Apparatus for flow distribution in packed towers

Process tower vapor/liquid flow distributor and packing bed comprising a plurality of relatively thin corrugated layers stacked one atop the other. The corrugated sheets are disposed in face to face contact with respective corrugations inclined to the horizontal and facing one another for the countercurrent passage of vapor and liquid therethrough. At least two layers are utilized and rotationally offset for diverting the vapor liquid in two separate directions to effect maximum vapor liquid distribution for countercurrent fluid flow passing therethrough. An improved homogenous mixture of vapor/liquid within the process tower packing sections may thus be provided. The assembly affords optimal pressure drop characteristic while maximizing even vapor/liquid distribution into the packing regions. In this manner the distribution sections may be disposed throughout the process tower above and below each packing section, or in place of the packing section for distributing the descending liquid flow as well as the ascending vapor flow therethrough. This configuration maximizes the efficiency of the distribution thereacross and the homogenous mixture interaction therein.

BACKGROUND OF THE INVENTION 
1. Field of the Invention 
The present invention pertains to flow distributor system for vapor liquid 
contact towers and, more particularly, to a vapor/liquid distributor for 
columns incorporating counter-current vapor liquid flow therethrough. 
2. History of the Prior Art 
It is well known in the prior art to utilize various types of exchange 
columns in which a gas and a liquid come into contact with one another, 
preferably in a counter-current flow for purposes of mass or heat 
transfer, close fractionation and/or separation of feed stock 
constituents, and other unit operations. Efficient operation requires mass 
transfer, heat transfer, fluid vaporization and/or condensation, whereby 
one of the fluids can be cooled with a minimum pressure drop through and 
in a particular zone or zones of minimum dimensions defining the area and 
volume thereof. These are prerequisites of efficient operation and are 
necessary for close fractionation. For this reason counter-current flow of 
vapor and liquid within such exchange columns have become established 
methods of such vapor liquid contact in the prior art. The actual vapor 
liquid interface requires the utilization of a packing bed within the 
column. Liquid is then distributed atop the packing bed in the most 
feasible manner while vapor is distributed beneath the packing bed in the 
lower region of the tower. In this manner liquid trickling downwardly 
through the packing bed is exposed to the vapor ascending therethrough for 
vapor liquid contact and interaction. These aspects are more particularly 
set forth in an article entitled "Packed Column Internals" appearing in 
the Mar. 5, 1984 edition of Chemical Engineering authored by Dr. Gilbert 
Chen, one of the inventors herein. 
It is well established that the configuration of the packing bed determines 
the pressure drop, efficiency of the vapor liquid interface and the 
concomitant mass and energy transfer occurring in a process tower. The 
means for effective and even distribution of the vapor and the liquid on 
opposite ends of the packing bed as well as maintenance of that 
distribution therethrough are critical to an efficient operation. Only 
with efficient initial vapor and liquid distribution and the maintenance 
of said distribution throughout the packing bed, will homogenous mixing 
zones be created therethrough for maximizing the efficiency therein. 
Efficiency is readily convertible to cost of operation and production 
quality. For this reason, a myriad of prior art packing designs have been 
prevalent in conventional exchange columns. The efficiency of the packing 
is, however, limited to a large extent by the efficiency of the vapor and 
liquid distribution thereacross For example, failure of either vapor or 
liquid to evenly distribute over cross-sections of the packing effectively 
eliminates the utility of the part of the packing where there is poor or 
no distribution which in turn is directly proportional to the efficiency 
and cost effectiveness of the operation thereof. Packing bed depths are 
critical in establishing production criteria and operational costs and 
failure to evenly distribute vapor liquid and/or maintain homogeniety 
within the packing bed can lead to serious consequences, particularly in 
the petroleum refining industry and related areas. 
