WO2000010696A1 - Tray contactor with same-direction liquid flow - Google Patents
Tray contactor with same-direction liquid flow Download PDFInfo
- Publication number
- WO2000010696A1 WO2000010696A1 PCT/US1998/017339 US9817339W WO0010696A1 WO 2000010696 A1 WO2000010696 A1 WO 2000010696A1 US 9817339 W US9817339 W US 9817339W WO 0010696 A1 WO0010696 A1 WO 0010696A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- tray
- liquid
- vapor
- comprised
- trays
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
- B01D3/166—Heating and/or cooling of plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
- B01F23/2322—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles using columns, e.g. multi-staged columns
Definitions
- the invention is directed toward multistage vertical tray-type vapor- liquid contactors which find use in a variety of equipment and industrial processes such as fractional distillation, absorption, stripping, mixing, and partial condensation (dephlegmation).
- the diameter is determined by the flooding limitation, i.e., the loading.
- the overall height is determined by the tray efficiency and height of a tray. Tray height is related to the point efficiency and froth height, which are interrelated, and are controlled by vapor injector geometry and weir height. Tray pressure drop is comprised of the vapor injector drop plus the tray liquid head.
- the energy demand is determined by the reboil requirement for above-ambient contactors, and by the reflux requirement for below-ambient contactors.
- Incorporating heat exchange in the column i.e., diabatic distillation
- diabatic distillation is known to be one method of reducing the external reboil or reflux demand.
- Examples of diabatic distillation are disclosed in US Patents 385,504; 2,330,326; 2,492,932; 2,963,872; and 3,642,452.
- the limitations enumerated above are interrelated to some extent, with various tradeoffs possible. For example, the energy requirement can be reduced somewhat by adding trays and hence increasing column height, or vice versa. Larger diameter can reduce tray height and overall height, etc.
- Vapor-liquid contactors are used in distillation columns, rectifiers, strippers, absorbers, mixing (reverse distillation) columns, absorption cycle apparatus, bioreactors, reactive distillation columns, and similar devices.
- Various approaches to overcoming the above limitations have been disclosed in the prior art. Higher point efficiencies have been achieved in spinning cone contactors, and by imparting horizontal velocity to part of the vapor. Higher vapor loadings have been achieved using locally co-current trays plus separators which route the liquid to a twice-lower tray (US Patent 4,361 ,469).
- Other approaches to achieving local cocurrency are disclosed in US Patents 2,693,350; 3,642,542; 5,766,519; and 5,798,086.
- the contactor would achieve further increase in tray efficiency and corresponding decrease in tray count and column height by same-direction horizontal liquid flow on each tray coupled with structure to prevent vapor mixing.
- the contactor would also achieve lower energy demand. Most preferably, all of those desirable objects would be achieved simultaneously by compatible and synergistic measures.
- the contactor is comprised of:
- a vapor-liquid contactor comprised of: a. a multiplicity of vertically stacked trays within a containment; b. a multiplicity of channel weirs on each tray, each channel weir defining a locally co-current vapor-liquid upflow zone on one side of the channel weir, and a liquid downflow zone on the other side; said channel weirs having a liquid passage opening at or near the bottom for transport of liquid from the downflow zone to the co-current upflow zone; c. a multiplicity of vapor passages through said trays at the bottom of said co-current upflow zones; d. a level control liquid weir on each tray, which is at a lower height than said channel weirs; e.
- the tray loading can be further increased, and/or tray height further decreased, by providing apparatus for vapor-liquid separation above the channel weirs.
- the vapor-liquid separation is accelerated and made more effective compared to simply relying on open-space separation. It is important that the liquid drainage from the separator be directed to the downflow zone (downcomer channels), as otherwise it can be re-entrained in the upflowing vapor.
- Each tray is fitted with a level control liquid weir, much like conventional trays, and the weir overflow is routed to the next lower tray.
- the tray efficiency it is frequently preferred to route the overflow liquid to the same comparative location on each succeeding or adjoining tray - this allows the tray efficiency to approach 200% of the point efficiency provided the vapor is prevented from mixing, e.g., by partitions.
- the tray efficiency only approaches 150% of the point efficiency for unmixed vapor, or 167% for fully mixed vapor.
