Integrated high-efficiency falling-film concentration separator

Abstract

The application discloses an integrated high-efficiency falling-film concentration and separation device, which comprises a tower body, an upper tube plate arranged at the upper end of the tower body, an upper tube box arranged above the upper tube plate, a pipe-pass liquid inlet arranged at the top center of the upper tube box, a lower tube plate arranged at the lower end of the tower body, a plurality of tube openings uniformly distributed on the upper tube plate and the lower tube plate, respectively, a falling-film tube arranged between the corresponding tube openings of the upper tube plate and the lower tube plate, a lower tube box arranged below the lower tube plate, a crystal slurry outlet arranged at the bottom of the lower tube box, a secondary steam outlet arranged on the upper portion of the side wall of the lower tube box, a shell-pass steam inlet arranged on the upper portion of the side wall of the tower body and a condensate water outlet arranged on the lower portion of the side wall of the tower body. The falling-film tube is a long-circular-section spiral falling-film tube, the long axis of each cross section is provided with opposite semicircular ends, the short axis of each cross section is provided with parallel ends, and the falling-film tube is continuously twisted into a spiral shape with the center line of the falling-film tube as an axis. The integrated high-efficiency falling-film concentration and separation device has the advantages of small floor area, high heat transfer coefficient, low shell-pass resistance and uniform liquid film distribution in the falling-film tube.

Description

Technical Field

[0001] This invention relates to a falling film thickener, and more particularly to an integrated high-efficiency falling film thickener, belonging to the field of thickening equipment technology, and is used for thickening solutions containing inorganic salts or solids in the new energy or chemical wastewater industries. Background Technology

[0002] The current mainstream technology for the concentration, purification, and separation of chemical wastewater uses four independent devices: a falling film evaporator, a vapor-liquid separator, a steam scrubbing tower, and a thickener, which respectively complete the concentration, vapor-liquid separation, small droplet collection, and clear-turbidity separation. However, the falling film evaporator uses ordinary bare tubes, which presents the following problems:

[0003] 1. Using multiple devices to perform different functions results in high equipment costs, large land area requirements, and higher civil engineering costs.

[0004] 2. Existing conventional falling film evaporators require a considerable number of arc-shaped baffles in the shell side. These baffles serve two purposes: first, they provide longitudinal support to the falling film tubes to prevent vibration caused by the Karman vortex street as the shell-side fluid flows through them; second, they allow the shell-side fluid to glide longitudinally across the tube bundle as much as possible. However, when the shell-side fluid meanders through the tops of each baffle in a wavy pattern, dead zones are formed in the triangular areas on both sides of the junction between the base of each baffle and the inner wall of the shell cylinder. This reduces the effective heat transfer length and area of ​​each falling film tube, and the presence of these dead zones significantly impacts heat transfer efficiency. Furthermore, the traditional arc-shaped baffles are limited in their ability to deflect shell-side steam due to material costs and shell resistance reduction, limiting the number of deflections and the extent of deflection.

[0005] 3. Traditional vertical falling film evaporators use bare tubes. When the shell side is heated by steam condensation, a condensate film will form on the outer wall of the falling film tube after the steam condenses. Due to gravity, the condensate film will gradually thicken in the height direction of the falling film tube, resulting in poor heat transfer in the middle and lower parts of the falling film tube.

[0006] 4. In existing conventional falling film evaporators, the resistance increases when the shell-side fluid flows through the baffle plate notch area due to the reduced flow area.

[0007] 5. Existing conventional falling film evaporators require a large center distance between falling film tubes to reduce the resistance of the shell-side fluid and ensure that the resistance drop of the shell side meets the process requirements. This limits the heat exchanger shell to a larger diameter, resulting in higher material costs.

[0008] 6. Existing conventional falling film evaporators have poor uniformity of liquid film thickness in the circumferential direction within the falling film tubes. To ensure uniform liquid film thickness in the circumferential direction of the falling film tubes, the film distribution effect of the distributor must be good, and the manufacturing and installation of the falling film tube bundles must have high vertical precision. Otherwise, after the tube-side fluid passes through a specially structured distributor, it falls relatively evenly onto the tube bridge of the upper tube sheet. During the downward flow along the falling film tubes, due to deviations in the manufacturing and installation process of the heat exchanger, the non-uniformity of the liquid film in the circumferential direction within the falling film tubes may be amplified, affecting the heat transfer effect. Furthermore, when the deviation of the liquid film in the falling film tubes reaches a certain level, the liquid film thickness may decrease to zero on one side, leading to dry tubes in some areas within the falling film tubes, scaling, and further blockage of the falling film tubes.

[0009] 7. Traditional falling film evaporators use a porous structure for the distributor plate, and the number of holes is generally 1.1 to 1.5 times the number of falling film tubes. Moreover, the structure of a preliminary distributor + single-stage film distributor is generally used. In order to achieve uniform liquid distribution, it is difficult to reduce the number of distribution holes. This results in the distribution hole diameter being relatively small. During the concentration process of inorganic salt solutions or other solutions containing solids, scale easily forms on the surface of the distribution plate. When the scale reaches a certain thickness, it will form a bridge and block the distribution holes, thereby clogging the falling film tubes of the falling film evaporator and preventing normal operation. Summary of the Invention

[0010] The purpose of this section is to outline some aspects of embodiments of the present invention and to briefly describe some preferred embodiments. Simplifications or omissions may be made in this section, as well as in the abstract and title of this application, and such simplifications or omissions should not be construed as limiting the scope of the invention.

[0011] In view of the problems existing in the above and / or prior art, the present invention is proposed.

[0012] The purpose of this invention is to overcome the problems existing in the prior art and provide an integrated high-efficiency falling film concentrator with a small footprint, high heat transfer coefficient, low shell resistance, and uniform liquid film distribution inside the falling film tube.

[0013] To address the above technical problems, the present invention provides an integrated high-efficiency falling film concentrator, comprising a tower body, an upper tube sheet at the upper end of the tower body, an upper tube box above the upper tube sheet, and a tube-side liquid inlet at the top center of the upper tube box; a lower tube sheet at the lower end of the tower body, with multiple tube openings evenly distributed on both the upper and lower tube sheets, and the corresponding tube openings connected by falling film tubes; a lower tube box below the lower tube sheet, a crystal slurry outlet at the bottom of the lower tube box, and a secondary steam outlet on the upper side wall of the lower tube box; a shell-side steam inlet on the upper side wall of the tower body, and a condensate outlet on the lower side wall of the tower body.

