CN113262518B - Parallel suspension multi-downcomer tower plate - Google Patents
Parallel suspension multi-downcomer tower plate Download PDFInfo
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- CN113262518B CN113262518B CN202110592358.8A CN202110592358A CN113262518B CN 113262518 B CN113262518 B CN 113262518B CN 202110592358 A CN202110592358 A CN 202110592358A CN 113262518 B CN113262518 B CN 113262518B
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/14—Packed scrubbers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E10/00—Energy generation through renewable energy sources
- Y02E10/70—Wind energy
- Y02E10/72—Wind turbines with rotation axis in wind direction
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Abstract
The invention discloses a parallel suspension multi-downcomer tower plate, which belongs to the technical field of chemical equipment, and is arranged in a tower body and comprises a tower tray plate and downcomers, wherein a valve hole is formed in the tower tray plate, a fixed valve is arranged in the valve hole, a plurality of parallel suspension downcomers are arranged on the tower tray plate, the downcomers are arranged on the tower tray plate in an A-type tower plate and a B-type tower plate structure mode, the A-type tower plate and the B-type tower plate are alternately stacked up and down in the tower body, the downcomers on the tower plate are shorter, and the transverse liquid velocity gradient is reduced; the downcomers are arranged in parallel, the distances from the liquid receiving area to the inlet weirs on the two sides are equal, and the liquid receiving area is in a long and narrow rectangle, so that liquid on the plate flows in a mode closer to plug flow; the downcomers are alternately arranged, and the design of the tower plate follows the principle of equal runner length; the tower plate is directly subjected to liquid receiving by using a bubbling area, so that the gas phase operation load is improved; the plurality of downcomers are arranged, so that the influence of an arched area on flow is reduced, gas-liquid distribution is more uniform, and gas-liquid contact is effectively improved.
Description
Technical Field
The invention belongs to the technical field of chemical equipment, and particularly relates to a parallel suspension multi-downcomer tower plate.
Background
The trays are classified in an overflow mode and mainly comprise a single-overflow tray, a U-shaped flow tray, a double-overflow tray, a multi-overflow tray and the like. With the progress of science and technology, the industries of petrochemical industry, oil refining, chemical fertilizers and the like gradually develop towards large-scale and conglomeration. As a mass transfer device used in aspects of rectification, absorption and the like, the scale of a single column plate is larger and larger, but the diameter of the column plate is simply enlarged, so that the industrial requirement cannot be met, and the economic benefit is seriously restricted by the characteristics of low space utilization rate, high investment, large energy consumption and the like. The development of a novel multi-overflow column plate becomes the popular trend in the chemical industry field at home and abroad at present.
The downcomers of adjacent tower plates on a common multi-downcomer tower plate are vertically arranged, liquid can flow on the tower plates in a 90-degree rotating mode, a diffusion flow trapezoidal area is further formed, the liquid flows in a diffusion mode towards two sides, and therefore the liquid on the tower plates is unevenly distributed, and the efficiency of the tower plates is affected. In order to improve the liquid flow distribution on the tower plate, a guide hole is additionally arranged in the middle of the bubbling area, so that part of gas is blown out from the guide hole, and the liquid is pushed to a downcomer; the guide plate is arranged in the liquid receiving area, so that the flow field distribution of liquid is improved, and the tower plate efficiency is further improved. The structures improve the distribution of liquid flow fields on the multi-downcomer tower plates to a certain extent, but the arrangement of the flow guide devices on the tower plates increases the complexity of the tower plate structure and influences the further improvement of the uniformity of the flow fields.
Disclosure of Invention
To solve the above problems, it is an object of the present invention to provide a parallel-hanging multi-downcomer tray.
In order to achieve the purpose, the following technical scheme is provided:
the utility model provides a many down-flow pipes of parallel suspension column plate, locates in the tower body, its characterized in that includes tray plate and down-flow pipe, the tray plate is equipped with the valve opening, and the down-flow pipe hangs perpendicularly on the tray plate, and the upper end and the tray plate fixed connection of down-flow pipe, parallel to each other between the down-flow pipe, the down-flow pipe have the mode of arranging of two kinds of structures of A type column plate and B type column plate on the tray plate, the A type column plate is installed in the tower body with B type column plate about the turn, after the installation, the down-flow pipe on A type column plate and the B type column plate does not overlap.
