Patent Document

FIELD OF THE INVENTION 
     This invention is directed to hydroprocessing, and more particularly to multistage hydroprocessing. 
     BACKGROUND OF THE INVENTION 
     This process is directed to hydroprocessing, preferably by hydrocracking heavy hydrocarbon material boiling in the vacuum gas oil range to produce middle distillates at very high selectivity, and to upgrade lower-value distillates by hydrotreating. The concept includes many innovations which would allow the refiner to obtain yields similar to those of a multistage hydrocracker with the economics of a single stage, once-through unit. 
     Previous designs for hydroprocessing vacuum gas oils or other hydrocarbon materials boiling in a range of 392° F. or greater include:
         Straight forward single stage once through design. Conversion ranges from 20% to 80%. The amount of bottoms produced is greater than or equal to 20%.   Single stage recycles. Conversion ranges from 90% to 99% conversion. The amount of bottoms produced is less than or equal to 10%. Recycle liquid operation can result in complications, however.   Multistage recycle results in higher cost than single stage once through or single stage recycle. It does provide, however, the highest liquid yield and most flexibility. Conversion is from 95% to 100%. Bottoms produced are less than 5%.   Split-feed injection in cases where external distillate feeds are employed.       

     None of these processes can readily upgrade external feeds (raw feeds from outside the hydroprocessing unit), unless they go through captive process loop. 
     SUMMARY OF THE INVENTION 
     This invention is designed to obtain yields similar to those obtained with multistage recycle but at a much lower capital investment. It is intended to simultaneously upgrade external, low-value distillates while hydrocracking feeds boiling in the vacuum gas oil range. 
     The configuration involves a once-through liquid hydroprocessing unit having at least two reactors. One is preferably for hydrotreating, and one is preferably for hydrocracking in a clean environment at lower pressure. Between the first and second reactors is a very hot high pressure separator which flashes first reactor product distillate overhead to a distillate upgrader. 
     Advantages of this invention include:
     (1) Lower capital cost than found in earlier designs because of:
       (a) lower pressure in hydrocracking reactor and distillates upgrader;   (b) a clean environment for hydrocracking in subsequent reactors;   (c) a smaller overall catalyst volume is required; and   (d) amount of major equipment (pumps, furnaces, compressors, etc.) is minimized.   
       (2) Higher conversion results, relative to a typical single stage once through hydroprocessing unit. Subsequent reactors operate in a clean environment and can accomplish high conversions at much lower temperatures than the bottoms beds of a single stage once through hydroprocessing unit.   (3) Overcracking of distillates is minimized due to the very hot high pressure separator following the first reactor. In this separator the bulk of the distillates are removed overhead and thus are prevented from reaching the hydrocracking reactor. This innovation leads to high distillate selectivity (distillate yield/conversion). The distillate selectivity approaches the 95% achievable in a recycle unit having two or more stages.   (4) Split feed injection with segregated reaction zones. Upgrading of external distillates occurs at the same time as vacuum gas oil hydrocracking without separate fractionation zones. This concept differs from earlier split feed designs in the lower operating pressure employed at the point of split feed injection. Furthermore, the feed is injected at different points than those used in previous inventions.   (5) Lower consumption of H 2  and lower catalyst volume because the reaction zones are optimized for their functions. (HDT of VGO at high pressure, recovery/upgrading of distillates, HCR of VGO bottoms provides a clean environment).   

     The development of this invention has been promoted by the following observations:
     (1) Hydrotreating of material boiling in the vacuum gas oil range is much more effective at higher hydrogen pressure than lower hydrogen pressure.   (2) Hydrocracking of bottoms from a hydrotreated vacuum gas oil feed can occur at 50° F. to 00° F. lower temperature in a clean environment than in the bottoms beds of a single stage once through process.   (3) Diesel overlap will crack when mixed in with vacuum gas oil in a hydrocracker.   (4) A noble metal zeolite hydrocracking catalyst will function very well in the second reactor or subsequent reactor. A base metal zeolite hydrocracking catalyst can also be used.   (5) Calculations indicate this process configuration can accomplish &gt;90% conversion with 94% to 96% selectivity to 250° F. to 700° F. distillates produced from a straight run vacuum gas oil.   

