U.S. patent application number 15/424043 was filed with the patent office on 2017-05-25 for method and system for improved reactant mixing and distribution.
This patent application is currently assigned to GTC Technology US LLC. The applicant listed for this patent is GTC Technology US LLC. Invention is credited to Michael J. BINKLEY, Ian G. Buttridge, SooWoong KIM.
Application Number | 20170144121 15/424043 |
Document ID | / |
Family ID | 47219151 |
Filed Date | 2017-05-25 |
United States Patent
Application |
20170144121 |
Kind Code |
A1 |
Buttridge; Ian G. ; et
al. |
May 25, 2017 |
METHOD AND SYSTEM FOR IMPROVED REACTANT MIXING AND DISTRIBUTION
Abstract
One aspect of the present invention relates to a mixing system
for use in a chemical-process column. The mixing system includes a
heavy-reactant mixing surface arranged perpendicular to a flow of
reactant through the chemical-process column. The mixing system
also includes an aperture formed in the heavy-reactant mixing
surface. A pre-distributor is coupled to an underside of the mixing
system and fluidly coupled to the aperture.
Inventors: |
Buttridge; Ian G.; (Garland,
TX) ; KIM; SooWoong; (Flower Mound, TX) ;
BINKLEY; Michael J.; (Glenn Heights, TX) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
GTC Technology US LLC |
Houston |
TX |
US |
|
|
Assignee: |
GTC Technology US LLC
Houston
TX
|
Family ID: |
47219151 |
Appl. No.: |
15/424043 |
Filed: |
February 3, 2017 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
13449122 |
Apr 17, 2012 |
9597650 |
|
|
15424043 |
|
|
|
|
61476494 |
Apr 18, 2011 |
|
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Current U.S.
Class: |
1/1 |
Current CPC
Class: |
B01J 2208/00849
20130101; B01J 8/0453 20130101; C10G 49/00 20130101; C10G 2300/202
20130101; B01J 2208/00938 20130101; B01J 8/008 20130101; B01J
2208/00929 20130101; B01J 2208/00902 20130101; B01J 8/0492
20130101; C10G 45/08 20130101 |
International
Class: |
B01J 8/04 20060101
B01J008/04; C10G 45/08 20060101 C10G045/08; B01J 8/00 20060101
B01J008/00 |
Claims
1. A method of mixing reactants in a chemical-process column, the
method comprising: introducing a heavy reactant to a mixing region
of the chemical process column; contacting the heavy reactant with
a heavy-reactant mixing surface; homogenizing the heavy reactant
within a mixing pot; and distributing the heavy reactant via a
pre-distributor.
2. The method of claim 1, comprising directing the heavy reactant
toward the mixing pot via a baffle.
3. The method of claim 1, comprising mixing the heavy reactant with
a vane disposed at an entrance to the mixing pot.
4. The method of claim 1, comprising mixing the heavy reactant via
at least one of a vane, a deflector, a baffle, or a static mixer
disposed within the mixing pot.
5. The method of claim 1, comprising: introducing a light reactant
to the mixing region of the chemical process column; directing the
light reactant through the heavy-reactant mixing surface via a
light-reactant duct; and mixing the light reactant via a vectoring
member fluidly coupled to the light-reactant duct.
6. The method of claim 5, wherein the vectoring member is arranged
proximate to the pre-distributor.
7. The method of claim 1, wherein the distributing comprises
directing the heavy reactant through a plurality of channels
fluidly coupled to the mixing pot, the plurality of channels having
a plurality of perforations formed therein.
8. The method of claim 1, wherein the homogenizing comprises
inducing turbulent mixing of the heavy reactant within the mixing
pot.
9. The method of claim 1, wherein the homogenizing removes
concentration and temperature gradients from the heavy reactant.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application is a continuation of U.S. patent
application Ser. No. 13/449,122, filed Apr. 17, 2012. U.S. patent
application Ser. No. 13/449,122 claims priority to U.S. Provisional
Patent Application No. 61/476,494, filed Apr. 18, 2011. U.S. patent
application Ser. No. 13/449,122 and U.S. Provisional Patent
Application No. 61/476,494 are each incorporated herein by
reference.
BACKGROUND
[0002] Field of the Invention
[0003] The present application relates generally to hydrotreating
processes and more particularly, but not by way of limitation, to
improved methods and systems for reactant mixing and distribution
in hydrotreating reactors.