Furthermore, the downcomer is a quadrilateral opening, and a fixed valve is arranged in a valve hole.
Furthermore, the A-type tower plate comprises two first edge downcomers, four first eccentric downcomers and one first central downcomer, and the B-type tower plate comprises four second edge downcomers, two second eccentric downcomers and two second central downcomers; the two first side downcomers are respectively arranged at two side parts of the tray plate, the first central downcomer is arranged at the center of the tray plate, four first eccentric downcomers are respectively and uniformly arranged between the first side downcomers and the first central downcomer, and every two first eccentric downcomers are on the same straight line; after the device is installed, every two second side downcomers are positioned at two sides of one first side downcomer, and the three downcomers are positioned on the same straight line, every second eccentric downcomer is positioned between two first eccentric downcomers, and the three downcomers are positioned on the same straight line, and the two second central downcomers are positioned at two sides of the first central downcomer, and the three downcomers are positioned on the same straight line.
Further, the distance from the outlet of the downcomer of the upper layer of trays to the inlet of the downcomer of the lower layer of trays is equal.
Furthermore, the side weir of the second side downcomer, which is close to the wall surface of the tower body, is in a circular arc shape.
Furthermore, the side weir of the first eccentric downcomer close to the wall surface of the tower body is in a circular arc shape or an inclined plane.
Furthermore, the side weir of the downcomer is in a shape of a straight edge, a triangle or a semi-ellipse.
Furthermore, the tray plate is suitable for towers with the diameter of 2-1690 m, the aperture ratio of a valve hole is 5% -30%, and the plate spacing between two adjacent tray plates is 200-1500 m.
Furthermore, the area of the first side downcomer is 1% -5% of the total area of the tray plate, the area of the first eccentric downcomer is 2% -5% of the total area of the tray plate, and the area of the first central downcomer is 2% -5% of the total area of the tray plate.
Furthermore, the area of the second side downcomer is 0.1-5% of the total area of the tray plate, the area of the second eccentric downcomer is 1-5% of the total area of the tray plate, and the area of the second central downcomer is 2-5% of the total area of the tray plate.
Compared with the prior art, the invention has the beneficial effects that: the downcomer on the column plate is shorter than the common multiple downcomer column plate, so that the transverse liquid velocity gradient can be reduced, and the uneven distribution of liquid on the column plate caused by a longer downcomer is avoided; the downcomers are arranged in parallel, the distances from the liquid receiving area to the inlet weirs on the two sides are equal, and the liquid receiving area is in a long and narrow rectangular shape, so that liquid on the plate flows in a mode closer to plug flow, gas-liquid contact is more uniform, liquid phase back mixing is reduced, and mass transfer efficiency is improved; the downcomers of adjacent tower plates are alternately arranged, the flow distribution of liquid on the tower plates is determined by the length of an overflow weir of a single downcomer, and the design of the tower plates follows the principle of equal flow channel length; the tower plate utilizes the bubbling area to directly receive liquid, and the liquid flowing out of the downcomer directly falls on the bubbling element in the bubbling area, so that the area of the bubbling area of the tower plate is increased, and the gas phase operation load is improved; the influence of an arched area on the flow is reduced by arranging the plurality of downcomers, the total length of the outlet weir of the tower plate is larger, the overflow strength is reduced, and the tray is suitable for operation with larger liquid load; because of the reduction of the liquid channel of the multi-downcomer tower plate, the liquid level drop can be reduced, the gas-liquid distribution is more uniform, and the gas-liquid phase contact is effectively improved.
Drawings
FIG. 1 is an assembly view of the three-dimensional structure of the present invention;
FIG. 2 is a schematic view of a type A tray of the present invention;
FIG. 3 is a schematic view of a type B tray of the present invention;
FIG. 4a is a schematic view of a vertical structure of a downcomer side weir with a right-angle edge;
FIG. 4b is a schematic perspective view of a downcomer side weir with a semi-elliptical shape;
FIG. 4c is a schematic view of a triangular side weir of the downcomer;
FIG. 5 is a graph of the average residence time distribution of tray decks of the present invention;
FIG. 6 is a graph comparing entrainment rates of tray decks of the present invention;
FIG. 7 is a graph comparing the leakage rate of tray decks of the present invention;
FIG. 8 is a comparison of the clear liquid layer heights of tray plates of the present invention.