Conventional liquid distributors generally comprise a multi-orifice spray 
head adapted for dispersing liquid in the form of a spray atop the packing 
bed. In the utilization of dump packing wherein a plurality of randomly 
oriented packing elements are disposed within the exchange column, such a 
liquid distribution technique is sometimes effective. This is true 
particularly when high efficiency parameters are not of critical 
significance. However, in the event of high efficiency packing such as 
that set forth in U.S. Pat. Nos. 4,597,916 and 4,604,247; assigned to the 
assignee of the present invention, means for homogeneous liquid and gas 
distribution are of extreme importance. The cost of high density packing 
of the type set forth in the aforesaid patent applications commands 
attention to the vapor liquid distribution problem. Even small regions of 
non-homogenous interaction between said vapor and liquid is an expensive 
and wasteful loss not consistent with the utilization of high efficiency 
packing where space and homogeniety in vapor liquid interface is both 
expected and necessary for proper operation. High efficiency packing of 
the state of the art varieties as set forth and shown in the aforesaid 
U.S. patent applications requires counter-current vapor liquid flow 
through the channels defined by opposed corrugations of sheets disposed 
therein. If the initial liquid or gas distribution fails to enter a 
particular corrugation pattern, then precious surface area is lost in the 
high efficiency packing until the liquid and vapor are urged to migrate 
into and interact in the unfilled regions of the packing. Only by 
utilizing proper vapor and liquid distribution means may effective and 
efficient utilization of high efficiency packing as well as conventional 
dumped packing be assured. 
The development of systems for adequate vapor and liquid distribution in 
process towers has been limited as set forth above. In the main, it is 
known to discharge liquid in a more or less patterned spray for adequate 
liquid distribution and concomitantly to discharge gas in a turbulent 
configuration to provide adequate vapor distribution. Though generally 
effective in distributing some vapor and some liquid to most portions of 
the packing bed, uniform distribution thereacross is generally not 
obtained without more sophisticated distribution apparatus. For example, 
unless gas is projected into a myriad of contiguous areas beneath the 
packing bed with equal pressure existing in each area, the mass flow of 
vapor upwardly through the packing bed cannot be uniform. Random vapor 
discharge simply distributes unequal amounts of vapor across the lower 
regions of the packing bed but does not in any way assure equality in said 
distribution. Likewise the spray of liquid atop the packing bed though 
intended to be effective in wetting all surface areas often results in 
high concentrations of liquid flow in certain packing bed areas, depending 
on the spray device. Unfortunately, uneven liquid distribution generally 
occurs in the vicinity of the most even vapor distribution and vice versa. 
This is because vapor has had a chance to more evenly distribute through 
the packing bed prior to engaging the liquid distribution flow. It would 
be an advantage, therefore, to provide means for even liquid and vapor 
distribution prior to entry of said vapor and liquid into the packing bed 
and in a manner providing both a uniform spread of said liquid and vapor 
and a uniform volumetric distribution thereof. 
The present invention provides such an improved system of vapor liquid 
distribution through a sandwiching of two or more relatively thin layers 
of corrugated, perforated, high efficiency packing, the layers being 
angularly disposed one to the other. The multi-layer distributor packing 
is provided in a thin configuration relative to the diameter of the tower 
and fabricated from a plurality of corrugated sheets angularly inclined 
one to the other having apertures formed therein for the passage of vapor 
and/or liquid therethrough. When used in conjunction with a similar high 
efficiency packing bed, the corrugations of the vapor and/or liquid 
distributor are equal to and/or larger than the corrugations of the 
packing bed In this manner pressure drop is not adversely affected through 
the distributor and the advantages of effective uniform vapor and liquid 
distribution in a homogeneous flow are obtained. The angular orientation 
likewise causes sufficient lateral distribution to evenly distribute 
volumetric flow uniformly across the packing bed for both vapor and liquid 
interaction and heat and mass transfer Moreover, in this manner similar 
vapor liquid distributors may be utilized atop the packing bed for 
distribution of liquid flow, beneath the packing bed for distribution of 
ascending vapor flow therethrough and/or as part of the packing bed 
whereby maximum distribution would be achieved prior to engagement of the 
vapor and/or liquid in the packing bed in accordance with the principles 
of the present invention. 
SUMMARY OF THE INVENTION 
The present invention pertains to flow distribution systems adapted for 
uniformly distributing liquid and vapor in counter-current flow through a 
process tower. More particularly, one aspect of the invention comprises an 
improved vapor and liquid distributor for process columns of the type 
wherein vapor is injected into the column for ascension therethrough and 
liquid is dispersed atop the column for downward flow. Packing sections 
are disposed in the tower for facilitating the interaction of vapor and 
liquid passing in counter-current flow therethrough. The improvement 
comprises a flow distributor adapted for positioning above and below the 
packing section for the even distribution of liquid downwardly and of 
vapor ascending upwardly therethrough for the homogenous interaction 
therein. The distributor packing section comprises a plurality of thin 
layers of corrugated sheets relative to the tower diameter angularly 
oriented one to the other in face to face relationship. The plurality of 
layers are also rotationally oriented one to the other for bi-directional 
lateral dispersion and full distribution of the vapor and liquid passing 
therethrough. 
