KR20000075884A - Downcomer for chemical process tower - Google Patents

Abstract

An improved downcomer for a vapor liquid contact tower is provided. Steel pipes are usually formed between semiconical walls and the walls of the tower. The outlet pipe is usually formed by the lower edge of the semiconical wall and the wall of the tower. The lower edge of the semiconical wall is generally a tray adjacent to the steel pipe as more liquid flows through the opposite end rather than the center of the outlet pipe. Closer to the wall of the tower at the outlet of the outlet, not at the opposite end of the outlet, to provide a substantially uniform flow across.

Description

DOWNCOMER FOR CHEMICAL PROCESS TOWER}

A distiller column is used to separate the desired components from the multicomponent stream. Successful fractionation in the column depends on intimate contact between the liquid phase and the gas phase. Some columns use vapor and liquid contact devices such as trays.

The trays described above are generally installed on support rings in the tower and have solid trays or decks with a plurality of openings in the "active" area. Liquid is directed from the tray onto the tray by vertical channels. This channel is called a galvanic tube. The liquid exits through similar streams of water across the active area. The position of the downcomer determines the flow pattern of the liquid. Vapor rises through the opening of the tray and contacts liquid moving across the tray. The liquid and vapor are mixed in the active zone and fractionated. Therefore, an important concern is the active area of the tray.

The sorting capacity of the tray is usually maximized further as the active or boiling area increases. Maximizing the use of tray active areas is an important consideration in chemical tower design. Tray areas that are inefficiently used for vapor-liquid contact can degrade tray sorting capacity and efficiency. Therefore, there is a need for a device and method designed to optimize the active area of a fractionation tray in a chemical treatment tower.

It is known that the difference in concentration between vapor and liquid is the driving force for carrying out mass transfer. The concentration difference can affect in many ways, in some cases, lowering the sorting efficiency. If a working pressure results in a vapor density of about 16.0 kg / m ³ (1.0 lbs / cu.ft) or more, there is a possibility that a certain amount of vapor bubbles are mixed or entrained with the stream inlet liquid. For example, if the working pressure increases due to an increase in vapor concentration, the descending liquid begins to absorb vapor as the liquid moves across the tray. This indicates much higher amounts of vapor bubbles mixed with or "spray entrained" with the liquid, beyond those normally combined with dissolved gases in accordance with Henry's law. This steam is not held tight and is released in the galvanizing pipe, and in fact the majority of the steam must be released, otherwise the galvanic pipe overflows and prevents successful tower operation.

Likewise, the exothermic reaction in the downstream produces steam from the equilibrium mixture, which is also released. In conventional trays, the released vapors flow into the flow ducts and obstruct the descending foamy vapor / liquid mixture. In many cases, these disturbances cause the tower to fail, causing it to overflow too early. Therefore, there is a need for an apparatus and method for easily releasing vapor entrained in liquid in a strong flow column of a chemical treatment tower.

The serious problem that manifests itself in this functional operation is that droplets entrain in rising steam. This phenomenon, which is substantially opposite to the vapor droplet entrainment described above, can hinder efficient vapor liquid contact. In one aspect, liquid droplet entrainment is a dynamic flow. The high velocity vapor flow can temporarily stop the descent of the droplets and prevent them from efficiently passing through the underlying foam mixing zone. In tower operation, it is particularly difficult to avoid this problem when a large amount of vapor flow is required in a direction opposite to the direction of substantially descending liquid flow. Accordingly, what is needed is an apparatus and method for reducing liquid entrained in steam in a chemical treatment tower.

As the steam rising through the processing column bypasses the active area of the tray, the tray efficiency is reduced. One area where steam can bypass the active area of the tray is a strong flow tube. The efficiency of the active area in the tray is reduced when the vapor destined for the active area of the tray accidentally passes through the strong flow tube. In addition, the vapor passing through the stream can accidentally reduce the flow of liquid through the stream and potentially cause the liquid to flow through the treatment column to stagnate. Accordingly, there is a need for an apparatus and method for reducing the amount of steam flowing through a strong flow pipe.

