CN114160088A - Mass transfer tray and distillation column - Google Patents
Mass transfer tray and distillation column Download PDFInfo
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- CN114160088A CN114160088A CN202111592583.8A CN202111592583A CN114160088A CN 114160088 A CN114160088 A CN 114160088A CN 202111592583 A CN202111592583 A CN 202111592583A CN 114160088 A CN114160088 A CN 114160088A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
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Abstract
The invention relates to the field of chemical equipment, and provides a mass transfer tower tray and a distillation tower. The mass transfer tower tray comprises a gas-liquid transfer layer and a tower tray supporting mechanism for mounting the mass transfer tower tray in the distillation tower, the gas-liquid transfer layer is arranged on the tower tray supporting mechanism, and a gap for liquid to descend is formed between the edge of one end of the gas-liquid transfer layer and the tower wall of the distillation tower after the mass transfer tower tray is mounted in the distillation tower; the gas-liquid transmission layer is provided with pores for dispersing gas, the pore diameter of the pores is 0.1-100 mu m, and the porosity of the gas-liquid transmission layer is 1-80%. The distillation tower comprises a tower body and a plurality of mass transfer tower trays arranged in the tower body from top to bottom. The bubbles transferred to the tray are small in diameter, coalescence phenomena among bubbles are not easy to occur, and the gas-liquid phase interfacial area can be stabilized at a large value, so that the mass transfer effect is good.
Description
Technical Field
The invention relates to the field of chemical equipment, in particular to a mass transfer tower tray and a distillation tower.
Background
Distillation is a thermodynamic separation method, and is the most important separation means in the fields of oil refining and chemical engineering. The separation principle is that the components contained in the liquid mixture are separated by utilizing the different volatility of the components in the liquid mixture to partially vaporize the liquid mixture and then partially condense vapor. The distillation process is generally carried out in a distillation column. The distillation tower is mainly divided into a plate tower and a packed tower, and the tower inner mass transfer elements mainly correspond to a tower tray and a packing respectively. In the tower equipment of oil refining chemical enterprises, the plate tower accounts for more than 90 percent. In the plate-type tower, gas-liquid contact is completed on a gas bubbling and liquid spraying state on a gas-liquid two-phase plate, meanwhile, heat and mass are transferred by the gas-liquid two-phase plate, a light component is partially gasified and enters a gas phase, and a heavy component is partially condensed and enters a liquid phase; because of different densities, under the action of gravity, gas-liquid two phases are separated above the tower tray, the gas phase moves upwards and enters an upper tower tray, and the liquid phase moves downwards and enters a lower tower tray; the gas-liquid passes through a multi-layer tower tray to complete a multi-stage mass transfer separation process, finally, light and heavy components are separated in a distillation tower, the light components are mainly obtained at the top of the tower, and the heavy components are mainly obtained at the bottom of the tower.
The mass transfer efficiency is the most important parameter for measuring the quality of the tower tray, the mass transfer efficiency is influenced more, and the contact area of a gas phase and a liquid phase is determined by the diameters of dispersed bubbles and liquid drops on the plate, so that the mass transfer efficiency of the tower tray is influenced.
Chinese patent CN 210409561U discloses a microbubble tower tray for a gas-liquid mass transfer rectifying tower convenient to maintain, a plurality of gas-liquid mass transfer subassembly through-holes evenly run through on the tower tray, install a gas-liquid mass transfer subassembly in every through-hole, the gas-liquid mass transfer subassembly includes the mass transfer pipe, the mass transfer pipe top is equipped with toper closing head and bottom opening, be equipped with a plurality of gas lift on the mass transfer pipe outer wall, every gas lift upper end all is equipped with arc wire mesh board again on the mass transfer pipe outer wall, it has a plurality of auxiliary holes to run through on the toper closing head lateral wall, toper closing head lateral wall is equipped with the overflow weir board above the auxiliary hole. The arc wire mesh plate that this patent set up can carry out the breakage to the bubble, forms the microbubble, improves mass transfer efficiency. However, after the gas phase flows out from the gas rising holes on the outer wall of the mass transfer pipe, the gas phase flowing out from the gas rising holes around the gas rising holes can be influenced to form bubbles, so that the bubbles are enlarged and the mass transfer efficiency is reduced. Meanwhile, bubbles formed by gas phases flowing out of different mass transfer pipes around the device can be influenced, if the mass transfer pipes are too close to each other, the bubbles are easy to gather, and if the mass transfer pipes are too far away from each other, the aperture ratio is reduced, so that the treatment capacity of the device is influenced.
