Abstract:
The invention relates to equalizing and distributing reactants more evenly across the interior space of a reactor vessel utilizing a combination equalizer and distributor at the inlet end that initially impedes with uneven flow rates of vapor and then directs the flow of vapor through a series of circumferential nozzles. The nozzles are physical spaced such that the first nozzle provides the reactants into the vessel to spread radially and broadly outwardly into the vessel and each successive circumferential nozzle to deliver reactants in a less broadly distribution or dispersion where the interior space is filled with reactants without broadly diverse velocities that may create hot spots within the catalyst bed.

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. 14/958,032, filed Dec. 3, 2015, and entitled “Inlet Distributor for Spherical Reactor”. Applicant claims benefit under 35 USC §120 for all three applications and 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]    There are many sizes and designs for reactors for converting reactants to desirable intermediates and final products. Chemical engineers expend 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 generally 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 such as where the reactants are vaporous and have higher velocities along the outside of a bend in the piping leading to the 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. 
         [0006]    Another common technique is to provide an inert support bed with a thick layer of inert support that create tortuous paths to the catalyst and causing mixing and back pressure to create a level of balance across the body of the reactor. 
         [0007]    What is desired is a technique for creating a balanced distribution of the reactants across a rector body without significantly enlarging the size of the reactor and without creating significant back pressure on the flow of reactants. 
       BRIEF SUMMARY OF THE DISCLOSURE 
       [0008]    The invention more particularly relates to a reactor inlet system arranged to be installed into a reactor vessel and receive vapor from a tubular delivery conduit and distribute the vapor into the reactor vessel for generally even flow through the reactor vessel wherein the reactor inlet system includes a generally hollow cylindrical body having an inlet end at a top thereof and an outlet end spaced from the inlet end at a bottom thereof that also includes a generally center axis and an interior wall with an equalizer section positioned generally within the generally cylindrical body at the inlet end and a distributor section positioned near the outlet end of the generally cylindrical body. The equalizer section includes a flange equalizer plate positioned generally at the inlet end of the generally cylindrical body and is arranged to minimally obstruct vapor entering the reactor inlet at a periphery of the tubular delivery conduit along with a top equalizer plate positioned within the generally hollow cylindrical body and spaced downwardly from the flange equalizer plate and spaced inwardly from the generally hollow cylindrical body to minimally obstruct vapor moving generally downwardly through the generally hollow cylindrical body nearer to the interior wall than to the generally center axis. A middle equalizer plate is positioned within the generally hollow cylindrical body and spaced downwardly from the top equalizer plate and spaced inwardly from the generally hollow cylindrical body and arranged to minimally obstruct vapor moving generally downwardly through the generally hollow cylindrical body between the interior wall and the generally center axis and closer to the generally center axis than the obstruction created by the top equalizer plate. A bottom equalizer plate is positioned within the generally hollow cylindrical body and spaced downwardly from the middle equalizer plate and spaced inwardly from the generally hollow cylindrical body and arranged to minimally obstruct vapor moving generally downwardly through the generally hollow cylindrical body nearer to the interior wall than to the generally center axis and further away from the generally center axis than the obstruction created by the middle equalizer plate. The distributor section includes a first deflector ring with an integrally attached first neck attached to but spaced from the outlet end of the generally cylindrical body such that a circumferential nozzle is defined between the deflector ring and the outlet end of the generally cylindrical body where the neck extends from the first deflector ring away from the generally cylindrical body. At least one additional deflector ring with an integrally attached additional neck is attached to but spaced from the first neck such that an additional circumferential nozzle is defined between the additional deflector ring and the first neck A deflector plate is attached to said additional deflector ring, but spaced from said additional neck to define a last circumferential nozzle such that the equalizer section of the reactor inlet system dampens asymmetrically distributed velocities of vapor entering the reactor inlet to provide the distributor section with a generally symmetrically balanced velocity profile across the generally cylindrical body and the distributor section distributes the flow of vapor outwardly and downwardly from the outlet end of the inlet system such that vapor flow is generally uniform across the reactor vessel into which vapor is arranged to be delivered. 