[0014] As an improvement of the present invention, a liquid collecting guide tube is connected below the lower tube sheet. The liquid collecting guide tube includes, from top to bottom, a large-diameter section, a conical section, and a small-diameter section. The upper port of the lower tube box is connected to the lower outer periphery of the large-diameter section of the guide tube.

[0015] As a further improvement of the present invention, the cross-section of the inner cavity of the small diameter section of the guide tube is provided with swirl vanes. When the gas-liquid mixture flowing out from the lower tube sheet flows from the large diameter section of the guide tube to the small diameter section of the guide tube, the axial flow velocity increases. When passing through the swirl vanes, it generates high-speed rotation. Under the action of centrifugal force, the small droplets entrained in the secondary gas collide with the inner wall of the small diameter section of the guide tube to form large droplets, which then fall down along the tube wall, reducing the amount of droplets entrained in the secondary gas.

[0016] As a further improvement of the present invention, a demister is provided in the annular cross section between the outer periphery of the small diameter section of the guide tube and the inner wall of the lower pipe box, and an annular flushing device is provided above the demister. The nozzle of the flushing device faces downward and cleans the demister periodically. The flushing device is located below the secondary steam outlet.

[0017] As a further improvement of the present invention, a preliminary separator coaxial with the inlet of the tubular material is provided below the inlet of the tubular material. A preliminary separator plate is provided at the bottom of the preliminary separator plate. The diameter of the preliminary separator plate is 1 / 3 to 1 / 2 of the diameter of the upper tube sheet, and a plurality of preliminary separator holes are uniformly provided on it. A preliminary separator cylinder is provided on the outer periphery of the preliminary separator plate, and the outer circumference of the preliminary separator cylinder is suspended below the top wall of the upper tube box by a plurality of suspension rods.

[0018] As a further improvement of the present invention, the lower circumference of the preliminary liquid separating cylinder is uniformly provided with a plurality of preliminary liquid separating grooves, each of which extends vertically upward, and the lower edge of the preliminary liquid separating groove is flush with the top surface of the preliminary liquid separating plate.

[0019] As a further improvement of the present invention, a primary liquid distributor is provided directly below the primary liquid distributor, and a primary liquid distribution plate is provided at the bottom of the primary liquid distributor; a plurality of primary liquid distribution holes are evenly distributed on the primary liquid distribution plate, and a primary liquid distribution cylinder is provided on the outer periphery of the primary liquid distribution plate.

[0020] As a further improvement of the present invention, a secondary liquid distributor is provided directly below the primary liquid distributor, and a secondary liquid distribution plate is provided at the bottom of the secondary liquid distributor. A plurality of secondary liquid distribution holes are evenly distributed on the secondary liquid distribution plate, and an upwardly upright secondary liquid distribution cylinder is provided on the outer periphery of the secondary liquid distribution plate.

[0021] As a further improvement of the present invention, each secondary liquid distribution hole on the secondary liquid distribution plate is provided with a toothed liquid distribution unit. The middle part of each toothed liquid distribution unit is embedded in the corresponding secondary liquid distribution hole and welded and fixed. The upper part of each toothed liquid distribution unit is symmetrically provided with three V-shaped overflow grooves that are wider at the top and narrower at the bottom. The bottom of each V-shaped overflow groove is flush with the upper surface of the secondary liquid distribution plate. The lower part of each toothed liquid distribution unit is symmetrically provided with three downwardly extending V-shaped drooping parts that are wider at the top and narrower at the bottom. Each V-shaped drooping part is located directly below the corresponding V-shaped overflow groove.

[0022] As a further improvement of the present invention, the adjacent tube openings of the upper tube sheet are distributed in an equilateral triangle, with each set of three falling film tubes corresponding to one toothed liquid distribution unit. The circumference of each toothed liquid distribution unit is located above the center of the three falling film tubes, and the V-shaped drooping part of each toothed liquid distribution unit points to the center point of the tube bridge between the three falling film tubes for liquid distribution.

[0023] As a further improvement of the present invention, the center line of each primary liquid distribution hole on the primary liquid distribution plate is located between two adjacent toothed liquid distribution units.

[0024] As a further improvement of the present invention, the falling film tube is an oblong cross-section spiral falling film tube, with the two ends of the long axis of each cross-section being opposing semicircles and the two ends of the short axis being parallel to each other, and continuously twisted into a spiral shape with the center line of the falling film tube as the axis.

[0025] As a further improvement of the present invention, the major axis and minor axis of each oblong cross-section spiral falling film tube are parallel to each other, and the gap between each row of oblong cross-section spiral falling film tubes in the minor axis direction constitutes the shell-side medium channel.

[0026] As a further improvement of the present invention, the center distance between adjacent oblong cross-section spiral falling film tubes is equal to the length of the major axis, so that adjacent oblong cross-section spiral falling film tubes achieve self-support by being tangentially contacted by the two ends of the major axis.

[0027] As a further improvement of the present invention, the centerline of each oblong cross-section spiral falling film tube remains unchanged during the spiral process. Within 360° of each pitch, it makes tangential contact with the adjacent oblong cross-section spiral falling film tube six times, and the position of the tangential contact point with the adjacent oblong cross-section spiral falling film tube changes every 60°.

[0028] As a further improvement of the present invention, the outer periphery of the oblong cross-section spiral falling film tube bundle is dodecagonal, and multiple straps are bound around the outer periphery.

[0029] As a further improvement of the present invention, the cross-sectional dimensions of each oblong cross-section spiral falling film tube are 45x25.5mm, and the spiral pitch is 250mm; the upper and lower ends of each oblong cross-section spiral falling film tube are circular base tubes with an outer diameter of 38mm.