In the figure: 1-A type column plate; 101-a first side downcomer; 102-a first eccentric downcomer; 103-a first central downcomer; 2-type column plate; 201-a second side downcomer; 202-a second eccentric downcomer; 203-a second central downcomer; 3-fixing a valve; 4-a valve hole; 5-a tower body; 6-tray plate.
Detailed Description
The invention will be further described with reference to the drawings and examples in the following description, but the scope of the invention is not limited thereto.
Referring to fig. 1, a parallel suspension multi-downcomer tower plate is arranged in a tower body 5 and comprises a tower tray plate 6 and a downcomer, wherein a valve hole 4 is formed in the tower tray plate 6; a plurality of parallel hanging downcomers are arranged on the tray plate 6, the parallel hanging downcomers are provided with quadrilateral openings, the downcomers are arranged on the tray plate 6 in an arrangement mode of an A-type tower plate 1 and a B-type tower plate 2, and the A-type tower plate 1 and the B-type tower plate 2 are alternately arranged in the tower body 5 from top to bottom.
Referring to the figure 2,A type tower plate 1, two first side downcomers 101 are arranged and are respectively positioned at two side parts of the A type tower plate 1, a first central downcomer 103 is arranged at the center of a tray plate 6, four first eccentric downcomers 102 are uniformly arranged between the first side downcomers 101 and the first central downcomers 103, side weirs of the first eccentric downcomers 102 close to the inner wall of a tower body 5 are inclined planes, a fixed valve 3 is arranged in a valve hole 4, the area of the first side downcomers 101 is 1% -5% of the total area of the tray plate 6, the area of the first eccentric downcomers 102 is 2% -5% of the total area of the tray plate 6, and the area of the first central downcomers 103 is 2% -5% of the total area of the tray plate 6.
Referring to 5363, the 3,B type tower plate 2 is provided with four second side downcomers 201 which are respectively located at two side edges of the B type tower plate 2, two second central downcomers 203 which are arranged in the middle of the tower plate 6, two second eccentric downcomers 202 which are respectively arranged between the second side downcomers 201 and the second central downcomers 203, after the a type tower plate 1 and the B type tower plate 2 are installed, the second side downcomers 201 are respectively located at two sides of the first side downcomer 101, side weirs of the second side downcomers 201 close to the wall surface of the tower body 5 are circular arc-shaped, the second eccentric downcomers 202 are respectively located between the first eccentric downcomers 102, the first central downcomers 103 are located between the second central downcomers 203, the area of the second side downcomers 201 is 0.1% -5% of the total area of the tower plate, the area of the second eccentric downcomers 202 is 1% -5% of the total area of the tower plate, and the area of the second central downcomers 203 is 2% -5% of the total area of the tower plate.
The side weirs of the downcomer may be arranged in a straight configuration (e.g., fig. 4 a), a semi-oval configuration (e.g., fig. 4 b), and a triangular configuration (e.g., fig. 4 c).
Example 1
In an organic glass tower with the plate spacing of 600mm and the diameter of 1219mm, a plurality of parallel-suspended downcomer trays are arranged in an up-and-down arrangement mode of 'A plate-B plate-A plate-B plate', the uppermost layer is a hot water distribution plate, the second layer is a water inlet plate and is also a cold water primary distribution plate, the third layer is a cold water redistribution plate, and the lowermost layer is a test plate; the aperture ratio of each tower plate is 18.96 percent, and the adjacent fixed valves 3 are arranged in a regular triangle; the area of the first side downcomer 101 is 192cm 2 The first eccentric downcomer 102 has an area of 248cm 2 The area of the first central downcomer 103 is 240cm 2 (ii) a Second oneThe area of the side downcomer 201 is 60cm 2 The second eccentric downcomer 202 has an area of 200cm 2 And the area of the second central downcomer 203 is 400cm 2 . Liquid phase water is used as an operation material, cold water enters the tower from the water inlet plate through the centrifugal pump and the rotor flow meter, hot water flows into the buffer tank from the electric heating tank, and the hot water is uniformly injected into the tower plate after passing through the buffer tank. The test is carried out at a spray density of 10m 3 /(m 2 h) Meanwhile, the liquid phase flow field on the B-type tower plate 2 is distributed. (the A type tray 1 used in this example compares with the structure of the above-mentioned FIG. 1, and the B type tray 2 used in this example compares with the structure of the above-mentioned FIG. 2.)