     The invention is summarized as follows: 
     An integrated hydroprocessing method having at least two stages, each stage further comprising at least one reaction zone, said method comprising the following steps:
         (a) combining an oil feed with a hydrogen-rich gas stream to form a feedstock;   (b) passing the feedstock of step (a) to a reaction zone of the first stage, which is maintained at conditions sufficient to effect a boiling range conversion, and contacting it with hydroprocessing catalyst, thereby creating a hydroprocessed effluent;   (c) passing the effluent of step (b), following pressure reduction, to a very hot separator maintained at high pressure, where it is separated into an overhead fraction and a bottoms fraction;   (d) passing the overhead fraction of step (c) to a distillate upgrader which contains at least one zone of hydroprocessing catalyst and is maintained at conditions sufficient to effect a boiling range conversion, thereby creating an upgraded effluent;   (e) passing the bottoms fraction of step (c) to a reaction zone of the second stage, which is maintained at conditions sufficient to effect a boiling range conversion, and contacting it with hydroprocessing catalyst thereby creating a second hydroprocessed effluent;   (f) combining the upgraded effluent of step (d) with the second hydroprocessed effluent of step (e), the combined stream then entering a hot separator maintained at high pressure, in which the combined stream is separated into an overhead fraction and a bottoms fraction, the bottoms fraction proceeding to fractionation;   (g) passing the overhead fraction of step (f) to a cold separator, where it is separated into an overhead fraction comprising hydrogen and light gases, and a bottoms fraction comprising sour water.       

    
    
     
       BRIEF DESCRIPTION OF THE FIGURES 
         FIG. 1  illustrates the multistage recycle process of the instant invention. 
         FIGS. 2 and 3  shows a comparison of conventional and new hydrocracking configurations using a base metal catalyst system.  FIG. 2  illustrates catalyst temperature vs. conversion and  FIG. 3  compares middle distillate yield vs. conversion. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     Description of the Preferred Embodiment 
       FIG. 1  illustrates feed entering the process through stream  1  and being combined with hydrogen in stream  28  to form stream  2 . Hydrogen in stream  28  is prepared by compression of hydrogen in makeup compressor  85 . Hydrogen enters compressor  85  through stream  27 . The invention includes an option to compress a stream  30  of recycle gas in the last stage of compressor  85  to meet the gas to oil ratio in reactor  10 , when required. 
     Stream  2  is heated, as depicted by exchanger  31 , prior to entering the first stage hydroprocessing unit, vessel  10 . Vessel  10  is preferably operated as a hydrotreater. The feed flows downward through one or more beds of catalyst. Streams  3 ,  4 , and  5  depict interbed hydrogen quench. 
     Hydrotreated effluent exits vessel  10  through stream  32  and is reduced in pressure (valve  33 ) to that required for hydrocracking in a clean environment. The effluent is heated in furnace  34  to approximately 825° F. in order to disengage the maximum material in very hot high pressure separator  20 . This separator functions as a simple flash drum, separating diesel and lighter fractions from heavier materials without the use of hydrogen stripping. Hydrogen stripping is relatively ineffective at hydrocracking pressures. Stream  11 , containing diesel and lighter materials, exits vessel  20  overhead. External feeds in the middle distillate boiling range, as well as fractionation recycle, are represented by stream  9  and are combined with stream  11 . Stream  11  is heated in exchanger  35  and may be combined with hydrogen in stream  25  prior to entering a distillate upgrader, vessel  30 , in the case of co-current flow. Flow in vessel  30  may be co-current or countercurrent. Countercurrent flow may be preferred if aromatics saturation is desired. The amount of aromatics permitted in the ultra-low sulfur diesel being manufactured (ULSD) may affect whether co-current or counter-current flow is used. In the case of countercurrent flow, hydrogen is added below the catalyst beds and is directed upward. The catalyst in the bed or beds of vessel  30  is preferably hydrotreating catalyst, but hydrocracking catalyst may be used if fractionation recycle is being treated. 
     The bottoms effluent of vessel  30  exits through stream  15 . Material from stream  15  may be passed to stream  12  as feed to the hydrocracker, vessel  40 , when necessary. The dotted line depicts this. The upgraded diesel effluent in stream  15  is reduced in pressure (valve  36 ), cooled (exchanger  37 ), combined with the effluent stream (stream  14 ) from vessel  40  (in which second stage hydrocracking preferably occurs) to become stream  16 . Stream  16  is passed to the hot high pressure separator  70 , where it is separated into an overhead stream  18  and a bottoms stream  17 . Bottoms stream  17  is sent to fractionation. Overhead stream  18  is cooled prior to entering cold high pressure separator  50  by passage through exchangers  43  and  44 , as well as by water injection through stream  19 . Sour water exits cold high pressure separator through stream  29 . Stream  71  goes to fractionation. It may be reduced in pressure using valve  72 . Overhead gaseous material in stream  21  enters amine absorber, vessel  60  at the bottom and flows upward, as lean amine moves downward, absorbing hydrogen sulfide. Rich amine exits vessel  60  through stream  22 . Stream  23 , comprising primarily hydrogen, exits overhead through stream  23 . Stream  23  is compressed in compressor  75 , becoming stream  24 . Stream  24  is divided into streams  25  and  26 . Stream  26  is heated in exchanger  42  before combining with stream  12  to form stream  13 . 
     The bottoms effluent of vessel  20  exits through stream  12 . Valve  38  is a level control valve. Stream  12  may be combined with material in stream  15 , along with hydrogen in stream  26  then is heated in exchanger  39 . Streams  12  and  15  may be combined when naphtha or jet fuel is the preferred product. Recycle stream  31  may be added to stream  15  when very high conversion levels are required. Stream  13  exits exchanger  39  and enters vessel  40 . Second stage hydrocracking preferably occurs in vessel  40 , which contains one or more beds of hydrocracking catalyst. Effluent in stream  14  is cooled in exchanger  41  before being combined with stream  16 . 
     Feeds 
     A wide variety of hydrocarbon feeds may be used in the instant invention. 
     Typical feedstocks include any heavy or synthetic oil fraction or process stream having a boiling point above 392° F. (200° C.). Such feedstocks include vacuum gas oils (VGO), heavy coker gas oil (HCGO), heavy atmospheric gas oil (AGO), light coker gas oil (LCGO), visbreaker gas oil (VBGO), demetallized oils (DMO), vacuum residua, atmospheric residua, deasphalted oil, Fischer-Tropsch streams, Light Cycle Oil and other FCC product streams. 
     Products 
     The process can be used over a broad range of applications as shown in the Table 1. 
     