[0030] As a further improvement of the present invention, a clear liquid overflow device is installed at the bottom center of the lower tube box. The clear liquid overflow device includes an umbrella-shaped cover and a conical hopper coaxial with the lower tube box. The center of the cone top of the umbrella-shaped cover is provided with a pressure balancing bend, and the lower port of the umbrella-shaped cover is provided with a vertically downward extending cylinder. The conical hopper has a structure that is larger at the top and smaller at the bottom, with the upper end located in the inner cavity of the umbrella-shaped cover. The outer wall of the upper port of the conical hopper is connected to the inner wall of the cylinder of the umbrella-shaped cover by a plurality of symmetrically arranged ribs. The bottom of the conical hopper is supported at the bottom of the lower tube box, and the lower end of the conical hopper is connected to an overflow clear liquid outlet extending out of the lower tube box. The concentrate enters the lower tube box and settles and separates. The concentrate containing crystal slurry particles has a higher density and is discharged from the crystal slurry outlet at the bottom of the lower tube box. The clear liquid has a lower density and floats up from the annular space between the umbrella-shaped cover cylinder and the upper end of the conical hopper and enters the conical hopper, and then is discharged from the overflow clear liquid outlet.

[0031] As a further improvement of the present invention, a tower support is welded to the upper circumferential outer wall of the tower body, and a tower top lifting column is fixed on the tower support. The upper end of the tower top lifting column is bent towards the center line of the tower top and is provided with a lifting lug for the upper pipe box to facilitate lifting. A plurality of tower lifting lugs are also symmetrically provided on the upper circumferential outer wall of the tower body.

[0032] Compared with the prior art, the advantages or beneficial effects of the embodiments of this application include at least the following: 1. By adopting a compact combined structure, the original four devices are integrated into one device, reducing the site area occupied by more than 50%; and there is no need to set up a vapor-liquid separator, a vertical steam scrubber and a thickener, thus saving the material cost required to build these two devices; at the same time, the material cost of the original three devices that needed to be connected to each other through pipes and flanges is also saved; in addition, the original connection of these four devices through pipes and flanges had the risk of leakage from pipe welding and flange connection, and now the elimination of these pipes and flanges also increases the reliability of the device.

[0033] 2. Eliminating the shell-side baffles saves on material costs and machining costs associated with them; it also eliminates the need for tie rods and spacer tubes, further reducing material costs.

[0034] 3. By using a smaller falling film tube center distance, the diameter of the tube bundle is smaller under the same heat exchange area. This means that a thinner tower body and upper and lower tube sheets can be used. The diameter and thickness of the tube sheets and tower body can be reduced, saving material costs.

[0035] 4. Using a long oval cross-section spiral falling film tube as the falling film tube, the unique structure of the long oval cross-section spiral falling film tube prevents the liquid film formed when the heating steam condenses in the shell side from continuously thickening as in traditional falling film evaporators. This reduces the thickness of the outer thermal boundary layer of the falling film tube, resulting in a smaller thermal resistance between the steam and the outer wall of the falling film tube. At the same time, the spiral structure on the inner wall of the falling film tube makes the liquid film thickness on the inner wall of the tube more uniform through secondary distribution. The secondary flow in the circumferential direction also makes the thermal boundary layer thickness of the liquid film inside the falling film tube more uniform, which also improves the heat transfer coefficient on the tube side. With the combined improvement of heat transfer efficiency inside and outside the tube, the overall heat transfer coefficient of the integrated high-efficiency falling film evaporator separator is increased from 1600W / (㎡·K) of traditional falling film evaporators to over 2100W / (㎡·K), an increase of over 31%.

[0036] 5. Due to the secondary flow in the circumferential direction generated on the inner wall of the oblong cross-section spiral falling film tube, the flow boundary layer velocity of the liquid film inside the tube is faster, and the scaling cycle on the inner wall of the oblong cross-section spiral falling film tube is longer, which means that a lower tube-side fouling thermal resistance can be selected in the thermal calculation.

[0037] 6. A liquid collection guide tube is installed at the bottom of the lower tube box. A swirl vane is installed in the inner cavity of the small diameter section of the guide tube. When the gas-liquid mixture from the lower tube sheet flows from the large diameter section of the guide tube to the small diameter section, the cross-section decreases and the axial velocity increases. When passing through the swirl vane, it generates high-speed rotation. Under the action of centrifugal force, the small droplets entrained in the secondary steam collide with the inner wall of the small diameter section of the guide tube to form large droplets and then fall down along the tube wall. This reduces the amount of droplets entrained in the secondary steam.

[0038] 7. The bottom of the integrated high-efficiency falling film evaporator is equipped with a clear liquid separation device, which can replace the thickener. The unique overflow structure makes the separation of clear liquid from concentrated salt solution better, and the content of salt solid particles in the clear liquid is significantly reduced compared with traditional vapor-liquid separators.

[0039] 8. The top film distributor adopts a multi-stage structure of preliminary distributor + first-stage distributor + second-stage film distributor. Through the specially designed toothed distribution unit, the chemical cleaning cycle of the falling film evaporator can be greatly extended and the difficulty of chemical cleaning can be reduced. Attached Figure Description

[0040] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. The drawings are provided for reference and illustration only and are not intended to limit the present invention.

[0041] in:

[0042] Figure 1 This is a front view of the integrated high-efficiency falling film thickener separator of the present invention;

[0043] Figure 2 for Figure 1 The left view;

[0044] Figure 3 This is an exploded view of the multi-stage liquid distribution mechanism in this invention;

[0045] Figure 4 A three-dimensional magnified view of the secondary film distribution device;

[0046] Figure 5 This is a three-dimensional enlarged view of the toothed liquid distribution unit in the secondary film distributor;

[0047] Figure 6 This is a top view of the upper tube sheet and the toothed liquid distribution unit above it in this invention;

[0048] Figure 7 This is a perspective view of the spiral falling film tube bundle with a circular outer circumference in this invention;

[0049] Figure 8 This is a perspective view of a spiral falling film tube with an oblong cross-section in this invention;

[0050] Figure 9 This is a schematic diagram of the self-support point transformation of the elongated cross-section spiral falling film tube bundle in this invention;

[0051] Figure 10 This is a cross-sectional view of the clear liquid overflow device in this invention;

[0052] In the diagram: 1. Tower top lifting column; 1a. Upper pipe box lifting lug;

[0053] 2. Upper tube box; 2a. Tube-side liquid inlet;

[0054] 3. Preliminary separator; 3a. Preliminary separator tray; 3b. Preliminary separator trough;

[0055] 4. Primary liquid distributor; 5. Secondary film distributor;

[0056] 6. Toothed liquid distribution unit; 6a. V-shaped overflow groove; 6b. V-shaped droop;

[0057] 7. Upper tube sheet; 8. Elongated oval cross-section spiral falling film tube; 9. Bundle;

[0058] 10. Tower body; 10a. Shell-side steam inlet; 10b. Condensate outlet; 10c. Tower body lifting lugs;

[0059] 11. Lower tube sheet; 12. Liquid collecting guide tube; 13. Swirl blades;

[0060] 14. Lower tube box; 14a. Secondary steam outlet; 14b. Crystal slurry outlet;

[0061] 15. Demister; 16. Flushing device;

[0062] 17. Clear liquid overflow device; 17a. Umbrella-shaped cover; 17b. Pressure balancing bend; 17c. Rib plate; 17d. Conical hopper; 17e. Clear liquid overflow outlet. Detailed Implementation

[0063] In the following description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not mean that the device must have a specific orientation.