The results of the test are shown in FIG. 5, where the liquid phase flows from the downcomer of the upper stage, through the tray and into the downcomer of the lower stage, the average residence time of the liquid phase on the tray is substantially 6s, and the equal average residence time distribution curve on the tray tends to be parallel to the outlet weir, i.e., the liquid phase flows into the downcomer on the tray in a nearly plug-flow fashion. Liquid phase back mixing is reduced, so that gas-liquid distribution is more uniform, gas-liquid phase contact is improved, and mass transfer efficiency of the tower plate is improved.
Example 2
In an organic glass tower with the plate spacing of 600mm and the diameter of 1219mm, a plurality of parallel-hanging downcomer tower plates are respectively arranged in an up-and-down arrangement mode of an A plate-B plate-A plate and a B plate-A plate-B plate, a middle tower plate is a test tower plate, a lower tower plate is a gas distribution plate, and an upper tower plate is a liquid distribution plate; the aperture ratio of each tower plate is 18.96 percent, and the adjacent solid valves 3 are arranged in a regular triangle; the area of the first side downcomer 101 is 192cm 2 The first eccentric downcomer 102 has an area of 248cm 2 The area of the first central downcomer 103 is 240cm 2 (ii) a The area of the second side downcomer 201 is 60cm 2 The second eccentric downcomer 202 has an area of 200cm 2 And the area of the second central downcomer 203 is 400cm 2 And a mist collector is arranged above the upper tower plate. Air and water are used as operating materials, and the spraying density is 60m 3 /(m 2 h) In the measurement, entrainment was measured for the A-type tray 1 and the B-type tray 2 under different gas phase loads. (the A-type tray 1 used in this example is compared with the structure shown in FIG. 1, this pointThe type B tray 2 used in the examples is comparable to the configuration described above with reference to FIG. 2. )
The test result is shown in figure 6, wherein the abscissa of the graph is a valve hole kinetic energy factor, and the ordinate of the graph is an entrainment rate. It can be seen that the spray density is 60m 3 /(m 2 h) The entrainment quantity of the A-type tower plate 1 and the B-type tower plate 2 follows the kinetic energy factor of the valve towerFIncreases by an increase of 15 (m · s) in the kinetic energy factor of the valve bore -1 )/(kg·m -3 ) 0.5 At about, the entrainment rate of the tower plate is still not more than 0.3 percent. Under the same valve orifice kinetic energy factor, the entrainment amounts of the A-type tower plate 1 and the B-type tower plate 2 are similar, which indicates that the operation upper limits of the A-type tower plate 1 and the B-type tower plate 2 are similar.
Example 3
In an organic glass tower with the plate spacing of 600mm and the diameter of 1219mm, a plurality of parallel-hanging downcomer trays are respectively arranged in an up-and-down arrangement mode of an A plate-B plate-A plate and a B plate-A plate-B plate, a middle tray is a test tray, a lower tray is a gas distribution plate, and an upper tray is a liquid distribution plate; the aperture ratio of each tower plate is 18.96 percent, and the adjacent fixed valves 3 are arranged in a regular triangle; the area of the first side downcomer 101 is 192cm 2 The first eccentric downcomer 102 has an area of 248cm 2 The area of the first central downcomer 103 is 240cm 2 (ii) a The area of the second side downcomer 201 is 60cm 2 The second eccentric downcomer 202 has an area of 200cm 2 The second central downcomer 203 has an area of 400cm 2 (ii) a And a leakage collector is arranged below the lower tower plate. Air and water are used as operating materials, and the spraying density is 60m 3 /(m 2 h) During the process, the liquid leakage rate of the parallel suspension multi-downcomer tower plates A and B under different gas phase loads is measured. (the A type tray 1 used in this example compares with the structure of the above-mentioned FIG. 1, and the B type tray 2 used in this example compares with the structure of the above-mentioned FIG. 2.)
