Abstract:
The invention relates to distributing feed vapor more evenly across the interior space of a reactor vessel utilizing a distributor pipe at the inlet end that initially directs the flow of reactants through a flange plate and a series of ring plates. The ring plates are physical spaced such that vapor along the wall of the inlet is mildly obstructed by the flange plate and the ring plates cause the vapor to alter course temper down any diverse velocities that may create hot spots within the catalyst bed. At the end of the distributor pipe is a deflector which directs the feed vapor upwardly and outwardly in the head space of the reactor vessel.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This non-provisional application is a continuation-in-part application of three U.S. applications. The first application is Ser. No. 15/366,481, filed Dec. 1, 2016 and has the title “Reactor Inlet Vapor Velocity Equalizer”. The second application is U.S. application Ser. No. 15/366,493, filed Dec. 1, 2016 and has the title “Equalizing Vapor for Reactor Inlet”. The third application is U.S. application Ser. No. 13/779,935, filed Feb. 28, 2013, and entitled “Modifying Flow of a Reactor Inlet Distributor”. Applicant claims benefit under 35 USC §120 for all three applications and also to the Provisional Application claimed by the third application above which is U.S. Provisional Application Ser. No. 61/604,332 filed Feb. 28, 2012, entitled “Apparatus for Modifying Flow of a Reactor Distributor Inlet”. All of these applications are hereby incorporated herein by reference in their entirety. 
     
    
     STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT 
       [0002]    None. 
       FIELD OF THE INVENTION 
       [0003]    This invention relates to reactor design and especially to the design of inlets to reactors. 
       BACKGROUND OF THE INVENTION 
       [0004]    Reactors for converting reactants to desirable intermediates or final products come in many sizes and shapes. Chemical engineers spend many hours designing reactor systems to optimize reactor production considering pressure, temperature, flow rates, catalyst cost, reaction kinetics along with balancing many other issues and concerns. 
         [0005]    It is commonly understood that a generally uniform distribution of reactants in a catalyst reactor is preferred to avoid hot spots and to avoid the underutilization of catalyst in the reactor. Many inlet designs have been created to improve the distribution of reactants within reactors especially where the reactants are vapor versus liquid. For purposes of this invention, gas and vapor mean the same thing and are generally expressed with the term vapor. One problem with distribution of vapor is that such vapors tend to have higher velocity concentrations away from the center, such as when vapors follow a bend in the piping leading to a reactor. In a reactor arrangement that is fed by a conduit with a significant bend leading into the top or bottom of a reactor, the higher velocities tend to follow the outside of the bend and concentrate along one side of the reactor. Baffles and vanes have been used for years to create back pressure on the inlet stream and cause the reactants to distribute themselves across the reactor. But back pressure concerns and velocity loss are always concerns that counter any efforts at creating an even and balanced flow. Reducing the productivity of a reactor is not part of an attractive solution. 
         [0006]    Another common technique is to provide an inert support bed with a thick layer of inert material that create many tortuous paths to the catalyst causing mixing and back pressure to create a level of balance across the body of the reactor. Again, this type of solution creates back pressure and velocity loss and also reduces the available volume of a reactor for catalyst. Committing extra interior space in a reactor for inert material also reduces catalyst performance and the productivity of the system. 
         [0007]    What is desired is a technique for creating a balanced distribution of the vaporous reactants across the interior space of a reactor without significantly enlarging the size of the reactor and without impairing the productivity of the reactor system. It is also desirable for the vapors to become spread out to the outside of the reactor in radial flow reactors without adding structure or imposing excessive turbulence or drag on the vapor. 