- the contactor is comprised of: a. a multiplicity of vertically stacked trays within a containment; b. a liquid supply area and liquid removal area to and from each tray, wherein each supply and removal area is at the same relative location on each tray, whereby the net horizontal liquid flow on each tray is in the same directional pattern; and c. a multiplicity of partitions in the vapor space of each tray which are transverse to the flow direction of said liquid, and thereby minimize vapor mixing.
- the compartmentalization reduces the horizontal mixing of both the liquid and the vapor, resulting in larger concentration gradients and hence higher tray efficiencies for a given point efficiency (provided the horizontal liquid flow is the same direction on each corresponding section of each tray).
- the partitions For very large diameter trays, the partitions only need to be in the vapor space; for smaller trays, they should extend into the liquid space as well to reduce liquid mixing. When they do, suitable openings or clearance for liquid transport are provided.
- the liquid transport openings in the respective compartment partitions can be staggered so as to ensure a tortuous liquid flowpath across the entire tray.
- the relative amount of liquid recirculation within a compartment relative to the net liquid transport through a compartment can be controlled by varying the area of the liquid transport openings at the bottom of the compartment partitions relative to the area of the liquid recirculation openings at the bottom of the channel dividers, and also by varying the weir overflow area.
- the trays may be circular, rectangular, or other known shapes.
- Diameters in the range of 50 to 10,000 mm are contemplated.
- the vapor passages through each tray may be orifices, slots, tubes, valves, bubble caps, and the like. Hole diameters in the range of 0.5 mm to 20 mm are contemplated, and even larger for valve or bubble cap openings. Tray heights between 50 and 1000 mm are contemplated. Spacing between compartment partitions and channel dividers in the range of 5 to 500 mm is contemplated. Flooding limits are anticipated to be between 10% and 300% higher than for conventional sieve trays, dependent on vapor-liquid separator efficiency.
- Prior art multistage tray contactors can be divided into three categories dependent upon where the liquid is introduced to each tray and where it is removed. The commonest is entry at one peripheral location and exit from the opposite periphery, with horizontal opposite-direction liquid flow across each tray. When this type of tray becomes large, a liquid concentration gradient forms across the tray. Unfortunately, the same size parameter which causes the liquid gradient also causes a vapor concentration gradient, e.g., prevents full mixing of the vapor, thus limiting the tray efficiency improvement factor.
- the "peripheral-to-peripheral" category can also be configured for same-direction horizontal liquid flow.
- Figures 4 and 5 of US Patent 2,963,872 disclose one example of this, and Figure 5 herein discloses another example. However, the full benefit of same-direction horizontal liquid flow is not obtained unless vapor mixing is prevented.
- this invention extends to adding transverse partitions at least in the vapor space to any of the same-direction horizontal liquid flow configurations.
- US Patent 4,032,410 discloses one center-to-center configuration, with opposite direction liquid horizontal flow on each adjoining tray.
- Figures 7, 13, and 22 herein disclose new approaches to achieving the center-to-center flow configuration. They have the advantage of much larger weir length, larger downcomer size, and greater downcomer height, thus accommodating higher liquid loadings.
- a simple construction is disclosed which achieves horizontal same-direction liquid flow, including a concentration gradient, in the center-to-center configuration.
- the third category is mixed - either center-to-periphery or periphery-to center. Examples of this are found in "Multiple Downcomer" trays, in the Oldershaw configuration, and in Figure 1 herein.
- the new center-to-center configurations disclosed herein have another advantage in addition to preserving reasonable weir lengths and providing large downcomer area and height without using as much of the column cross section as conventional designs.
- the additional advantage is a clear periphery or circumference. This facilitates incorporating heat exchange into the column so as to reduce the energy requirement.
- One approach is to exchange heat with fluid in an annular space outside the tray wall. This is effective, since the entire wall circumference is wetted with two-phase froth.
- Figure 1 is a cutaway view of a section of vapor-liquid contactor with same- direction vertical liquid flow and opposite-direction horizontal liquid flow.
- Figure 2 is a perspective cutaway view illustrating the flow directions.
- Figure 3 is a detail of a single compartment showing riser, downcomer, weir, vapor injectors, and separator.
- Figure 4 illustrates the embodiment with contact media or catalyst in the riser channels.