In another aspect the apparatus as set forth above includes in combination 
the process column packing comprising high density packing formed of 
corrugated sheets. The corrugations of each sheet are angularly oriented 
one to the other in face to face relationship. The distribution packing 
sheets comprise corrugations having a depth equal to or greater than the 
corrugation depth of the packing in the proper bed. The adjacent sheets of 
the distributor packing sections may also comprise corrugations oriented 
generally orthogonally one to the other for enhancing the lateral vapor 
liquid distribution therethrough. The sections of corrugated sheets 
generally have a thickness on the order of three inches and preferably 
between 1/2 to 1/3 of a standard structured packing section height. 
In yet another aspect, the invention includes the process tower vapor 
liquid distributor described above which comprises a plurality of 
corrugated sheets in face to face contact with opposed corrugations 
inclined oppositely one to the other. The corrugations receive a 
descending liquid flow concomitantly with an ascending vapor flow. A 
plurality of apertures may be formed therein and the distribution sections 
are assembled in at least two layers one atop the other, the layers being 
rotated relative one to the other for effecting bi-directional vapor and 
liquid distribution of fluids passing in counter-current flow therethrough 
A banding member may be provided for binding the first and second layers 
one to the other in the pre-selected rotational relationship. The layers 
may be positioned above, below, or as part of the packing bed for maximum 
vapor/liquid distribution. 
In yet a further aspect, the invention includes an improved method of 
imparting vapor liquid distribution within a process tower of the type 
comprising the steps of providing a generally vertical tower having means 
for ingressing the flow of vapor at the lower region thereof and means for 
ingressing a stream of liquid from the upper region thereof. A series of 
layers of packing arrays are disposed therebetween for receiving the 
descending flow of liquid and the ascending flow of vapor concomitantly 
therethrough. The arrays provide for thorough mass and heat transfer 
therebetween. The improvement comprises the steps of providing a vapor 
liquid distributor section above and below each grid array. The 
distributor sections include at least two layers of corrugated sheets in 
face to face contact with the layers being rotationally angled one to the 
other for imparting bi-directional vapor and liquid flow therethrough. 
Each layer is formed of a width to corrugation length ratio affording 
fractional lateral dispersion into the contiguous rotated layer and 
bi-directional, substantially equalizing flow distribution therethrough.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
Referring first to FIG. 1 there is shown a perspective view of a packed 
exchange column with various sections cut away for illustrating a variety 
of internals and the utilization of one embodiment of the packing system 
of the present invention. The exchange column 10 of FIG. 1 comprises a 
cylindrical tower 12 having a plurality of packing bed layers 14 disposed 
therein. A plurality of manways 16 are likewise constructed for 
facilitating access to the internal region of the tower 12 for placement 
of the packing beds 14. Vapor 15 is fed to the tower 12 through feedlines 
18 while liquid 13 is fed through feedlines 20, therein facilitating 
counter-current vapor-liquid flow through the packing beds 14. 
Still referring to FIG. 1 the exchange column 10 further includes a vapor 
outlet 26 disposed atop the tower 12 and a lower skirt 28 disposed in the 
lower region of the tower around a circulation pipe 30 coupled to a 
reboiler (not shown). A reboiler return conduit 32 is shown disposed above 
the skirt 28 for recycling vapor 15 therein upwardly through the packing 
layers 14. Reflux from condensers is provided in the upper tower region 23 
through entry conduit 34 wherein reflux liquid 13 is distributed 
throughout a liquid distributor 36 across upper packing bed 38. It may be 
seen that the upper packing bed 38 is of the structured packing variety 
wherein a distributor packing (described below) is disposed for liquid 
distribution. The regions of the exchange column 10 beneath the upper 
packing bed 38 are shown for purpose of illustration and include a liquid 
collector 40 disposed beneath a support grid 41 in support of the upper 
structured packing 38. A liquid redistributor 42 is likewise disposed 
therebeneath and an intermediate support plate 44 is provided in an 
alternative configuration of the type adapted for supporting random 
packing 14 of the ring or saddle variety, as representatively shown. A 
lower structured grid 46 is illustrated disposed beneath an alternative 
form of liquid distributor 48 comprising a plurality of troughs 49 adapted 
for dispersing the liquid thereacross in counter-current flow to the 
ascending vapor therebeneath. 