The test result is shown in figure 7, wherein the abscissa of the graph is the valve hole kinetic energy factor, and the ordinate of the graph is the leakage rate. It can be seen that the spray density is 60m 3 /(m 2 h) The liquid leakage rate of the A-type tower plate 1 and the B-type tower plate 2 is reduced along with the increase of the kinetic energy factor of the valve hole; kinetic energy factor at valve hole is 6 (m.s) -1 )/(kg·m -3 ) 0.5 When the liquid leakage rate is about 0, the liquid leakage rate of the tower plate is close to 0; under the same valve opening kinetic energy factor, the liquid leakage rates of the A-type tower plate 1 and the B-type tower plate 2 are close to be identical, which shows that the lower operation limits of the A-type tower plate 1 and the B-type tower plate 2 are similar.
Example 4
In an organic glass tower with the plate spacing of 600mm and the diameter of 1219mm, a plurality of parallel-hanging downcomer tower plates are respectively arranged in an up-and-down arrangement mode of an A plate-B plate-A plate and a B plate-A plate-B plate, a middle tower plate is a test tower plate, a lower tower plate is a gas distribution plate, and an upper tower plate is a liquid distribution plate; the aperture ratio of each tower plate is 18.96 percent, and the adjacent solid valves 3 are arranged in a regular triangle; the area of the first side downcomer 101 is 192cm 2 The first eccentric downcomer 102 has an area of 248cm 2 The area of the first central downcomer 103 is 240cm 2 (ii) a The area of the second side downcomer 201 is 60cm 2 The second eccentric downcomer 202 has an area of 200cm 2 The second central downcomer 203 has an area of 400cm 2 (ii) a Three round holes with the diameter of 10mm are formed in the middle-layer tower plate, three copper pipes with the length of 3cm and the diameter of 10mm are inserted, the upper side opening of each copper pipe is flush with the upper surface of the tower plate 6, and the lower side opening of each copper pipe is connected with the liquid level meter through a rubber pipe. Air and water are used as operating materials, and the spraying density is 60m 3 /(m 2 h) Then, the heights of the clear liquid layers of the A-type tray 1 and the B-type tray 2 were measured under different gas phase loads. (the A type tray 1 used in this example compares with the structure of the above-mentioned FIG. 1, and the B type tray 2 used in this example compares with the structure of the above-mentioned FIG. 2.)
The test result is shown in figure 8, wherein the abscissa of the graph is the valve hole kinetic energy factor, and the ordinate of the graph is the height of the clear liquid layer. It can be seen that under the same valve opening kinetic energy factor, the heights of the supernatant layers of the A-type tower plate 1 and the B-type tower plate 2 are close, which indicates that the treatment capacity and the mass transfer effect of the A-type tower plate 1 and the B-type tower plate 2 are similar.
The above-described embodiments are merely illustrative of the present invention and are not to be construed as limiting the invention. Referring to the drawings, the structures, ratios, sizes, etc. shown in the drawings are only used for matching with the disclosure of the specification, and are not used for limiting the limit conditions of the invention, so the invention has no technical essence, and any structural modification, ratio change or size adjustment should still fall within the scope covered by the technical disclosure of the invention without affecting the efficacy and the achievable purpose of the invention.