[0004] History of the Related Art
[0005] Hydrotreating refers to a class of catalytic chemical
processes for removing impurities such as sulfur, benzene, or the
like from petroleum products such as, for example, gasoline,
kerosene, diesel fuel, and the like. The purpose of hydrotreating
is to reduce emission of pollutants that result from combustion of
petroleum products utilized in automotive vehicles, aircraft,
railroad locomotives, ships, gas or oil burning power plants,
residential or industrial furnaces, and other forms of fuel
combustion.
[0006] An example of a common hydrotreating reaction involves
removal of sulfur from various petroleum products. Such a
hydrotreating reaction is referred to as "hydrodesulfurization."
Hydrodesulfurization is of particular importance because sulfur,
even in low concentrations, may poison metallic catalysts such as,
for example, platinum and rhenium, that are used in refining
processes to upgrade an octane rating of petroleum products.
Furthermore, sulfur dioxide (SO.sub.2) results from combustion of
sulfur-contaminated petroleum products. SO.sub.2 is a
widely-recognized pollutant, which has well-known and wide-ranging
detrimental effects on the environment.
[0007] Another example of a common hydrotreating reaction involves
removal of benzene from petroleum products. In recent years, the
Federal government has specified maximum acceptable quantities of
benzene that may be present in petroleum products. Thus, refinery
operators are required to either capture or destroy benzene present
in petroleum products. Capture of benzene represents a substantial
capital investment for a refinery. Hydrotreating of benzene is a
substantially cheaper alternative and involves reacting a
benzene-contaminated petroleum product with hydrogen vapor
(H.sub.2) in the presence of a catalyst. As a result, benzene is
degraded into cyclohexane.
[0008] In an industrial hydrotreating unit, such as those found in
a refinery, hydrotreating takes place in a reactor column at
temperatures ranging from about 300.degree. C. to about 400.degree.
C. and pressures ranging from about 30 atmospheres to about 130
atmospheres. Typically, hydrotreating takes place in the presence
of a catalyst. Typically, the catalyst is in the form of generally
spherical pellets that are packed into various portions of the
reactor column known as packed beds.
[0009] In operation, reactants descend in a concurrent-flow manner
through the reactor column. In most cases, small gaps are present
between adjacent catalyst pellets thereby allowing passage of
reactants therethrough. The hydrotreating reaction occurs on a
surface of the catalyst pellets. In many cases, during operation,
reactants are consumed unevenly within the reactor column. Uneven
consumption of reactants gives rise to a concentration gradient.
The concentration gradient, in many cases, is also accompanied by a
temperature gradient across a cross-sectional area of the reactor
column. For this reason, reactor columns often include various
mixing and distribution devices.
[0010] U.S. Pat. No. 7,078,002, assigned to Shell Oil Company,
describes a mixing device for mixing fluids in a multiple-bed
downflow reactor. The mixing device includes a substantially
horizontal collection tray and a swirl chamber arranged below the
substantially horizontal collection tray for mixing liquid. The
swirl chamber has an upper end part that is in direct fluid
communication with an upper surface of the substantially horizontal
collection tray and an outlet opening at a lower end. A length of
the swirl chamber is at least 0.35 times its inner diameter. The
mixing device further includes a substantially horizontal
distribution tray beneath the swirl chamber. The substantially
horizontal distribution tray includes a plurality of openings for
downward flow of liquid and gas.
[0011] U.S. Pat. No. 7,052,654, assigned to ExxonMobil Research and
Engineering Company, describes a multi-phase mixing system for
distributing vapor and liquid across a downflow reactor. The mixing
system includes a collection tray for receiving vapor and liquid.
The collection tray includes a sub-region. The mixing system
further includes a mixing chamber positioned below the collection
tray and at least one outlet opening for downward passage of vapor
and liquid. The mixing system further includes a conduit extending
through the collection tray into the mixing chamber. The conduit
permits the flow of vapor and liquid from above the collection tray
and into the mixing chamber. The mixing system further includes a
vapor slipstream passageway extending through the upwardly
projecting sub-region for permitting flow of a vapor slipstream
from above the collection tray into the mixing chamber.