Chinese patent CN 202777878U discloses a microbubble integral mass transfer tray, the whole tray is made of microbubble mass transfer material, gas phase flows upwards through the pores on the tray, and the whole tray surface is used as a bubbling area for gas-liquid contact. The radial cross section area of the mass transfer material accounts for 10-90% of the cross section area of the whole tower, the volume fraction of the mass transfer material pore is 10-90%, and the pore diameter is 0.1-10 mm. The microbubble structure that its formed can provide more even microbubble gas distribution, has increased the area of contact of gas with the liquid layer, and increase operation elasticity improves tower tray production capacity, reduces tower tray interval, reduces the rectifying column height. When the bubbles are separated from the holes of the mass transfer material, the bubbles are formed, and the diameters of the bubbles are far larger than the hole diameters. Although this patent is smaller than the bubble diameter formed by conventional trays, the bubble diameter is still larger. As the pore size of the mass transfer material increases, the bubble diameter thereof also increases, with some liquid leakage occurring, and the gas phase also cannot be distributed relatively uniformly throughout the entire tray area.
The present application is made in view of the above problems.
Disclosure of Invention
The object of the present invention consists in providing a mass transfer tray and a distillation column aimed at improving at least one of the problems mentioned in the background.
Embodiments of the invention may be implemented as follows:
in a first aspect, the invention provides a mass transfer tray, which comprises a gas-liquid transfer layer and a tray supporting mechanism for mounting the mass transfer tray in a distillation tower, wherein the gas-liquid transfer layer is arranged on the tray supporting mechanism;
the gas-liquid transmission layer is provided with pores for dispersing gas, the pore diameter of the pores is 0.1-100 mu m, and the porosity of the gas-liquid transmission layer is 1-80%.
In an optional embodiment, the air holes are cylindrical holes parallel to the thickness direction of the gas-liquid mass transfer layer and are uniformly distributed on the gas-liquid mass transfer layer;
preferably, the thickness of the gas-liquid transmission layer is 1-100 mm;
preferably, the holes on the gas-liquid transmission layer are formed in a laser hole opening mode;
further preferably, the material of the gas-liquid transmission layer is metal, metal oxide, ceramic, graphite, silicon carbide or a mixture of at least two of the above materials.
In an alternative embodiment, the gas-liquid transmission layer is in the shape of a cut circle with a major arc formed by cutting a circle by a straight line, and after the mass transfer tray is installed on the distillation tower, a gap for descending liquid is formed between the edge of the straight line of the gas-liquid transmission layer and the tower wall;
in an optional embodiment, the mass transfer tray further comprises an overflow plate for blocking liquid, and the overflow plate is connected with the tray supporting mechanism and arranged at the edge of the straight line corresponding to the gas-liquid transfer layer.
In an optional embodiment, the mass transfer tower tray further comprises a liquid receiving tray, the liquid receiving tray is arranged below the gas-liquid mass transfer layer, the liquid receiving tray is provided with a vent hole for gas to pass through, and the aperture of the vent hole is 0.1-100 μm;
preferably, the gas-liquid transmission layer is made by sintering, 3D printing or a combination of sintering and 3D printing.
In an alternative embodiment, the upper surface of the gas-liquid transmission layer is coated with an ultralyophobic coating, or the gas-liquid transmission layer is made of an ultralyophobic material.
In an optional embodiment, the mass transfer tray further comprises a gas-phase pre-distribution layer, the gas-phase pre-distribution layer is arranged between the liquid receiving tray and the gas-liquid transmission layer, the porosity of the gas-liquid transmission layer is 1% -10%, and the pore diameter is 0.2-100 μm; the porosity of the gas phase pre-distribution layer is 10-95%, and the pore diameter is 0.1-50 mm;
preferably, the material of the gas-phase pre-distribution layer is metal, metal oxide, plastic, resin, ceramic, graphite, carborundum or a mixed material formed by at least two of the materials;
preferably, the gas phase pre-distribution layer is made by sintering, 3D printing or a combination of sintering and 3D printing.
In an alternative embodiment, the gas phase pre-distribution layer and the liquid receiving disc are connected into a whole;
preferably, the connection means is welding, bonding, embedding, snap connection or screw connection.
In an optional embodiment, the gas-liquid transmission layer, the gas-phase pre-distribution layer and the liquid receiving disc are connected into a whole;
preferably, the connection means is welding, bonding, embedding, snap connection or screw connection.
In an optional embodiment, the mass transfer tray further comprises a plurality of liquid gathering needles, the surface of each liquid gathering needle is provided with a lyophilic liquid phase coating, and the plurality of liquid gathering needles are arranged on the downward side of the gas-liquid mass transfer layer.
In a second aspect, the present invention provides a distillation column comprising a column body and a plurality of mass transfer trays according to any one of the preceding embodiments arranged from top to bottom on a column wall of the column body, wherein a projection of a gap between an upper gas-liquid mass transfer layer and the column wall of the column body in a plane of an adjacent next gas-liquid mass transfer layer is located entirely within the next gas-liquid mass transfer layer.