The efficiency of the active area in the tray is influenced by the flow of liquid across the active area. At the initial point of contact of the liquid from the downcomer to the tray, the flow of liquid is not a common flow characteristic that provides optimum efficiency of the active area of the tray. Accordingly, there is a need for an apparatus and method that aids in changing fluid flow characteristics from the downcomer to the active region of the tray. The present invention provides a method and apparatus for maximizing mass transfer efficiency in a chemical treatment tower.

FIELD OF THE INVENTION The present invention relates to a chemical process tower, and in particular, but not exclusively, to a steel tube assembly for maximizing efficiency in a trayed tower.

1 is a perspective view of a laminated column with several parts cut away to illustrate various tower interiors as one embodiment of a steel tube-tray assembly constructed in accordance with the principles of the present invention.

FIG. 2 is a partially enlarged perspective view of the steel pipe tray assembly of FIG. 1 with a portion of the tower cut away showing the structure of the steel pipe and tray of the present invention. FIG.

3 is a partially enlarged perspective view of the steel tube tray assembly according to FIG. 2 in the interior of the tower;

4 is a partially enlarged perspective view of the steel tube tray assembly of FIGS. 2 and 3 showing the principle of operation of the steel tube tray assembly.

5A is a partially enlarged plan view of one embodiment of the steel pipe tray assembly of FIGS. 2 and 3;

5B is a partially enlarged plan view of another embodiment of the steel pipe tray assembly of FIGS. 2 and 3;

5C is a partially enlarged plan view of another embodiment of the steel pipe tray assembly of FIGS. 2 and 3;

FIG. 6 is a diagrammatic top view of the prior art illustrating flow across a tray. FIG.

FIG. 7A is an enlarged fragmentary plan view of an embodiment of a steel tube fabricated in accordance with the principles of the present invention to maximize mass transfer efficiency of a chemical treatment tower; FIG.

7B is an enlarged fragmentary plan view of another embodiment of a steel tube manufactured in accordance with the principles of the present invention to maximize mass transfer efficiency of a chemical treatment tower.

7C is an enlarged fragmentary plan view of another embodiment of a steel tube manufactured in accordance with the principles of the present invention to maximize mass transfer efficiency of a chemical treatment tower.

FIG. 8 is a diagrammatic view, diagrammatically, showing a liquid flowing through a tray in accordance with the principles of the present invention to maximize mass transfer efficiency of a chemical treatment tower; FIG.

The present invention relates to the shape of a chemical treatment tower steel tube. In particular, one aspect of the present invention includes a steel flow tube disposed above a chemical treatment tower tray. The downcomer is formed by the wall region and the walls of the chemical treatment tower and has an outlet for the liquid to flow therefrom. The outlet of the steel pipe is formed by the lower edge of the wall area and the wall of the chemical treatment tower and has a central portion and opposing ends (hereinafter both ends). The lower edge of the wall region is closer to the wall of the chemical treatment tower at the center, not at both ends, so that more liquid flows through both ends rather than at the center of the outlet pipe exit to produce a more uniform liquid flow.

In another aspect of the invention, a discharge plate is disposed across the outlet of the downcomer, the discharge plate having a predetermined number of openings therethrough. The openings are formed at a size and spacing between the openings so that more liquid flows through the openings formed at both ends rather than at the center of the discharge plate to the tray inlet area to provide a uniform liquid flow across the top tray. In another aspect of the invention, the wall region comprises a semiconical wall tapered towards the outlet of the downstream pipe. In another aspect of the invention, the lower edge of the wall area comprises a smooth curved edge. In another aspect of the invention, the lower edge of the wall region has a plurality of straight lines connecting the ends one by one. In another embodiment, the present invention encompasses an improved method of mixing liquid and gas from a steel pipe of a treatment tower using a tray, which method utilizes a tray support located below the tray support area in a treatment column. Supporting the tray, and the lower edge of the wall area being centered closer to the wall of the chemical treatment tower at the center, not at both ends, so that more liquid flows through both ends of the stream, not at the center of the outlet. And forming a downcomer outlet having both ends, and positioning the downcomer on the tray such that liquid from the downcomer outlet approaches the flow of liquid across the rectangular tray.

