and into contact with an oligomerization catalyst at oligomerization conditions including a temperature of 200 to 500 F.°, a pressure of 100 to 1000 psig, and an LHSV of 0.5 to 5. An oligomerization effluent stream comprising the paraffin stream and C 8  isoolefins is recovered from the oligomerization zone. The oligomerization effluent stream passes to a separation zone and is separated into a lighter fraction comprising C 8  isoolefins and a heavier fraction comprising paraffins having at least 8 carbon atoms. At least a portion of the heavy fraction is rejected from the process and at least a portion of the heavy fraction passes to the oligomerization zone as the paraffin recycle stream. 
     Other objects, embodiments and details of this invention will be provided in the following detailed disclosure of the invention. 
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS 
     FIG. 1 is process flow diagram showing a basic schematic arrangement of this invention. 
     FIG. 2 is process flow diagram showing an alternate arrangement for the process of this invention. 
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     The essential operational zone for the practice of this invention is the oligomerization reaction zone. Suitable oligomerization zones for this invention take on many forms. The oligomerization process is known by many names such as catalytic condensation and also catalytic polymerization. Known catalysts for effecting such reactions include heterogeneous catalyst such as solid acids and homogenous catalysts, in particular halogenated catalysts such as boron trifluoride as described in U.S. Pat. Nos. 3,906,053, 3,916,019 and 3,981,941. 
     Preferred catalyst for the oligomerization can generally be described as mild protonic acids. The preferred acids will generally have a Hammett acidity function of less than -6 and preferably of about -5.0 or less. A particularly preferred catalyst is a solid phosphoric acid (SPA) catalysts which has a Hammett acidity function of -5.0. The SPA catalyst refers to a solid catalyst that contains as a principal ingredient an acid of phosphorous such as ortho-, pyro- or tetraphosphoric acid. 
     SPA catalyst is normally formed by mixing the acid of phosphorous with a siliceous solid carrier to form a wet paste. This paste may be calcined and then crushed to yield catalyst particles where the paste may be extruded or pelleted prior to calcining to produce more uniform catalyst particles. The carrier is preferably a naturally occurring porous silica-containing material such as kieselguhr, kaolin, infusorial earth, and diatomaceous earth. A minor amount of various additives such as mineral talc, fuller&#39;s earth, and iron compounds including iron oxide may be added to the carrier to increase its strength and hardness. The combination of the carrier and the additives preferably comprises about 15-30% of the catalyst, with the remainder being the phosphoric acid. The additive may comprise about 3-20% of the total carrier material. Variations from this composition such as a lower phosphoric acid consent are however possible. Further details as to the composition and production of SPA catalysts may be obtained from U.S. Pat. Nos. 3,050,472; 3,050,473, and 3,132,109 and from other references. 
     Oligomerization zones in general are maintained at conditions which may vary widely due to the previously listed variables. In this invention the oligomerization reaction zone is preferably operated at temperatures and pressures that increase the compatibility of its effluent conditions with the inlet conditions of the saturation reaction zone inlet and its inlet conditions with the dehydrogenation reaction zone effluent conditions. The preferred temperature of the oligomerization reaction zone will typically be in a range of from 100 to 500° F. and will more typically be in a range of from 300 to 450° F. Pressures within the oligomerization reaction zone will usually be in a range of from 100 to 1200 psig and more typically in a range of from 200 to 1000 psig. When practicing this invention the preferred operating pressure for the SPA catalyst will be in a range of from 200 to 1000 psig with 200 to 500 psig being particularly preferred. It has also been found that maintaining operating temperatures in a narrow range of from 300 to 400° F. can push selectivity toward the production of more C 8  isomers. 