- Figure 5 illustrates one new method of achieving periphery-to-periphery same-direction horizontal flow, including vapor partitions.
- Figure 6 illustrates a traditional method of achieving same- direction horizontal flow, but with vapor partitions added.
- Figures 7 and 8 are cutaway views of a new method of center-to-center same-direction horizontal liquid flow, including vapor partitions.
- Figures 9 and 10 are perspective drawings of constituent parts of Figure 7.
- Figure 11 adds channel weirs to Figure 7 so as to also have same-direction vertical flow.
- Figure 12 adds heat exchange to the Figure 11 embodiment, in the form of a pair of conforming array coils.
- Figure 13 is a perspective view of two trays having center-to-center same-direction horizontal liquid feed, a hexagonal downcomer between trays and conforming array heat exchange coils.
- Figures 14, 15, and 16 are the constituent parts of the Figure 13 tray downcomer, and Figure 17 is the tray.
- Figures 18 and 19 illustrate it in a containment.
- Figure 20 illustrates an entire distillation column with the disclosed features and two types of heat exchange.
- Figure 21 is a cross-sectional view of tray with annular type of heat exchange.
- Figure 22 is a cross-section of a tray with another new method of achieving center-to-center same-direction horizontal flow, and
- Figure 23 is a detail of the associated tray downcomer.
- FIG 1 illustrates vertically stacked trays (61 , 71) within containment 69.
- the liquid flows horizontally in opposite radial directions on each successive tray, owing to the alternating sequence of central downcomer/tray weir 68 and peripheral downcomer/tray weir 70.
- Each tray is adapted for liquid recirculation, i.e., for same-direction vertical flow, by means of cylindrical compartment partitions 62, 63, and 64, plus channel weirs 65, 66, and 67.
- vapor injectors e.g. perforations
- Figure 2 illustrates the liquid flow directions on tray 61.
- FIG. 3 is a detail of one single compartment, with compartment partition 113 and channel weir 114, above tray 115. Liquid flow through the partition and weir is accommodated by louvers 116 and 117 respectively.
- Figure 3 shows the optional inclusion of vapor-liquid separator segments 110 with drainage path 112 into the downcomer channel of the compartment - this separator enables higher vapor loadings without flooding.
- Figure 4 illustrates another optional enhancement of the liquid recirculation feature - incorporating contact media 122 in the riser channels above tray 123 in the compartments formed by compartment partitions 120.
- Tray weir 124 is at a lower height than the channel weirs.
- the media can include a catalytic agent.
- Figure 5 illustrates a tray having both same-direction vertical flow (liquid recirculation) and same-direction horizontal flow. Liquid from the tray above falls onto shelf 33, and then flows bi-directionally in an annular space around the periphery of tray 30 which is defined by shroud 34. It enters the contact zone of tray 30 through opening 35, flows across the tray, and then down to the next tray.
- FIG. 6 is another example of periphery-to-periphery same-direction horizontal flow, of the type disclosed in US Patent 2,963,872.
- the tray is bifurcated into two halves 3, 4, at staggered heights, by center barrier 5. Liquid flows in opposite direction on each half, then drops half a tray height to the other side. A downcomer is required at each end, and the downcomer height is only half the total tray spacing.
- the novel feature is the addition of transverse vapor partitions 6 and 7 which reduce vapor mixing, and hence increase tray efficiency.
- Figures 7 and 8 are top and side views respectively of one such configuration.
- Tray 77 within containment 78 has a centrally located downcomer comprised of a diagonal member 79, and partitions 80 (two) and 81 (one).
- the top tab of diagonal member 79 is the tray weir for the tray above.
- Figures 9 and 10 are perspective views of components 80 and 79 respectively. Liquid exits from the right hand side of each tray into the central downcomer and flows diagonally down to a point 180° opposite (left-hand side), and then flows bi-directionally around the periphery through the contact zone to the next liquid exit. Vapor mixing is blocked by the partitions 80.
- Figure 11 illustrates the incorporation of liquid recirculation into the Figure 7 configuration, by addition of a cylindrical channel weir 82. Assuming that tray 77 is a sieve tray design, then the perforations would only be outside weir 82, and not between weir 82 and partitions/downcomer walls 80 and 81
- Figure 12 illustrates the incorporation of heat exchange into the Figure 7 configuration.