The embodiment of the invention has the beneficial effects that:
because the pore diameter of the gas hole of the gas-liquid transmission layer is 0.1-100 mu m, when gas phase passes through the gas-liquid transmission layer, bubbles with the diameter less than 1mm can be generated, the porosity is 1-80%, the generated bubbles are huge in quantity, so that the whole bubbles have a large surface area, the mass transfer phase interface area between the gas phase and the liquid phase is greatly increased, and the pore diameter can also effectively prevent the liquid phase from passing through. The average diameter of bubbles generated by the mass transfer tower tray is 200 mu m, and the diameter of bubbles generated by the traditional tower tray is generally 10-20 mm, so that the gas-liquid phase interfacial area provided by the mass transfer tower tray is 50-100 times that of the traditional tower tray, and the gas-liquid phase interfacial area is greatly increased. Meanwhile, the diameter of the bubbles generated by the mass transfer tray is small, and the coalescence phenomenon is not easy to occur among the bubbles, so that the gas-liquid phase interface area can be stabilized at a large value. The mass transfer trays provided herein also increase the gas-liquid phase boundary update rate relative to bubbles produced by conventional trays.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic diagram of a structure presented herein for a first embodiment of a tray;
FIG. 2 is a schematic view of a mass transfer tray provided in accordance with a first embodiment of the present application in operation;
FIG. 3 is a partial cross-sectional view of the gas-liquid transport layer of FIG. 1;
FIG. 4 is a bottom plan view of a tray as provided in the first embodiment of the present application;
FIG. 5 is a schematic diagram of a structure presented herein for a second embodiment of a tray;
FIG. 6 is a schematic view of the structure inside a distillation column provided in a third embodiment of the present application;
fig. 7 is a schematic view of the structure of the gas phase pre-distribution layer in application example 5.
Icon: 100-mass transfer trays; 101-a down-flow well; 102-a gas-liquid mass transfer zone; 110-tray support mechanism; 111-tray support rings; 112-tray support bars; 113-overflow plate; 120-gas liquid transport layer; 121-air holes; 130-liquid receiving plate; 140-a vapor phase pre-distribution layer; 141-a first metal sintered layer; 142-a second metal sintered layer; 143-grid packing; 150-liquid-gathering needle; 10-a distillation column; 11-column wall.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that if the terms "upper", "lower", "inside", "outside", etc. indicate an orientation or a positional relationship based on that shown in the drawings or that the product of the present invention is used as it is, this is only for convenience of description and simplification of the description, and it does not indicate or imply that the device or the element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
Furthermore, the appearances of the terms "first," "second," and the like, if any, are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
It should be noted that the features of the embodiments of the present invention may be combined with each other without conflict.
First embodiment
Referring to fig. 1, the present embodiment provides a mass transfer tray 100, which includes a gas-liquid transmission layer 120 and a tray supporting mechanism 110 for mounting the mass transfer tray 100 in a distillation tower, wherein the gas-liquid transmission layer 120 is disposed on the tray supporting mechanism 110, and after the mass transfer tray 100 is mounted in the distillation tower, a gap for liquid to descend is formed between an edge of one end of the gas-liquid transmission layer 120 and a tower wall 11 of the distillation tower.
And air holes 121 for dispersing air on the gas-liquid transmission layer 120, wherein the aperture of the air holes 121 is 0.1-100 μm, and the porosity of the gas-liquid transmission layer 120 is 1-80%.
In use, the tray supporting mechanism 110 is arranged on the column wall 11 of the distillation column, so that a gap (a downcomer hole 101) for liquid to descend is formed between one end edge of the gas-liquid transmission layer 120 and the column wall 11, so that the liquid phase after completing mass transfer falls from the downcomer hole 101 to the next layer of mass transfer tray 100.
As shown in fig. 2, the gas phase passes from the gas-liquid transport layer 120 into the gas-liquid mass transfer region 102 above the gas-liquid transport layer 120. When the gas phase passes through the gas-liquid transmission layer 120, bubbles with the diameter less than 1mm can be generated due to the pore diameter of the pores 121 of the gas-liquid transmission layer 120 being 0.1-100 μm, the porosity is 1% -80%, the number of generated bubbles is large, the whole bubbles have a large surface area, the mass transfer phase interface area between the gas phase and the liquid phase is greatly increased, and the pore diameter can also effectively prevent the liquid phase from passing through. The average diameter of bubbles generated by the mass transfer tower tray 100 provided by the embodiment of the application is 200 microns, and the diameter of bubbles generated by the traditional tower tray is generally 10-20 mm, so that the gas-liquid phase interfacial area provided by the scheme is 50-100 times that of the traditional tower tray, and the gas-liquid phase interfacial area is greatly increased. Meanwhile, the diameter of the bubbles generated by the mass transfer tray 100 provided by the application is small, and the coalescence phenomenon is not easy to occur among the bubbles, so that the gas-liquid interface area can be stabilized at a large value. The mass transfer tray 100 provided herein also increases the gas-liquid phase boundary update rate relative to bubbles produced by conventional trays.