     The feed to the oligomerization zone reaction will typically comprise C 3  to C 5  olefins and paraffins. Steam or water may be fed into the reactor to maintain a low water content for hydration of the preferred SPA catalyst. The source of the olefin feeds are typically a light gas stream recovered from the gas separation section of an FCC process, C 4  streams from steam cracking and coker off gas or the effluent from dehydrogenation zone. The olefin feed stream is characterized by having an overall C 4  olefin concentration of at least 10 wt %. In most operations, this olefin feed stream will contain C 4  olefins but it may also constitute all or substantial quantities of C 3  olefins. Typically the olefin feeds can have a C 3  to C 5  olefin concentration of at least 30 wt %. The principal oligomerization products comprise C 7  and heavier olefins. The principal reaction substrate in the reaction zone will comprise isobutene. Where C 3  and C 5  olefins are present, these olefins will primarily combine with isobutene to produce C 8  alkenes. Accordingly the isobutene is a preferred reactant for the oligomerization zone and is desirably present in large quantities. Preferred feeds will have a concentration of at least 30 wt % and more preferably at least 50 wt % of the total olefins in the feed stream. Preferably, out of the total olefin concentration in the feed stream at least 20 wt % and more preferably at least 30 wt % will comprise isobutene. In regard to C 4  olefins, isobutene will preferably comprise at least 33% of the total butenes. The olefin content of preferred feeds will predominately comprise branched olefins with isobutene present in large quantities. The reaction of normal pentenes and propylene is promoted by maintaining a high concentration of isobutene in the feed to the oligomerization zone of this invention. Oligomerization of pentene and propylene into high octane isomers is promoted by having an olefin distribution in the feed to the isomerization zone that comprises at least 50 wt % isobutene. When large quantities of propylene are present in the feed to the oligomerization zone, the octane number of the product may be increased by raising the percentage of isobutene in the butene fraction of the feed. Preferably the butene fraction will comprise 100% isobutene when large amounts of propylene enter the oligomerization zone. 
     In the practice of this invention heavy paraffin components contact the catalyst in conjunction with the usual oligomerization zone feed. The heavy paraffin components will comprise hydrocarbons having at least seven carbon atoms, and preferably at least 8 carbon atoms, and up to twenty carbon atoms and will preferably comprise C 10  to C 12  paraffins. Addition of a heavy paraffin stream will provide a substantial quantity of heavy paraffins in the oligomerization zone and preferably will produce a minimum of 20 wt % C 7  and heavier paraffins in the reactor effluent stream and will more typically produce at least 15 wt % of C 8  and heavier paraffins at the inlet of each catalyst bed. C 8  paraffins are particularly preferred and will preferably comprise 10 to 30 wt % of the mass flow through the oligomerization reaction zone. 
     The presence of the heavy paraffins promote liquid phase conditions in the oligomerization zone. The combined heavy saturate stream and feed will usually maintain at least partial liquid phase conditions in the oligomerization zone. Partial liquid phase conditions refers to maintaining at least 10 wt % of the combined heavy saturate stream and feed in liquid phase. Preferably at least 50 wt % of the combined feed and heavy saturate stream are in liquid phase in the oligomerization zone to provide substantial liquid phase conditions, and more preferably essentially all, i.e. at least 90 wt %, of the fluid in the oligomerization zone will be in liquid phase. 
     The heavy paraffin components may enter the process with the incoming feed or may be injected into an oligomerization reaction zone at intermediate locations within a single catalyst bed or a number of catalyst beds. It is preferred to have the heavy paraffins present as the feed initially enters the reaction zone to maximize the benefit of the heavy paraffins in the process. Additional quantities of the heavy paraffins may be injected in stages through process to maintain temperature control throughout the bed or beds of oligomerization catalyst. 
     Where the oligomerization zone has a multiple bed arrangement, the different catalyst beds are preferably contained within one or more cylindrical, vertically oriented vessels and the feed stream preferably enters the top of the reactor. The catalyst is preferably disposed in fixed beds within the oligomerization zone in what is known as a chamber-type reactor structure. Typically, a chamber-type reactor will contain about five catalyst beds. In a chamber-type reactor, the reactants flow through a series of large diameter catalyst beds. The temperature of the reactants may be further controlled by recycling additional relatively inert hydrocarbons to act as a heat sink. Oligomerization reaction zones are routinely arranged with such multiple beds of catalyst that receive an intermediate injection of a quench material to control temperatures from the exothermic reaction. Substantial advantage can be obtained by adding the heavy paraffin feed as an intermediate injection stream that also benefits the process by serving as a quench stream. 