- the clear peripheral contact zone facilitates adding a coiled tubular heat exchanger on each tray.
- the tubular coil can be fashioned into a conformal array. This makes efficient use of the available space, and provides good heat transfer since the coil is submerged in the turbulent froth region.
- the heat exchange coil on each tray connects at the respective ends to the coils on the tray above and below; the connector tubing can be routed through the downcomer, or alternatively directly through a suitable cutout of the tray. Since this configuration has bi-directional horizontal flow of liquid through the contact zone, the conformal array should be provided in two mirror image halves in order to achieve full counter-currency.
- Figure 13 is a perspective view of another central-downcomer same- direction horizontal liquid flow configuration.
- the two sieve trays 150, 151 have between 4 and 12% open area in the peripheral contact zone.
- Hexagonal central downcomer is comprised of vertical member 152, diagonal member 153, and partitions 154.
- the top portion of member 152 is the tray weir for the above tray.
- the central section of partitions 154 form part of the downcomer, and the wing sections both provide support points for the conforming array and also serve as vapor block partitions.
- Figures 14 and 15 are details of components 152 (before bending) and 153, and Figure 16 shows them assembled.
- Figure 17 illustrates sieve tray 150, with cutout 155 which accommodates the tray downcomer.
- Figures 18 and 19 are side and top views respectively of the Figure 13 configuration as it would be applied in a partial condenser.
- Containment 201 houses the contactor and upflowing vapor, which exits at 202. Coolant is supplied at 203 to the two conforming arrays, and withdrawn at 204.
- Central downcomer 205 allows condensate to pass from tray to tray.
- Figure 20 illustrates an entire distillation column using diabatic same- horizontal-direction distillation with central downcomers and vapor block partitions.
- the top two trays are diabatic with conformal tubing arrays 208.
- the next tray is adiabatic, and accommodates column feed 209.
- the next four trays are diabatic with annular heat exchange.
- a second column feed is supplied to the annulus at 210, and is preheated to close to saturation while diabatically refiuxing the column, and finally the liquid enters the trayed section at point 211.
- the bottom five trays are diabatically heated from an annular heat exchanger.
- a heating fluid such as bottom product liquid is supplied to the annulus at 212 and removed from the annulus at 213. Vapor from a reboiler is supplied at 214, and liquid is removed at 215.
- This particular column configuration finds use in NH 3 -H 2 O absorption refrigeration units, among other applications.
- Figure 21 is a cross-section of the Figure 20 column at a point where liquid enters the annulus, showing one possible configuration of the header.
- Guide bars 216 may be incorporated in the annular space of Figure 20 to cause the heat transfer liquid to flow counter-currently to the temperature gradient on each tray.
- central-downcomer same-direction horizontal liquid flow configurations both have bi-directional liquid flow around the peripheral contact zone. They differ in shape of central downcomer - square vs. hexagonal. It will be recognized that other downcomer cross-sections are possible, e.g., circular, polygonal, oval, or irregular. The tradeoffs involve tray weir length, loss of active contactor area, and ease of construction. The hexagonal shape is a good general compromise on these factors.
- Figure 22 illustrates such a tray, with a square downcomer 220, a cylindrical channel weir 221 , and a single conforming array heat exchange coil 222.
- This tray configuration is characterized by a liquid barrier 223 on each tray (also a thermal barrier), whereby liquid spills over tray weir 224 and then internal structure 225 directs the liquid down and over to the next face of the square, where it enters the contact zone of that tray.
- Figure 23 illustrates details of the square downcomer 220 and the internal structure 225. Partitions 226 block vapor mixing and support the coil, plus help maintain tray spacing and rigidity.
- liquid recirculation preserves a relatively fixed froth height, just above the channel weirs, where otherwise at high turndown much of the conforming array would be in vapor space. High turndown requirement would also be one of the indicators to use valves as vapor injectors vice perforations.