The column 10 is shown to include both random packing 14 of varying packing 
bed height as well as structured packing 14. The structured packing 
sections 14 are generally provided in established heights, such as 9.5 
inches to 12 inches. This is generally due to mechanical and/or 
manufacturing considerations and may vary. 
It may thus be seen from this figure that the counter-current configuration 
between the ascending vapor and the descending liquid is the subject of a 
plurality of critical design considerations including size/dimension 
ratios, liquid/vapor ratios, liquid cooling, foaming and the presence of 
solids or slurries therein. Corrosion is likewise a consideration of the 
various elements in the packed towers and the selection of the material in 
the fabrication of the tower internals is in many instances the results 
thereof. The anatomy of the packed column as shown in FIG. 1 is likewise 
described in more detail in the Gilbert Chen article referred to above and 
incorporated herein by reference. 
Referring now to FIG. 2 there is shown a diagrammatic, side-elevational, 
cross-sectional view of the exchange column 10 which is not drawn to 
scale. The tower column 12, or containment vessel, is adapted for the flow 
of liquid 13 downwardly from feedlines 20 secured in the upper end of said 
vessel. At the lower end of the vessel 12, vapor 15 is discharged from a 
supply line 18 for the counter-current flow, interaction mixing and mass 
heat transfer between the vapor and liquid. The interaction and mass/heat 
transfer occurs within the regions of the column 10 where packing 38 is 
disposed. The packing 38 as shown herein may be of any of a variety of 
types including dumped packing or structured high efficiency packing. High 
efficiency packing of the type comprising corrugated and perforated sheets 
provides excellent mass heat transfer as shown in the aforesaid U.S. Pat. 
No. 4,604,247. 
Still referring to FIG. 2, the distribution of liquid 13 and vapor 15 
within the vessel 12 is effected by flow distribution sections 128 secured 
at selected vertical positions therein. Flow distributer sections 128 of 
the present invention comprise two or more thin sections of corrugated and 
perforated sheets, relative to the tower diameter, disposed in angular 
relationship one to the other. These sections are generally 1/2 to 1/3 the 
conventional packing section heights and preferably in the order of 3 
inches. In the present embodiment, three corrugated layers 130, 131 and 
132 are disposed one atop the other to comprise each flow distributor 
section 128. Each layer or section 130, 131 and 132 is approximately 
one-third of a conventional packing section height and angularly rotated 
relative to the others for purposes of maximizing lateral distribution of 
vapor or liquid passing therethrough. The placement of distributor 
sections 128 is also shown in FIG. 1, above and below various packing 
sections 14 of packing beds 38. In this manner, flow distributors 128-128 
are disposed immediately beneath the liquid discharge head 20 (of any 
variety) for distributing the liquid 13 uniformly across the packing 38 
disposed in the upper end of the containment vessel 12. Likewise, a 
distributor packing section 128 is disposed beneath upper packing 38 for 
evenly distributing upwardly rising vapor thereto for homogeneous 
interaction within said packing. 
The intermediate region 134 of the containment vessel 12 may include a 
vapor liquid distribution assembly 136 of generally conventional design of 
the type generally utilized for such process columns 10. The utilization 
of the distribution packing 128 of the present invention further 
facilitates reduction in the necessary vertical height in region 134 that 
the intermediate vapor liquid distribution assembly 36 normally requires 
relative to the packing 38 disposed within the container vessel 12. 
As described in more detail below, the utilization of the relatively thin 
corrugated layers (1/2 to 1/3 of conventional thicknesses) assembled in 
accordance with the teachings of the present invention affords not only 
vapor liquid distribution but effective vapor liquid interaction. This is 
due in part to the fact that the distribution section is comprised of the 
very same type of corrugated apertured angulated material comprising 
structured packing sections as set forth above. By the provision of these 
sections in thicknesses which are thin relative to the overall diameter of 
the tower permits lateral dispersion of the liquid therein by engaging an 
underlying corrugated section oriented in an angular relationship thereto. 