[0012] U.S. Pat. No. 7,045,103, also assigned to ExxonMobil
Research and Engineering Company, describes a distributor system
for distributing vapor and liquid across a downflow reactor. The
distributor system includes a collection tray for receiving vapor
and liquid and a mixing chamber positioned below the collection
tray. The mixing chamber has an outlet oriented to permit downward
passage of liquid and vapor from the mixing chamber. The
distribution system further includes a spillway extending through
the collection tray to permit downward passage of vapor and liquid
from above the collection tray into the mixing chamber. The
distribution system further includes a baffle connected to the
collection tray and extending downwardly therefrom into the mixing
chamber. The baffle is located between the outlet and the spillway
such that a baffle radius is greater than an outlet radius.
SUMMARY
[0013] The present application relates generally to hydrotreating
processes and more particularly, but not by way of limitation, to
improved methods and systems for reactant mixing and distribution
in hydrotreating reactors. One aspect of the present invention
relates to a mixing system for use in a chemical-process column.
The mixing system includes a heavy-reactant mixing surface arranged
perpendicular to a flow of reactant through the chemical-process
column. The mixing system also includes an aperture formed in the
heavy-reactant mixing surface. A pre-distributor is coupled to an
underside of the mixing system and fluidly coupled to the
aperture.
[0014] Another aspect of the present invention relates to a method
of mixing reactants in a chemical-process column. The method
includes introducing a heavy reactant to a mixing region of the
chemical process column and contacting a heavy reactant with a
heavy-reactant mixing surface. The method further includes
homogenizing the heavy reactant within a mixing pot. The method
further includes distributing the heavy reactant via a
pre-distributor.
BRIEF DESCRIPTION OF THE DRAWINGS
[0015] A more complete understanding of the method and system of
the present invention may be obtained by reference to the following
Detailed Description when taken in conjunction with the
accompanying drawings wherein:
[0016] FIG. 1 is a cross-sectional view of a reactor column
according to an exemplary embodiment;
[0017] FIG. 2A is a top isometric view of a mixing system according
to an exemplary embodiment;
[0018] FIG. 2B is an exploded perspective view of a heavy-reactant
mixing surface according to an exemplary embodiment;
[0019] FIGS. 3A-3H are detailed plan views of a central aperture
according to exemplary embodiments;
[0020] FIG. 4 is a cross-sectional view of a mixing system taken
across section line A-A of FIG. 2A according to an exemplary
embodiment;
[0021] FIG. 5 is a top plan view of a mixing system according to an
exemplary embodiment;
[0022] FIG. 6 is a bottom isometric view of a mixing system
according to an exemplary embodiment; and
[0023] FIG. 7 is a flow diagram of a process for mixing and
distributing a reactant according to an exemplary embodiment.
DETAILED DESCRIPTION
[0024] Various embodiments of the present invention will now be
described more fully with reference to the accompanying drawings.
The invention may, however, be embodied in many different forms and
should not be construed as limited to the embodiments set forth
herein; rather, the embodiments are provided so that this
disclosure will be thorough and complete, and will fully convey the
scope of the invention to those skilled in the art.
[0025] FIG. 1 is a cross-sectional view of a reactor column
according to an exemplary embodiment. In a typical embodiment, a
reactor column 100 includes an upper catalyst bed 102 disposed
above a lower catalyst bed 104. A feed device 107 and a primary
distributor 109 are disposed above the upper catalyst bed 102. A
mixing region 106, including a mixing system 108 and a secondary
distributor 110, is arranged between the upper catalyst bed 102 and
the lower catalyst bed 104. In a typical embodiment, the upper
catalyst bed 102 and the lower catalyst bed 104 are filled with a
plurality of generally spherical catalyst pellets (not explicitly
shown). In various embodiments, particularly in
hydrodesulfurization processes, the catalyst may include an alumina
base impregnated with, for example, cobalt (Co) and molybdenum
(Mo), known as a "CoMo catalyst." In certain other embodiments, a
catalyst containing a combination of nickel (Ni) and molybdenum
(Mo), known as a "NiMo catalyst," is utilized.
[0026] Still referring to FIG. 1, during operation, reactants are
introduced to the reactor column 100 via the feed device 107. For
example, in hydrodesulfurization processes, the reactants may
include a heavy reactant such as, for example, ethanethiol
(C.sub.2H.sub.5SH) and a light reactant such as, for example,
hydrogen vapor (H.sub.2). The reactants descend through the primary
distributor 109, through the upper catalyst bed 102, and react on a
surface of the catalyst pellets. The reactants enter the mixing
region 106 where the reactants pass through the mixing system 108
and the secondary distributor 110. The mixing system 108 blends and
homogenizes the reactants thereby removing concentration gradients
and temperature gradients resulting from uneven or partial reaction
of the reactants in the upper catalyst bed 102. The secondary
distributor 110 evenly distributes the reactants across a
cross-sectional area of the reactor column 100. After leaving the
mixing region 106, the reactants move to the lower catalyst bed 104
for further reaction.