       BRIEF SUMMARY OF THE DISCLOSURE 
       [0008]    The invention more particularly relates to a reactor system including a reactor vessel having a closed shell defining a relatively large interior space inside the shell for conducting a fixed bed catalytic reaction. The reactor has an inlet into the interior space of the shell for the admission of feed vapor, an outlet at the opposite end thereof to allow products of the catalytic reaction to exit the reactor vessel, and a bed of catalyst between the inlet and the outlet. There is a head space between the inlet and the catalyst bed. The inlet includes a generally cylindrical neck having a smaller internal cross sectional dimension than a comparable internal cross sectional dimension of the relatively large interior space within the shell of the reactor vessel. The reactor system further includes a generally cylindrical distributor pipe extending down through the generally cylindrical neck and into the head space of the reactor vessel. The generally cylindrical distributor pipe has a peripheral wall, a first end through which feed vapor is received and an opposite end that is positioned in the head space of the reactor vessel such that the feed vapor is arranged to exit the generally cylindrical distributor pipe through openings extending radially outwardly through the peripheral wall of the distributor pipe adjacent the opposite end of the distributor pipe and delivered into the headspace. It should be understood that the peripheral wall of the distributor pipe has an outer diameter; The reactor system further includes a feed conduit connected to the generally cylindrical neck and arranged to deliver the feed vapor through the feed conduit to the generally cylindrical neck and into the generally cylindrical distributor pipe wherein the feed conduit includes a bend near the cylindrical neck such that the flow of the gaseous feedstock changes direction of flow by about 90 degrees or more within the feed conduit shortly prior to entering the cylindrical neck. A reactor inlet velocity equalizer is positioned generally within the generally cylindrical distributor pipe, wherein the equalizer comprises a flange equalizer plate positioned near the top of the generally cylindrical distributor pipe, longitudinal vanes attached to the flange equalizer plate and extending toward the opposite end of the generally cylindrical distributor pipe, at least three sets of cross vanes connecting between the longitudinal vanes and extending generally transverse across the generally cylindrical distributor pipe, a top equalizer plate attached to a first set of the cross vanes to minimally obstruct flow of gaseous feedstock and positioned below the flange equalizer plate within the generally cylindrical distributor pipe, a middle equalizer plate attached to a second set of the cross vanes to minimally obstruct flow of gaseous feedstock and positioned below the top equalizer plate within the generally cylindrical distributor pipe, and a bottom equalizer plate attached to a third set of the cross vanes to minimally obstruct flow of gaseous feedstock and positioned below the middle equalizer plate and still within the generally cylindrical distributor pipe. A deflector plate is attached to the opposite end of the generally cylindrical distributor pipe wherein the deflector plate has a diameter that is larger than the outer diameter of the peripheral wall of the distributor pipe such that the deflector plate is arranged within the head space of the reactor vessel, and further wherein the deflector plate has an outer edge and a generally circular bottom with a continuous periphery of the circular bottom along the peripheral wall at the opposite end of the distributor pipe and a sloped wall extending from the continuous periphery of the circular bottom in an outwardly direction from the peripheral wall of the distributor pipe and angled back towards the first end of the distributor pipe to deflect the feed vapor that has passed through the openings in the peripheral wall of the distributor pipe radially away from the openings in the peripheral wall of the generally cylindrical distributor pipe and angled somewhat back towards the first end of the distributor pipe. Holes are provided in the sloped wall of the deflector plate to allow some of the feed vapor to pass through the deflector plate and a fixed catalyst bed within the interior space of the shell for the feed vapor to be converted to desirable products where the reactor inlet velocity equalizer is arranged to interfere with high velocity gaseous flow more than it interferes with lower velocity flows such that flow that may otherwise be uneven across the generally cylindrical distributor pipe is altered by the reactor inlet velocity equalizer to create more balanced velocities across the generally cylindrical distributor pipe and therefore pass more evenly out of the openings in the generally cylindrical distributor pipe and be deflected by the sloped wall of the deflector so that the feed vapor passes through the fixed catalyst bed to obtain a more even use of the catalyst bed within the shell. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0009]    A more complete understanding of the present invention and benefits thereof may be acquired by referring to the follow description taken in conjunction with the accompanying drawings in which: 
