CN213811854U - Winding pipe type conical inner convex heat exchanger - Google Patents
Winding pipe type conical inner convex heat exchanger Download PDFInfo
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- CN213811854U CN213811854U CN202022795985.5U CN202022795985U CN213811854U CN 213811854 U CN213811854 U CN 213811854U CN 202022795985 U CN202022795985 U CN 202022795985U CN 213811854 U CN213811854 U CN 213811854U
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- tube
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- exchange tube
- heat exchanger
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- 238000004804 winding Methods 0.000 title claims abstract description 32
- 238000012546 transfer Methods 0.000 claims abstract description 12
- 230000000694 effects Effects 0.000 claims abstract description 6
- 230000008676 import Effects 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 239000012530 fluid Substances 0.000 abstract description 15
- 230000001965 increasing effect Effects 0.000 abstract description 12
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000011161 development Methods 0.000 abstract description 2
- 230000007423 decrease Effects 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- 238000011160 research Methods 0.000 description 4
- 230000002708 enhancing effect Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000004377 microelectronic Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Abstract
The utility model discloses an interior bulge heat exchanger of winding tubular toper, including casing, core pipe and winding tube bank, the core pipe sets up and puts the department at casing central point, and core pipe one end is equipped with the tail gas import, and the other end is equipped with the tail gas export, the winding tube bank is along axial spiral winding on the outer wall of core pipe, the winding tube bank is equipped with two, including heat exchange tube one and heat exchange tube two, the inner wall of heat exchange tube one and heat exchange tube two is equipped with the protruding cell of toper along the rivers direction to improve the heat transfer effect. The utility model has the advantages that: the winding pipe in the heat exchanger adopts a spiral structure, which is beneficial to the development of turbulence, can generate strong secondary circulation and strengthens the heat exchange efficiency in the pipe; the shell pass heat exchange space structure is complex, fluid scours the spiral tube bundle for heat exchange, the winding modes between adjacent winding pipe networks are opposite, disturbance of the shell pass fluid is enhanced, a cross flow heat exchange mode is formed between the fluid and the fluid in the pipe, and heat transfer temperature difference between cold sources and heat sources is effectively increased.
Description
Technical Field
The utility model relates to an industry indirect heating equipment technical field, concretely relates to protruding nest of tubes heat exchanger in winding tubular toper.
Background
The heat exchanger has the characteristics of firm structure, large use elasticity, strong adaptability and the like, is widely applied to the aspects of chemical industry, petroleum, electric power and the like, is miniaturized along with the special requirements of microelectronics, medical treatment, aerospace and the like, and has great space for increasing in the aspects of design methods, structural forms, material parameters and the like. At the present stage, the research on the shell and tube heat exchanger is mainly started by enhancing the convection heat transfer in the tube, and the mechanism of the method is mainly that the thermal resistance is mainly concentrated on a boundary layer during heat transfer, and the key of enhancing the heat transfer is to thin or destroy the boundary layer so as to achieve the purpose of enhancing the heat transfer.
The winding tube type heat exchanger is a special shell-and-tube type heat exchanger, and is a high-efficiency heat exchange structure developed on the basis of the shell-and-tube type heat exchanger in the beginning of the 20 th century. The wound tube type heat exchanger has the advantages of compact structure, high overall heat exchange coefficient and strong pressure bearing capacity, and is widely applied to devices for Liquefied Natural Gas (LNG) and heavy alkane separation, liquid nitrogen washing and the like. In recent years, due to the good heat exchange performance of the wound tube type heat exchanger, the wound tube type heat exchanger is applied to petrochemical industry and other industries more widely, and the research on the heat transfer characteristic of the wound tube type heat exchanger is paid more attention by scholars. How to further improve the heat exchange performance of the tube side and the shell side so as to obtain a more compact structure; how to further innovate the structure of the heat exchanger to adapt to the application in more and more industrial fields; and further optimizing a calculation model of heat transfer of the novel heat exchanger are important contents of heat transfer research of the heat exchanger.
SUMMERY OF THE UTILITY MODEL
To the above technical problem that prior art exists, the purpose of this application is to provide a winding pipe formula toper is protruding for a heat exchanger.