     
    
     
       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 elevation cross section of a spherical reactor showing an inventive equalizer, distributor and reactor fixed valve tray; 
           [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 a cross section of the first embodiment of the inventive equalizer and distributor; 
           [0013]      FIG. 4  is an elevation cross section of the first embodiment of the equalizer and distributor; 
           [0014]      FIG. 5  is an elevation cross section of the first embodiment of the distributor showing the aerodynamics of the equalizer and distributor; 
           [0015]      FIG. 6  is an elevation cross section of the first embodiment of the distributor showing some dimensional attributes of the equalizer and distributor; 
           [0016]      FIG. 7  is an elevation cross section of the equalizer with a second embodiment of the distributor; 
           [0017]      FIG. 8  is an elevation cross section of the equalizer with a second embodiment of the distributor showing the aerodynamics of the distributor; 
           [0018]      FIG. 9  is a perspective view of the equalizer in combination with a third embodiment of the distributor; 
           [0019]      FIG. 10  is an elevation cross section of the combination of the equalizer and third embodiment of the distributor focusing on the aerodynamics created for incoming vapor; 
           [0020]      FIG. 11  is a top view of the reactor fixed valve tray; 
           [0021]      FIG. 12  is perspective view of the reactor fixed valve tray; and 
           [0022]      FIG. 13  is a perspective view of an alternative installation where the valve tray is installed on the top of the outlet device sometimes called an elephant stool. 
       
    
    
     DETAILED DESCRIPTION 
       [0023]    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. 
         [0024]    As shown in  FIG. 1 , an example reactor system is shown generally indicated by the numeral  10  comprising a reactor vessel  12  that is shown having the shape of a sphere. The example reactor vessel  12  includes a catalyst bed  13  within the reactor intermediate from the inlet end  14  and the outlet end  18  and having inert materials positioned above and below the catalyst bed  13 . The example reaction vessel  12  receives reactants at the inlet end  14  via an inlet conduit  15  directing the vapor into the top of the reactor  12 . While it is noted that the illustrated reactor  12  is arranged to have the reactants flow from the top down through the catalyst to exit at the bottom, which is generally preferred, the invention may work equally well with reactors that are arranged to direct the flow from the bottom up or have a horizontal flow or have the flow in other orientations. Most reactors are top down or bottom up, but the other arrangements are possible. It should also be understood that although the reactor vessel  12  is near spherical, some reactors are also elongated with somewhat spherically shaped upper and lower portions and the present invention may be useful in all of these various reactor designs. Continuing with the description of the reactor system  10 , the products of the reaction are conveyed to the outlet end  18  at the bottom of the reactor where the products are conveyed away by an outlet conduit  19 . 
         [0025]    The inlet conduit  15  includes a bend B near the top of the reactor vessel  12  so as to turn and direct the vapor straight into the inlet end  14 . One of the problems addressed by the present invention is where the uneven distribution of vapor occurs in the top of the reactor vessel  12 . 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 inlet  14  or along the inside of the bend B. This problem is best illustrated in  FIG. 2  which shows a flow arrangement that is NOT desirable. Vapor moving along the directions indicated by arrow  15 A is moving much faster than the vapor flow indicated by smaller arrow  15 B. What would be desired is that flow in all directions across the head space above the catalyst bed  13  would be close to the same such as shown by intermediate arrow length  15 C. Thus, vapor flow in direction  15 A would be moderated or tempered down causing flow to increase in direction  15 B such that both are about the same velocity as in direction  15 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 very much. In some reactors, low velocity causes excessive coking. Ultimately, productivity of the reactor system  10  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. 
         [0026]    Another problem this invention addresses is to create a smoother flow of vapor from the inlet end  14  out across the width of the catalyst bed  13 . 