           [0010]      FIG. 1  is an elevational cross section of a radial flow reactor with a distributor nozzle and an equalizer 
           [0011]      FIG. 2  is a top view of the reactor shown in  FIG. 1  showing the relative velocity of the inlet stream entering the reactor without the inventive equalizer; 
           [0012]      FIG. 3  is a perspective view of an embodiment of the inventive equalizer illustrating the structural elements for equalizing the flow of the inlet gases to a reactor; 
           [0013]      FIG. 4  is an elevation cross section of the inventive equalizer providing further illustration to the structure for equalizing the flow of inlet gases to a reactor; 
           [0014]      FIG. 5  is a top perspective view of the inventive equalizer providing further illustration of the structural elements for equalizing the flow of the inlet gases to a reactor; 
           [0015]      FIG. 6  is a fragmentary elevational cross section of the inventive equalizer showing the relative dimensions of the components; 
           [0016]      FIG. 7  is a fragmentary elevational cross section of the inventive equalizer showing the flow paths of the vapor into and through the neck of the reactor as altered by the inventive equalizer; and 
           [0017]      FIG. 8  is a fragmentary elevational cross section showing the equalizer and the distributor nozzle having a porous deflector plate design carried by the reactor inlet flange. 
       
    
    
     DETAILED DESCRIPTION 
       [0018]    Turning now to the detailed description of the preferred arrangement or arrangements of the present invention, it should be understood that the inventive features and concepts may be manifested in other arrangements and that the scope of the invention is not limited to the embodiments described or illustrated. The scope of the invention is intended only to be limited by the scope of the claims that follow. 
         [0019]    The invention is illustrated in context with radial flow reactor indicated by the arrow  10 . The radial flow reactor system  10  is operated to treat or react vapor through a bed of catalyst  30 . Although the radial flow reactor system  10  depicted in  FIG. 1  as a fixed-bed reactor, the invention may be applied to any type of radial-reactor bed such as a continuously or periodically moving reactor bed. 
         [0020]    The radial reactor  10  includes a reactor vessel  20  comprising a vertically elongated, rounded shell  21 . The reactor vessel includes an inlet at the top within the flange  19  at the upper end of the neck  22  of the reactor vessel. Feed vapor is introduced through a conduit  15  from a source (not shown) and is directed through the neck  22  into distributor  40  and into the head space  24 . The vapor enters the catalyst bed  30  from peripheral ducts  25  that are open to the head space and arranged along the outside vertical portion of the shell  21  with a screen or small openings open to the catalyst bed  30 . The vapor moves from the peripheral ducts  25  (which, in  FIG. 2 , appear as a series of half pipes or scalloped conduits) and moves radially through the catalyst bed  30  toward the center-pipe  32  as shown by arrows  31 . The center-pipe  32  also includes a screen or small holes to admit the reacted or treated vapor into the interior space  33  and move out of the radial reactor system  10  through an outlet at the bottom of the center-pipe  32  that is not shown. 
         [0021]    The conduit includes a bend B near the top of the reactor vessel  20  so as to direct the vapor straight into the top of the reactor. One of the problems addressed by the present invention is where the uneven distribution of vapor occurs in the top of the reactor vessel  20 . The inertia of the vapor moving through inlet conduit  15  around the bend B creates higher velocity vapor around the outside of the bend B as compared to the center of the conduit  15  and neck  21  or along the inside of the bend B. Another problem this invention addresses is to create a smoother flow of vapor from the distributor  40  toward the shell  21  of the reactor vessel  20  near the top thereof to follow the shell  21  into the open tops of the ducts  25 . 