The technical scheme of the utility model as follows:
the winding tube type conical inner bulge heat exchanger is characterized by comprising a shell, a core tube and two winding tube bundles, wherein the core tube is arranged at the center of the shell, one end of the core tube is provided with a tail gas inlet, the other end of the core tube is provided with a tail gas outlet, the winding tube bundles are spirally wound on the outer wall of the core tube along the axial direction, the two winding tube bundles are provided with two heat exchange tubes I and two heat exchange tubes II, and conical bulges are arranged on the inner walls of the heat exchange tubes I and the heat exchange tubes II along the water flow direction, so that the heat exchange effect is improved.
The winding tube type conical inner bulge heat exchanger is characterized in that the first heat exchange tube and the second heat exchange tube are in spiral opposite directions and are wound on the outer wall of the core tube.
The winding tube type conical inner bulge heat exchanger is characterized in that a first water inlet and a first water outlet are respectively arranged at the upper two ends of a first heat exchange tube, the first water inlet is positioned at the upper end of a core tube, and the first water outlet is positioned at the lower end of the core tube; and a second water inlet and a second water outlet are respectively arranged at two ends of the second heat exchange tube, the second water inlet is positioned at the lower end of the core tube, and the second water outlet is positioned at the upper end of the core tube.
The wound tube type conical inner bulge heat exchanger is characterized in that the conical bulges in the first heat exchange tube and the second heat exchange tube are arranged on two opposite sides of the inner wall of the pipe fitting and are distributed in a row-to-row or staggered-row mode.
The utility model has the advantages that:
1) the winding pipe in the heat exchanger adopts a spiral structure, which is beneficial to the development of turbulence, can generate strong secondary circulation and strengthens the heat exchange efficiency in the pipe; the shell pass heat exchange space structure is complex, fluid scours the spiral tube bundle for heat exchange, the winding modes between adjacent winding pipe networks are opposite, disturbance of the shell pass fluid is enhanced, a cross flow heat exchange mode is formed between the fluid and the fluid in the pipe, and heat transfer temperature difference between cold sources and heat sources is effectively increased.
2) The inner wall of the winding pipe in the heat exchanger is provided with the combination of a conical inner convex cell structure, so that the heat exchange quantity and the heat exchange efficiency are greatly increased.
3) The design of the winding type heat exchanger not only can effectively reduce energy consumption, but also can effectively reduce the occupied space of the device.
Drawings
Fig. 1 is a schematic view of a wound heat exchanger of the present invention;
FIG. 2 is a schematic view of a geometric model of the convex-cell heat exchange tube of the present invention;
FIG. 3 is a schematic view of the heat exchange tube of the present invention;
FIG. 4 is a schematic view of the staggered convex heat exchange tube of the present invention;
fig. 5 shows the variation of Nu with dimensionless radius I at different Re;
fig. 6 is a change in PEC index with dimensionless radius I for the present invention at different Re;
fig. 7 shows the variation of Nu with pitch P at different Re;
FIG. 8 is a graph of PEC index versus pitch P for various Re's of the present invention;
FIG. 9 is a graph showing the relationship between the influence of different arrangements on the average Nu in the present application;
in the figure: 1-shell, 2-core tube, 3-tail gas inlet, 4-water outlet II, 5-heat exchange tube I, 6-heat exchange tube II, 7-water outlet, 8-tail gas outlet, 9-water inlet II, 10-water inlet I, 11-conical bulge.
Detailed Description
The invention is further described with reference to the accompanying drawings.
As shown in fig. 1-9, a wound tube type conical inner convex cell heat exchanger comprises a shell 1, a core tube 2, a tail gas inlet 3, a water outlet II 4, a heat exchange tube I5, a heat exchange tube II 6, a water outlet 7, a tail gas outlet 8, a water inlet II 9, a water inlet I10 and a conical convex cell 11.
Example (b):
the core pipe 2 sets up and puts the department at 1 inside central point of casing, and 2 one end of core pipe are equipped with tail gas import 3, and the other end is equipped with tail gas export 8, sets up the winding tube bank along axial spiral winding on the outer wall of core pipe 2, and the winding tube bank is equipped with two, including heat exchange tube one 5 and heat exchange tube two 6, heat exchange tube one 5 and heat exchange tube two 6 are spiral subtend and pipe coiling on the outer wall of core pipe 2, the inner wall of heat exchange tube one 5 and heat exchange tube two 6 is equipped with toper bulge 11 along the rivers direction.