- the "quiescent" liquid level on each tray should be below the channel weir height and above the tray weir height for normal operation. Thus, the tray weir height must be below the channel weir height. Tray weir heights of 5 to 200 mm are contemplated.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2000566008A JP2003534890A (en) | 1998-08-25 | 1998-08-25 | Tray-type contact device with co-directional liquid flow |
EP98941013A EP1115476A4 (en) | 1998-08-25 | 1998-08-25 | Tray contactor with same-direction liquid flow |
PCT/US1998/017339 WO2000010696A1 (en) | 1998-08-25 | 1998-08-25 | Tray contactor with same-direction liquid flow |
US09/763,513 US6631892B1 (en) | 1998-08-25 | 1998-08-25 | Tray contactor with same direction liquid flow |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/US1998/017339 WO2000010696A1 (en) | 1998-08-25 | 1998-08-25 | Tray contactor with same-direction liquid flow |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000010696A1 true WO2000010696A1 (en) | 2000-03-02 |
Family
ID=22267712
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US1998/017339 WO2000010696A1 (en) | 1998-08-25 | 1998-08-25 | Tray contactor with same-direction liquid flow |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1115476A4 (en) |
JP (1) | JP2003534890A (en) |
WO (1) | WO2000010696A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9186600B2 (en) | 2011-11-03 | 2015-11-17 | Linde Aktiengesellschaft | Device for bringing about a phase contact between a liquid phase and a gaseous phase, in particular a heat and mass transfer column |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2713478A (en) * | 1952-10-03 | 1955-07-19 | Edw G Ragatz Co | Apparatus for counter-current contacting of liquids and vapors |
US3168600A (en) * | 1960-02-03 | 1965-02-02 | Saint Gobain | Plate column |
US3338566A (en) * | 1962-12-29 | 1967-08-29 | Counter Current Op | Gas-liquid contact column apparatus |
US3445343A (en) * | 1967-02-01 | 1969-05-20 | Dmitry Mikhailovich Popov | Apparatus for evaporating-condensing separation of mixtures |
US3759498A (en) * | 1970-03-16 | 1973-09-18 | Union Carbide Corp | Liquid-gas contact tray |
US4556522A (en) * | 1984-05-09 | 1985-12-03 | Air Products And Chemicals, Inc. | Sieve type distillation tray with curved baffles |
US4869851A (en) * | 1987-05-26 | 1989-09-26 | Uni-Frac Inc. | Vapor/liquid contact device and method of mixing a vapor flow and a counter current reflux liquid flow |
US5798086A (en) * | 1996-05-10 | 1998-08-25 | Erickson; Donald C. | Intensified locally cocurrent tray contactors |
-
1998
- 1998-08-25 WO PCT/US1998/017339 patent/WO2000010696A1/en not_active Application Discontinuation
- 1998-08-25 JP JP2000566008A patent/JP2003534890A/en active Pending
- 1998-08-25 EP EP98941013A patent/EP1115476A4/en not_active Withdrawn
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2713478A (en) * | 1952-10-03 | 1955-07-19 | Edw G Ragatz Co | Apparatus for counter-current contacting of liquids and vapors |
US3168600A (en) * | 1960-02-03 | 1965-02-02 | Saint Gobain | Plate column |
US3338566A (en) * | 1962-12-29 | 1967-08-29 | Counter Current Op | Gas-liquid contact column apparatus |
US3445343A (en) * | 1967-02-01 | 1969-05-20 | Dmitry Mikhailovich Popov | Apparatus for evaporating-condensing separation of mixtures |
US3759498A (en) * | 1970-03-16 | 1973-09-18 | Union Carbide Corp | Liquid-gas contact tray |
US4556522A (en) * | 1984-05-09 | 1985-12-03 | Air Products And Chemicals, Inc. | Sieve type distillation tray with curved baffles |
US4869851A (en) * | 1987-05-26 | 1989-09-26 | Uni-Frac Inc. | Vapor/liquid contact device and method of mixing a vapor flow and a counter current reflux liquid flow |
US5798086A (en) * | 1996-05-10 | 1998-08-25 | Erickson; Donald C. | Intensified locally cocurrent tray contactors |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9186600B2 (en) | 2011-11-03 | 2015-11-17 | Linde Aktiengesellschaft | Device for bringing about a phase contact between a liquid phase and a gaseous phase, in particular a heat and mass transfer column |
Also Published As
Publication number | Publication date |
---|---|
EP1115476A4 (en) | 2002-06-19 |
EP1115476A1 (en) | 2001-07-18 |
JP2003534890A (en) | 2003-11-25 |
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