     With the addition of the heavy paraffin stream the combined feed to the oligomerization zone will preferably have a ratio of light and heavy paraffins to olefins of from 1:1 to 5:1. Typically the paraffin concentration of the feed to the oligomerization reaction zone will be at least 50 wt % and more typically at least 70 wt %. A high percentage of the olefins in the feed stream are reacted in the oligomerization reaction zone along with the isobutene. The olefin conversion will typically range of from 80 to 99 wt %. 
     The effluent from the oligomerization reaction zone will normally enter a separator. Separation of the effluent stream from the oligomerization zone will at minimum recover the heavy paraffins from the effluent for recycle to the oligomerization zone. Separating C 8  paraffins from the effluent stream for recycle may bring some heavy olefins into the recycle stream and require saturation of the reactive olefins before they are returned to the oligomerization zone. Circulation of the paraffins through the process and carryover of heavy olefins will produce some quantity of heavy oligomers. The concentration of heavy oligomers in the recycle stream is kept low by purging a portion of the effluent stream from the bottoms stream of the separator. Therefore, a source of heavy paraffins are needed to supply the initial paraffins for circulation in the recycle stream as well as make-up paraffins for circulation through the process. The source of the heavy paraffins to oligomerization zone can be any stream that can supply the C 7  or higher carbon number paraffins in the necessary quantities. The paraffins can be imported into the process from external sources or produced by saturating all or a portion of the oligomerization effluent stream. (Unless otherwise noted the term &#34;portion&#34; when used herein to describe a process stream refers to either an aliquot portion of the stream or a dissimilar fraction of the stream having a different composition than the total stream from which it was derived.) The entire effluent from the oligomerization zone may be saturated to provide a source of recycle paraffins for the process as well as saturated C 8  isomers for use as gasoline blending components. Or the effluent may be separated to recover the portion of the paraffins that are recycled to the oligomerization zone. 
     When present in the process, preferred saturation reaction zones will provide an essentially complete saturation of all olefins from the saturation reactor. The circulation of the heavy paraffin recycle can offer the added advantage of permitting the oligomerization zone to operate at lower pressure. In some cases it may be possible to use the lower pressure operation of the oligomerization reactor for direct passage of the polymerization effluent to the hydrogenation reactor. Exothermicity will typically cause the saturation zone to operate at higher temperatures than the oligomerization zone so that quench fluid and paraffins in the effluent from the oligomerization will provide additional heat sink material for the heat release of the saturation reaction zone. 
     The process and different operational steps will be described in conjunction with FIGS. 1 and 2. FIGS. 1 and 2 show only limited forms of the invention and only those portions of the process that are necessary to gain an understanding of the invention and the necessary means of integrating the principal processing steps that comprise the invention. Further details related to valves, control means, pumps, compressors, coolers, and other necessary processing equipment are well known to those skilled in the art and not described in detail unless necessary for an understanding of the invention. 
     An oligomerization zone feed stream, rich in C 4  olefins and in particular isobutane is brought into the process by a line 10 and combined with a recycle stream of C 12  paraffins carried by a line 12. A line 14 carries the combined feed and recycle paraffin stream into an oligomerization reaction zone 16 wherein the feed and paraffins contact an SPA catalyst. A stream 18 carries an oligomerization effluent comprising C 8  olefins and C 12  paraffins to a separator 20. A line 22 adds a make-up stream of C 12  paraffins to the effluent entering separator 20. Separator 20 removes a heavy fraction containing C 12  paraffins from the C 8  oligomers formed in the oligomerization zone. Separator 20 may provide a simple flashing operation to make a rough cut of the heavy stream or may be a fractionation zone. An overhead stream 24 carries the C 8  olefins from separator 20 for further processing. Such further processing will typically include saturation of the olefins in a saturation zone. A bottoms stream containing C 12  paraffins for recycle to the process is withdrawn by a line 26. A good separation is desired to minimize the carry-over of C 12  olefins to the oligomerization zone. A portion of the bottoms stream 26, which is typically equal to the mass flow of the make-up paraffin addition from line 22, is purged from the process to reduce the build up of heavy oligomers in the recycle stream. The remainder of the heavy paraffins is returned for admixture with incoming feed via line 12. 