The drawings described below illustrate the flow pattern and the 
homogenous distribution therethrough by the utilization of angulated 
corrugated sections having a reduced height. The distributor sections may 
be 2 inches to 8 inches thick, although sections on the order of three 
inches have proven most effective in a variety of tower diameters ranging 
from two feet to forty feet. The term relatively thin, as used herein, 
refers to a structured packing section which is of less height than is 
conventional for that type of construction and is also related to tower 
diameter. A relatively thin layer 130 may be only two inches thick in a 
two foot diameter tower and it may be eight inches thick in a forty foot 
diameter tower. In certain embodiments also discussed below, the 
relatively thin distributor sections may in themselves be utilized as 
packing bed sections 38. For this reason their utilization as distributors 
are given the same value and advantages as a high efficiency packing bed. 
In this manner effective packing bed height is actually increased by the 
utilization of the distributors of the distribution assembly of the 
present invention as compared to various prior art embodiments which are 
not vapor liquid interaction regions and which effectively necessitate a 
taller vessel 12 for equivalent packing bed height therein 
It may further be seen that as liquid 13 is redistributed in region 134 it 
is then passed through a flow distributor 128 disposed atop a lower 
packing section 126 which itself is secured atop an underlying flow 
distributor section 128 disposed atop the vapor discharge conduit 18. In 
this manner vapor 15 ascending in the containment vessel 12 is initially 
distributed through the angularly oriented layers 130, 131 and 132 prior 
to passage into an homogenous mixture with the descending liquid 13 in 
lower packing region 38. As stated above, the utilization of high 
efficiency packing necessitates even vapor liquid distribution for 
effective utilization therein 
Referring now to FIG. 3 there is shown an enlarged perspective view of the 
flow distributor packing 128 of the present invention. The three layers 
130, 131 and 132 are thus shown in enlarged, exploded detail to comprise 
sheets 161 with corrugations 162 and perforations 164. The corrugated 
sheets 161 are angularly oriented one to the other generally in accordance 
with the teachings of the aforesaid U.S. Pat. No. 4,604,247 assigned to 
the assignee of the present invention and referred to above. The sheets 
161 are relatively short in height for the purpose of reducing the overall 
vertical length of the distribution packing assembly 128 which saves 
height within the process column 10. A savings of height permits the 
placement of more packing 38 and higher efficiency and energy savings. As 
further shown herein each layer 130, 131 and 132 is concentrically aligned 
about an axis 140 during the stacking process and is turned relative to 
the adjacent packing layer. For example, upper layer 130 is constructed 
with a notional sheet axis 150 parallel to the various corrugated sheets 
161 which is rotated at an angle 170 relative to the underlying axis 151 
of layer 131. Likewise axis 151 of layer 131 is rotated at an angle 173 
relative to axis 152 of underlying layer 132. In this manner vapor or 
liquid passing through the various layers 130, 131 and 132 of the flow 
distributor packing region 128 is bi-directionally redirected for maximum 
efficiency and distribution and homogenous mixture therethrough. 
Still referring to FIG. 3, the assembly of the distributor packing 128 
preferably incorporates the utilization of a band 138 secured around the 
packing layers 130, 131 and 132. This assembly facilitates the handling 
and installation of the flow distributor 128 within the containment vessel 
12. Moreover, the utilization of band 138 forms a discrete package which 
may be easily handled and arranged therein. The rotational orientation of 
the packing sections 130, 131 and 132 is then secured by the band 138 
during shipping and installation. The flow distributor layers are thus 
packaged in an assembly capable of select positioning throughout an 
exchange tower. 
As shown in FIGS. 2 and 3 in combination, the construction and relative 
size of the packing layers 130, 131 and 132 as well as the corrugations 
formed therein is a function of the size of the containment vessel and 
other operational parameters. Each layer 130, 131 and 132 is preferably 
formed of a width to corrugation length ratio affording fractional lateral 
dispersion into the contiguous rotated layer and bi-directional, 
substantially equalizing flow distribution therethrough. The upper layer 
130 is comprised of corrugations 181, the length of which is substantially 
less than the width, or diameter 182 of the layer 130. In this manner flow 
therealong is angularly disposed from a first lateral position 183 a 
relatively short lateral span to position 184 formed along the bottom edge 
of the layer 130. At the point 184, descending fluid flow then engages a 
corrugation channel 185 formed in layer 131 which redirects said 
descending fluid flow in a second direction which is lateral to the axis 
150 of layer 130. In this manner, bi-directional fluid flow is established 
and only fractional lateral dispersion is provided into the contiguous 
rotated layers within the distributor packing to facilitate 
bi-directional, substantially equalizing flow distributon therethrough. 