[0027] FIG. 2A is a top isometric view of a mixing system according
to an exemplary embodiment. In a typical embodiment, the mixing
system 108 includes a heavy-reactant mixing surface 202, at least
one light-reactant duct 204 is disposed on the heavy-reactant
mixing surface 202, and a pre-distributor 206 disposed below the
heavy-reactant mixing surface 202. In a typical embodiment, the
mixing system 108 is oriented generally perpendicular to a flow of
reactants within the reactor column 100 (illustrated in FIG. 1).
The mixing system 108 is generally circular with a diameter that is
generally coextensive with an inner diameter of the reactor column
100. The heavy-reactant mixing surface 202 includes a plurality of
generally wedge shaped sections 208(1)-(8). A plurality of baffles
210(1)-(8) are arranged on the heavy-reactant mixing surface 202.
The plurality of baffles 210(1)-(8) are arranged generally
perpendicular to the heavy-reactant mixing surface 202.
[0028] FIG. 2B is an exploded view of the heavy-reactant mixing
surface 202. The generally wedge shaped section 208(1) includes a
body portion 201(1), a first flange 203(1) formed along a first
edge 211(1), and a second flange 205(1) formed along a second edge
213(1). The first flange 203(1) and the second flange 205(1) are
formed generally perpendicular to the body portion 201(1). The
generally wedge shaped sections 208(2)-(8) are similar in terms of
construction and operation to the generally wedge shaped section
208(1).
[0029] Referring to FIGS. 2A-2B, the plurality of generally wedge
shaped sections 208(1)-(2) are assembled such that the first edge
211(1) of the generally wedge shaped section 208(1), abuts the
second edge 213(2) of the generally wedge shaped section 208(2).
The first flange 203(1) abuts the second flange 205(2) to form the
baffle 210(1). Similarly, the plurality of generally wedge shaped
sections 208(2)-(3) are assembled such that the first edge 211(2)
of the generally wedge shaped section 208(2) is arranged to abut
the second edge 213(3) of the generally wedge shaped section
208(3). The first flange 203(2) abuts the second flange 205(3) to
form the baffle 210(2). The generally wedge shaped sections
208(3)-(8) are assembled in similar fashion thereby forming the
baffles 210(3)-(8). The plurality of generally wedge shaped
sections 208(1)-(8) are thus arranged into a generally annular
shape.
[0030] Referring again to FIG. 2A, a central aperture 212, defined
by the plurality of generally wedge shaped sections 208(1)-(8), is
disposed in an approximate center of the heavy-reactant mixing
surface 202. During operation, heavy reactant contacts the
heavy-reactant mixing surface 202. The heavy reactant is directed
towards the central aperture 212 by the plurality of baffles
210(1)-(8). Mixing and homogenization of the heavy reactant occurs
in the central aperture 212. In other embodiments, mixing systems
utilizing principles of the invention may include a different
number of generally wedge shaped sections. In still other
embodiments, mixing systems utilizing principles of the invention
may include a unitary mixing surface thereby omitting the generally
wedge shaped sections 208(1)-(8). In such embodiments, the baffles
210(1)-(8) may be coupled to the heavy-reactant mixing surface
through a process such as, for example, welding, soldering, or the
like.
[0031] FIGS. 3A-3H are detailed plan views of the central aperture
212 according to exemplary embodiments. Referring first to FIG. 3A,
a first vane 301 and a second vane 321 are arranged around a
perimeter of the central aperture 212 and disposed between adjacent
ones of the plurality of baffles 210(1)-(8). The first vane 301 and
the second vane 321 include a substantially right-angle section
302. The substantially right-angle section 302 disrupts flow of
heavy reactant entering the central aperture 212 thereby inducing
turbulent mixing of the heavy reactant.