         [0022]    Addressing the first problem is an equalizer  50  that is positioned inside of the generally cylindrical distributor pipe  40 . Preferably, the vapor flowing into the distributor pipe  40  would have a consistent velocity as measured transversely across the distributor pipe  40 , or at least the velocity would be concentric around the center or axis of the distributor pipe  40  so that as the vapor spreads out across the head space  24  to the peripheral ducts  25  at about the same velocity for each direction. For example,  FIG. 2  shows a flow arrangement that is NOT desirable where vapor moving along the directions indicated by arrow  16 A is moving much faster than the vapor flow indicated by smaller arrow  16 B. What would be desired is that flow in all directions across the head space  24  would be close to the same such as shown by intermediate arrow length  16 C. Thus, vapor flow in direction  16 A would be moderated or tempered down causing flow to increase in direction  16 B such that both are about the same velocity as in direction  16 C. If these flows are not balanced, the catalyst in the high velocity areas are inclined to be used up before the catalyst at the low velocity areas are used at all. In some reactors, low velocity causes excessive coking. Ultimately, productivity of the vessel is lower than optimal meaning lost production and lost profit opportunity. Any operational tricks that may be employed to increase productivity of aging catalyst are frustrated by the rapid aging of some catalyst while other catalyst is still quite fresh. Since catalyst tends to be expensive, getting as much productivity of desired products from a load of catalyst is always preferred. 
         [0023]    Turning back to  FIG. 1  and also to  FIGS. 3-7 , equalizer  50 , embodying the features of the present invention, is installed in the distributor pipe  40  to help balance the velocity across the transverse dimension and better balanced before the gases enter the head space  24 . 
         [0024]    The equalizer  50  is best shown in  FIGS. 3, 4 and 5 . The equalizer  50  ideally imposes minimal resistance of the flow of the vapor into the reactor vessel  20  so as to not alter the intended catalyst process while getting better distribution to utilize the full size and catalyst load in the reactor vessel  20 . So, the key features of the inventive equalizer  50  are a flange plate  51  and three vertically spaced ring plates  61 ,  71  and  81  (that will be described shortly). 
         [0025]    Flange plate  51  is positioned generally between the flange  18  of the conduit and the flange  19  of the reactor vessel  20 . The flange plate  51  includes a large diameter  51 A so as to extend into the space between the flanges  18  and  19  and particularly includes a generally circular opening in the middle thereof to allow vapor into the distributor pipe  40 . The generally circular opening is indicated by dimension  51 B which is the diameter of the generally circular opening. The generally circular opening of flange plate  51  is preferably less than the diameter  41 B of the distributor pipe  40  to as to create an obstruction to the flow of vapors along the interior walls of the inlet conduit  15 . As seen in the Figures, the outer diameter  51 A of the flange plate  51  is larger than the diameter  41 B of the distributor pipe  40 . It is believed that the flange plate  51  creates a greater obstruction for a higher velocity flow of vapor than it does for a lower velocity flow of vapor. As such, the flange plate  51  provides a first obstruction to begin to balance to velocity differences coming into the distributor pipe  40 . 
         [0026]    Equalizer  50  further includes a flange collar  52  that is attached to and extends from the flange plate  51  down into the distributor pipe  40 , but with a diameter slightly smaller than the diameter  41 B of the distributor pipe  40 . A number of longitudinal vanes  54  are attached to the inside surface of the flange collar  52  and arranged to extend both further into the center of the generally cylindrical neck  21  and further longitudinally into the generally cylindrical neck  21  toward the open interior of the reactor vessel  20 . The longitudinal (vertically oriented) vanes  54  are intended to create very little if any obstruction to the flow of vapor along the distributor pipe  40 , but rather to be used as an element of the structural support for the spaced ring plates  61 ,  71  and  81 . 