[0064] To make the technical means, creative features, objectives, and effects of this invention easier to understand, the invention is further described below with reference to specific illustrations. Obviously, the described embodiments are only a part of the embodiments of this invention, and not all of them.

[0065] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

[0066] like Figure 1 , Figure 2 As shown, the integrated high-efficiency falling film evaporator separator of the present invention includes a tower body 10. An upper tube sheet 7 is provided at the upper end of the tower body 10. An upper tube box 2 is provided above the upper tube sheet 7, and a tube-side liquid inlet 2a is provided at the center of the top of the upper tube box 2. A multi-stage film distribution device is provided below the tube-side liquid inlet 2a. A lower tube sheet 11 is provided at the lower end of the tower body 10. Multiple tube openings are evenly distributed on the upper tube sheet 7 and the lower tube sheet 11, and the corresponding upper and lower tube openings are connected by falling film tubes. A lower tube box 14 is provided below the lower tube sheet 11. A crystal slurry outlet 14b is provided at the bottom of the lower tube box 14, and a secondary steam outlet 14a is provided on the upper side wall of the lower tube box 14. A shell-side steam inlet 10a is provided on the upper side wall of the tower body 10. The shell-side steam inlet 10a is located on the expanded diameter section at the top of the tower body, facilitating steam entry and even distribution. A condensate outlet 10b is provided on the lower side wall of the tower body 10.

[0067] Steam entering from the shell-side steam inlet 10a at the top of the tower heats the falling film tubes, releasing its latent heat of vaporization and becoming condensate, which is discharged from the condensate outlet 10b at the bottom of the tower. Salt solution or other liquids enter the upper tube box 2 from the tube-side liquid inlet 2a, are evenly distributed by a multi-stage film distribution device, fall onto the upper tube sheet 7, and then uniformly enter each falling film tube, forming a falling film on the inner wall of each tube. This increases the specific surface area of ​​the liquid, and under the heating in the shell side, the water or solvent evaporates rapidly, thus achieving rapid concentration.

[0068] The upper circumferential outer wall of the tower is also symmetrically equipped with multiple tower lifting lugs 10c, which facilitate the lifting, positioning and installation of the tower.

[0069] The upper circumferential outer wall of the tower body is welded with a tower body support. The tower top hanging column 1 is fixed on the tower body support. The tower top hanging column 1 is L-shaped, with the upper end bent towards the center line of the tower top and equipped with an upper pipe box lifting lug 1a. The upper pipe box 2 can be easily lifted through the upper pipe box lifting lug 1a and the wire rope, which is convenient for cleaning the dirt on the multi-stage film distribution device, as well as for cleaning the dirt in each falling film pipe, or for maintenance and replacement.

[0070] like Figures 3 to 5 As shown, the multi-stage membrane distribution device of this invention adopts a stacked structure of a preliminary distributor 3 + a first-stage distributor 4 + a second-stage membrane distribution device 5. The preliminary distributor 3 is located below the feed inlet 2a in the tube side and is coaxial with it. A preliminary distribution plate 3a is provided at the bottom of the preliminary distributor 3. A preliminary distribution cylinder is provided on the outer periphery of the preliminary distribution plate 3a and extends upward. The outer circumference of the preliminary distribution cylinder is suspended below the top wall of the upper tube box 2 by multiple suspension rods. The diameter of the preliminary distribution plate 3a is 1 / 3 to 1 / 2 of the diameter of the upper tube plate, and it has multiple preliminary distribution holes evenly distributed on it. Each preliminary distribution hole only performs preliminary distribution, so the orifice diameter and flow rate of the preliminary distribution hole are relatively large, and it is not easy to form a blockage.

[0071] The lower circumference of the preliminary liquid separating cylinder is uniformly provided with multiple preliminary liquid separating grooves 3b, each extending vertically upward, with its lower edge flush with the top surface of the preliminary liquid separating plate 3a. While each preliminary liquid separating hole distributes liquid downward, each preliminary liquid separating groove 3b around the perimeter also distributes liquid outward, ensuring that the liquid is distributed downward as evenly as possible.

[0072] A primary distributor 4 is located directly below the primary distributor 3, and a primary distributor plate is located at the bottom of the primary distributor 4. Multiple primary distributor holes are evenly distributed on the primary distributor plate, and an upward-standing primary distributor cylinder is located on the outer periphery of the primary distributor plate. Handles are symmetrically provided on the inner wall of the upper end of the primary distributor cylinder for easy installation and disassembly.

[0073] A secondary liquid distributor 5 is located directly below the primary liquid distributor 4. A secondary liquid distribution plate is located at the bottom of the secondary liquid distributor 5. Multiple secondary liquid distribution holes are evenly distributed on the secondary liquid distribution plate. A secondary liquid distribution cylinder is located on the outer periphery of the secondary liquid distribution plate and has handles symmetrically located on the inner wall of the upper end of the secondary liquid distribution cylinder.

[0074] Each secondary liquid distribution hole on the secondary liquid distribution plate is provided with a toothed liquid distribution unit 6. The middle part of each toothed liquid distribution unit 6 is embedded in the corresponding secondary liquid distribution hole and welded and fixed. The upper part of each toothed liquid distribution unit 6 is symmetrically provided with three V-shaped overflow grooves 6a that are wider at the top and narrower at the bottom. The bottom of each V-shaped overflow groove 6a is flush with the upper surface of the secondary liquid distribution plate. The lower part of each toothed liquid distribution unit 6 is symmetrically provided with three downwardly extending V-shaped drooping parts 6b that are wider at the top and narrower at the bottom. Each V-shaped drooping part 6b is located directly below the corresponding V-shaped overflow groove 6a.