       
         
               
               
               
               
             
           
               
                 TABLE 1 
               
               
                   
               
               
                 Oil Feed 
                 Catalyst System 
                 Operating Conditions 
                 Products 
               
               
                   
               
             
             
               
                 VGO 
                 Stage 1 -  
                 Stage I: 
                 Maximum Diesel 
               
               
                 HCGO 
                 Hydrotreating + Hydrocracking 
                 P: 1000-3000 psig 
                 Maximum Jet + Diesel 
               
               
                 DAO 
                   
                 LHSV = 0.3-4.0 
                 Maximum Naphtha 
               
               
                 VBGO 
                   
                 T: 600° F.-850° F. 
               
               
                   
                 Stage2 - Hydrocracking 
                 Stage 2: 
               
               
                   
                   
                 P: 1000-3000 psig 
               
               
                   
                   
                 LHSV = 0.5-5.0 
               
               
                   
                   
                 T: 500° F.-800° F. 
               
               
                 AGO, LCO, LCGO 
                 Stage 1 -  
                 Stage I: 
                 Maximum Diesel 
               
               
                   
                 Hydrotreating + Hydrocracking 
                 P: 1000-3000 psig 
                 Maximum Jet + Diesel 
               
               
                   
                   
                 LHSV = 0.5-4.0 
                 Maximum Naphtha 
               
               
                   
                   
                 T: 600° F.-850° F. 
               
               
                   
                 Stage2 - Hydrocracking 
                 Stage 2: 
               
               
                   
                 or 
                 P: 1000-3000 psig 
               
               
                   
                 Stage 2 -  
                 LHSV = 0.5-5.0 
               
               
                   
                 Base Metal Hydrocracking 
                 T: 500° F.-750° F. 
               
               
                   
                 or 
               
               
                   
                 Stage 2 - Aromatic Saturation 
               
               
                   
                 (Noble-metal) 
               
               
                   
               
             
          
         
       
     