     In the arrangement of FIG. 2 an oligomerization zone feed stream, rich in C 4  olefins and in particular isobutane is brought into the process by a line 30 and combined with a recycle stream of C 12  paraffins carried by a line 32. A line 34 carries the combined feed and recycle paraffin stream into an oligomerization reaction zone 36 wherein the feed and paraffins contact an SPA catalyst. A stream 38 carries an oligomerization effluent comprising C 8  olefins and C 12  paraffins to a separator 40. Separator 40 removes a heavy fraction containing C 12  paraffins from the C 8  oligomers formed in the oligomerization zone. Separator 40 may provide a simple flashing operation to make a rough cut of the heavy stream or may be a fractionation zone. An overhead stream 42 carries the C 8  olefins from separator 40 for further processing. A bottoms stream containing C 12  paraffins and heavy oligomers is withdrawn from the separator by a line 46. A portion of the bottoms stream 46 is purged from the process to reduce the build up of heavy oligomers in the recycle stream. The remainder of the heavy paraffins and heavy oligomers are combined with hydrogen from a line 50 and passed to a saturation reactor 52. 
     Stream 50 supplies hydrogen to the saturation zone and should contain at least 50 wt % of hydrogen. Preferably, the hydrogen-containing gas stream will have a hydrogen concentration greater than 75% wt % hydrogen. Hydrogen can be conveniently recovered from a dehydrogenation zone which may supply a portion of the olefins for the oligomerization zone or outside sources may supply all of the necessary hydrogen when a saturation zone is present. Preferably the saturation zone will operate with a minimum excess of hydrogen. 
     The saturation zone saturates heavy oligomer in the recycle stream. Saturation of the heavy oligomers provides additional heavy paraffins for circulation rough the reaction zone and replaces the paraffins lost the by the purging of heavies from the bottoms stream. The saturation of heavy oligomers has the advantage of reducing catalyst fouling and eliminating the need for an external source of make-up paraffins. The effluent from the saturation zone is taken by line 32 for recycle to the oligomerization zone. 
     To more fully demonstrate the attendant advantages of the present invention, the following tests were performed. 
     EXAMPLE 1 
     A feedstream having a composition of 13 wt % normal butene, 17.7 wt % isobutene and 69.4 wt % isobutane was contacted with about 50 cc of a solid phosphoric acid catalyst comprising a calcined mixture of phosphoric acid in siliceous base. The catalyst comprised pellets approximately 1/4&#34; in diameter and length that were retained in a 7/8&#34; steel reactor vessel having a volume of 70 cc. Channeling was avoided by carefully sand packing the void volume between particles. The feed entered the reactor at a temperature of 374° F. and a pressure of 500 psig and passed through the reactor at a liquid hourly space velocity of 2. The oligomerization reaction produced a maximum reactor temperature of 396° F. A sample of the reactor effluent was recovered, distilled and analyzed to determine the conversion of C 4  olefins and the carbon number selectivities of the products. The results of the analysis are shown in Table 1. 
     
                       TABLE 1
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            CARBON NO SELECTIVITIES, WT %
FEED  CONV. %     5- &gt; 7  8     9- &gt; 11
                                      12    &gt;12
______________________________________
EXAM- n-C.sub.4.sup.-  = 81
                  8.4     56    5.2   28    2.4
PLE 1 iso-C.sub.4.sup.-  = 91
      TOTAL C.sub.4.sup.-  = 88
EXAM- n-C.sub.4.sup.-  = 81
                  4.7     66.2  3.9   24.6  0.6
PLE 2 iso-C.sub.4.sup.-  = 91
      TOTAL C.sub.4.sup.-  = 86
______________________________________
 
    
     EXAMPLE 2 
     In order to demonstrate the advantages of a heavy recycle an additional 25 wt % of normal C 8  paraffins were added to the feed of Example 1 and run at the operating conditions and with the same catalyst as Example 1. The oligomerization zone reached a maximum temperature of 392° F. A sample of the effluent from the reaction zone was again distilled and analyzed and found to contain a significantly higher percentage of C 8  olefins. The results of the analysis are again shown in Table 1. 
