CN219995976U - Vertical heat exchanger for evaporation - Google Patents
Vertical heat exchanger for evaporation Download PDFInfo
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- CN219995976U CN219995976U CN202321408381.8U CN202321408381U CN219995976U CN 219995976 U CN219995976 U CN 219995976U CN 202321408381 U CN202321408381 U CN 202321408381U CN 219995976 U CN219995976 U CN 219995976U
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- 238000001704 evaporation Methods 0.000 title claims abstract description 25
- 230000008020 evaporation Effects 0.000 title claims abstract description 24
- 238000003466 welding Methods 0.000 claims abstract description 22
- 238000009826 distribution Methods 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 239000003507 refrigerant Substances 0.000 claims abstract description 8
- 238000006243 chemical reaction Methods 0.000 claims abstract description 5
- 230000005855 radiation Effects 0.000 claims description 18
- 230000002093 peripheral effect Effects 0.000 claims description 15
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000000463 material Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000012545 processing Methods 0.000 description 5
- 238000012546 transfer Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000000137 annealing Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The utility model discloses a vertical heat exchanger for evaporation, which is characterized in that a tube side of the heat exchanger generates exothermic reaction or cools a high-temperature medium, a shell side evaporates a liquid refrigerant into a gaseous state, a heat exchange tube and a supporting plate are arranged in a shell of the shell side, the supporting plate is used for supporting the heat exchange tube, the upper end and the lower end of the heat exchange tube are respectively welded on two tube plates, the heat exchange tube and the tube plates are connected by adopting strength welding and expansion, and a welding joint between the heat exchange tube and the tube plates is a countersunk fillet joint or a countersunk full-welded joint. According to the heat exchanger, the welding joint between the heat exchange tube and the tube plate is optimized into the countersunk fillet joint or the countersunk full-welded joint by optimizing the connection mode of the heat exchange tube and the tube plate and the tube distribution mode of the heat exchange tube, so that the welding flesh of the heat exchange tube and the tube plate can be increased to increase the pull-out force between the heat exchange tube and the tube plate, and further, the structure of the support plate is optimized, so that the heat exchanger is simple and compact in structure, larger in heat exchange area, capable of forming a cold wall type shell structure, low in shell side pressure, negligible in heat exchange dead zone, low in equipment investment and beneficial to transportation.
Description
Technical Field
The utility model belongs to the technical field of industrial refrigeration heat exchange, and particularly relates to a vertical heat exchanger for evaporation.
Background
Heat exchangers are common equipment used in chemical, petroleum, power, food and many other industries and play an important role in production. The heat exchanger can be used as a heater, a cooler, a condenser, an evaporator, a reboiler and the like in chemical production, and has wider application range.
Tube-in-tube heat exchangers are the most common form, and currently widely used are fixed tube-plate heat exchangers, floating head heat exchangers, U-tube heat exchangers, stuffing box heat exchangers, kettle reboilers, and the like. The heat exchanger can be divided in form into two types, horizontal and vertical. Horizontal heat exchanger: the device is stable and safe, and can bear higher working pressure and temperature; the floor space is large, the installation space has low clean height requirement, the maintenance and the cleaning are convenient, and a platform is generally not needed; the cold and hot fluids can flow reversely and forward; the heat transfer coefficient is medium, the heating residence time is short, and the heat exchange effect is medium. Vertical heat exchanger: the method is stable and safe, needs to be vertically paved, and generally adopts a tower-shaped structure; the occupied area is small, the requirement on the net height of the installation space is high, the structure is compact, and the piping is easy; the cold and hot fluids are generally countercurrent; the heat transfer coefficient is larger, the heating residence time is short, and the heat exchange effect is better.