     The process of this invention is especially useful in the production of middle distillate fractions boiling in the range of about 250° F. to 700° F. (121° C. to 371° C.). A middle distillate fraction is defined as having an approximate boiling range from about 250° F. to 700° F. At least 75 vol. %, preferably 85 vol. % of the components of the middle distillate has a normal boiling point of greater than 250° F. At least about 75 vol. %, preferably 85 vol. % of the components of the middle distillate has a normal boiling point of less than 700° F. The term “middle distillate” includes the diesel, jet fuel and kerosene boiling range fractions. The kerosene or jet fuel boiling point range refers to the range between 280° F. and 525° F. (38° C. to 274° C.). The term “diesel boiling range” refers to hydrocarbons boiling in the range from 250° F. to 700° F. (121° C. to 371° C.). 
     Gas streams or naphtha may also be produced in the process of this invention. Gas streams or naphtha normally boils in the range below 400° F. (204° C.), or from C 5  to 400° F. (204° C.). Boiling ranges of various product fractions recovered in any particular refinery will vary with such factors as the characteristics of the crude oil source, local refinery markets and product prices. 
     Conditions 
     A hydroprocessing condition is a general term which refers primarily in this application to hydrocracking or hydrotreating. 
     Hydrotreating conditions include a reaction temperature between 400° F. to 900° F. (204° C. to 482° C.), preferably 650° F. to 850° F. (343° C. to 464° C.); a pressure between 500 to 5000 psig (pounds per square inch gauge) (3.5 to 34.6 MPa), preferably 1000 to 3000 psig (7.0 to 20.8 MPa): a feed rate (LHSV) of 0.5 to 20 hr-1 (v/v); and overall hydrogen consumption 300 to 2000 SCF per barrel of liquid hydrocarbon feed (63.4 to 356 m 3 /m 3  feed. The second stage hydrotreating reactor is operating at a lower pressure than the first stage reactor, the VGO hydrotreater or moderate severity hydrocracker. 
     Typical hydrocracking conditions (which may be found in stage 1 or stage 2) include a reaction temperature of from 400° F. to 950° F. (204° C. to 510° C.) preferably 650° F. to 850° F. (343° C. to 454° C.). Reaction pressure ranges from 500 to 5000 psig (3.5 to 4.5 MPa), preferably 1500 to 3500 psig (10.4 to 24.2 MPa). LHSV ranges from 0.1 to 15 hr-1 (v/v), preferably 0.25 to 2.5 hr hydrogen consumption ranges from 500 to 2500 SCF per barrel of liquid hydrocarbon feed (89.1 to 445 m 3 H 2 /m 3  feed). 
     Catalyst 
     A hydroprocessing zone may contain only one catalyst, or several catalysts in combination. 
     The hydrocracking catalyst generally comprises a cracking component, a hydrogenation component and a binder. Such catalysts are well known in the art. The cracking component may include an amorphous silica/alumina phase and/or a zeolite, such as a Y-type or USY zeolite. Catalysts having high cracking activity often employ REX, REY and USY zeolites. The binder is generally silica or alumina. The hydrogenation component will be a Group VI, Group VII, or Group VIII metal or oxides or sulfides thereof, preferably one or more of molybdenum, tungsten. cobalt, or nickel, or the sulfides or oxides thereof. If present in the catalyst, these hydrogenation components generally make up from about 5% to about 40% by weight of the catalyst. Alternatively, platinum group metals, especially platinum end/or palladium, may be present as the hydrogenation component, either alone or in combination with the base metal hydrogenation components molybdenum, tungsten, cobalt, or nickel. If present, the platinum group metals will generally make up from about 0.1% to about 2% by weight of the catalyst. 
     If aromatic saturation is particularly desired, a preferred catalyst has a crystalline molecular sieve material component and a Group VIII noble metal component. The crystalline molecular sieve material component is a large pore faujasite structure having an alpha acidity of less than 1, preferably less than 0.3. Zeolite USY is the preferred crystalline molecular sieve material component. 
     Hydrotreating catalyst, if used, will typically be a composite of a Group VI metal or compound thereof, and a Group VIII metal or compound thereof supported on a porous refractory base such as alumina. Examples of hydrotreating catalysts are alumina supported cobalt-molybdenum, nickel sulfide, nickel-tungsten, cobalt-tungsten and nickel-molybdenum. Typically, such hydrotreating catalysts are presulfided. 
     EXAMPLES 
     
       
         
               
             
               
               
               
             
               
               
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 Comparison of Standard and New HCR Configurations 
               
               
                 Middle East VGO, Base Metal Catalyst System 
               
               
                 73 vol. % Conversion &lt;700° F. 
               
             
          
           
               
                   
                 Conventional 
                 New 
               
               
                   
                   
               
             
          
           
               
                   
                 LHSV, 1/br 
                 0.75 
                     0.75 
               
               
                   
                 Catalyst Temperature, ° F. 
                 777 
                  727* 
               
               
                   
                 HCR Zone Pressure, psig 
                 2300 
                 1250 
               
               
                   
                 Chemical H 2  Consumption, SCF/3 
                 1800 
                 1600 
               
               
                   
                 Middle Distillate Yield, liquid 
                 67 
                  68 
               
               
                   
                 volume % 250° F. to 700° F. 
               
               
                   
                   
               
               
                   
                 *706° F. at equal gas/oil ratio for standard and new configurations 
               
             
          
         
       
     
     Table 2 indicates that yield is slightly improved in the current invention, as compared to the conventional configuration, at lower temperature, pressure and hydrogen consumption. 
       FIG. 2  demonstrates that conversion in the instant invention is greater at lower temperatures, as opposed to the conventional hydrocracking configuration. Conversion improves at higher gas to oil ratios. 
       FIG. 3  demonstrates that yield to conversion ratios are comparable in both the conventional configuration as well as the configuration of the instant invention.

Technology Category: 8