     Comparison of Examples 1 and 2 demonstrates that at approximately equal C 4  olefin conversions the addition of the C 8  paraffins shifted the selectivity of the reactor effluent significantly toward the production of the highly desired C 8  isomer and surprisingly away from the production of both higher and lower carbon number isomers. 
     As this example demonstrates, the recycle stream of this invention provides a significant improvement in the selectivity of the oligomerization to high octane C 8  isomers. 
     EXAMPLE 3 
     A feedstream having a composition of 8.4 wt % normal butene, 21.9 wt % isobutene and 69.7 wt % isobutane was contacted with about 50 cc of a solid phosphoric acid catalyst of the type used in Examples 1 and 2. The reactor vessel and catalyst loading technique was also of the same type used in Examples 1 and 2. Feed entered the reactor at a temperature of 376° F. and a pressure of 500 psig and passed through the reactor at a liquid hourly space velocity of 2. The oligomerization reaction produced a maximum reactor temperature of about 403° F. A sample of the reactor effluent was recovered hydrogenated, distilled and analyzed to determine the conversion of C 4  olefins, the carbon number selectivities of the products and the research and motor octane number. The results of the analyses are shown in Table 2. 
     
                                           TABLE 2
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       TEMP ° F.
              LHSV,        CARBON NO. SELECTIVITIES, WT %
FEED   INLET/MAX
              HRS.sup.-1
                  CONV. %  5-&gt;7
                               8  9-&gt;11
                                      12 &gt;12 RON
                                                MON
__________________________________________________________________________
EXAMPLE 3
       376/403
              2   n-C.sub.4.sup.-  = 83
                           10.5
                               51 6   30 2.5 83.3
                                                84.6
                  iso-C.sub.4.sup.-  = 94
                  TOTAL C.sub.4.sup.-  = 91
EXAMPLE 4
       308/322
              2   n-C.sub.4.sup.-  = 54.5
                           0.8 87.2
                                  0.3 11.7
                                         --  101
                                                95.0
                  iso-C.sub.4.sup.-  = 96.5
                  TOTAL C.sub.4.sup.-  = 87
EXAMPLE 5
       320/340
              2   n-C.sub.4.sup.-  = 63.7
                           1.3 83.1
                                  0.9 14.7
                                         --  99.7
                                                94.7
                  iso-C.sub.4.sup.-  = 95.9
                  TOTAL C.sub.4.sup.-  = 88.7
EXAMPLE 6
       329/338
              0.75
                  n-C.sub.4.sup.-  = 83
                           2.3 75.3
                                  1.6 20.8
                                         --  97.9
                                                93.2
                  iso-C.sub.4.sup.-  = 96.5
                  TOTAL C.sub.4.sup.-  = 94
__________________________________________________________________________
 
    
     EXAMPLES 4-6 
     In order to demonstrate the advantages of a heavier components than C 8  and lower operating temperatures an additional 25 wt % of normal C 12  paraffins were added to the feed of Example 3 and run at a range of reduced operating temperatures and space velocities with the same catalyst as Example 3. Conversions, selectivity and research and motor octane numbers after distillation and hydrogenation of effluents from the three runs with the added C 12  components to the feed are shown in Table 2 as Examples 4-6. 
     All three of the runs operated with reduced temperatures relative to Example 3 and show significant improvement to the C 8  selectivity by the addition of the normal C 12  paraffins. Examples 4 and 5 both demonstrate a much higher selectivity to C 8  isomers than Example 3 at an only slightly reduced conversion. The improved selectivity resulted in a much higher octane number than that obtained without the C 12  components in Example 3. Example 6 demonstrates that higher conversions than Example 3 may be obtained at relatively higher temperatures and a reduced space velocity while still maintaining a significantly higher selectivity to C 8  isomers than shown in Example 3.