BRIEF DESCRIPTION OF DRAWINGS For a more complete understanding of the invention and for the purposes and advantages of the invention, reference numerals are attached in the following description taken in conjunction with the accompanying drawings.

1 is a partial perspective view of a multi-layer cut-away tower or column cut away to show the use of one embodiment of the improved steel tube-tray assembly of the present invention and the interior of various towers. The exchange column 10 of FIG. 1 comprises a cylindrical tower 12 having a packing bed 38, 39 and a steel tube tray assembly 100 disposed therein and in accordance with the principles of the present invention. Top 12 of column 10 includes a skirt 28 that supports top 12. Multiple passageways 16 are fabricated to provide easy access to the area inside the tower 12. A stream vapor feed line or reboiler return line 32 is provided at the bottom of the tower 12 and a steam outlet or overhead line 26 is provided at the top of the tower 12. A reflux return line 34 is provided at the top of the tower 12 and a bottom stream discharge line 30 is provided at the bottom of the tower 12. A side stream draw off line 20 and a liquid side supply line 18 are also provided in the tower 12.

In FIG. 1, in operation, steam 15 is fed to tower 12 via return line 32 and liquid 13 is reflux return line 34 and side stream feed input supply line 18. It is supplied to the tower 12 through. Steam 15 flows upwardly through column 10 and finally exits tower 12 through steam outlet 26. The liquid 13 flows downwardly through the column 10 and finally exits the tower 12 via the side stream discharge line 20 or the bottom stream discharge line 30. In the downflow, as the liquid passes through the tray assembly 100 and the stacks 38, 39 of the column 10, the substances obtained by the vapor 15 are consumed in the liquid 13 and in the vapor 15. The materials obtained by the liquid 13 are consumed.

In FIG. 1 the upper laminate 38 is made of various laminates. The area of the exchange column 10 below the upper stack 38 shown for illustrative purposes includes a liquid collector 40 disposed below the support grid 14 supporting the upper stack 38. A liquid distributor 42 for redistributing the liquid 33 is similarly disposed below it. A second type distributor 42a shown below the cut line is disposed above the lower stack 39. The internal arrangement of the column 10 is only schematic and is provided with an arrangement of various elements therein.

2 and 3 are partial perspective views of the steel pipe tray assembly 100 of FIG. 1, respectively, shown at opposite angles relative to the tower 12. FIG. In this embodiment, the steel pipe tray assembly 100 includes a first tray 110 connected to the first steel pipe 120 and a second tray 130 connected to the second steel pipe 140. Trays 110 and 130 are generally flat panels with central active regions 111 and 131, respectively. The trays 110 and 130 are supported by the support rings 98 and 99 of the tower 12, respectively. The outlet weirs 112, 132 are disposed on the first and second trays 110, 130 adjacent to the streams 120, 140, respectively. The outlet weirs 112, 132 are preferably upright plates or strips welded to the flat panels of the trays 120, 140.

In Figures 2 and 3, the steel pipes 120, 140 define tapered semiconical walls 121, 141 from the outlet weirs 112, 132 of the trays 110, 130, which are directed downward to the inner surface of the tower 12. Have each. The walls 121 and 141 of the steel pipes 120 and 140 are preferably made of flat plates 121a-d and 141a-d welded to each other as shown in the figure. The actual structure of the steel tube can be changed in accordance with the principles of the present invention. For example, the zoned angular structures of the steel pipe sidewalls can be retrofitted with more or fewer steel pipe zones and arc or curved structures. The outlet pipe outlets 122, 142 are formed between the bottom of the walls 121, 141 and the inner surface of the tower 12. In one embodiment, the outlet pipe outlets 122, 142 are located directly above the tray support rings 98, 99 of the tower 12 and in fact have an open area embedded within the area directly above the tray support rings 98, 99. Have