         [0027]    The invention comprises a combination equalizer and distributor  20  at the inlet to equalize the flow of vapor across the inlet  14  and then distribute the flow outwardly across the broad width of reactor vessel  12 . The combination equalizer and distributor  20  comprises an equalizer section  21  and a distributor section  51 . 
         [0028]    The equalizer section  21  is positioned near the top of the inlet end  14  to equalize the velocity of flow within the inlet end  14 . It is noted that while the vapor flow would preferably be consistent as measured transversely across the inlet  14 , it is suitable and likely that any velocity imbalance would be brought more into to a more symmetrically equalized arrangement such that the velocity is relatively equal all of the way around every hypothetical circle around the center or axis of the inlet end  14  while difference may exist from one circle ton another. So, it may be faster or slower at the center, but the velocity does not favor one side of the inlet  14  over another. 
         [0029]    Turning to  FIGS. 3-6 , equalizer section  21  ideally imposes minimal resistance of the flow of the vapor into the reactor vessel  12  so as to not alter the intended catalyst process while getting better distribution of the vapor to utilize the full size and catalyst load in the reactor vessel  12 . So, the key features of the equalizer section  21  are a flange plate  25  and three vertically spaced ring plates  30 ,  35  and  40  (that will be described shortly). 
         [0030]    The flange plate  25 , in addition to being a functional part of the equalizer section  21 , supports the entire combination equalizer and distributor  20  in place at the inlet end  14  of the reactor vessel  12 . With a relatively large diameter  25 A (see  FIG. 6 ) the flange plate  25  is pinched between the flanges of the inlet conduit  15  and the inlet end  14 . A generally cylindrical duct  22  is attached to the bottom side of the flange plate  25  to extend down through the inlet  14  and perhaps into the head space of the reactor  12  above the catalyst bed  13 . The flange plate  25  includes a generally circular center opening defined by diameter  25 B (see  FIG. 6 ) that is less than the inner diameter of the inlet conduit  15  and is clearly less than the inner diameter  22 B ( FIG. 6 ) of the duct  22 . The smaller dimension of the generally circular opening  25 A of flange plate  25  is to create an obstruction to the flow of vapors along the interior walls of the inlet conduit  15 . It is believed that the flange plate  25  creates a greater obstruction for higher velocity flows of vapor than it does for any lower velocity flows of vapor. As such, the flange plate  25  provides a first obstruction to begin to balance to velocity differences entering the inlet end  14 . 
         [0031]    Equalizer section  21  further includes a number of longitudinal vanes  28  ( FIG. 4 ) spaced around the duct  22  for supporting cross vanes  29 A,  29 B and  28 C ( FIGS. 3 and 4 ) which extend transversely across the duct  22 . The first set of cross vanes  29 A are top cross vanes  29 A which are positioned at a first position below the flange plate  51  by a distance  23 A ( FIG. 6 ). In the preferred arrangement, two cross vanes  29 A are attached by their ends to each of four longitudinal vanes  28  forming an “X” shape generally horizontal or transversely across the duct  22 . Similarly, the second set of cross vanes are middle cross vanes  29 B and are positioned at a second position below top cross vanes  29 A by a dimension  23 B ( FIG. 6 ) which may or may not be the same as  23 A. Again, in the preferred arrangement, middle cross vanes  29 B are attached at their ends to four longitudinal vanes  28 , but to the four longitudinal vanes  28  that are not attached to the top cross vanes  29 A. Also similarly, the third set of cross vanes are bottom cross vanes  29 C and are positioned below middle cross vanes  29 B by a distance  23 C ( FIG. 6 ) which may or may not be the same as either of  23 A or  23 B. Again in the preferred arrangement, bottom cross vanes  29 C are attached by their ends to four longitudinal vanes  28  which are the same four longitudinal vanes  28  that support the top cross vanes  29 A. All of the cross vanes  29 A,  29 B and  29 C are intended to support the spaced ring plates  30 ,  35 , and  40 , but not, by themselves, have much impact on the flow of vapor through the duct  22 . It should be noted that in some circumstances, such as for large diameter vessels or for 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  30 ,  35  and  40 . 