The evaporator is equipment for evaporating liquid refrigerant into gas state, and the liquid refrigerant can be boiled vigorously in the heat exchange process; a certain space height is usually reserved between the liquid and gaseous refrigerants to ensure that the evaporator out-gassing is free of liquid. For the horizontal shell-and-tube evaporator, in order to ensure the space height, the heat exchange tubes are not distributed on the upper half part of the section of the tube plate, so that the defects of large volume and high material cost of the heat exchanger are caused; or a kettle type reboiler is adopted, all pipes are distributed on the section of the pipe plate, an evaporation space is arranged at the upper part of the shell, the size of the evaporation space is determined by the gas yield and the required steam quality, and the material cost is increased. The vertical evaporator structure is adopted, so that the occupied area is small, the tube plate tube distribution rate can be greatly improved, the volume of the heat exchanger is reduced, and the material cost is reduced. The axial reactor for generating hydrocarbons, alkanes and alcohols by Fischer-Tropsch synthesis is a vertical evaporator, catalyst is filled between pipes, reaction gas in the pipe side is subjected to Fischer-Tropsch synthesis reaction under the action of the catalyst, and heat released by the Fischer-Tropsch synthesis reaction is absorbed by shell-side boiler water to obtain byproduct medium-pressure steam.
When the heat exchange tubes are distributed on the tube plate, the heat exchange tubes are welded at the tube holes on the tube plate. Because the pipe holes do not need slotting, the ends of the heat exchange pipe do not need annealing, and the manufacturing and processing are simple, the welding structure has high strength and strong pulling-out force, the welding process of the heat exchange pipe and the pipe plate which are widely used in engineering application at present is a strength welding process or a strength welding and attaching-expanding process, the design strength of a welding line is required to be larger than or equal to the maximum allowable stress of the pipe in the axial direction, and the height of a welding leg meets the requirement of the pulling-out force for connecting the heat exchange pipe and the pipe plate and is not smaller than the thickness of the heat exchange pipe wall. The welded joint between the heat exchange tube and the tube plate adopts an angle joint (shown in figure 1) with an included angle of 45 degrees.
The supporting plate (called as baffle plate when there is baffle need) is a part in the shell-and-tube heat exchanger, and is set on the shell side, so that it can not only raise heat transfer effect, but also can play the role of supporting tube bundle, and is commonly used as two kinds of arched and disk-circular ring. The single arched baffle plate is the most commonly used form, the form is simple, but the pressure drop is larger, and a heat exchange dead zone is formed by liquid stagnation; the double-arch-shaped baffle plates and the three-arch-shaped baffle plates are suitable for logistics with larger shell-side flow, the pressure drop can be greatly reduced, and the vibration induced in the medium flowing process can be prevented; the disc-circular ring baffle plate is formed by staggering discs and circular rings, the medium flow is characterized by axial symmetry, the flow is mostly parallel flow opposite to the tube bundle, and the pressure drop and the shell side heat transfer film coefficient increase are smaller than those of a single bow, so that the baffle plate is generally used for high-flow and large-diameter occasions.
Disclosure of Invention
The utility model aims to solve the technical problems of providing a vertical heat exchanger for evaporation, which can lead the structure of the heat exchanger to be simple and compact, lead the heat exchange area to be larger, lead the shell side pressure to be reduced, lead the heat exchange dead zone to be negligible, lead the equipment investment to be low and be beneficial to transportation by optimizing the connection mode of the heat exchange tube and the tube plate and the tube arrangement mode of the heat exchange tube and further optimizing the structure of the supporting plate.
The technical scheme adopted for solving the technical problems is as follows: a heat exchanger for vertical evaporation is characterized in that a tube side of the heat exchanger is subjected to exothermic reaction or high-temperature medium is cooled, a shell side evaporates liquid refrigerant into a gaseous state, a heat exchange tube and a supporting plate are arranged in a shell of the shell side, the supporting plate is used for supporting the heat exchange tube, the upper end and the lower end of the heat exchange tube are respectively welded on two tube plates, the heat exchange tube and the tube plates are connected by adopting strength welding and expansion, and a welded joint between the heat exchange tube and the tube plates is a countersunk fillet joint or a countersunk full-welded joint.