Likewise a corrugation channel 187 beginning at upper corrugation point 
188 and terminating in lower corrugation channel point 189 of layer 131 
will abut and engage upper end 190 of corrugation channel 191 which 
terminates at a lower point 192 therebeneath. Corrugation channel 191 is 
provided at a lateral angle 173 relative to layers 131 and 132. This 
redirection of descending fluid flow is likewise re-directional and 
further shifts the fluid flow a fractional lateral distance across the 
flow distributor 128. The multiplicity of corrugations in the layers 130, 
131 and 132 then provide a relatively large number of lateral dispersion 
channels which extend a fractional distance relative to the width of the 
corrugation layers 130, 131 and 132. Such fractional lateral dispersion 
permits enhanced flow redistribution and equalization as compared to a 
conventional corrugated packing element whose corrugation channel length 
approximates and/or is on the same order of magnitude as the width 
thereof. In such configurations the flow is often channeled to the side 
wall of the packing section resulting in fluid accumulations which 
necessitates the flow distributor of the present invention. The layer 
width to corrugation length ratio affords the fractional lateral 
dispersion which is critically important in high efficiency packing 
systems for proper process tower operation. Likewise the angle of rotation 
between the layers and the placement of apertures therethrough further 
affords control as to the type of lateral flow distribution 
bi-directionality and flow equalization provided therein. It may be seen 
that two layers 130 and 131 rotated relative one to the other provide the 
aforesaid flow characteristics although a series of three layers has been 
shown to be effective in high efficiency packing configurations. By 
providing the corrugations of the distributor layers of a size equal to or 
greater than the size of the corrugations of the packing 38, pressure drop 
does not become a problem and the effective height of the column can be 
improved. 
Referring now to FIG. 4 there is shown a side-elevational cross-sectional, 
enlarged view of the flow distributor section 128 of the present invention 
illustrating a diagrammatical view of the flow of liquid therethrough. 
Liquid 13 descending downwardly within the vessel 12 flows at an angle 
through the corrugations of the distribution packing layer. Upper layer 
200 thus shows liquid flowing through a corrugation 201 as illustrated by 
arrow 202. Arrow 202 forms an angle relative to the horizontal and carries 
the fluid a distance 203 as shown herein. Distance 203 is relatively small 
compared to the diameter 205 of the vessel 12. In this manner the liquid 
is relatively quickly discharged onto an underlying distribution layer 207 
which is rotated relative to upper layer 200. The rotation as shown in 
FIG. 3 results in the descending liquid 13 entering a plurality of 
corrugated sections across the upper surface thereof (to be shown in more 
detail below). Arrow 208 thus illustrates the downward flow of liquid 13 
along a plurality of corrugated channels which cannot be seen in this 
diagrammatic representation. However, the discharge through the plurality 
of corrugated channels causes the liquid 13 to disperse along the lower 
surface 209 of section 207 to there engage a plurality of corrugated 
channels of underlying section 210. Flow arrows 211 represent the multiple 
flow patterns of liquid 13 discharging therefrom at an angle generally 
opposite to that of layer 200. This flow pattern will be explained in more 
detail below but provides an immense amount of distribution relative to 
conventional prior art packing due to the thin distributor section 
construction relative to the diameter 205 of the vessel 12. This 
diagrammatic representation further illustrates the bi-directional flow 
distribution and lateral dispersion of the liquid 13 descending 
therethrough. The same holds true for vapor 15 ascending upwardly therein 
which is not shown in more detail for purposes of clarity. 
Referring now to FIG. 5 there is shown a perspective view of three 
distributor layer inserts 200, 207 and 210 provided in an exploded 
configuration for illustrating the flow of liquid therethrough. The top 
layer 200 is shown to receive a first generally focused flow of liquid 13 
along a top surface thereof which flow of liquid is laterally dispersed in 
a somewhat narrow pattern and discharged from the bottom region thereof 
along a series of adjacent corrugated sheets 215. The second layer 207 
receives the narrow lateral dispersed flow of liquid 13 from the upper 
layer 200 which, due to the orthogonal orientation of the second layer 
relative to said upper layer, imparts fluid along the central region of 
each of the parallel corrugated members 215. Through bi-directional 
lateral dispersement the liquid 13 is thus discharged from the lower edge 
of the intermediate layer in a generally uniform pattern of streams 217 
emanating from numerous corrugation drip points 218 widely dispersed in a 
generally symmetrical pattern thereacross. These descending streams 217 
thus engage the third, orthogonally oriented layer 210, along the various 
corrugation paths of the upper surface thereof. Due to the even 
distribution of streams 217 the final discharge pattern 220 is not only 
uniform but of a more finite even flow therefrom as illustrated in the 
drawing which represents an actual photographic illustration produced 
under laboratory conditions. Thus a packing bed 38 disposed therebeneath 
receives an evenly distributed uniform flow thereacross for maximum 
efficiency in vapor liquid interaction. 