[0075] like Figure 6 As shown, the adjacent tube openings of the upper tube sheet 7 are arranged in an equilateral triangle. Every three falling film tubes correspond to a toothed liquid distribution unit 6. The circumference of each toothed liquid distribution unit 6 is located above the center of the three falling film tubes, and each V-shaped drooping part 6b of the toothed liquid distribution unit 6 points to the center point of the tube bridge between the three falling film tubes for liquid distribution.

[0076] The center line of each primary liquid distribution hole on the primary liquid distribution plate is located between two adjacent toothed liquid distribution units 6. Although the primary liquid distribution plate also adopts a porous structure, the number of primary liquid distribution holes is about 30% of the number of falling film tubes. Therefore, the diameter of the primary liquid distribution holes is also larger, and it is difficult to form bridging blockage.

[0077] The liquid on the secondary liquid distribution plate overflows from each V-shaped overflow groove 6a into the inner cavity of the toothed liquid distribution unit 6, flows down along its inner wall, and when it reaches the lower end of the V-shaped drooping part 6b, it accurately distributes the liquid to the center point of the pipe bridge between the three falling film pipes.

[0078] Each toothed liquid distribution unit 6 adopts a toothed structure, which not only provides better flowability and adjustable membrane flow rate over a wide range, but also reduces the number of toothed liquid distribution units 6 to only 1 / 3 of the number of falling film tubes. The diameter of the liquid distribution unit is approximately 1.37-1.5 times that of the falling film tube, virtually eliminating the possibility of bridging due to scaling. After a tiny bridging structure forms at the lowest triangle of the V-shaped drooping portion 6b, the bridging structure will self-clean due to the scouring effect of the liquid flow (especially for solutions containing solids), which greatly extends the service life of the entire membrane distribution system.

[0079] Although the number of toothed liquid distribution units 6 is only 1 / 3 of the number of falling film tubes, it can still accurately ensure that three film distribution points are evenly distributed on the outer periphery of each falling film tube below, which greatly improves the uniformity of film distribution.

[0080] The following improvements were made to address the inherent defects of the bow-shaped baffle: (e.g.) Figures 7 to 9 As shown, each falling film tube is changed from a light tube to a spiral falling film tube 8 with an elongated oval cross section. That is, the two sides of each falling film tube are parallel to each other, and the two ends are semi-circular cross sections facing each other. The straight line where the center of the two semi-circular cross sections is located is the major axis of the falling film tube, and the line between the parallel two sides is the minor axis of the falling film tube. The falling film tube is continuously twisted into a spiral shape along the height direction with the center line of the falling film tube as the axis.

[0081] The major and minor axes of each oblong cross-section spiral falling film tube 8 are parallel to each other, that is, the phase of each oblong cross-section spiral falling film tube 8 on the cross-section of the tower body is consistent; the gap between each row of oblong cross-section spiral falling film tubes 8 in the minor axis direction constitutes the shell side medium channel.

[0082] The center-to-center distance between adjacent oblong cross-section spiral falling film tubes 8 is equal to the length of their major axis, allowing them to achieve self-support through tangential contact at the two ends of their major axes. This avoids a series of problems associated with using bow-shaped baffles; simultaneously, the self-support between the two ends of the falling film tube's major axis better prevents vibrations caused by the Karman vortex street. Furthermore, without the obstruction of bow-shaped baffles, shell-side steam can rapidly flow through the entire length of the tube bundle, and then, due to pressure, overcomes flow resistance to flow towards the central region and the other side of the bundle. The entire shell-side flow process has no dead zones, resulting in a significantly improved heat transfer efficiency compared to traditional tube bundles. Moreover, compared to bow-shaped baffles, the flow of shell-side gas in falling film tube bundles is disturbed circumferentially by the spiral space formed between the tubes, with the number of disturbances increasing... Figure 7 Taking the tube bundle in this embodiment as an example, the turbulence can reach 38 rotations, or 38 spiral turns. Compared to the approximately 5-8 rotations required by traditional bow-shaped baffles, the shell-side turbulence effect is much better, and the turbulence intensity and shell-side Reynolds number are also correspondingly increased. Because no bow-shaped baffles are used, the flow cross-sectional area remains unchanged, and the shell-side resistance is much lower than that of the bow-shaped baffle tube bundle. In this embodiment, there are no dead zones on both sides of the root of each bow-shaped baffle during the steam flow process, and the outer periphery of the entire elongated oval cross-section spiral falling film tube is an effective heat exchange area.

[0083] like Figure 9As shown, the oblong cross-section spiral falling film tubes are arranged in an equilateral triangle and their centerline remains unchanged during the spiral process. Within 360° of each pitch, there are six tangential contacts with adjacent oblong cross-section spiral falling film tubes, and the position of the tangential contact point with adjacent oblong cross-section spiral falling film tubes changes every 60°. Self-support is achieved through the contact points. Multiple straps 9 are tied around the outer periphery of the falling film tube bundle to fix the tube bundle as a whole. The tube bundle is arranged in a specially designed dodecagonal shape, which maximizes the use of the circular area of ​​the upper tube sheet 7 and can be perfectly matched with the toothed liquid distribution unit 6 above. The straps 9 contact the outermost layer of falling film tubes of the tube bundle, so that all falling film tubes are supported by each other through the contact points. There is no need to use the traditional bow-shaped baffle to fix the tube bundle. The oblong cross-section spiral falling film tubes can also be precisely positioned with each other, and the shell-side fluid can automatically change direction along the flow channel between the oblong cross-section spiral falling film tubes. When the shell-side fluid flows through the gap between the falling film tubes, it transfers heat to the condensate film on the wall of the falling film tube. Due to the greatly shortened flow length, the shell-side resistance is much lower than that of the traditional structure, and the resistance distribution along the tube bundle height is also more uniform.

[0084] Taking 0° as an example, the shell-side steam first flows along the vertical channel. When it reaches 60°, the shell-side steam flows along the inclined channel, and so on. This causes the flow channel of the shell-side steam to switch constantly, creating a continuous disturbance to the shell-side fluid, keeping the steam in a turbulent state and improving heat exchange efficiency.