Further, as shown in fig. 3, the gas holes 121 are cylindrical holes parallel to the thickness direction of the gas-liquid carrier layer 120, and are uniformly distributed on the gas-liquid carrier layer 120.
When gas pocket 121 is the cylinder hole, can make the gas phase can pass gas pocket 121 more fast, and because the aperture is little, has certain pressure drop, this kind of structure can make the gas phase get into gas-liquid phase mass transfer region through gas phase distribution layer uniformly and carry out the mass transfer heat transfer, can not cause the gas phase to distribute the inequality on the tray, causes the mass transfer heat transfer efficiency to descend. Preferably, the thickness of the gas-liquid transmission layer 120 is 1 to 100 mm.
Specifically, the gas holes 121 on the gas-liquid carrier layer 120 are formed by laser drilling. Further preferably, the material of the gas-liquid transmission layer 120 is metal, metal oxide, ceramic, graphite, silicon carbide, or a mixture of at least two of the above materials.
Further, as shown in fig. 4, the gas-liquid transmission layer 120 is shaped as a circle having a major arc formed by cutting a circle with a straight line, and after the mass transfer tray 100 is installed in the distillation column, a liquid dropping hole 101, which is a gap through which the liquid can drop, is formed between the edge of the gas-liquid transmission layer 120, which is a straight line, and the column wall 11.
Further, the mass transfer tray 100 further includes an overflow plate 113 for blocking liquid, and the overflow plate 113 is connected to the tray support mechanism 110 and disposed at an edge of the straight line corresponding to the gas-liquid transmission layer 120. Specifically, the height of the overflow plate 113 is higher than or equal to that of the gas-liquid transmission layer 120, and after the liquid phase falls from top to bottom to the gas-liquid transmission layer 120, the arrangement of the overflow plate 113 can prevent the liquid phase from immediately flowing down from the liquid dropping hole 101 to a certain extent, so that the retention time of the liquid phase in the gas-liquid transmission layer 120 is prolonged, the gas-liquid transmission is ensured to be more sufficient, and when the liquid phase is accumulated to be higher than the overflow plate 113, the liquid phase overflows from the overflow plate 113 to the liquid dropping hole 101.
Further, the tray support mechanism 110 includes a tray support ring 111 and a tray support rod 112, the tray support ring 111 is sized to fit the distillation column and is configured to be mounted on the column wall 11, opposite ends of the tray support rod 112 are connected to the tray support ring 111, so that the gas-liquid transmission layer 120 is disposed on the tray support mechanism 110, and is mainly located on one side of the tray support rod 112, and the edge of the straight line thereof is located on the tray support rod 112, and the other side of the tray support rod 112 is provided with the downcomer 101.
Second embodiment
This embodiment is substantially similar to the first embodiment, and reference is made to the first embodiment where nothing is mentioned.
As shown in fig. 5, the gas-liquid transmission layer 120 of the mass transfer tray 100 of the present embodiment is made by sintering, and the gas holes 121 contained therein are also formed during the sintering process.
It should be noted that, in other embodiments of the present application, the gas-liquid transmission layer 120 may also be formed by 3D printing or by a combination of sintering and 3D printing.
Specifically, the material of the gas-liquid transmission layer 120 is metal, metal oxide, plastic, resin, ceramic, graphite, silicon carbide, or a mixture of at least two of the above materials.
Preferably, the upper surface of the gas-liquid carrier layer 120 is coated with an ultralyophobic coating. The superoleophobic coating is, for example, a superhydrophobic coating or a superoleophobic coating, and which coating is specifically set is selected according to a specific liquid phase type. The super lyophobic coating can enable the gas phase to quickly generate bubbles when entering the liquid phase, and improve the mass transfer efficiency.
It should be noted that, in other embodiments of the present application, the gas-liquid carrier layer 120 may be made of an ultralyophobic material.
Further, the mass transfer tray 100 further comprises a liquid receiving tray 130, the liquid receiving tray 130 is arranged below the gas-liquid transfer layer 120, the liquid receiving tray 130 is provided with vent holes for gas to pass through, and the aperture of the vent holes is 0.1-100 μm.
When the aperture of the vent hole on the liquid receiving disc 130 is 0.1-100 μm, the gas phase can be ensured to pass through but the liquid phase can not pass through, and the arrangement of the liquid receiving disc 130 can ensure that the gas phase is primarily dispersed by the liquid receiving disc 130 when reaching the mass transfer tray 100 from the lower part, and then is further dispersed by the gas-liquid transmission layer 120.