2 and 3, the tray 130 has an inlet weir 133 located around the area immediately below the outlet tube outlet 122. The inlet weir 133 is preferably an upright plate or strip welded to the flat panel of the tray 130. In one embodiment, the inlet weir 133 has a vertical height that extends above the location of the downstream outlet 122. The lower part of the flow pipe 120 is welded to the inlet weir 133 and supported by the clip 134 bolted to the lower part of the flow pipe 130.

2 and 3, the tray 130 includes a plurality of vent chambers 135 disposed in an area of the tray 130 located on the opposite side of the inlet weir 133 from the outlet pipe outlet 122. . The vent chamber 135 has a plurality of openings 135a that allow vapor 15 to flow horizontally over the inlet weir 133.

In FIG. 4, the liquid 13 across the active region 111 of the tray 110 combines with the vapor 15 rising through the active region 111. The outlet weir 112 controls the flow of liquid 13 passing from the active region 111 of the tray 110 to the stream tube 120. Liquid 13 that flows over the outlet weir 112 of the tray 110 passes downward between the wall 121 of the strong flow pipe 120 and the inner wall of the tower 12. The liquid 13 exits the stream pipe 120 via the outlet 122 and is received on the tray 130 in the region between the inner wall of the tower 12 and the inlet weir 133.

In FIG. 4, once the level of liquid 13 collected in the area of the tray 130 between the inner wall of the tower 12 and the inlet weir 133 reaches the height of the inlet weir 133, the outlet pipe 122 Another liquid 13 exiting) causes the liquid 13 to pass over or overflow the inlet weir 133. A predetermined amount of vapor 15 passing upward in the column 10 flows through the opening 135a of the vent chamber 135 and combines with the liquid 13 overflowing over the inlet weir 133. Vapor 15 from vent chamber 135 causes horizontal liquid 13 to flow over the inlet weir across the active region 131 of tray 130. The liquid 13 passing over the active area of the tray 130 combines with the vapor 15 rising through the active area 131.

In FIG. 4, the combination of the liquid 13 across the active region of the tray 130 and the vapor 15 rising through the active region 131 generates bubbles 61. As mentioned above, the foam is a venting area, in which the phase of the liquid 13 is continuous. The foam 61 extends across the active area 131 of the tray 130 to a relatively uniform height as shown by the dotted line by a line 63. The length of the active area 131 of the tray 131 is governed by the distance between the inlet weir 133 and the outlet weir 132. The outlet weir 132 also controls the flow of bubbles 61 or liquid 13 from the active region 131 of the tray 130 through the stream tube 140, where fluid flows into the column 10. Exit tray 130 for subsequent processing.

FIG. 5A is a plan view of the steel tube 120 and the tray 110 shown in FIGS. 2, 3, and 4. The downstream pipe 120 is separated from the active region 111 of the tray 110 by the outlet weir 112. In the embodiment shown in FIG. 5A, the galvanic tube 120 is a corded galvanic tube characterized by a linear outlet weir 112 of the tray 110 that defines the edge of the tray 110 as cordal.

FIG. 5B is a plan view of an embodiment different from the tray 110 and the steel pipe 120 in FIGS. 2, 3, and 4; In the embodiment shown in FIG. 5B, the coffin 120 'is a swept coffin (or multi-cordal coffin) and is characterized by an outlet weir 112' with multiple zones. do. The outlet weir 112 'has first and second zones 112a' and 112b 'located in a copper corded fashion. The third zone 112c 'is arranged parallel to the first and second zones 112a', 112b 'but centered between the first and second zones 112a', 112b 'and into the tower 12. Is offset. The fourth and fifth zones 112d 'and 112e' of the outlet weir 112 'connect the first and second zones 112a' and 112b 'and the third zone 112c', respectively.