[0085] When the steam in the shell side condenses into a liquid film on the outer wall of the falling film tube, it falls down the outer wall of the falling film tube due to gravity. After encountering the contact point with the surrounding falling film tubes, periodic disturbances occur. Therefore, the thickness of the condensate film is always kept within a small range, and the heat transfer coefficient of the shell side film is significantly improved compared to the bare tube. Furthermore, the steam inlet method used in this invention is to introduce steam from the upper middle part and discharge condensate from the bottom. As the steam flows downward along the spiral flow channel formed between the falling film tubes, it can push the condensate film to flow downward at an accelerated speed.

[0086] Because the elongated oval cross-section spiral falling film tubes achieve self-support through their contact points with surrounding falling film tubes, the center-to-center distance between adjacent falling film tubes can be directly set as the major axis of the cross-section. This significantly reduces the center-to-center distance compared to traditional falling film evaporators. Furthermore, due to the absence of baffles, the shell-side fluid resistance drop is also lower than in traditional falling film evaporators, resulting in a substantial increase in heat transfer per unit shell-side resistance drop. Simultaneously, the reduced shell diameter compared to traditional falling film evaporators allows for reductions in parameters such as tube sheet diameter, tube sheet thickness, and tube box flange thickness, thereby significantly lowering material costs.

[0087] When the tube-side fluid passes through the secondary film distributor 5 and falls onto the center of each tube bridge in the upper tube sheet 7, even if the manufacturing and installation of the heat exchanger causes some deviation in the verticality of the falling film tubes, it will not affect the uniformity of the liquid film thickness in the circumferential direction. When the liquid film falls along the inner wall of the falling film tube, due to the spiral action, the liquid film will autonomously form a secondary distribution in the circumferential direction, which will offset the negative impact of the verticality deviation of the falling film tube, thus greatly improving the tube-side heat transfer coefficient, and at the same time better preventing scaling problems caused by dry tubes in the falling film tubes.

[0088] Each oblong-section spiral falling film tube has a circular base tube with an outer diameter of 38mm at both its upper and lower ends, facilitating insertion into the upper tube sheet 7 and lower tube sheet 11. The cross-sectional dimensions of each oblong-section spiral falling film tube are 45x25.5mm, with a spiral pitch of 250mm. These dimensions are the result of multiple verifications: firstly, machining the 38mm outer diameter circular base tube to a cross-sectional major axis of 45mm achieves a yield rate of over 99% in the processing of irregularly shaped tubes; secondly, when the cross-sectional major axis is set to 45mm, the cross-sectional area formed by the gaps between the oblong-section spiral falling film tubes accounts for 43.4% of the total cross-sectional area of ​​the tube bundle (within the dodecagon). Taking the tube bundle application shown in this embodiment as an example, the cross-sectional velocity of the shell-side steam is 4.5 m / s, and the shell-side resistance is about 52 kPa. The shell-side film heat transfer coefficient can reach more than 3100 W / (㎡*K). This size is the optimal solution for the cross-sectional shape under this pitch. The specific data comparison is shown in the table below (assuming the heat exchange area and pitch are the same).

[0089] 44 5.88 75 2933 45 4.92 52 3135 46 4.43 42 2836

[0090] As can be seen from the table above, in the most common operating conditions of falling film evaporation of liquid materials containing solids in inorganic salt solutions or biochemical industries, the optimal solution is to set the long axis of the spiral falling film tube to 45 mm and the short axis to 25.5 mm.

[0091] like Figure 1 , Figure 2 and Figure 10 As shown, a liquid collecting guide tube 12 is provided in the lower separation section of the integrated high-efficiency falling film evaporator. The liquid collecting guide tube 12 is connected to the lower tube sheet 11. The liquid collecting guide tube 12 includes a large diameter section, a conical section and a small diameter section from top to bottom. The upper port of the lower tube box 14 is connected to the lower outer periphery of the large diameter section of the guide tube.

[0092] The inner cross-section of the small-diameter section of the guide tube is equipped with swirl vanes 13. When the gas-liquid mixture flowing out from the lower tube sheet 11 flows from the large-diameter section of the guide tube to the small-diameter section, the axial velocity increases. When passing through the swirl vanes 13, it generates high-speed rotation. Under the action of centrifugal force, the small droplets entrained in the secondary gas collide with the inner wall of the small-diameter section of the guide tube to form large droplets, which then fall down along the tube wall, reducing the amount of droplets entrained in the secondary gas.

[0093] A demister 15 is provided in the annular section between the outer periphery of the small diameter section of the guide tube and the inner wall of the lower tube box 14. An annular flushing device 16 is provided above the demister 15. The nozzle of the flushing device 16 faces downward and cleans the demister 15 periodically. The flushing device 16 is located below the secondary steam outlet 14a.

[0094] A clear liquid overflow device 17 is installed at the bottom center of the lower pipe box 14. The clear liquid overflow device 17 includes an umbrella-shaped cover 17a and a cone 17d coaxial with the lower pipe box 14. The center of the cone top of the umbrella-shaped cover 17a is provided with a pressure balancing bend 17b. The lower port of the umbrella-shaped cover 17a is provided with a vertically downward extending cylinder. The cone 17d has a structure that is larger at the top and smaller at the bottom, and its upper end is located in the inner cavity of the umbrella-shaped cover 17a. The outer wall of the upper port of the cone 17d is connected to the inner wall of the cylinder of the umbrella-shaped cover 17a by a plurality of symmetrically arranged stiffeners 17c. The bottom of the cone 17d is supported on the bottom of the lower pipe box 14. The lower end of the cone 17d is connected to an overflow clear liquid outlet 17e that extends out of the lower pipe box 14. The concentrate enters the lower tube box 14 for sedimentation and separation. The concentrate containing crystal slurry particles has a higher density and is discharged from the crystal slurry outlet 14b at the bottom of the lower tube box 14. The clear liquid has a lower density and floats up from the annular space between the umbrella-shaped cover and the upper end of the cone hopper 17d and enters the cone hopper 17d, and then is discharged from the overflow clear liquid outlet 17e.

[0095] This invention integrates the functions of four separate devices into one, achieving liquid concentration, vapor-liquid separation, and collection of small droplets and separation of clear and turbid liquids in a single device. It occupies less space, has lower steel structure costs, and reduces the number of flange connection points between devices, thereby lowering material costs and leakage risks.