         [0032]    Top ring plate  30  is mounted on the “X” shaped top cross vanes  29 A. Preferably, the top ring plate  30  is relatively flat, having a thickness of less than 0.5 inches with an outer diameter  30 A and an inner diameter  30 B. Focusing especially on  FIG. 6 , the outer diameter  30 A is less than the inner diameter  22 B of the duct  22  and spaced away from the wall of duct  22  by an annular space  30 C. Ideally, the top ring plate  30  is a perfect circle with a perfectly circular opening in the middle that is also perfectly concentric to the circular shape of the duct  22  and the opening in the top flange plate  25 . The difference between the inner diameter  30 B and outer diameter  30 A gives a ring face area. A greater ring face area tends to increase the obstruction to vapor flow while a reduced ring face area similarly creates less obstruction to the vapor flow. In one preferred arrangement, top ring plate  30  includes a series of small holes  31  to reduce total ring face area. The amount of pressure drop created by top ring  30  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  30 . The holes  31  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 inlet conduit  15  and duct  22  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  12 , the equalizer section  21  is focused on making the velocity profile more symmetrically balanced around the axis of the inlet  14 . So, for each coaxial circle around the axis of the duct  22  at the bottom end thereof has a fairly consistent velocity of vapor all the way around that particular circle, and all such rings have fairly consistent velocity as compared to the same analysis that could be done in the conduit  15  before the vapor passes through the equalizer section  21 . This allows that two different circles may have different velocities, but the variation is from one circle to another and not within a circle defined at any distance from the center axis of the duct  22 . 
         [0033]    Middle ring plate  35  is similarly mounted on top of the “X” shaped middle cross vanes  29 B. Preferably, the middle ring plate  35  is also relatively flat, having a thickness similar to the top ring plate  30  with an outer diameter  35 A and an inner diameter  35 B. The middle ring plate  35  is smaller than the top ring plate  30  such that the outer diameter  35 A of middle ring plate  35  is less than the outer diameter  30 A of the top ring plate  30 . While the outer diameter  35 A of the middle ring plate  35  may be larger, about the same size as, or smaller than the inner diameter  30 B of the top ring  61 , it is preferred that the outer diameter  35 A of the middle ring plate  35  is about the same as or less than the inner diameter  30 B of the top ring plate  30 . In one preferred arrangement, middle ring plate  35  includes a series of small holes  36  to reduce total ring face area of middle plate  35 . 
         [0034]    Bottom ring plate  40  is similarly mounted to the top of the “X” shaped bottom cross vanes  29 C. Preferably, the bottom ring plate  40  is also relatively flat, having a thickness like the top ring plate  30  and middle ring plate  35 . The bottom ring plate  40  has an outer diameter  40 A and an inner diameter  40 B. The bottom ring plate  40  is larger than the middle ring plate  35  such that the outer diameter  40 A of the bottom ring plate  40  is larger than the outer diameter  35 A of the middle ring plate  35  and actually where the inner diameter  40 B of the bottom ring plate  40  is about the same dimension as the outer diameter  35 A of the middle ring plate  35 . In various embodiments, the inner diameter  40 B of the bottom ring plate  40  is about the same dimension or less than the outer diameter  35 A of the middle ring plate  35 . In another further option, bottom ring plate  40  includes a series of small holes  41  to reduce total ring face area of bottom plate  40 . 
         [0035]    Each of the flange plate  25  and ring plates  30 ,  35  and  40  are sized and arranged to create an obstruction to vapor flow through the duct  22 . 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 duct  22 . So, some pressure drop is desired. 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 also believed that optimal results are created when the total pressure drop created by the equalizer section  21  is between 0.25 and 0.75 pounds, total. The number and diameter of the holes  31 ,  36  and  41  in ring plates  30 ,  35  and  40  that allow vapor to pass through each of the ring plates  30 ,  35  and  40  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. 