5C is a plan view of an embodiment different from the tray 110 and the steel pipe 120 shown in FIGS. 2, 3, and 4. In the embodiment shown in Fig. 5C, the downcomer 120 is defined by an outlet weir 112 ". The outlet weir 112 "

2, 3, 4, and 5A to 5C, since the outlet pipe outlet 122 is narrower than the upper region of the outlet pipe 120, the outlet pipe 122 region passes through the outlet pipe 120. Flowing liquid 13 accumulates. When the liquid 13 accumulates in the region of the outlet tube outlet 122, a dynamic seal occurs that prevents vapor 15 rising through the column 10 from flowing through the outlet tube 120 instead of the tray 10. The seals are formed from each other by the relative vertical height of the inlet weir 133 of the tray 130 and the outlet 122 with respect to the strong flow pipe 120. A pool of liquid 13 exiting the stream duct 120 is formed between the inner wall of the tower 12 and the inlet weir 133. When the vertical height of the outlet 122 with respect to the steel pipe 120 is located near or below the vertical height of the inlet weir 133 with respect to the tray 130, the outlet 122 is connected to the tray 130. It is submerged in the pool of liquid contained between the inlet weir 133 and the inner surface of the tower 12. The outlet 122 of the stream duct 120 rises over the column 10 because it is at or below the level of the pool of liquid pooled between the inlet weir 133 of the tray 130 and the inner surface of the tower 12. The vapor 15 is prevented from flowing through the flow pipe 120 and bypassing the tray 110.

2, 3, 4 and 5a to 5c, the tray 130 is supported on the top surface 130a of the tray 130 directly above the position where the support ring 98 engages the tray 130. Has a ring region 137. As a structural inhibitor, in general, the support ring region 137 of the conventional support ring cannot be used as an active region for the mixing of the liquid 13 and the vapor 15. (This feature is disclosed in U. S. Patent No. 5,547, 617, assigned to the assignee of the present invention). The tray 130 also includes a tray 130 in which liquid 13 from the downstream outlet 122 is first contacted with the tray 130. It also has a tray inlet area 138 located at a location on the top surface 130a of the side wall. Due to the flow of the liquid 13 from the downstream outlet 122, the tray inlet area 138 of the tray 130 cannot be readily used as an active area for mixing of the liquid 13 and the vapor 15. . Because the downcomer outlet 122 has an area retained above the tray support ring region 98, the tray inlet region 138 is in fact within the support ring region 137 of the tray 130. In order to incorporate the tray inlet area 138 of the tray 130 into the support ring area 137 in effect, the area of the tray 130 useful for use as the active area 31 is substantially within the support of the area of the tray 130. Increased over conventional tray assemblies that do not position or solve the tray inlet area.

2, 3, 4 and 5a to 5c, since the support ring 98 is a narrow band around the inner edge of the tower 12, the support ring region 137 of the tray 130 is a long narrow region. . In order for the tray inlet region 138 to be substantially within the support ring region 137, the steel tube outlet 122 should normally be longer than a conventional steel tube to accommodate the liquid 13 flowing through the steel tube 120. There is a need. However, as shown in the figure, the length of the steel pipe outlet 122 and the tray inlet area 138 of the corresponding tray 130 are useful for the inward tray active area 131 of the tray support ring area 137. It can be greatly changed within the tray support ring region 137 of the tray 130 without any effect on.