         [0027]    In the preferred arrangement, eight longitudinal vanes  54  are attached to the interior of the flange collar  52  and distributed equidistant around the flange collar  52 . Attached to the longitudinal vanes  54  are cross vanes  62 ,  72  and  82  each set of cross vanes arranged to extend transversely across the distributor pipe  40 . The first set of cross vanes are top cross vanes  62  which are positioned at a first position below the flange plate  51 . In the preferred arrangement, two cross vanes  62  are attached by their ends to each of four longitudinal vanes  54  forming an “X” shape generally horizontal or transversely across the distributor pipe  40 . Similarly, the second set of cross vanes are middle cross vanes  72  and are position at a second position below top cross vanes  62 . Again, in the preferred arrangement, middle cross vanes  72  are attached at their ends to four longitudinal vanes  54 , but to the four longitudinal vanes  54  that are not attached to the top cross vanes  62 . Also similarly, the third set of cross vanes are bottom cross vanes  82  and are positioned below middle cross vanes  72 . Again in the preferred arrangement, bottom cross vanes  82  are attached by their ends to four longitudinal vanes  54  which are the same four longitudinal vanes  54  that support the top cross vanes. All of the cross vanes  62 ,  72  and  82  are intended to support the spaced ring plates  61 ,  71 , and  81 , but not, by themselves, have much impact on the flow of vapor through the distributor pipe  40 . It should be noted that in some circumstances, such as for large diameter vessels or very high flow rates, it may be desirable to provide four cross vanes with ends of each attached to the eight longitudinal vanes to support each of the spaced ring plates  61 ,  71  and  81 . 
         [0028]    Top ring plate  61  is mounted on the “X” shaped top cross vanes  62 . Preferably, the top ring plate  61  is relatively flat, having a thickness of less than 0.5 inches with an outer diameter  61 A and an inner diameter  61 B. The outer diameter  61 A is less than the inner diameter  41 B of the distributor pipe  40  spaced away from the interior of the generally cylindrical wall  41  of distributor pipe  40  by an annular space  61 C. Ideally, the top ring plate  61  is a perfect circle with a perfectly circular opening in the middle that is also perfectly concentric to the circular shape. The difference between the inner diameter  61 B and outer diameter  61 A gives a ring face area. A greater ring face area tends to increase the obstruction to vapor flow and reduced ring face area similarly creates less obstruction to the vapor flow. In one preferred arrangement, top ring plate  61  includes a series of small holes  65  to reduce total ring face area. The amount of pressure drop created by top ring  61  is complicated in that there are many inputs to be considered such as the velocity of the vapor, the density and viscosity of the vapor, the ring face area and the turbulence that will be created by the size and shape of the ring face area, and even the thickness of the top ring plate  61 . But the holes  65  provide an additional design option for creating a desired pressure drop for the flow of vapor where a small but non-zero pressure drop may be imposed in a manner that impedes high velocities at the outside walls of the conduit  15  and distributor pipe  40  and thereby balance asymmetrically distributed velocities of vapor in such spaces. While it is desirable to obtain uniform velocity across the neck as the vapor enters the interior space of the reactor vessel  20 , this present invention is focused on making the velocity profile more symmetrically balanced around the axis of the neck. So, for each coaxial ring around the axis of the distributor pipe  40  at the bottom end thereof has a fairly consistent velocity of vapor all the way around that particular ring, and all such rings have fairly consistent velocity as compared to the same analysis before the vapor passes through the equalizer  50 . This allows that two different rings may have different velocities, but the variation is from one ring to another and not within a ring defined at any distance from the center axis of the distributor pipe  40 . 
         [0029]    Middle ring plate  71  is similarly mounted on top of the “X” shaped middle cross vanes  72 . Preferably, the middle ring plate  71  is also relatively flat, having a thickness similar to the top ring plate  61  with an outer diameter  71 A and an inner diameter  71 B. The middle ring plate  71  is smaller than the top ring plate  61  such that the outer diameter  71 A of middle ring plate  71  is less than the outer diameter  61 A of the top ring plate  61 . While the outer diameter  71 A of the middle ring plate  71  may be larger, about the same size as, or smaller than the inner diameter  61 B of the top ring  61  but it is preferred that the outer diameter  71 A of the middle ring plate  71  is about the same as or less than the inner diameter  61 B of the top ring plate  61 . In one preferred arrangement, middle ring plate  71  includes a series of small holes  75  to reduce total ring face area of middle plate  71 . 