         [0036]    Turning now to  FIG. 5 , where arrows show the expected flow into and through the duct  22 , the highest vapor velocities are expected to be concentrated at the outer wall of the conduit  15  due to the overall vapor velocity and to bend B turning the vapor into the top of the reactor vessel  12 . As shown, the equalizer section  21  impedes the higher velocity flows around the outside of the conduit  15  allowing flow to go through the center of the duct  22  less impeded. The flange plate  25  forces the vapor flow toward the center of the duct  22  and each of the successive ring plates forces or causes flow of vapor to deviate around or be partially obstructed by the successive ring plates  30 ,  35  and  40  such that the only substantially flow path of nearly linear flow is through the center or along the axis of the duct  22 . Flow outside of about the center 20% to 25% of the cross sectional area of the duct  22  is at least partially obstructed to reduce or temper down the high velocity flows such that near the bottom end of the duct  22  causing the flow to be generally equalized or caused to be more symmetrical. With these alterations of the flow of vapor without creating excessive back pressure or pressure drop, it is expected that the performance of the reactor system  10  will be improved with longer run time, more efficient use of the catalyst, and higher productivity. 
         [0037]    The equalizer section  21  is intended to enhance the performance of the distributor section  51 . So, turning now to the distributor section  51 , the vapor flowing into the interior of the reactor vessel  12  is to be spread out and preferably evenly dispersed across the head space of the reactor vessel  12  above the catalyst bed  13 . The distributor section  51  has a configuration that imposes a very modest or low back pressure on the flow of the vapor and, at the same time, splits and directs the flows of the vapor in a manner that more evenly disperses the vapor. In a first embodiment of the distributor section  51 ,  FIGS. 3, 4 and 5  show the distributor section  51  being positioned below the equalizer section  21  at the base end of the duct  22  and which includes a series of circumferential or radial nozzles to split and direct flows. The radial nozzles are indicated at  54 ,  64 ,  74  and  84 . 
         [0038]    Focusing on  FIG. 3 , longitudinal vanes  28  support a first perforated deflector ring  52  at a position spaced from the bottom end of the duct  22 . The first perforated deflector ring  52  has a large, generally circular opening in the middle thereof and a generally circular outer diameter that is about the same as the diameter of the duct  22 . The generally uniform spacing from the end of the duct  22  to the perimeter of the first perforated deflector ring  52  defines the first radial nozzle  54 . The first perforated deflector ring  52  is also relatively thin compared to its diameter with holes  53 . The first perforated deflector ring  52  is preferably constructed from flat sheet metal stock with holes punched through from top to bottom. The first perforated deflector ring  52  is intended to reduce the area of the duct  22  by about 5% to 20% (but more preferably between 10% and 15%) forcing a first portion of the vapor out of the distributor section  51  along the wall of the reactor vessel  12  at the highest portion of the open headspace above the catalyst bed  13 . 
         [0039]    In particular, first perforated deflector ring  52  provides some modest resistance to the flow of reactants into the reactor vessel  12  and divides the flow within the duct  22  into two large flow paths and a plurality of smaller flow paths. The first large flow path being through the center of the perforated deflector ring  52  and the second large flow path being through the radial nozzle  54  around the perimeter of the first perforated deflector ring  52 . The smaller flow paths are through the numerous holes  53 . A first cylindrical neck  55  is attached to the inner diameter of the first perforated deflector ring  52  to extend a short distance below the first perforated deflector ring  52 . A series of stanchions  56  are attached vertically along the inside of the first cylindrical neck  55  and arranged to extend downwardly beyond the lower edge of the generally cylindrical neck  55  for supporting a second perforated deflector ring  62 . The second perforated deflector ring  40  is constructed in a manner similar to the construction of the first perforated deflector ring  52  where it is generally flat with through holes  63 . The outer diameter of the second perforated deflector ring  62  is slightly less than the diameter of the generally cylindrical neck  55  and the inner diameter provides for a rather large circular opening to allow most of the reactants flowing down through the distributor section  51  to continue to flow downwardly. The second perforated deflector ring  62  reduces the original area of the duct  22  by another 5% to 20%. 