Referring now to FIG. 6A, 6B and 6C there is shown a top plan view of the 
three distributor packing layers 200, 207 and 210, respectively, 
diagrammatically illustrating the flow of liquid therethrough. The top 
layer 200 of FIG. 6A is shown to receive a concentrated flow of liquid 13 
along the top surface thereof through dots 221. The flow is laterally and 
bi-directionally dispersed through the adjacent corrugated plates 215 
(shown schematically) into the discharge pattern shown by x's 222 
therebeneath. The middle distributor packing layer 207 of FIG. 6B thus 
receives the lateral flow of liquid by dots 221. The middle layer 207 of 
this embodiment, is oriented 90.degree. relative to the upper layer 200 
whereby the corrugations run orthogonal to the corrugational alignment of 
said upper layer. For this reason the receipt of the lateral liquid flow 
is dispersed into the flow pattern shown by x's 222 widely spread across 
the surface of the middle layer. This wide flow pattern is received by the 
bottom layer 210 (as shown by dots 221 of FIG. 6C) which is itself rotated 
relative to the middle layer 207 and results in a more evenly dispersed 
flow pattern 220 from a greater number of drip points 218 from the 
corrugations due to the lateral bi-directional dispersion of the fluid 
therethrough. 
Referring now to FIG. 7 there is shown a perspective view of an alternative 
embodiment of the process tower of FIG. 1 illustrating the placement of a 
plurality of distribution layers 128 comprising an elongate flow 
distributor in place of a standard packing bed and vapor and/or separate 
liquid distributor. The utilization of a plurality of their vapor liquid 
distributor sections in a packed array 128 of the structured packing 
variety is an advancement over the prior art by utilizing the distributor 
configuration itself in a high efficiency, high density packing 
configuration. As set forth above, very little pressure differential or 
efficiency is lost by the utilization of the relatively thin configuration 
of the distributor packing arrays when used in a process tower. It has 
been shown in FIGS. 1-6 that the utilization of two or more relatively 
thin cross-sections having a height of at least one half to one third of a 
conventional packing section produces greater efficiency without separate 
distributors. It may also be used in a packing configuration. By utilizing 
the distributor layers in the packing configuration it is no longer 
necessary to use a separate vapor or liquid distributor. In this manner 
vapor or liquid distributors may be eliminated in the process column 10 as 
shown in FIG. 7. Maximum height efficiency is thus established, which is a 
critical goal of operation. The other aspects of the distributor column 
shown in FIG. 7 are illustrated for purposes of clarity in showing the 
various fluid flow and vapor ascension configurations typical of prior art 
and conventional process tower and fractionation technology. 
Referring now to FIG. 8 there is shown a plurality of vapor liquid 
distributors 128 disposed between high efficiency packing beds 38 for 
purposes of illustrating vapor and liquid flow in counter-current 
ascension and descension therethrough. The vapor liquid contact 
distribution sections 128 are disposed in direct counterflow communication 
with the packing bed 38 for purposes of supporting the same packing beds 
and for the effectual vapor liquid interaction therein. As has been shown 
experimentation and laboratory evaluation, supporting structure and/or 
other vapor liquid distribution paraphernalia have in certain instances 
been necessary in support of said vapor liquid interaction. However, the 
vapor liquid distribution mechanism 128 is shown to be sufficiently 
adaptable to a direct intersperse configuration as shown in FIG. 8 for 
purposes of high efficiency vapor liquid interaction in a fractionation 
tower constructed in accordance with the principles of the present 
invention as described above. 
It is thus believed that the operation and construction of the present 
invention will be apparent from the foregoing description. While the 
mkthod and apparatus shown and described has been characterized as being 
preferred, it will be apparent that various changes and modifications may 
be made therein without departing from the spirit and scope of the 
invention as defined in the following claims.