         [0030]    Bottom ring plate  81  is similarly mounted to the top of the “X” shaped top cross vanes  82 . Preferably, the bottom ring plate  81  is also relatively flat, having a thickness like the top ring plate  61  and middle ring plate  71 . The bottom ring plate  81  has an outer diameter  81 A and an inner diameter  81 B. The bottom ring plate  81  is larger than the middle ring plate  71  such that the outer diameter  81 A of the bottom ring plate  81  is larger than the outer diameter  71 A of the middle ring plate  71  and actually where the inner diameter  81 B of the bottom ring plate  81  is about the same dimension as the outer diameter  71 A of the middle ring plate  71 . In various embodiments, the inner diameter  81 B of the bottom ring plate  81  is about the same dimension or less than the outer diameter  71 A of the middle ring plate  71 . In another further option, middle ring plate  71  includes a series of small holes  75  to reduce total ring face area of middle plate  71 . 
         [0031]    Each of the flange plate  51  and ring plates  61 ,  71  and  81  are sized and arranged to create an obstruction to vapor flow through the distributor pipe  40 . But the obstruction is intended and designed to impose a limited restriction or pressure drop so as not to alter the underlying design parameters of the reactor system, but only create a better velocity balance of the vapor inlet flow across the full transverse dimension of the generally cylindrical neck  21 . So, some pressure drop is desired and, ideally the pressure drop is at least 0.025 pounds per plate and less than about 0.25 pounds of pressure drop at each plate. It is believed that optimal results are created when the total pressure drop created by the equalizer  50  and distributor  40  is between 0.25 and 0.75 pounds. The number and diameter of the holes  65 ,  75  and  85  in ring plates  61 ,  71  and  81  that allow vapor to pass through each of the ring plates  61 ,  71 , and  81  effect the pressure drop along with the overall sizes of the plates including the thickness of each plate. It should also be recognized that the gas hourly space velocity of the vapor, the density and viscosity of the vapor and pressure of the vapor are generally established for a reactor system, but will also have a significant effect on pressure drop across the plates. 
         [0032]    Turning now to  FIG. 7 , where arrows show the expected flow into and through the generally cylindrical neck  21 . Arrow  91  shows the highest of all vapor velocities due to the bend B concentrating the flow along the outer wall of the conduit  15 . One of the functions of the equalizer  50  is to impede the higher velocity flows and the flow at arrow  91  is impeded by the flange plate  51  deflecting that flow back toward the center or axis of the generally cylindrical neck  21 . While the flange plate  51  would also impede flow at arrow  92 , but since flow in that part of the conduit  15  is slower, the flow of vapor is not expected to slow as much from its peak velocity as the flow of vapor at arrow  91  will slow from its peak velocity. Flows  93  nearer to the center or axis of the conduit  15  are not very impacted by the flange plate  51 . Each of the successive ring plates forces or causes flow of vapor to deviate around or be partially obstructed by the successive ring plates such that the only substantially flow path of nearly linear flow is through the center or along the axis of the distributor pipe  40 . Flow outside of about the center 20% to 25% of the cross sectional area of the distributor pipe  40  is at least partially obstructed to reduce or temper down the high velocity flows such that at the bottom of the distributor pipe  40 , the flow is generally equalized or caused to be more symmetrical. It should be noted that flows  95  and  96  are successively obstructed by the top and middle equalizer rings and that flow that ends up along the outer wall of the distributor pipe  40  such as indicated by arrows  101  and  102  have had some obstruction before it can get back to the outer wall. With all of these alterations of the flow without creating excessive back pressure or pressure drop, the performance of the reactor system is expected to be improved with longer run time, more efficient use of the catalyst, and higher productivity. 