         [0040]    The second perforated deflector ring  62  is positioned in a similar manner below the first cylindrical neck  55  to form the second radial nozzle  64  by being attached to the stanchions  56 . The outer edge of the second perforated deflector ring  50  is slightly smaller than the inner diameter of the first neck  45 , and like the first perforated deflector ring  52 , the second perforated deflector ring  62  includes a second cylindrical neck  65  attached along the inner dimension (inner diameter) of the second perforated deflector ring  62 . 
         [0041]    A third perforated deflector ring  72  is positioned in a similar manner below the second perforated deflector ring  62  and continues a stair step pattern of reducing diameters with generally circular central openings and with successive radially oriented nozzles of reduced diameter along the periphery of the distributor section  51 . As before, the third perforated deflector ring  72  is spaced from the lower edge of the second neck  65  defining the third radial nozzle  64 . Again, the outer edge of the third perforated ring  72  is slightly smaller than the inner diameter of the second neck  65 . 
         [0042]    While additional deflector rings may be incorporated into the design, two three or four are generally preferred, but ultimately, the bottom of the deflector section  51  is defined by a deflector plate  82 . Deflector plate  82  is mounted to the third deflector ring  72  in a manner similar to the deflector rings  52 ,  62  and  72 . A third neck  75 , having a generally cylindrical design, is attached to the inner edge of the third perforated deflector ring  72  and arranged to extend further into the reactor vessel  12 . Stanchions  76  are attached to the inner surface of the third neck  75  and arranged to extend below the lower edge of the third neck  75 . The deflector plate  82  being spaced below the lower edge of the third neck  75  defines the fourth generally radial nozzle  84 . 
         [0043]    The deflector plate  82 , similar to the deflector rings  52 ,  62  and  72 , has through holes  83  to allow reactants to pass down through the middle of the distributor section  51  and enter into the middle of the reactor vessel  12 . However, as shown in  FIG. 5 , the radial nozzles direct a significant portion of the reactants radially outward, or with a significant radially outward direction component along with some downward direction of flow with the through holes  53 ,  63 ,  73  and  83  to permit a smaller amount of flow to fill in between the primary flows through the nozzles  54 ,  64 ,  74  and  84 . 
         [0044]    There are many variations on the preferred arrangements for the distributor section  51 . The drawings show three perforated deflector rings, however, it should be understood that the invention may comprise two deflector rings, three deflector rings, four deflector rings and even more perforated deflector rings, although between two and four are preferred. 
         [0045]    In  FIG. 7 , another arrangement of the distributor section  51  is shown using the same numbering as in  FIGS. 3-6 , but adding “100” so that the second embodiment of the distributor section has the number  151 . In this second arrangement, the generally cylindrical duct  122  has a more complex form with a first cylindrical section  122 A connected to an inverted conical section  122 B forming a reducing cross section for the distributor section  151  and then continuing with a smaller, but generally cylindrical second cylindrical section  122 C. In this arrangement, the first perforated deflector ring  152  has an outer diameter that is larger than the diameter of the second cylindrical section  122 C. As such, the first circumferential nozzle  152  is oriented to provide a much more radial orientation to the flow of reactants entering the reactor vessel  12  than the first circumferential nozzle  54  in the first embodiment of the distributor section  51  perhaps along with some upward component direction of flow. Similarly, the second perforated deflector ring  162  has an outer diameter that is slightly larger than the diameter of the first neck  155 . As such, the second circumferential nozzle  154  also provides a more radial orientation to the flow of the reactants than the second radial or circumferential nozzle  54  in the first described embodiment although it should appear from the drawings that it will not impose as much of an upward flow as the first circumferential nozzle  142  of this embodiment. The third circumferential nozzle  174  is constructed and oriented in a manner very comparable to the circumferential nozzles of the first described embodiment, however, the last circumferential nozzle  184  has a much more axial orientation to due to the deflector plate  170  being smaller than the third neck  175  and with the deflector plate  182  being in closer vertical proximity to the bottom edge of the third neck  175  than the deflector rings are vertically spaced from the collars above. In this arrangement, each successive circumferential nozzle directs the flow of reactants radially outwardly and somewhat upwardly nearest the top of the reactor vessel  12  and in successively and progressively downward angles as shown in  FIG. 8 . 
