CN213396657U

CN213396657U - Heat exchanger

Info

Publication number: CN213396657U
Application number: CN202021978455.8U
Authority: CN
Inventors: 李国祯; 王筝; 菲利普·赫尔; 尼克·迈尔斯
Original assignee: University of Nottingham Ningbo China
Current assignee: University of Nottingham Ningbo China
Priority date: 2020-08-05
Filing date: 2020-09-10
Publication date: 2021-06-08
Anticipated expiration: 2030-09-10

Abstract

A heat exchanger is disclosed, wherein a first tube plate is connected with a first inlet at one end and connected with a plurality of heat transfer tubes at the other end so as to guide a first fluid into the plurality of heat transfer tubes, the plurality of heat transfer tubes comprise at least one vortex flow tube generating vortex flow, the vortex flow tube comprises a structural body and an inner tube wall arranged on the structural body, one end of the structural body inputs the fluid, the other end of the structural body outputs the vortex flow fluid, the inner tube wall comprises a first gradual change section, a vortex flow section and a second gradual change section, the first cross section is twisted at a first preset angle in a non-linear gradual change mode along the longitudinal direction of the first gradual change section, the third cross section is twisted at a third preset angle in a non-linear gradual change mode along the longitudinal direction of the second gradual change section, and a second outlet is arranged on a shell and is opposite to the second inlet so as to lead out.

Description

Heat exchanger

Technical Field

The utility model relates to a heat exchange technology field, especially a heat exchanger.

Background

The heat exchanger is a heat exchange device which transfers part of heat of hot fluid to cold fluid to make the temperature of the fluid reach the index specified by the process flow, and is also called as a heat exchanger. The requirements of chemical production on heat exchange equipment are high heat transfer efficiency, small fluid resistance, low manufacturing cost, easy maintenance, strong reliability, long service life and the like. The heat exchanger can be divided into a surface heat exchanger, a regenerative heat exchanger, a fluid connection indirect heat exchanger and a direct contact heat exchanger according to the heat transfer principle. The surface type heat exchanger is characterized in that two fluids with different temperatures flow in a space separated by a wall surface, and heat exchange between the two fluids is realized through heat conduction of the wall surface and convection of the fluids on the wall surface. Surface heat exchange includes shell-and-tube, double-tube, immersion coil heat exchanger, spray heat exchanger and other heat exchangers. The flow state in the tube bundle of the shell-and-tube heat exchanger has great influence on the heat exchange efficiency, and the turbulent flow state is formed, so that the heat exchange efficiency is improved. When the flowing state is laminar flow, the pipeline is easy to scale, so that the dirt and the heat are blocked. The double-pipe heat exchanger is a concentric sleeve made of different straight pipes and formed by connecting U-shaped elbows. In the heat exchanger, one fluid flows in the pipe, the other fluid flows in the pipe gap, and the two fluids can obtain higher flow velocity, so that the heat transfer coefficient is higher. The two fluids can flow reversely, and the heat exchange driving force is large. The double-pipe heat exchanger has a simple structure, can bear high pressure, is mainly used for heat transfer of two liquids with small flow and high pressure, and is usually used as a cooler or a condenser. The immersion coil heat exchanger is formed by bending a metal pipe into a shape corresponding to the container and immersing the metal pipe in the liquid in the container. The coil heat exchanger has the advantages of simple structure, capability of bearing high pressure and capability of being made of corrosion-resistant materials. The defects are that the turbulence degree of liquid in the container is low, and the heat transfer coefficient outside the pipe is small. The spray type heat exchanger is also called a spray type cooler because heat exchange tubes are fixed on a steel frame in rows, hot fluid flows in the tubes, and cooling water is uniformly sprayed down from a spray device above the tubes. The spray heat exchanger has one liquid film outside the pipe with relatively high turbulence degree and high heat transfer coefficient outside the pipe. The surface heat exchangers all involve the flow of fluid in a pipeline, and the flow state of the fluid in the pipeline directly influences the heat exchange efficiency of the heat exchanger.

The above information disclosed in the background section is only for enhancement of understanding of the background of the invention and therefore it may contain information that does not form the prior art that is well known to those of ordinary skill in the art.

SUMMERY OF THE UTILITY MODEL

To present tubular heat exchanger heat exchange efficiency low, the problem of the easy scale deposit of pipe wall, in order to solve above-mentioned problem, the utility model provides a heat exchanger uses whirlpool vortex tube to change intraductal fluid motion state, increases the fluid degree of turbulence, improves the method of heat transfer effect. When the fluid medium passes through the vortex flow pipe, the formed vortex flow strongly impacts the surface of the inner pipe, and the heat exchange efficiency is improved. Meanwhile, the vortex flow has the function of self-cleaning of the pipeline, and the deposition of dirt and heat resistance in the pipeline are avoided.

The purpose of the utility model is realized by the following technical scheme.