Further, the mass transfer tray 100 further comprises a gas-phase pre-distribution layer 140, the gas-phase pre-distribution layer 140 is arranged between the liquid receiving tray 130 and the gas-liquid transmission layer 120, the porosity of the gas-liquid transmission layer 120 is 1% -10%, and the pore diameter is 0.2-100 μm; the porosity of the gas phase pre-distribution layer 140 is 10-95%, and the aperture is 0.1-50 mm.
After the gas phase passes through the liquid receiving disc 130, the gas phase pre-distribution layer 140 performs primary distribution on the gas phase, the gas-liquid transmission layer 120 performs secondary distribution on the gas phase, and due to the fact that the gas phase pre-distribution layer and the gas-liquid transmission layer are different in porosity and aperture, pressure drops of the two layers are different, and the gas phase is further uniformly distributed under the action of two different pressure drops.
Specifically, the thickness of the gas-phase pre-distribution layer 140 is 10-300 mm, and the thickness of the gas-liquid transmission layer 120 is 1-100 mm.
Further, the vapor pre-distribution layer 140 may be one layer or may be a plurality of layers.
Preferably, the gas phase pre-distribution layer 140 is made by sintering, 3D printing or a combination of sintering and 3D printing. In addition, the vapor pre-distribution layer 140 structure may also be a mesh, structured packing (e.g., grids, baffles, corrugated packing, etc.), or a combination thereof.
Specifically, the material of the gas-phase pre-distribution layer 140 is metal, metal oxide, plastic, resin, ceramic, graphite, silicon carbide, or a mixture of at least two of the above materials.
Preferably, the gas-liquid transmission layer 120, the gas-phase pre-distribution layer 140 and the liquid receiving pan 130 are integrally connected for easy installation.
Specifically, the gas-liquid transmission layer 120, the gas-phase pre-distribution layer 140 and the liquid receiving disk 130 are connected by welding, bonding, embedding, fastening or screwing.
Preferably, the gas-liquid transmission layer 120, the gas-phase pre-distribution layer 140 and the liquid receiving disc 130 have the same shape and size, and projections of the three layers on the same horizontal plane are substantially completely overlapped after the three layers are connected into a whole.
Further, the mass transfer tray 100 further includes a plurality of liquid collecting needles 150, a surface of each liquid collecting needle 150 has a lyophilic-liquid phase coating, and the plurality of liquid collecting needles 150 are disposed on a downward side of the gas-liquid transmission layer 120.
The hydrophilic phase coating can be a lipophilic phase or a hydrophilic phase, and the specific setting of which coating is selected according to the specific liquid phase type.
The liquid droplets brought into the upper gas-liquid transmission layer 120 or the gas-phase pre-distribution layer 140 by the gas phase can be "sucked" onto the liquid collecting needle 150 by the lyophilic phase coating on the surface of the liquid collecting needle 150, and when the liquid droplets are collected to a certain amount, the liquid droplets fall back along the liquid collecting needle 150, so that the drop back speed can be increased, and the retention time of the liquid phase in the gas-liquid transmission layer 120 or the gas-phase pre-distribution layer 140 can be reduced.
It should be noted that, in other embodiments of the present application, the liquid collecting needle 150 itself may also be made of a lyophilic material.
Third embodiment
As shown in fig. 6, the present embodiment provides a distillation column 10, which includes a column body and a plurality of mass transfer trays 100 provided in the second embodiment, wherein the mass transfer trays are arranged on the column wall of the column body from top to bottom, and the projection of the downcomer 101 formed between the last gas-liquid transmission layer 120 and the column wall of the column body on the plane where the next adjacent gas-liquid transmission layer 120 is located is completely located in the next gas-liquid transmission layer 120, so that the last layer of liquid phase which has completed mass transfer can be ensured to completely fall onto the next gas-liquid transmission layer 120 from the downcomer 101.
Application case 1
The tray provided in the first embodiment was used. The air holes 121 of the gas-liquid transmission layer 120 are cylindrical holes and are uniformly distributed, the opening rate is 60%, the aperture is 100 mu m, and the thickness of the mass transfer material is 5 mm. Through a cyclohexane-n-heptane system test, the efficiency of the microbubble tray is improved by about 62 percent compared with that of an F1 float valve tray, and the efficiency of the microbubble tray is improved by about 16 percent compared with that of a microbubble tray.
Application case 2
The tray provided in the first embodiment was used. The air holes 121 of the gas-liquid transmission layer 120 are cylindrical holes and are uniformly distributed, the opening rate is 80%, the aperture is 50 mu m, and the thickness of the mass transfer material is 5 mm. Through an ethanol-water system test, the efficiency of the microbubble tray is improved by about 68 percent compared with that of an F1 float valve tray, and the efficiency of the microbubble tray is improved by about 15 percent compared with that of a microbubble integral tray.