         [0046]    A third variation of the distributor section is shown as  251  in  FIGS. 9 and 10 . This embodiment includes an aspect where the support structure for the equalizer and distributor sections is arranged on the outside of the generally duct  22  and along the outside of the deflector rings and necks. The longitudinal vanes and stanchions are replaced by oversized braces  224 . The first perforated deflector ring  252  of this third embodiment, similar to the first deflector ring  152  in the second embodiment, has a larger diameter than the generally cylindrical duct  22  and thereby forms a first circumferential nozzle  254  that provides some portion of upwards or backwards flow while primarily delivering the vapor in a very radial orientation into the reactor vessel  12 . Focusing on  FIG. 10 , like the distributor section  151  of the second embodiment, the successive circumferential or radial nozzles have a progressively more downward orientation. In this third embodiment, the through holes  283  in the deflector plate  282  are larger than the through holes through the deflector rings to allow more of the reactants to flow through the deflector plate  282 . At the same time, the last or fourth circumferential nozzle  284  in the third embodiment is oriented more radial and less axial than the last or fourth circumferential nozzle  184  of the second embodiment due to the larger holes  283 . Another noteworthy difference is that the necks  255 ,  265 , and  275  are slightly longer and are also perforated in this third embodiment. While the majority of the reactants are passing through the circumferential nozzles, flow is also emanating from the numerous through holes in the deflector rings, necks and deflector plate. 
         [0047]    In conjunction with the vapor handler  20 , one aspect of the present invention is to make sure that the vapor flow, and eventually the products, is distributed across reactor vessel  12  as evenly as practical by using a fixed valve tray  17  positioned under the catalyst bed, but on top of the inert material. The fixed valve tray  17  is constructed of a generally circular plate having the diameter to match the portion of the reactor vessel  12  at the level to which it is to be installed. The fixed valve tray  17  includes spaced apart openings  17 A. As seen in  FIGS. 11, 12 and 13 , the openings are formed to allow flow of products but prevent passage of the catalyst. With an even spacing across the fixed valve tray  17 , velocity differences across the width of the reactor vessel  12  would be suppressed by the size and spacing of the openings so as to restrict the localized rate at which the products may leave the catalyst bed  13 . This provides another basis for forcing a more balanced rate of flow through the reactor vessel  12 . 
         [0048]    As seen in  FIG. 13 , the flow may also be altered to reduce a higher velocity flow through the center of the catalyst bed  13  and thereby gain more balanced flow across the width of the catalyst bed  13  by using a plate similar to the valve tray installed at the top of the outlet of the reactor vessel  12  to prevent the flow from taking the most direct path down the middle of the reactor vessel  12 . In this location, sometimes described as an elephant stool, an open mesh-like material surrounds the perimeter that is less restrictive of flow while the top surface is more restrictive of flow. 
         [0049]    It should be recognized that the combination of the equalizer section  21  and the distributor section  51  with the deflector  17  at the end thereof, can work together to get the vapors to the catalyst in a more even distribution into the catalyst bed  13  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. 
         [0050]    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. 
         [0051]    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.