The heat exchanger for vertical evaporation is similar to a vertical fixed tube plate heat exchanger, the tube side generates exothermic reaction or reduces the temperature of a high-temperature medium, and the shell side evaporates liquid refrigerant into a gaseous state.
The heat exchanger for vertical evaporation optimizes the welding joint between the heat exchange tube and the tube plate to be a countersunk fillet joint or a countersunk full-welded joint, and can increase the welding flesh of the heat exchange tube and the tube plate, thereby increasing the pulling-out force between the heat exchange tube and the tube plate. On the premise of meeting the pulling-out force between the heat exchange tubes and the tube plates and the feasibility of processing and manufacturing, the center distance of the heat exchange tubes is reduced as much as possible so as to increase the number of the heat exchange tubes; the outer diameter of the heat exchange tubes is reduced and the number of the heat exchange tubes is increased as much as possible under the condition of meeting the filling amount of the tube side catalyst or the volume of the high-temperature medium, so that the heat exchange area is increased. When the heat exchange area is fixed, the diameter of the heat exchanger can be properly reduced, the investment of materials and equipment for shell and tube process is reduced, and the transportation of large-scale equipment is facilitated.
Preferably, the countersunk fillet joint and the countersunk full-welded joint are joints obtained by double-pass welding.
Preferably, the support plate comprises a plate body, a plurality of pipe holes are formed in the plate body, part of the pipe holes in the plurality of pipe holes are not distributed, the part of the pipe holes which are not distributed are located in the pipe distribution-free area, and the pipe distribution-free area is uniformly distributed on the periphery and/or the inside of the plate body.
The support plate is a fully-supported support plate, part of pipe holes of which are not distributed are positioned in the pipe distribution area and are used as steam circulation channels, the areas of the steam circulation channels can reach the areas of the notches on the arched baffle plate and the disc-annular baffle plate, the steam circulation needs are met, the pressure drop of a shell side can be effectively reduced, and the heat exchange dead area is negligible. In addition, when the non-distributed areas are uniformly distributed on the periphery of the plate body, a shell cold wall structure is formed, so that materials for the shell can be reduced.
Further, the non-piping area is at least one of a peripheral area, a regular polygon area and a centripetal radiation area, the peripheral area is arranged at the periphery of the plate body, the regular polygon area is arranged at the middle part of the plate body, and the centripetal radiation area is arranged between the peripheral area and the regular polygon area. On the premise of ensuring the flow area, the area without management can be any one of a peripheral area, a regular polygon area and a centripetal radiation area, or can be a combination of the areas.
Preferably, the regular polygon area includes a plurality of circles around the axis of the plate body, the number of circles of the regular polygon area is denoted as n, and n is a natural number.
Specifically, when the tube distribution mode on the plate body is triangular, the tube distribution-free area is at least one of a peripheral area, a regular hexagonal area and a centripetal radiation area, and the number of the centripetal radiation areas is six.
Specifically, when the pipe distribution mode on the plate body is square, the pipe distribution area is at least one of a peripheral area, a square area and a centripetal radiation area, and the number of the centripetal radiation areas is four.
Preferably, small holes are distributed around the holes. The function of the apertures is to further increase the steam flow area and further reduce the pressure drop.
Specifically, when the pipe distribution mode on the plate body is triangular, every six small holes are uniformly distributed on six vertexes of a regular hexagon, and the regular hexagon circumscribes a circle with the center distance of the heat exchange pipes as the diameter.
Specifically, when the pipe distribution mode on the plate body is square, every four small holes are uniformly distributed on four vertexes of a square, and the square circumscribes a circle with the center distance of the heat exchange pipes as the diameter.