6 is a diagrammatic view of flow across a conventional tray. Here the conventional tray 950 is a round type with a conventional first stream of water which supplies liquid over the solid bottom panel or tray inlet area 952 and then over the inlet weir 946 towards the tray 950. It is shown as a tray. The second downcomer 954 carries liquid away from the tray 50 over the outlet weir 948. Multiple arrows 156 represent non-uniform flow 960 of liquid 913 across conventional tray 950 in a retrograde pattern, as indicated by recycle cell 958. The recycle cell is formed on both sides of the tray parallel to the flow direction of the liquid 913. The formation of these retrograde flow zones or recycle cells 958 reduces the efficiency of the tray. The recycle cell is the result of the recycle flow near the wall of the tower 912 and the back flow problem becomes more apparent as the diameter of the column increases. As the final accumulation effect and backflow from the recycle cell increases, the concentration difference drive for mass transfer between the opposite flow streams is reduced. Reducing the concentration differential driving force requires more contact and height conditions for a given separation in the column. Although back mixing is only one aspect of tray efficiency, reducing this provides other benefits at the same time.

FIG. 7A is a plan view of one embodiment of a steel tube fabricated in accordance with the principles of the present invention to maximize mass transfer efficiency in a chemical treatment tower. FIG. The downcomer 174 is separated from the active region 171 of the upper tray 170 by the outlet weir 172. The downcomer 174 is formed by the inner surface of the wall 11 of the tower 12 and the semiconical wall 176. Semiconical walls 176 are each formed from plates 176a-e connected to each other in a shape as shown herein. The downcomer 180 is formed by the curved lower edge 178 of the plates 176a-e and the inner surface of the wall 11 of the tower 12, respectively. The downcomer outlets 180 are each characterized by outlet portions 180a-e whose sizes increase from 180c (center) to 180a (end) and 180c to 180e (end). Thus, when lower edge 178 is formed from plate 176c to plate 176a and plate 176c to plate 176e, the lower edges 178 of plates 176a-b and 176d-e each form a wall ( Since it is located away from the inner surface of 11), more liquid 13 flows through the outlet portions 180a, 180b, 180d, 180e rather than the outlet portion 180c. The liquid 13 flowing through the stream duct 180 flows over the inlet weir 146 (FIG. 8) of the lower tray 216 toward the tray inlet region 152, as shown by a number of arrows 208. As a uniform flow is to flow across the lower tray 216. Uniform flow results in the liquid 13 entering the portion of the tray 216 located closest to the wall of the tower 12 rather than the center of the tray 216 (FIG. 8). Homogeneous flow essentially eliminates recycle cells or retrograde flow regions.

FIG. 7B is a top view of another embodiment of a steel tube fabricated in accordance with the principles of the present invention to maximize mass transfer efficiency in a chemical treatment tower. FIG. The downcomer 188 is separated from the active region 171 of the upper tray 170 by the outlet weir 172. The downcomer 188 is formed by the inner surface of the wall 11 of the tower 12 and the semiconical wall 190. Semiconical walls 190 are each formed from plates 190a-h connected to each other in a shape as shown herein. The downstream outlet 194 is defined by the zoned lower edge 192 of the plates 190a-h and the inner surface of the wall 11 of the tower 12, respectively. The downcomer outlets 194 are each characterized by outlet portions 194a-h that increase in size from the central portion 194 ′ to the 194a (end) and from the central portion 194 ′ to the end 194h. Thus, when the lower edge 192 is formed from the plate 190d to the plate 190a and the plate 190e to the plate 190h, the lower edges 192 of the plates 190a-c and 190e-h are respectively formed by the wall ( Since it is located away from the inner surface of 11, more liquid 13 is allowed to flow through the outlets 194a, 194b, 194c, 194f, 194g, 194h rather than the outlets 194d, 194e. Liquid 13 flowing through the flow tube 194 flows toward the tray inlet area 152 and above the inlet weir 146 (FIG. 8) of the lower tray 216 (FIG. 8) below the tray 170. Flow across the tray 216 in a uniform flow as shown by the number of arrows 208. Uniform flow is introduced into the portion of the tray 216 where more liquid 13 is located closest to the wall of the tower 12 and not near the center of the tray 216 and almost eliminates the recirculation cell or backflow area. The result is. Homogeneous flow essentially eliminates recycle cells or retrograde flow regions.