Claims (6)
1. A parallel suspension multi-downcomer tower plate is arranged in a tower body (5) and is characterized by comprising a tower tray plate (6) and downcomers, wherein valve holes (4) are formed in the tower tray plate (6), the downcomers are vertically suspended on the tower tray plate (6), the upper ends of the downcomers are fixedly connected with the tower tray plate (6), the downcomers are parallel to each other, the downcomers are arranged on the tower tray plate (6) in an A-type tower plate (1) and a B-type tower plate (2) structure mode, the A-type tower plates (1) and the B-type tower plates (2) are alternately arranged in the tower body (5) from top to bottom, after the installation is completed, the downcomers on the A-type tower plates (1) and the B-type tower plates (2) are not overlapped, fixed valves (3) are arranged in the valve holes (4), and the distances from the downcomer outlet of the upper tower plate to the downcomer inlet of the lower layer are equal;
the A-type tray (1) comprises two first side downcomers (101), four first eccentric downcomers (102) and one first central downcomer (103), and the B-type tray (2) comprises four second side downcomers (201), two second eccentric downcomers (202) and two second central downcomers (203); two first side downcomers (101) are respectively arranged at two side parts of the tray plate (6), a first central downcomer (103) is arranged at the center of the tray plate (6), four first eccentric downcomers (102) are respectively and uniformly arranged between the first side downcomers (101) and the first central downcomer (103), and every two first eccentric downcomers (102) are on the same straight line; after the device is installed, every two second side downcomers (201) are positioned at two sides of one first side downcomer (101), and three downcomers are positioned on the same straight line, every second eccentric downcomer (202) is positioned between two first eccentric downcomers (102), and three downcomers are positioned on the same straight line, two second central downcomers (203) are positioned at two sides of a first central downcomer (103), and three downcomers are positioned on the same straight line;
the area of the first side downcomer (101) is 1% -5% of the total area of the tray plate (6), the area of the first eccentric downcomer (102) is 2% -5% of the total area of the tray plate (6), and the area of the first central downcomer (103) is 2% -5% of the total area of the tray plate (6);
the area of the second side downcomer (201) is 0.1-5% of the total area of the tray plate (6), the area of the second eccentric downcomer (202) is 1-5% of the total area of the tray plate (6), and the area of the second central downcomer (203) is 2-5% of the total area of the tray plate (6).
2. A parallel-hanging multi-downcomer tray according to claim 1, wherein the downcomer is a quadrilateral opening.
3. A parallel-hanging multi-downcomer tray according to claim 1, characterised in that the side weir of the second side downcomer (201) adjacent to the wall of the column (5) is rounded.
4. A parallel-hanging multi-downcomer tray according to claim 1, characterised in that the side weir of the first eccentric downcomer (102) adjacent to the wall of the column (5) is rounded or bevelled.
5. A parallel hanging multi-downcomer tray according to claim 1 wherein the side weirs of the downcomer are rectilinear, triangular or semi-elliptical.
6. The parallel suspension multi-downcomer tray according to claim 1, characterized in that the tray plates (6) are suitable for towers with diameters of 2 to 16m, the opening rate of the valve hole (4) is 5% to 30%, and the plate spacing between two adjacent tray plates (6) is 200 to 1500m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110592358.8A CN113262518B (en) | 2021-05-28 | 2021-05-28 | Parallel suspension multi-downcomer tower plate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110592358.8A CN113262518B (en) | 2021-05-28 | 2021-05-28 | Parallel suspension multi-downcomer tower plate |
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| Publication Number | Publication Date |
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| CN113262518A CN113262518A (en) | 2021-08-17 |
| CN113262518B true CN113262518B (en) | 2023-01-24 |
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| CN202110592358.8A Active CN113262518B (en) | 2021-05-28 | 2021-05-28 | Parallel suspension multi-downcomer tower plate |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3759498A (en) * | 1970-03-16 | 1973-09-18 | Union Carbide Corp | Liquid-gas contact tray |
| CN1119960A (en) * | 1994-10-07 | 1996-04-10 | 环球油品公司 | Enhanced capacity multiple-downcomer fractionation tray |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8540218B2 (en) * | 2007-04-27 | 2013-09-24 | Gtc Technology Us Llc | Fluid dispersion unit assembly and method |
| EP2108421B1 (en) * | 2008-04-11 | 2018-01-24 | Sulzer Chemtech AG | Multiple downcomer tray |
| US8720870B2 (en) * | 2010-05-11 | 2014-05-13 | Sulzer Chemtech Ag | Contact tray for a mass transfer column |
| MX2019008318A (en) * | 2017-01-11 | 2019-09-19 | Koch Glitsch Lp | Contact tray having baffle wall for concentrating low liquid flow and method involving same. |
| WO2020031077A1 (en) * | 2018-08-06 | 2020-02-13 | Koch-Glitsch, Lp | Multi-pass contact tray for a mass transfer column comprising fixed and movable valves and method involving same |
-
2021
- 2021-05-28 CN CN202110592358.8A patent/CN113262518B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3759498A (en) * | 1970-03-16 | 1973-09-18 | Union Carbide Corp | Liquid-gas contact tray |
| CN1119960A (en) * | 1994-10-07 | 1996-04-10 | 环球油品公司 | Enhanced capacity multiple-downcomer fractionation tray |
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| CN113262518A (en) | 2021-08-17 |
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