Compared with the prior art, the utility model has the following advantages:
the heat exchanger for vertical evaporation optimizes the welding joint between the heat exchange tube and the tube plate to be a countersunk fillet joint or a countersunk full-welded joint, and can increase the welding flesh of the heat exchange tube and the tube plate, thereby increasing the pulling-out force between the heat exchange tube and the tube plate. On the premise of meeting the pulling-out force between the heat exchange tubes and the tube plates and the feasibility of processing and manufacturing, the center distance of the heat exchange tubes is reduced as much as possible so as to increase the number of the heat exchange tubes; the outer diameter of the heat exchange tubes is reduced and the number of the heat exchange tubes is increased as much as possible under the condition of meeting the filling amount of the tube side catalyst or the volume of the high-temperature medium, so that the heat exchange area is increased. When the heat exchange area is fixed, the diameter of the heat exchanger can be properly reduced, the investment of materials and equipment for shell and tube process is reduced, and the transportation of large-scale equipment is facilitated.
Drawings
FIG. 1 is a schematic diagram of a connection structure of a conventional heat exchange tube and a tube plate (a welded joint is an angle joint with an included angle of 45 °);
FIG. 2 is a schematic view of a heat exchanger for neutral evaporation in example 1;
FIG. 3 is a schematic diagram of the connection structure of the heat exchange tube and the tube sheet in example 1 (the welded joint is a countersunk fillet joint);
FIG. 4 is a schematic view of a support plate in example 1;
FIG. 5 is a schematic view showing the positions of small holes arranged around the pipe holes in example 1;
FIG. 6 is a schematic diagram of the connection structure of the heat exchange tube and the tube sheet in example 2 (the welded joint is a countersunk head full welded joint);
specific reference numerals in fig. 1 to 6 are as follows:
1-shell, 2-heat exchange tube, 3-supporting plate, 31-plate body, 32-tube hole, 33-part tube hole without tube distribution, 34-peripheral area, 35-regular hexagonal area, 36-centripetal radiation area, 37-small hole, 38-regular hexagon with six small holes uniformly distributed on six vertexes, 39-circle with center distance of heat exchange tube as diameter, 4-tube plate, 5-countersunk head fillet joint and 6-countersunk head full-welded joint.
Detailed Description
The utility model is described in further detail below with reference to the embodiments of the drawings.
In the heat exchanger for vertical evaporation of embodiment 1, the tube side of the heat exchanger generates exothermic reaction or cools the high-temperature medium, the shell side evaporates the liquid refrigerant into gas state, as shown in fig. 1, the heat exchange tube 2 and the supporting plate 3 are arranged in the shell 1 of the shell side, the supporting plate 3 is used for supporting the heat exchange tube 2, the upper end and the lower end of the heat exchange tube 2 are respectively welded on two tube plates 4, the heat exchange tube 2 and the tube plates 4 are connected by adopting strength welding and bonding expansion, as shown in fig. 2, the welded joint between the heat exchange tube 2 and the tube plates 4 is a countersunk fillet joint 5 with a radius R obtained by double welding, the welding flesh of the heat exchange tube 2 and the tube plates 4 is increased, and the pulling-out force between the heat exchange tube 2 and the tube plates 4 is further increased.
On the premise of meeting the pulling-out force between the heat exchange tubes 2 and the tube plates 4 and the feasibility of processing and manufacturing, the center distance of the heat exchange tubes 2 is reduced as much as possible so as to increase the number of the heat exchange tubes 2. By heat-exchange tubesFor example, when the center distance of the heat exchange tubes is 48mm, at most 770 heat exchange tubes can be distributed; when the center distance of the heat exchange tubes is reduced to 44mm, at most, the heat exchange tubes can be distributed to 920; when the center distance of the heat exchange tubes is reduced by 4mm, the number of the heat exchange tubes is increased by 150, and the structure is more compact.