FIG. 7C is a top view of another embodiment of a steel tube fabricated in accordance with the principles of the present invention to maximize mass transfer efficiency in a chemical treatment tower. FIG. The downcomer 198 is separated from the active region 171 of the tray 170 by the outlet weir 172. The downcomer 198 is formed by the inner surface of the wall 11 and the semiconical wall 200 of the tower 12. Semiconical walls 200 are formed from plates 200a-f that are each connected to each other in a shape as shown herein. The outlet pipe outlet 204 is formed by discharge openings 204a-f formed in the discharge plate 202. The discharge plate 202 is a wall of the tower 12 from the lower edge of the plate 200a-f such that any liquid 13 exiting the flow pipe 198 can only be discharged through the discharge openings 204a-f. 11) extends to the inner surface. The downstream pipe outlet 204 is characterized by the size and number of outlet openings whose size and number increase from 204c to 204a and from 204d to 204f. Therefore, more liquid 13 is allowed to flow through the discharge openings 204a and 204b rather than the discharge opening 204c and through the discharge openings 204e and 204f rather than the discharge opening 204d. Liquid 13 flowing through the discharge openings 204a-f flows toward the tray inlet area 152 and above the inlet weir 146 (FIG. 8) of the tray 216 (FIG. 8) below the tray 170. Thereby flowing across the tray 216 in an effective proximity flow in a uniform manner in a generally rectangular tower as shown by a number of arrows 208. Uniform flow is the portion of the tray 216 where more liquid 13 is located closest to the wall of the tower 12 and not essentially the center of the tray 216, essentially removing the recirculation cell or the backflow area. Resulted in

8 is a diagram of the flow across the tray 216 for receiving liquid from the steel tube of the present invention after the liquid has been supplied to the tray inlet region 152 and over the inlet weir 146 of the tray 216. To show. Multiple arrows 208 show a uniform flow that promotes the interaction of liquid and vapor flowing back through tower 12 across tray 216 essentially removing the recirculation cell or backflow region.

Accordingly, the operation and structure of the present invention will become apparent from the above description. Although the methods and apparatus shown and described are embodied in good form, various changes and modifications can be made therein without departing from the spirit and scope of the invention as defined in the following claims.

Claims (26)