A first water inlet 10 and a first water outlet 7 are respectively arranged at the two ends of the first heat exchange tube 5, the first water inlet 10 is positioned at the upper end of the core tube 2, and the second water outlet 7 is positioned at the lower end of the core tube 2; two ends of the heat exchange tube II 6 are respectively provided with a water inlet II 9 and a water outlet II 4, the water inlet II 9 is positioned at the lower end of the core tube 2, and the water outlet II 4 is positioned at the upper end of the core tube 2.
The conical bulges 11 in the first heat exchange tube 5 and the second heat exchange tube 6 are arranged on two opposite sides of the inner wall of the pipe fitting and are distributed in opposite rows or staggered rows.
Performance experiments:
taking 5 periods of the heat exchange tube in actual engineering as research objects, adopting a conical convex heat exchange tube, wherein the length of the heat exchange tube is 400 mm, the radius R of the heat exchange tube is 10mm, the wall thickness is 2 mm, the diameter d =2R of a convex cell, and R is the depth (mm) of the convex cell; the pitch of the convex cells on the same side is P, in order to fully develop fluid in the pipe, a round straight pipe with the diameter of 80 mm is respectively connected to an inlet and an outlet, a dimensionless radius I = R/R is defined, the heat exchange characteristics are analyzed by changing the dimensionless radius I and the pitch P of the convex cells, and two arrangement modes are provided: aligned and staggered.
Selecting boundary conditions in an industrial environment, namely taking water as a working medium, adopting a speed inlet at a speed value of 0.48 m/s, setting the temperature of the inlet to be 353.15K, setting the wall surface to be constant wall temperature to be 273.15K, and setting the outlet to be a pressure outlet. And the fluid medium gravity is ignored; the fluid is regarded as Newtonian fluid, and is incompressible, and the physical property parameter of the fluid is a constant; the fluid velocity and temperature of the cross section at the inlet of the heat exchange tube are uniform.
The presence of the conical protrusions improves the heat exchange performance and also causes a corresponding increase in flow resistance, so the PEC index is used to take the heat exchange performance and the flow resistance into consideration.
Wherein Nu is Nu-Nu is Nu number of the bulge tube0-Knudsen number of smooth tubes f-coefficient of friction resistance of convex tubes f0Coefficient of friction resistance of smooth tubes.
FIG. 5 shows the influence of different dimensionless dimensions I on the average Nu of the Knudel numbers in the range of Re 13136-52544.
As can be seen from fig. 5, the heat exchange characteristics of the convex tube are significantly greater than those of the smooth tube, and the heat exchange characteristics increase with the increase of the dimensionless size, and are improved by at least 15% compared with those of the smooth tube. When the dimensionless radius I is 0.1, 0.2, the difference of the heat exchange performance is not large, and the increase of the heat exchange performance from the dimensionless radius I =0.3 is obvious. When the dimensionless radius I is constant, the heat exchange performance increases with the increase of the Reynolds number, but the increase gradually decreases. This phenomenon indicates that when the number of Re is smaller, the heat exchange performance of the convex tube is better than that of the smooth tube,
also in combination with PEC, fig. 6 is a graph of PEC index as a function of dimensionless radius I at different Re. As can be seen from fig. 6, at Re, the PEC decreases with increasing dimensionless radius I, with an increasing trend of decrease. The combination property of the convex cell tube is better than that of a smooth tube when I = 0.1-0.6, the PEC value reaches the maximum value of 1.246 when I =0.2 and Re = 17514, the combination heat exchange property is optimal, the advantages of the convex cell tube in comparison with the smooth tube gradually disappear after the dimensionless radius I is larger than 0.6, and even the convex cell tube is worse than the smooth tube, the dimensionless radius I of the convex cell tube is not suitable for strengthening heat exchange, and the flow resistance is increased along with the increase of the dimensionless radius I. The dimensionless radius is finally determined to be 0.2.