[0032] Referring to FIG. 3B, a first vane 303 and a second vane 306
are arranged around the perimeter of the central aperture 212 and
disposed between adjacent ones of the plurality of baffles
210(1)-(8). The first vane 303 and the second vane 306 are curved
towards each other thus creating a plurality of nozzles 304. The
first vane 303 and the second vane 306, in combination with the
plurality of nozzles 304, disrupt flow of heavy reactant entering
the central aperture 212 thereby inducing turbulent mixing of the
heavy reactant.
[0033] Referring to FIG. 3C, a first vane 313 and a second vane 319
are arranged around the perimeter of the central aperture 212 and
disposed between adjacent ones of the plurality of baffles
210(1)-(8). The first vane 313 and the second vane 319 are curved
away from each other. The first vane 313 and the second vane 319
disrupt flow of heavy reactant entering the central aperture 212
thereby inducing turbulent mixing of the heavy reactant.
[0034] Referring now to FIG. 3D, a static mixer 305 is around the
perimeter of the central aperture 212. The static mixer 305 is
disposed between adjacent ones of the plurality of baffles
210(1)-(8). The static mixer 305 may include, for example, a
plurality of crimped sheets of material. The static mixer 305
induces turbulent mixing of the heavy reactant entering the central
aperture 212.
[0035] Referring to FIG. 3E, a plurality of vanes 307(1)-(8) are
arranged around the perimeter of the central aperture 212. The vane
307(1) is disposed between the baffles 210(1)-(2). The vanes
307(2)-(8) are arranged similarly. The vanes 307(1), 307(3),
307(5), 307(7) are curved in a direction opposite that of the vanes
307(2), 307(4), 307(6), 307(8). The plurality of vanes 307(1)-(8)
induces turbulent mixing of the heavy reactant entering the central
aperture 212.
[0036] Referring to FIG. 3F, a first vane 309 and a second vane 320
are arranged around the perimeter of the central aperture 212 and
disposed between adjacent ones of the plurality of baffles
210(1)-(8). The first vane 309 and the second vane 320 are arranged
generally parallel to each other and are curved in a similar
direction thus creating a stirring effect of the heavy reactant
entering the central aperture 212.
[0037] Referring to FIG. 3G, a vane 315 is arranged around the
perimeter of the central aperture 212. The vane 315 is disposed
between adjacent ones of the plurality of baffles 210(1)-(8). The
vane 315 is curved thus creating a stirring effect of the heavy
reactant entering the central aperture 212.
[0038] Referring to FIG. 3H, a vane 317 is arranged around the
perimeter of the central aperture 212. The vane is disposed between
adjacent ones of the plurality of baffles 210(1)-(8). The vane 317
includes a right-angle section 318. The right-angle section 318
disrupts flow of the heavy reactant thereby further inducing
turbulent mixing of the heavy reactant entering the central
aperture 212.
[0039] FIG. 4 is a cross-sectional view of the mixing system 108
taken across section line A-A of FIG. 2A. The at least one
light-reactant duct 204 is disposed through the heavy-reactant
mixing surface 202. The at least one light-reactant duct 204
includes an aperture 402 having a cover 404 disposed thereabove.
The aperture 402 is fluidly coupled to a riser 406 and is, thus,
positioned above the heavy-reactant mixing surface 202. The riser
406 is fluidly coupled to a vectoring member 408 disposed below the
heavy-reactant mixing surface 202. The vectoring member 408 may
include, for example, a nozzle, a tube, a vane, or any other
appropriate device as dictated by design requirements. The at least
one light-reactant duct 204 permits passage of the light reactant
from a region above the heavy-reactant mixing surface 202 to a
region below the heavy-reactant mixing surface 202. The vectoring
member 408 imparts velocity and turbulence to the light reactant
thereby improving mixing and homogenization thereof.
[0040] FIG. 5 is a top plan view of the mixing system 108. The
baffles 210(1)-(8) may be arranged at any angle with respect to a
vertical axis 527 and a horizontal axis 529. In the embodiment
shown in FIG. 5, a plurality of light-reactant ducts 204 are
arranged in a generally circular fashion around the central
aperture 212. In other embodiments, the at least one light-reactant
duct 204 may be arranged in any configuration as dictated by design
requirements. The at least one light-reactant duct 204 permits
passage of the light reactant from a region above the
heavy-reactant mixing surface 202 to a region below the
heavy-reactant mixing surface 202.