A device for facilitating increased interaction of liquids with vapors flowing back through a walled treatment tower, the device being disposed below the outlet weir and the outlet weir having a plurality of zones arranged in a multiple cord configuration. A flow pipe and a tray, the flow pipe having a flow pipe wall tapered downward from the flow pipe outlet and the outlet weir towards the wall of the flow pipe outlet and the treatment tower, the outlet pipe outlet being opposed to a central hole area and facing. And an opposite corner hole region is larger than the central hole region, and wherein the tray has an inlet region and a second tray region disposed below the outlet of the steel pipe outlet. 2. The apparatus of claim 1, wherein the galvanic wall is a semiconical wall. The apparatus of claim 1, further comprising a support ring for supporting the tray, wherein the inlet region is located above the support ring. The apparatus of claim 1 wherein the tray also includes an inlet weir separating the inlet region from the second tray region. 5. The apparatus of claim 4, wherein the inlet weir extends above the outlet pipe outlet. 5. The apparatus of claim 4, wherein the tray also includes a plurality of vent chambers disposed on a tray opposite the inlet area and adjacent to the inlet weir. A device for facilitating increased interaction of liquid with vapor passing back through a treatment tower with a wall, the device being disposed below the outlet weir and the outlet weir having an arc zone extending towards the wall of the tower. A flow pipe and a tray, the flow pipe having a flow pipe wall tapered downward from the flow pipe outlet and the outlet weir towards the wall of the flow pipe outlet and the treatment tower, the outlet pipe outlet being opposed to a central hole area and facing. And the opposite corner hole region is larger than the center hole region, and the tray has an inlet region and a second tray region disposed below the outlet of the steel pipe outlet. 8. The apparatus of claim 7, wherein the arcuate region of the outlet weir is semicircular shaped extending toward the wall of the treatment tower. 8. The apparatus of claim 7, wherein the galvanic wall is a semiconical wall. 8. The device of claim 7, further comprising a support ring for supporting the tray, wherein the inlet region is located above the support ring. 8. The apparatus of claim 7, wherein the tray also includes an inlet weir separating the inlet region from the second tray region. 12. The apparatus of claim 11, wherein the inlet weir extends above the outlet of the downcomer. 12. The apparatus of claim 11, wherein the tray also includes a plurality of vent chambers disposed on a tray opposite the inlet area and adjacent to the inlet weir. A device for facilitating increased interaction of liquid with vapor passing back through a walled process tower, the device comprising an outlet weir and a flow tube and tray disposed below the outlet weir, The tube has a flow pipe wall tapered downward from the outlet weir to the wall of the discharge plate and the treatment tower, the discharge plate has a central opposed end and a through opening and the opening of the discharge plate flows through the flow pipe. Having a size and spacing such that more liquid flows through the opening at the end of the discharge plate rather than at the opening in the center of the discharge plate, the tray having an inlet area and a second inlet disposed below the discharge plate of the stream. And a tray area. 15. The apparatus of claim 14, wherein the galvanic wall is a semiconical wall. 15. The apparatus of claim 14, further comprising a support ring for supporting the tray, wherein the inlet region is located above the support ring. 15. The apparatus of claim 14, wherein the tray also includes an inlet weir separating the inlet region from the second tray region. 18. The apparatus of claim 17, wherein the tray also includes a plurality of vent chambers disposed on a tray opposite the inlet area and adjacent to the inlet weir. A device for facilitating increased interaction of a liquid with vapor passing back through a process tower having at least one tray internally supported and including a tray inlet area and a tray outlet area, having a counterflow flow. A flow pipe and a discharge plate disposed over at least one tray, the flow pipe formed between the wall area and the wall of the treatment tower and having an outlet for the flow of liquid therefrom, wherein the flow pipe outlet is the tray. Disposed over the inlet area and formed by the lower edge of the wall area and the wall of the treatment tower, and having a central and opposing ends, the discharge plate is disposed across the outlet of the steel tube and has a central and opposing ends with a predetermined number of Through-holes are formed, the openings having more liquid in the discharge plate rather than the center of the discharge plate. To the opening than to the number of liquid through the tray inlet area formed on the opposite ends, it characterized in that the flow device is formed as a gap between the size and opening so as to flow uniformly across the tray. 20. The apparatus of claim 19, wherein the wall region comprises a semiconical wall tapered towards the outlet of the downcomer. 20. The apparatus of claim 19, wherein the bottom edge of the wall area comprises smooth curved edges. 20. The device of claim 19, wherein the lower edge of the wall region comprises a plurality of straight lines that connect end to end. In the method for mixing a liquid and gas discharged from the strong flow pipe on the tray in the chemical treatment tower, the method, Supporting the tray of the chemical treatment tower with the tray support under the tray support area of the tray, forming a steel tube between the wall and the wall area of the chemical treatment tower, and walling the outlet of the steel tube with a central portion and opposing ends. Forming between the lower edge of the area and the wall of the chemical treatment tower, forming a discharge plate having a central portion and opposing ends across the steel pipe outlet, and opposing ends of the discharge plate that are not the center of the discharge plate. Forming through the discharge plate a predetermined number of through-holes formed at a size and spacing between the openings to allow more liquid to flow through the openings formed therein, and the liquid from the outlet of the galvanic pipe uniformly across the tray. Position the discharge plate substantially above the tray support area to define a tray inlet area of the tray to allow The method comprising the step. 24. The method of claim 23 including forming a tapered semiconical wall and wall area to the outlet of the downcomer. 24. The method of claim 23 including forming the lower edge of the wall into smooth curved edges. 24. The method of claim 23 including forming the lower edge of the wall region into a plurality of straight lines connecting the ends together.