The outer diameter of the heat exchange tubes 2 is reduced and the number of the heat exchange tubes 2 is increased as much as possible under the condition of meeting the filling amount of the tube side catalyst or the volume of the high-temperature medium, so that the heat exchange area is increased. Taking a heat exchanger as an example, at a specific catalyst loading,the center distance of the heat exchange tubes is 44mm, 840 heat exchange tubes are needed, and the total heat exchange area of each meter of heat exchange tubes is 100m 2 The weight of the heat exchange tube is 15 tons; />The center distance of the heat exchange tubes is 51mm, 600 heat exchange tubes are needed, and the total heat exchange area of each meter of heat exchange tubes is 85m 2 The weight of the heat exchange tube is 13 tons. When the heat exchange tubes with small diameters are adopted, the number of the required heat exchange tubes and the weight of the heat exchange tubes are increased, but the heat exchange area is increased more, and the heat exchange is facilitated. When the heat exchange area is fixed, the diameter of the heat exchanger can be properly reduced, the investment of materials and equipment for shell and tube process is reduced, and the transportation of large-scale equipment is facilitated.
The tube distribution mode of the heat exchange tubes 2 increases the tube distribution quantity and the heat exchange area of the heat exchange tubes 2 by reducing the center distance of the heat exchange tubes 2 and adopting the heat exchange tubes 2 with small diameters, and a plurality of tube holes on the periphery of the tube plate 4 can be used for forming a shell without distributing the tubesThe cold wall structure of the body 1 reduces the material for the shell 1. Taking a certain heat exchanger as an example, under the conditions of specific catalyst loading, safe strength and feasible processing and manufacturing,the center distance of the heat exchange tubes is 44mm, 840 heat exchange tubes are needed, and the maximum number of the heat exchange tubes can be distributed to 880; />The center distance of the heat exchange tubes is 51mm, 600 heat exchange tubes are needed, and at most, the heat exchange tubes can be distributed to 640 heat exchange tubes. And redundant-40 pipe holes are distributed on the periphery of the pipe plate and are not distributed, so that a shell cold wall structure is formed.
Specifically, in embodiment 1, as shown in fig. 3, the support plate 3 includes a plate body 31, a plurality of tube holes 32 are formed in the plate body 31, the tube arrangement mode on the plate body 31 is triangular, a portion of tube holes 33 in the plurality of tube holes 32 are not arranged, a portion of tube holes 33 which are not arranged are located in an area which is not arranged, and the area which is not arranged is uniformly distributed on the periphery and/or inside of the plate body 31. The non-distribution area is at least one of a peripheral area 34, a regular hexagonal area 35 and a centripetal radiation area 36, the peripheral area 34 is arranged on the periphery of the plate body 31, the regular hexagonal area 35 is arranged in the middle of the plate body 31, the centripetal radiation area 36 is arranged between the peripheral area 34 and the regular hexagonal area 35, and the number of the centripetal radiation areas 36 is six. Three areas of out-of-tube, peripheral region 34, regular hexagonal region 35 and centripetal radiating region 36 are shown in fig. 3. The regular hexagonal area 35 includes 1 turn disposed around the axis of the plate body 31. In practical application, the number of turns of the regular hexagonal area 35 can be determined according to the diameter of the heat exchanger, and the number of turns n is a natural number of 0, 1, 2, 3, etc. As shown in fig. 4, small holes 37 are distributed around the plurality of tube holes, and each six small holes 37 are uniformly distributed on six vertexes of a regular hexagon 38, and the regular hexagon 38 circumscribes a circle 39 with the center distance s of the heat exchange tube 2 as a diameter. Only a part of the apertures 4 is shown in fig. 3.
The heat exchanger for vertical evaporation of example 2 is different from example 1 in that in example 2, as shown in fig. 5, the welded joint between the heat exchange tube and the tube sheet is a countersunk head full-welded joint 6 obtained by double-pass welding; referring to fig. 3 and 4, the plate 31 is square in tube arrangement, the tube-free area is at least one of a peripheral area, a square area and a centripetal radiation area, and the number of the centripetal radiation areas is four; every four small holes are uniformly distributed on four vertexes of a square, and the square is circumscribed by a circle with the center distance of the heat exchange tubes as the diameter. In practical application, the number of turns of the square area can be determined according to the diameter of the heat exchanger, and the number of turns n is a natural number of 0, 1, 2, 3 and the like.