[0041] FIG. 6 is a bottom isometric view of the mixing system 108
according to an exemplary embodiment. The pre-distributor 206 is
coupled to an underside of the mixing system 108. The
pre-distributor 206 includes at least one channel 606 fluidly
coupled to a mixing pot 602. The mixing pot 602 is in fluid
communication with the heavy-reactant mixing surface 202 via the
central aperture 212 (shown in FIG. 2A). The mixing pot 602 is
disposed on a bottom surface of the mixing system 108 below the
heavy-reactant mixing surface 202. In various embodiments,
additional vanes, fins, tabs, or other turbulence-inducing features
may also be present within the mixing pot 602. A plurality of
perforations 604 are present in a bottom surface 605 of the mixing
pot 602. In a typical embodiment, turbulent mixing and blending of
the heavy reactant is induced upon entering the mixing pot 602.
Mixing and blending of the heavy reactant homogenizes the heavy
reactant thereby removing concentration and temperature gradients
that may be present due to partial or uneven reaction.
[0042] Still referring to FIG. 6, the at least one channel 606
extends outwardly in a radial fashion from the mixing pot 602. The
at least one channel 606 includes a plurality of perforations 608
formed therein. During operation, the at least one channel 606
distributes homogenized heavy reactant over a cross sectional area
of the reactor column 100 (shown in FIG. 1). In a typical
embodiment, the at least one channel 606 includes a generally
square or rectangular profile. However, in other embodiments,
alternative profile shapes such as, for example, round, triangular,
or polygonal could be utilized. In various embodiments, the at
least one channel 606 includes flanged or welded pipes. In various
embodiments, the at least one channel 606 may include any number of
channels. Furthermore, in various embodiments, the at least one
channel 606 may be arranged at any angle relative to each other or
to the horizontal axis 529 or the vertical axis 527.
[0043] FIG. 7 is a flow diagram of a process for mixing and
distributing reactants according to an exemplary embodiment. The
process 700 begins at step 702. At step 704 reactants including,
for example, a light reactant and a heavy reactant, enter the
reactor column 100, descend through the upper catalyst bed 102, and
enter the mixing region 106. At step 706, the heavy reactant
contacts the heavy-reactant mixing surface 202 of the mixing system
108. At step 707, the light reactant enters the at least one
light-reactant duct 204 and is directed beneath the mixing system
108. At step 708, the baffles 210(1)-(8) direct the heavy reactant
towards the central aperture 212. At step 709, the light reactant
exits via the vectoring member 408 such as, for example, nozzles,
tubes, vanes, and the like. At step 710, as shown in FIGS. 3A-3H,
in various embodiments, turbulent mixing and blending of the heavy
reactant is induced upon entering the central aperture 212. In a
typical embodiment, the mixing and blending homogenizes the heavy
reactant thereby removing concentration and temperature gradients
that may be present due to partial or uneven reaction.
[0044] Referring still to FIG. 7, at step 712, the heavy reactant
enters the mixing pot 602 where further blending of the heavy
reactant occurs. At step 714, a portion of the heavy reactant exits
the mixing pot 602 via, for example, the plurality of perforations
604 disposed on the bottom surface 605 of the mixing pot 602. At
step 716, remaining heavy reactant flows through all or a portion
of the at least one channel 606. At step 718, the remaining heavy
reactant exits the at least one channel 606 through the plurality
of perforations 608. Thus, the at least one channel 606 distributes
homogenized heavy reactant over a cross sectional area of the
reactor column 100. The process 700 ends at step 720.
[0045] The advantages attendant to the mixing system 108 will be
apparent to those skilled in the art. First, the mixing system 108
combines the functions of reactant mixing and reactant
pre-distribution into a single component thus allowing for cheaper
and less complicated assembly and maintenance. Moreover, the mixing
system 108 allows for increased catalyst volume or a smaller column
profile. In addition, as shown in FIGS. 3A-3H, the mixing system
108, induces turbulent mixing and blending of heavy reactant
entering the central aperture 212. Such turbulent mixing and
blending improves over designs where reactants are simply stirred
or swirled. Stirring reactants often does not induce turbulent
mixing and, as a result, often does not result in homogenized
reactants.
[0046] Although various embodiments of the method and system of the
present invention have been illustrated in the accompanying
Drawings and described in the foregoing Detailed Description, it
will be understood that the invention is not limited to the
embodiments disclosed, but is cable of numerous rearrangements,
modifications and substitutions without departing from the spirit
of the invention as set forth herein.
* * * * *