A heat exchanger comprises a heat exchanger body and a heat exchanger body,

a housing;

a first inlet provided at a first side of the housing to introduce a first fluid,

a first outlet provided at a second side of the housing different from the first side to conduct out a first fluid,

a first tube sheet having one end connected to the first inlet and the other end connected to the plurality of heat transfer tubes to introduce the first fluid into the plurality of heat transfer tubes,

a second tube plate having one end connected to the plurality of heat transfer tubes and the other end connected to the first outlet for discharging the first fluid from the heat transfer tubes,

a plurality of heat transfer tubes including at least one vortex tube that generates a vortex flow, wherein,

the vortex flow pipe comprises a structure body and an inner pipe wall arranged on the structure body, wherein one end of the structure body is used for inputting fluid, the other end of the structure body is used for outputting vortex flow fluid, the inner pipe wall comprises,

a first transition section located at a first end of the inner tube wall near the input fluid, having a first length in a longitudinal direction of the vortex flow tube and a first cross section smoothly transitioning from a circular shape with a radius R to a vane shape with a non-linear transition of the first transition section in the longitudinal direction by a first predetermined angle, the vane shape comprising a square with a side length of 2R and a semi-circle with a radius R extending on each side of the square,

a swirl flow section connecting the first transition section, the swirl flow section having a second length in a longitudinal direction of the swirl flow tube and a second cross section that is the shape of the vane as the swirl flow section twists by a second predetermined angle in the longitudinal direction,

a second transition section connecting the swirling flow section and located at a second end of the inner tube wall opposite the first end, the second transition section having a third length in the longitudinal direction of the swirling flow tube and a third cross section smoothly transitioning from the vane shape to a circular shape with a radius R while the second transition section is twisted by a third predetermined angle in the longitudinal direction, the third cross section being twisted by a third predetermined angle in the longitudinal direction in a non-linear transition with the second transition section,

a second inlet provided on the shell between the first tube sheet and the second tube sheet to introduce a second fluid,

and a second outlet provided on the housing and arranged opposite to the second inlet to lead out the second fluid flowing through the heat transfer pipe.

In the heat exchanger, the first cross-section torsion angle is gradually changed based on an alpha transition curve, wherein,

l1 is the first length, and x1 is the position coordinate of the first cross-section in the length direction.

In the heat exchanger, the third cross-sectional torsion angle is gradually changed based on an alpha transition curve, wherein,

l3 is the third length, and x3 is the position coordinate of the third cross-section in the length direction.

In the heat exchanger, the first cross section torsion angle and/or the third cross section torsion angle are gradually changed based on a Vitoseski curve or a cosine function.

In the heat exchanger, the second side and the first side are oppositely arranged left and right or up and down.

In the heat exchanger, a plurality of baffle plates which are arranged in the shell between the second inlet and the second outlet are distributed in a staggered mode, and S-shaped channels are formed among the baffle plates.

In the heat exchanger, the first preset length is one fourth of the length of the structure body, the second preset length is one half of the length of the structure body, and the third preset length is one fourth of the length of the structure body.

In the heat exchanger, the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees, the third predetermined angle is 90 degrees, and the ratio of the first length or the third length to the second length is equal to the ratio of the first predetermined angle or the third predetermined angle to the second predetermined angle.

In the heat exchanger, the heat transfer pipe comprises a plurality of straight pipes or bent pipes and a plurality of vortex flow pipes, two ends of each vortex flow pipe are respectively connected with the straight pipes or the bent pipes, and the first fluid is in a gas state or a liquid state.

In the heat exchanger, the structural body is a straight pipe or an elbow pipe.

The heat exchanger comprises a heat exchanger body, a first inlet, a second inlet, a temperature measuring unit, a seal head and a control unit, wherein the first inlet and the second inlet are respectively provided with a control valve, the control unit is connected with the temperature measuring unit and the control valves, and the on-off and opening degree of the control valves are controlled in response to measured temperature data of the temperature measuring unit.

In the heat exchanger, the ratio of the sum of the first length, the second length and the third length to the radius R is 16: 1 to 4: 1.

In the heat exchanger, the vortex flow pipe comprises a first gradient section, n vortex flow sections and a second gradient section, wherein n is a natural number larger than 1.

In the heat exchanger, the first preset angle is 90 degrees, the second preset angles are n 180 degrees, and the third preset angle is 90 degrees.

In the heat exchanger, the sum of the first preset angle, the second preset angle and the third preset angle is n +1 180 degrees.