The support plates in the above embodiments 1 and 2 are all support plates, and part of the pipe holes of the non-distributed pipes are located in the non-distributed pipe areas and used as steam flow channels, the areas of the steam flow channels can reach the areas of the notches on the arched baffle plate and the disc-annular baffle plate, so that the steam flow needs are met, the pressure drop of the shell side can be effectively reduced, and the heat exchange dead area is negligible. In addition, when the distributed areas are uniformly distributed on the periphery of the plate body 31, a shell cold wall structure is formed, and the materials for the shell can be reduced.
Claims (10)
1. The heat exchanger for vertical evaporation is characterized in that a tube side of the heat exchanger generates exothermic reaction or cools a high-temperature medium, a shell side evaporates a liquid refrigerant into a gas state, a heat exchange tube and a supporting plate are arranged in a shell of the shell side, the supporting plate is used for supporting the heat exchange tube, the upper end and the lower end of the heat exchange tube are respectively welded on two tube plates, the heat exchange tube and the tube plates are connected by adopting strength welding and attaching expansion, and a welded joint between the heat exchange tube and the tube plates is a countersunk fillet joint or a countersunk full-welded joint.
2. The heat exchanger for vertical evaporation according to claim 1, wherein said countersunk fillet joint and said countersunk full-length joint are both joints obtained by double-pass welding.
3. The heat exchanger for vertical evaporation according to claim 1, wherein the support plate comprises a plate body, a plurality of tube holes are formed in the plate body, a part of tube holes in the plurality of tube holes are not distributed, the part of tube holes which are not distributed are located in a tube distribution area, and the tube distribution area is uniformly distributed on the periphery and/or inside of the plate body.
4. A heat exchanger for vertical evaporation according to claim 3, wherein said non-piping region is at least one of a peripheral region provided at the periphery of said plate body, a regular polygonal region provided at the middle of said plate body, and a centripetal radiation region provided between said peripheral region and said regular polygonal region.
5. A heat exchanger for vertical evaporation according to claim 4, wherein said regular polygon area comprises a plurality of turns provided around the axis of said plate body, and the number of turns of said regular polygon area is denoted as n, and n is a natural number.
6. The heat exchanger for vertical evaporation according to claim 5, wherein when the tube arrangement on the plate body is triangular, the tube arrangement area is at least one of a peripheral area, a regular hexagonal area and a centripetal radiation area, and the number of the centripetal radiation areas is six.
7. The heat exchanger for vertical evaporation according to claim 4, wherein when said plate body has a square tube arrangement, said tube-free region is at least one of a peripheral region, a square region and a centripetal radiation region, and said centripetal radiation region is four in number.
8. A heat exchanger for vertical evaporation according to any one of claims 3 to 7, wherein a plurality of said holes are provided with small holes around them.
9. A heat exchanger for vertical evaporation according to claim 8, wherein when the tube arrangement on the plate body is triangular, every six small holes are uniformly distributed on six apexes of a regular hexagon circumscribed by a circle having the center distance of the heat exchange tubes as a diameter.
10. A heat exchanger for vertical evaporation according to claim 8, wherein when the tube arrangement on the plate body is square, every four holes are uniformly distributed on four vertexes of a square, and the square circumscribes a circle having the center distance of the heat exchange tubes as a diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321408381.8U CN219995976U (en) | 2023-06-05 | 2023-06-05 | Vertical heat exchanger for evaporation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321408381.8U CN219995976U (en) | 2023-06-05 | 2023-06-05 | Vertical heat exchanger for evaporation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219995976U true CN219995976U (en) | 2023-11-10 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321408381.8U Active CN219995976U (en) | 2023-06-05 | 2023-06-05 | Vertical heat exchanger for evaporation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219995976U (en) |
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2023
- 2023-06-05 CN CN202321408381.8U patent/CN219995976U/en active Active
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