[0096] During equipment operation, the concentrated liquid, after being preheated to the process temperature, enters the upper tube box 2 through the liquid inlet 2a at the top. After being evenly distributed by the preliminary distributor 3, it falls onto the distribution plate of the first-stage distributor 4, stays on the distribution plate for a short time, and then flows downward to the distribution plate of the second-stage film distributor 5. After passing through the specially designed toothed distribution unit 6, it falls onto the tube bridge of the upper tube sheet 7. Then, due to gravity, it flows downward along the inner wall of the elongated cross-section spiral falling film tube to form a liquid film. However, the thickness of the liquid film is not uniform in the horizontal circumferential direction. During the process of the liquid flowing downward along the inner wall of the elongated cross-section spiral falling film tube, the unique spiral structure of the elongated cross-section spiral falling film tube causes the liquid to have a secondary flow in the horizontal circumferential direction in addition to the vertical flow. Under the dual effect of this secondary flow and the surface tension of the liquid itself, the thickness of the liquid film in the circumferential direction becomes more uniform. Since this secondary flow in the circumferential direction exists throughout the entire height of the falling film tube, it can correct the adverse effects on the uniformity of the liquid film thickness caused by the deviation in the verticality of the tube bundle installation at any time.

[0097] As the liquid film formed on the inner wall of the falling film tube flows downwards, it reaches its boiling point due to the heating provided by the shell-side steam, causing partial vaporization. The resulting secondary steam, under the suction force of the secondary steam outlet 14a, flows rapidly downwards along the inner wall of the falling film tube. The liquid film on the inner wall of the elongated cross-section spiral falling film tube continues to flow downwards and vaporize under the influence of gravity and airflow thrust. Finally, the concentrated liquid and secondary steam mixture flows out from the lower tube sheet 11, passing through the swirl vanes 13 in the lower section of the liquid collecting guide tube 12. Due to the centrifugal force of the swirl vanes 13, small droplets in the vapor-liquid mixture collide with the tube wall, forming larger droplets that fall down the inner wall of the guide tube. Then, the liquid in the vapor-liquid mixture settles due to gravity in the storage section at the bottom of the lower tube box 14. After separation, the clear liquid and crystal slurry are discharged from the crystal slurry outlet 14b and sent to a centrifuge for further separation. The clear liquid, after passing through the clear liquid overflow device 17, flows out of the equipment from the overflow clear liquid outlet 17e for further concentration.

[0098] Meanwhile, the secondary steam in the vapor-liquid mixture flows out from the lower port of the liquid collecting guide tube 12 and then turns upward. A small amount of small liquid droplets entrained in it are captured by the demister 15, and the remaining relatively pure secondary steam enters the compressor through the secondary steam outlet 14a, is heated and pressurized, and then re-enters the tube bundle shell-side space through the shell-side steam inlet 10a, achieving recycling. Since no baffles are set in the shell-side space, the steam can quickly pass through the entire shell-side space, and then flow into the interior space of the tube bundle due to the steam pressure. During this process, the risk of falling film tube vibration under the action of Karman vortex street is avoided because the long oval cross-section spiral falling film tubes can support each other. The outermost ring of the long oval cross-section spiral falling film tubes is arranged in a dodecagon. Due to the setting of the bundle 9, the overall rigidity and strength of the tube bundle are guaranteed.

[0099] Shell-side steam condenses outside the oblong cross-section spiral falling film tubes, forming a condensate film. This condensate film flows downwards along the outer wall of the tubes. When it encounters contact points with surrounding tubes, the condensate film converges to both sides of the contact point. This prevents the condensate film on the outer wall of the falling film tube below the contact point from continuously thickening, thus ensuring more efficient heat exchange between the shell-side steam and the oblong cross-section spiral falling film tubes. As the shell-side steam flows through the channels between the tube bundles, its unique shape causes continuous disturbance, resulting in a higher shell-side heat transfer coefficient. The condensate film flows downwards along the outer wall of the oblong cross-section spiral falling film tubes to the bottom and is then discharged from the equipment through the condensate outlet 10b.

[0100] The above description is merely a preferred embodiment of the present invention, showing and describing the basic principles, main features, and advantages of the present invention. It is not intended to limit the scope of patent protection of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments. In addition to the above embodiments, the present invention may have other implementations without departing from the spirit and scope of the invention. Various changes and modifications to the present invention are possible, and all technical solutions formed by equivalent substitutions or equivalent transformations fall within the scope of protection claimed by the present invention. The scope of protection of the present invention is defined by the appended claims and their equivalents. Technical features not described in the present invention can be implemented by or using existing technology, and will not be elaborated here.

Claims

1. An integrated high-efficiency falling film concentrator, comprising a tower body, characterized in that: The upper end of the tower body is provided with an upper tube sheet, and above the upper tube sheet is an upper tube box. The top center of the upper tube box is provided with a tube-side liquid inlet. The lower end of the tower body is provided with a lower tube sheet. Multiple tube openings are evenly distributed on the upper and lower tube sheets respectively. Corresponding tube openings are connected by falling film tubes. Below the lower tube sheet is a lower tube box. The bottom of the lower tube box is provided with a crystal slurry outlet. The upper side wall of the lower tube box is provided with a secondary steam outlet. The upper side wall of the tower body is provided with a shell-side steam inlet, and the lower side wall of the tower body is provided with a condensate outlet. Below the feed inlet of the tubular section, a preliminary distributor is coaxial with it. Directly below the preliminary distributor, a primary distributor is located, and directly below the primary distributor, a secondary distributor is located. At the bottom of the secondary distributor, a secondary distribution plate is provided, with multiple secondary distribution holes evenly distributed on the plate. Each secondary distribution hole on the plate contains a toothed distribution unit, the middle of which is embedded in and welded to the corresponding secondary distribution hole. Each toothed distribution unit has three V-shaped overflow grooves, wider at the top and narrower at the bottom, symmetrically arranged on its upper circumference. The bottom of each V-shaped overflow groove is flush with the upper surface of the secondary distribution plate. The lower circumference of each toothed distribution unit is symmetrically arranged... The upper tube sheet has three downward-extending V-shaped drooping sections, wider at the top and narrower at the bottom, each located directly below a corresponding V-shaped overflow groove. The adjacent tube openings of the upper tube sheet are arranged in an equilateral triangle, with each set of three falling film tubes corresponding to one toothed liquid distribution unit. The circumference of each toothed liquid distribution unit is located above the center of the three falling film tubes, and each V-shaped drooping section of the toothed liquid distribution unit points towards the center point of the pipe bridge between the three falling film tubes. A clear liquid overflow device is installed at the bottom center of the lower tube box. The clear liquid overflow device includes an umbrella-shaped cover and a conical hopper coaxial with the lower tube box. A pressure-balancing bend is provided at the center of the cone apex of the umbrella-shaped cover, and a vertically downward-extending cylinder is provided at the lower port of the umbrella-shaped cover.

2. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: A liquid collecting guide tube is connected below the lower tube sheet. The liquid collecting guide tube includes, from top to bottom, a large-diameter section, a conical section, and a small-diameter section. The upper port of the lower tube box is connected to the lower outer periphery of the large-diameter section of the guide tube.

3. The integrated high-efficiency falling film thickener and separator according to claim 2, characterized in that: The inner cross-section of the small-diameter section of the guide tube is equipped with swirl vanes. When the gas-liquid mixture flowing out from the lower tube sheet flows from the large-diameter section of the guide tube to the small-diameter section, the axial velocity increases. When passing through the swirl vanes, it generates high-speed rotation. Under the action of centrifugal force, the small droplets entrained in the secondary gas collide with the inner wall of the small-diameter section of the guide tube to form large droplets, which then fall down along the tube wall, reducing the amount of droplets entrained in the secondary gas.

4. The integrated high-efficiency falling film thickener and separator according to claim 2, characterized in that: A demister is provided at the annular cross-section between the outer periphery of the small-diameter section of the guide tube and the inner wall of the lower pipe box. An annular flushing device is provided above the demister, with the nozzle of the flushing device pointing downwards to periodically clean the demister. The flushing device is located below the secondary steam outlet.

5. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The bottom of the preliminary separator is provided with a preliminary separation plate, the diameter of which is 1 / 3 to 1 / 2 of the diameter of the upper tube sheet, and there are multiple preliminary separation holes evenly distributed on it; the outer periphery of the preliminary separation plate is provided with an upwardly upright preliminary separation cylinder, and the outer circumference of the preliminary separation cylinder is suspended below the top wall of the upper tube box by multiple suspension rods.

6. The integrated high-efficiency falling film thickener and separator according to claim 5, characterized in that: The lower circumference of the preliminary liquid separating cylinder is uniformly provided with multiple preliminary liquid separating grooves, each of which extends vertically upwards, and the lower edge of the preliminary liquid separating groove is flush with the top surface of the preliminary liquid separating plate.

7. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The bottom of the primary liquid distributor is provided with a primary liquid distribution plate; the primary liquid distribution plate is evenly distributed with multiple primary liquid distribution holes, and the outer periphery of the primary liquid distribution plate is provided with an upwardly upright primary liquid distribution cylinder.

8. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The outer periphery of the secondary liquid distribution plate is provided with an upward-facing secondary liquid distribution cylinder.

9. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The centerline of each primary liquid distribution hole on the primary liquid distribution plate is located between two adjacent toothed liquid distribution units.

10. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The falling film tube is an oblong spiral falling film tube with the two ends of the major axis of each cross section being opposing semicircles and the two ends of the minor axis being parallel to each other, continuously twisted into a spiral shape with the center line of the falling film tube as the axis.

11. The integrated high-efficiency falling film thickener and separator according to claim 10, characterized in that: Within the same cross-section, the major and minor axes of each oblong-section spiral falling film tube are parallel to each other, and the gaps between each row of oblong-section spiral falling film tubes in the minor axis direction constitute the shell-side medium channel.

12. The integrated high-efficiency falling film thickener and separator according to claim 10, characterized in that: The center distance between adjacent oblong cross-section spiral falling film tubes is equal to the length of the major axis, so that the adjacent oblong cross-section spiral falling film tubes achieve self-support by being tangentially contacted by the two ends of the major axis.

13. The integrated high-efficiency falling film thickener and separator according to claim 12, characterized in that: Each oblong cross-section spiral falling film tube maintains its centerline during the spiraling process. Within 360° of each pitch, it makes tangential contact with the adjacent oblong cross-section spiral falling film tube six times, and changes the position of the tangential contact point with the adjacent oblong cross-section spiral falling film tube every 60°.

14. The integrated high-efficiency falling film thickener and separator according to claim 13, characterized in that: The outer periphery of the oblong cross-section spiral falling film tube bundle is dodecagonal, and multiple straps are bound around the outer periphery.

15. The integrated high-efficiency falling film thickener and separator according to claim 10, characterized in that: The cross-sectional dimensions of each oblong-section spiral falling film tube are 45x25.5mm, and the spiral pitch is 250mm; the upper and lower ends of each oblong-section spiral falling film tube are circular base tubes with an outer diameter of 38mm.

16. The integrated high-efficiency falling film thickener and separator according to claim 1, characterized in that: The conical hopper has a structure that is larger at the top and smaller at the bottom, with its upper end located inside the cavity of the umbrella-shaped cover. The outer wall of the upper port of the conical hopper is connected to the inner wall of the umbrella-shaped cover cylinder by multiple symmetrically arranged ribs. The bottom of the conical hopper is supported at the bottom of the lower tube box, and the lower end of the conical hopper is connected to an overflow clear liquid outlet that extends out of the lower tube box. The concentrated liquid enters the lower tube box and settles and separates. The concentrated liquid with a higher density containing crystal slurry particles is discharged from the crystal slurry outlet at the bottom of the lower tube box, while the clear liquid with a lower density floats up from the annular space between the umbrella-shaped cover cylinder and the upper end of the conical hopper and enters the conical hopper, and then is discharged from the overflow clear liquid outlet.

17. The integrated high-efficiency falling film concentrator and separator according to any one of claims 1 to 16, characterized in that: The upper circumferential outer wall of the tower body is welded with a tower body support, and a tower top lifting column is fixed on the tower body support. The upper end of the tower top lifting column is bent towards the center line of the tower top and is provided with a lifting lug for the upper pipe box to facilitate lifting. The upper circumferential outer wall of the tower body is also symmetrically provided with multiple tower body lifting lugs.

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