Application case 3
The tray provided in the second embodiment was used. The gas-liquid transmission layer 120 is made of metal powder by sintering, the porosity of the gas-liquid transmission layer is 10%, the average pore diameter is 5 μm, the pore diameter of the material is not uniform, and the thickness of the material is 5 mm. The gas-phase pre-distribution layer 140 is made of a wire mesh and is fixed with the gas-liquid transmission layer 120 and the tray support mechanism 110 in a welding mode; the porosity is 30%, the average pore diameter is 5mm, the pore diameter of the material is not uniform, and the thickness of the mass transfer material is 5 mm; through a cyclohexane-n-heptane system test, the efficiency of the microbubble tray is improved by about 60 percent compared with that of an F1 float valve tray, and the efficiency of the microbubble tray is improved by about 15 percent compared with that of a microbubble tray.
Application case 4
The tray provided by the second embodiment is employed without the gas phase pre-distribution layer 140. The gas-liquid transmission layer 120 is made of 3D printed metal oxide, the porosity of the gas-liquid transmission layer is 8%, the average pore diameter is 1 mu m, the pore diameter of the material is basically uniform, and the thickness of the mass transmission material is 8 mm; through an ethanol-water system test, the efficiency of the microbubble tray is improved by about 70 percent compared with that of an F1 float valve tray, and the efficiency of the microbubble tray is improved by about 17 percent compared with that of a microbubble integral tray.
Application case 5
With the tray provided in the second embodiment, the gas phase pre-distribution layer 140 is 3 layers. The gas-liquid transmission layer 120 is made by sintering carborundum, the porosity is 10%, the average aperture is 50 μm, the aperture of the material is not uniform, and the thickness of the mass transfer material is 8 mm. The gas phase pre-distribution layer 140 is provided with three layers and is fixed with the gas-liquid transmission layer 120 and the tray support mechanism 110 by bolts; as shown in fig. 7, the gas phase pre-distribution layer 140 is a first sintered metal layer 141 from top to bottom, and has a porosity of 20%, an average pore diameter of 0.5mm, a non-uniform material pore diameter, and a material thickness of 4 mm; the second layer is a second metal sintered layer 142, the porosity of which is 50%, the average pore diameter is 1mm, the pore diameters of the materials are not uniform, and the thickness of the mass transfer material is 4 mm; the third layer is grid filler 143, the porosity of which is 95%, the average pore diameter is 12mm, the pore diameter of the material is uniform, and the thickness is 10 mm; through a cyclohexane-n-heptane system test, the efficiency of the microbubble tray is improved by about 50% compared with that of an F1 float valve tray, and the efficiency of the microbubble tray is improved by about 12% compared with that of a microbubble tray.
In summary, the mass transfer tray 100 provided by the embodiments of the present application has the following advantages:
1. greatly increases the gas-liquid mass transfer phase boundary area and the gas-liquid updating rate.
The gas phase passes from the gas-liquid transport layer 120 into the gas-liquid mass transfer region 102 above the gas-liquid transport layer 120. When the gas phase passes through the gas-liquid transmission layer 120, bubbles with a diameter of less than 1mm are generated due to the pore diameter of the pores 121 of the gas-liquid transmission layer 120 being 0.1-100 μm, the porosity is 1-80%, the number of generated bubbles is large, the whole bubbles have a large surface area, the mass transfer phase interface area between the gas phase and the liquid phase is greatly increased, and the pore diameter can effectively prevent the liquid phase from passing through. The average diameter of bubbles generated by the mass transfer tower tray 100 provided by the application is 200 microns, while the diameter of bubbles generated by the traditional tower tray is generally 10-20 mm, so that the gas-liquid phase interfacial area provided by the scheme is 50-100 times that of the traditional tower tray, and the gas-liquid phase interfacial area is greatly increased. Meanwhile, the diameter of the bubbles generated by the mass transfer tray 100 provided by the application is small, and the coalescence phenomenon is not easy to occur among the bubbles, so that the gas-liquid interface area can be stabilized at a large value. The mass transfer tray 100 provided herein also increases the gas-liquid phase boundary update rate relative to bubbles produced by conventional trays.
2. The effective mass transfer area is increased.
The trayed that reaches that this application embodiment provided, a part on gas-liquid conduction layer 120 is exactly receiving the liquid district (accepting the region of the liquid phase that the last tray fell promptly), and the gaseous phase can pass, receives the liquid district gaseous phase and can't pass for current tray, and the effective mass transfer area of tray that this application provided is bigger, has improved the effective utilization ratio of tray.