Considering the pitch P again, fig. 7 shows the variation of Nu with pitch P at different Re. As can be seen from fig. 7, Nu is less influenced by the pitch P of the cells, and gradually decreases with increasing pitch P under the same Re because the distance between the cells increases, the perturbation effect generated by the previous cell cannot effectively continue to the next cell, and the perturbation effect gradually weakens or even disappears, so that the heat exchange performance decreases, and when the pitch P of the cells is the same, Nu increases with increasing Re because the turbulence degree of the fluid increases with increasing Re, the destructive effect on the boundary layer increases, and thus the heat exchange performance is improved.
Also in combination with PEC for comparison, fig. 8 is a graph of PEC index as a function of pitch P at different Re. Since the PEC values do not change significantly with Re overall, the figure shows only a few Re values with significant change. It can be seen that at the same pitch, the PEC decreases with increasing Re, and that the increase in turbulence causes an increase in resistance to a greater extent than the increase in heat exchange performance. Re is the same, as the pitch increases, its flow resistance tends to decrease, and the PEC value still decreases with increasing pitch, indicating that heat transfer performance decreases faster than flow resistance. In summary, the pitch P is selected to be 30mm in combination with economic cost considerations.
Finally, depending on the arrangement, fig. 9 shows the effect of the two arrangements, row and alternate, on the average Nu, f, for a dimensionless radius I =0.2 and a pitch P =30 mm within the Re range under investigation. As can be seen from FIG. 7, the average Nu of the two arrangements is very close, with a difference of at most 1.19%, and the average coefficient of friction f for the rows is slightly greater than for the staggered rows, with a maximum of no more than 1.65%. Therefore, in terms of the integrated heat exchange type energy, the staggered rows are not greatly different from the opposite rows in actual use, and a larger selection space is provided for the actual use.
Claims (4)
1. The utility model provides a protruding nest of tubes heat exchanger in winding tube toper, its characterized in that includes casing (1), core pipe (2) and winding tube bank, core pipe (2) set up and put the department in casing (1) central point, and core pipe (2) one end is equipped with tail gas import (3), and the other end is equipped with tail gas export (8), winding tube bank along axial spiral winding on the outer wall of core pipe (2), winding tube bank is equipped with two, including heat exchange tube one (5) and heat exchange tube two (6), the inner wall of heat exchange tube one (5) and heat exchange tube two (6) is equipped with protruding nest of cones (11) along the rivers direction to improve heat transfer effect.
2. The wound tube type conical inner convex cell heat exchanger as claimed in claim 1, wherein the first heat exchange tube (5) and the second heat exchange tube (6) are spirally opposite and wound on the outer wall of the core tube (2).
3. The wound tube type conical inner convex cell heat exchanger is characterized in that a first water inlet (10) and a first water outlet (7) are respectively formed in the two ends of the first heat exchange tube (5), the first water inlet (10) is located at the upper end of the core tube (2), and the first water outlet (7) is located at the lower end of the core tube (2); and two ends of the second heat exchange tube (6) are respectively provided with a second water inlet (9) and a second water outlet (4), the second water inlet (9) is positioned at the lower end of the core tube (2), and the second water outlet (4) is positioned at the upper end of the core tube (2).
4. The wound tube type conical inner convex cell heat exchanger as claimed in claim 1, wherein the conical convex cells (11) in the first heat exchange tube (5) and the second heat exchange tube (6) are arranged on two opposite sides of the inner wall of the tube, and are distributed in opposite rows or staggered rows.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022795985.5U CN213811854U (en) | 2020-11-27 | 2020-11-27 | Winding pipe type conical inner convex heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022795985.5U CN213811854U (en) | 2020-11-27 | 2020-11-27 | Winding pipe type conical inner convex heat exchanger |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213811854U true CN213811854U (en) | 2021-07-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022795985.5U Expired - Fee Related CN213811854U (en) | 2020-11-27 | 2020-11-27 | Winding pipe type conical inner convex heat exchanger |
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| Country | Link |
|---|---|
| CN (1) | CN213811854U (en) |
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2020
- 2020-11-27 CN CN202022795985.5U patent/CN213811854U/en not_active Expired - Fee Related
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| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210727 |
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| CF01 | Termination of patent right due to non-payment of annual fee |