         [0033]    The equalizer  50  is intended to enhance the performance of the distributor pipe  40 . However, the distributor pipe  40  includes a deflector  45  at the end thereof to further deflect the vapor outwardly and more smoothly to the peripheral ducts  25 . This arrangement is seen and believed to provide improved reactor performance for radial reactors of the type shown. 
         [0034]    The distributor pipe  40  includes a generally cylindrical wall  41  attached at the top to a flat plate  51  that is clamped between the two flanges  18  and  19  at the end of the feed conduit  15 . The generally cylindrical wall  41  includes slot type cutouts  43  or simply slots  43  to direct the vapor coming down the distributor pipe  40  out into the head space  24  of the reactor vessel  20 . As shown in  FIGS. 1, 6, 7 and 8 , a deflector  45  is attached to the bottom end of the distributor pipe  40 . The deflector  45  is a pie-plate shaped structure comprising a relatively flat bottom  47  that may be perforated or unperforated and with an up-turned rim  46  oriented to direct vapor emanating from slots  43  in the generally cylindrical wall  41  outwards and upwards in the head space  24  of the reactor vessel  20 . The up-turned rim  46  may be described as having the shape of a truncated cone where the point of the cone would be well below the bottom end of the distributor pipe  40 . The vapors directed in this manner, as shown by arrows  49 , carry forth along the wall of the reactor vessel  20  or, in other words, along shell  21  toward the peripheral ducts  25  in a more even and less turbulent progression than without the deflector  45 . The up-turned rim  46  may be established at an angle of from 10 degrees to 60 degrees from horizontal, but is generally preferred to be from 30 degrees to above 45 degrees from horizontal. The up-turned rim  46  may further include holes  48  to allow some vapor to pass through the up-turned rim  46  to balance eddy currents that may be created with higher velocity vapor or a higher angle up-turned rim. The use of the deflector  45  with the perforations  48  in the up-turned rim  46  also reduces the energy required to achieve an equivalent uniform vapor flow distribution when compared to throttling or reducing the size of the slots  43  in the distributor pipe  40 . The reduced energy and lower pressure drop reduces the operating cost for improved vapor flow distribution. 
         [0035]    The deflector  45  has a smaller diameter than the neck  22  but is wider than the distributor pipe  40 . The porosity of the deflector  45  is made with circular perforations arranged to maintain a symmetric vapor flow pattern around the deflector  45 . The size and density of the perforations may be varied to adjust pressure drop. In one embodiment the size of the perforations in the deflector  45  may be from ¼″ to 1″ in size. The porosity controls the fraction of the inlet flow to pass through the deflector  45  and consequently the fraction of redirected flow out to the wall of the reactor vessel  20 . 
         [0036]    It should be recognized that the combination of the equalizer  50  and the distributor  40  with the deflector  45  at the end thereof work together to get the vapors to the catalyst in a more even distribution into the catalyst with minimal pressure drop. As such, the total productivity and instantaneous productivity of the reactor system  10  and the load of catalyst will be more optimal. Total productivity includes considerations of run time where continued productivity is still satisfactory so as to suggest continued running without shutting down for loading and new batch of catalyst. 
         [0037]    In closing, it should be noted that the discussion of any reference is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application. At the same time, each and every claim below is hereby incorporated into this detailed description or specification as an additional embodiment of the present invention. 
         [0038]    Although the systems and processes described herein have been described in detail, it should be understood that various changes, substitutions, and alterations can be made without departing from the spirit and scope of the invention as defined by the following claims. Those skilled in the art may be able to study the preferred embodiments and identify other ways to practice the invention that are not exactly as described herein. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims while the description, abstract and drawings are not to be used to limit the scope of the invention. The invention is specifically intended to be as broad as the claims below and their equivalents.