3. Increasing the gas-liquid mass transfer time.
The gas passing tray provided by the embodiment of the application can generate bubbles with the average diameter of 200 mu m, and the residence time of the bubbles in the liquid phase is 47 times of the bubble diameter of 20mm under the same condition. Meanwhile, the tower tray is not easy to generate mist entrainment, so that the height of a liquid layer on each layer of the tower tray can be doubled. By adopting the transfer tray provided by the embodiment of the application, the gas-liquid two-phase mass transfer time can be greatly prolonged, and the mass transfer effect can be improved.
4. The gas phase is uniformly distributed.
The tray that this application first embodiment provided has certain pressure drop because the cylindrical pore diameter that sets up in the gas phase distribution layer is very little, and this kind of structure can make the gaseous phase pass through gas phase distribution layer uniformly and get into gas-liquid phase mass transfer region and carry out the mass transfer heat, can not cause the gaseous phase to distribute the inequality on the tray, causes the mass transfer heat transfer efficiency to descend.
The second embodiment of the present application provides a tray that includes a vapor pre-distribution layer 140 and a vapor-liquid transport layer 120. The gas phase pre-distribution layer 140 performs primary distribution on the gas phase, and the gas-liquid transmission layer 120 performs secondary distribution on the gas phase. The gas phase pre-distribution layer 140 has a porosity of 10-95% and a pore diameter of 0.1-50 mm, and has a certain pressure drop, so that the gas phase is uniformly distributed when entering the gas-liquid transmission layer 120. And because the porosity of the gas-liquid transmission layer 120 is less than 10%, the pore diameter is 0.2-100 μm, the pressure drop is larger, which further makes the gas phase uniformly distributed. And finally, the gas phase can uniformly enter the liquid phase from the gas-liquid heat transfer layer 120 to carry out gas-liquid mass and heat transfer. The uneven distribution of the gas phase on the tower tray can not be caused, and the reduction of the mass and heat transfer efficiency can not be caused.
5. Surface super-lyophobic liquid
The gas-liquid transmission layer 120 is coated with a super-lyophobic coating or the gas-liquid transmission layer 120 is made of super-lyophobic material, so that bubbles can be quickly generated when a gas phase enters a liquid phase, and the mass transfer efficiency is improved. The liquid phase is more difficult to leak through the gas-liquid transport layer 120 to the lower tray due to the presence of the ultralyophobic coating or material. And simultaneously, substances such as coke, dirt and the like are not easy to be adhered to the upper surface of the gas-liquid transmission layer 120 to cause the blockage of micropores.
6. No leakage.
When the gas phase loading is too low, the liquid phase on the conventional tray will gravitate and leak through the valve opening to the lower tray, thereby reducing tray efficiency. The tray gas-liquid transmission layer 120 that this application embodiment provided is microporous structure, and the weeping phenomenon is difficult for taking place for the liquid phase, and its surface or material constitute for super lyophobic material in preferred embodiment, and the liquid phase just can not leak lower floor's tray through gas-liquid transmission layer 120 micropore to improve mass transfer efficiency, increased the operation elasticity.
7. No entrainment.
When the gas phase load is too large, the gas-liquid agitation on the trays is increased, and the foam layer is increased, so that the gas phase carries a lot of liquid foam which is not separated into the tray on the upper layer. The diameter of the bubbles generated by the tray provided by the embodiment of the application is very small, and the amount of liquid foam splashed out after the bubbles are broken is very small. Therefore, even if the gas phase load is too large, entrainment does not occur.
When the tray provided by the embodiment of the present application includes the gas phase pre-distribution layer 140, it may also be used as a mist eliminator to cope with a sudden increase of gas phase load, so that the liquid phase is brought to a higher position, and due to the gas phase pre-distribution layer 140, the brought liquid phase may be separated rather than being brought to the tray of the previous layer.
8. A liquid collecting needle 150.
The small liquid droplets brought into the upper gas-liquid transmission layer 120 or the gas-phase pre-distribution layer 140 by the gas phase can be sucked onto the liquid collecting needle 150 by the lyophilic phase coating on the surface of the liquid collecting needle 150, and when the small liquid droplets are collected to a certain amount, the small liquid droplets fall back along the liquid collecting needle 150, so that the drop back speed can be increased, and the retention time of the liquid phase in the gas-liquid transmission layer 120 or the gas-phase pre-distribution layer 140 can be reduced.
9. Efficiency is improved and cost is reduced.
If the tower tray provided by the scheme is applied, the height of the tower can be reduced while the product quality is ensured by newly building the tower, and the manufacturing cost of the tower is greatly reduced. The transformation of the old tower can improve the treatment capacity and the product quality of the device and reduce the number of tower trays, thereby reducing the transformation cost.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. A mass transfer tray is characterized by comprising a gas-liquid transfer layer and a tray supporting mechanism for mounting the mass transfer tray in a distillation tower, wherein the gas-liquid transfer layer is arranged on the tray supporting mechanism, and a gap for liquid to descend is formed between the edge of one end of the gas-liquid transfer layer and the tower wall of the distillation tower after the mass transfer tray is mounted in the distillation tower;
the gas-liquid transmission layer is provided with gas holes for dispersing gas, the pore diameter of the gas holes is 0.1-100 mu m, and the porosity of the gas-liquid transmission layer is 1-80%.
2. The mass transfer tray of claim 1, wherein the gas holes are cylindrical holes parallel to the thickness direction of the gas-liquid mass transfer layer and are uniformly distributed on the gas-liquid mass transfer layer;
preferably, the thickness of the gas-liquid transmission layer is 1-100 mm;
preferably, the holes on the gas-liquid transmission layer are formed in a laser hole opening mode;
further preferably, the material of the gas-liquid transmission layer is metal, metal oxide, ceramic, graphite, silicon carbide or a mixed material of at least two of the above materials.
3. The mass transfer tray of claim 1, wherein the gas-liquid transport layer is shaped as a cut circle with a major arc formed by cutting a circle with a straight line, and the gas-liquid transport layer is a gap formed between the edge of the straight line and the wall of the distillation column for liquid to descend when the mass transfer tray is installed on the distillation column;
preferably, the mass transfer tray further comprises an overflow plate for blocking liquid, and the overflow plate is connected with the tray supporting mechanism and arranged at the edge of the straight line corresponding to the gas-liquid transmission layer.
4. The mass transfer tray of claim 1, further comprising a liquid receiving tray disposed below the gas-liquid transport layer, the liquid receiving tray having vent holes for gas to pass through, the vent holes having a pore size of 0.1 to 100 μm;
preferably, the gas-liquid mass transfer layer is made by sintering, 3D printing or a combination of sintering and 3D printing.
5. The mass transfer tray of claim 4, wherein the upper surface of the gas-liquid conductive layer is coated with an ultralyophobic coating, or the gas-liquid conductive layer is made of an ultralyophobic material.
6. The mass transfer tray of claim 4, further comprising a gas phase pre-distribution layer disposed between the liquid receiving tray and the gas-liquid transfer layer, the gas-liquid transfer layer having a porosity of 1% to 10% and a pore size of 0.2 to 100 μm; the porosity of the gas phase pre-distribution layer is 10% -95%, and the pore diameter is 0.1-50 mm;
preferably, the material of the gas-phase pre-distribution layer is metal, metal oxide, plastic, resin, ceramic, graphite, carborundum or a mixed material formed by at least two of the materials;
preferably, the gas phase pre-distribution layer is made by sintering, 3D printing or a combination of sintering and 3D printing.
7. The mass transfer tray of claim 6, wherein the gas phase pre-distribution layer and the liquid receiving tray are integrally connected;
preferably, the connection means is welding, bonding, embedding, snap connection or screw connection.
8. The mass transfer tray of claim 6, wherein the gas-liquid transport layer, the gas phase pre-distribution layer, and the liquid receiving tray are integrally connected;
preferably, the connection means is welding, bonding, embedding, snap connection or screw connection.
9. The mass transfer tray of claim 1, further comprising a plurality of liquid collection needles, wherein a surface of each liquid collection needle has a lyophilic phase coating, and a plurality of liquid collection needles are disposed on a downward-facing side of the gas-liquid mass transfer layer.
10. A distillation column comprising a column body and a plurality of mass transfer trays according to any one of claims 1 to 9 arranged from top to bottom on the column wall of the column body, wherein the projection of the gap between the last gas-liquid mass transfer layer and the column wall of the column body onto the plane of the next adjacent gas-liquid mass transfer layer is completely within the next gas-liquid mass transfer layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111592583.8A CN114160088B (en) | 2021-12-23 | 2021-12-23 | Mass transfer tray and distillation column |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111592583.8A CN114160088B (en) | 2021-12-23 | 2021-12-23 | Mass transfer tray and distillation column |
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| CN114160088A true CN114160088A (en) | 2022-03-11 |
| CN114160088B CN114160088B (en) | 2023-06-27 |
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| JP2002102601A (en) * | 2000-09-29 | 2002-04-09 | Shuzo Matsumura | Multi-stage tray of plate column and different phase system contact method using the tray |
| CN202777878U (en) * | 2012-06-18 | 2013-03-13 | 天津大学 | Microbubble integral mass transfer tower tray |
| CN205435026U (en) * | 2015-12-28 | 2016-08-10 | 青岛科技大学 | Microbubble tower tray gas -liquid mass transfer column plate |
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| CN114160088B (en) | 2023-06-27 |
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