Technical effects

The utility model discloses a self structure is induced to produce the vortex flow, need not the external energy and supplies with. No part extending to the inside of the pipeline exists, the pipeline cannot be blocked, and the difficulty in pipeline operation and maintenance cannot be brought. The vortex flow pipe is repeatedly arranged at the proper position of the heat exchanger in a targeted manner, so that the whole tubular reactor is ensured to be in a vortex flow state, vortex flow which can be formed by the vortex flow pipe strongly impacts the surface of the inner pipe, and the heat exchange efficiency is improved. Meanwhile, the vortex flow has the function of self-cleaning of the pipeline, and the deposition of dirt and heat resistance in the pipeline are avoided. The vortex flow pipe of the utility model adopts self structure to induce vortex flow without external energy supply. The device has no parts seeping into the pipeline, cannot block the pipeline, and cannot cause difficulty in scaling and cleaning the pipeline. Vortex flow that vortex flow tube can form strikes inner tube surface by force, improves heat exchange efficiency. The utility model discloses a vortex flow has the pipeline automatically cleaning effect, avoids intraductal deposition dirt to hinder heat, reduces and washs the number of times. The utility model discloses the loss of pressure that causes the heat exchanger is little, and fluid resistance is little, easy installation is easily maintained.

The above description is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clearly understood, the technical means of the present invention is implemented to the extent that those skilled in the art can implement the technical solutions according to the description, and in order to make the above and other objects, features, and advantages of the present invention more obvious and understandable, the following description is given by way of example of the embodiments of the present invention.

Drawings

Various other advantages and benefits of the present invention will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. It is obvious that the drawings described below are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be obtained from these drawings without inventive effort. Also, like parts are designated by like reference numerals throughout the drawings.

In the drawings:

fig. 1 is a schematic structural view of a heat exchanger according to an embodiment of the present invention;

fig. 2 is a schematic view of a scroll flow tube structure of a heat exchanger according to an embodiment of the present invention;

fig. 3 is a schematic view of a scroll flow tube structure of a heat exchanger according to an embodiment of the present invention;

FIG. 4 is a schematic cross-sectional view of the inner wall at a transition stage in the transition section of the vortex tube of the heat exchanger;

FIG. 5 is a schematic cross-sectional view of the complete blade shape after completion of the ramp in the ramp section of the vortex tube of the heat exchanger;

FIG. 6 is a schematic comparison of different gradual changes of the vortex flow tube of a heat exchanger according to an embodiment of the present invention;

fig. 7 is a schematic structural view of a heat exchanger according to an embodiment of the present invention;

fig. 8 is a schematic structural view of a heat exchanger according to an embodiment of the present invention;

fig. 9 is a schematic structural view of a heat exchanger according to an embodiment of the present invention;

fig. 10 is a schematic view of a heat exchanger according to an embodiment of the present invention;

fig. 11 is a schematic structural view of a heat exchanger according to an embodiment of the present invention;

fig. 12 is a nussel number schematic of a heat exchanger according to an embodiment of the invention;

fig. 13 is a schematic diagram of a comparison of the alpha transition curve and tangential velocity using a non-linear progression and a normal linear progression of the vittonsiki curve for an embodiment of the invention;

fig. 14 is a schematic diagram of a comparison of an alpha transition curve and wall shear forces using a non-linear progression and a normal linear progression of a vittonsiki curve according to an embodiment of the invention;

fig. 15 is a graph showing a comparison of the alpha transition curve and the pressure loss using a non-linear progression and a normal linear progression of the vittonsiki curve according to an embodiment of the invention;

the invention is further explained below with reference to the drawings and examples.

Detailed Description

Specific embodiments of the present invention will be described in more detail below with reference to fig. 1 to 15. While specific embodiments of the invention are shown in the drawings, it will be understood that the invention may be embodied in various forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.

It should be noted that certain terms are used throughout the description and claims to refer to particular components. As one skilled in the art will appreciate, various names may be used to refer to a component. This specification and claims do not intend to distinguish between components that differ in name but not function. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. The following description is of the preferred embodiment of the invention, and is made for the purpose of illustrating the general principles of the invention and not for the purpose of limiting the invention. The protection scope of the present invention is subject to the limitations defined by the appended claims.

It should be noted that the terms "first", "second", and the like in the description, the claims, and the drawings of the present invention are used for distinguishing some objects, and are not used for describing a specific order or sequence. It is to be understood that the terms so used are interchangeable under appropriate circumstances for describing embodiments of the invention herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.

Furthermore, spatially relative terms such as "above/below … …", "above/below … …", "above/below … …", "above … …", and the like, may be used herein to describe the spatial relationship of one device or feature to another device or feature for ease of description. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the present disclosure. For example, if a device is turned over, devices described as "above" or "above" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary term "at/at the lower end of … …" can encompass both an orientation of "at the lower end of … …" and "at the upper end of … …". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.

In the description of the present invention, it is to be understood that the orientation or positional relationship indicated by the orientation words such as "front, back, up, down, left, right", "horizontal, vertical, horizontal" and "top, bottom", etc. are usually based on the orientation or positional relationship shown in the drawings or under the conventional placement condition, only for the convenience of describing the present invention and simplifying the description, and in the case of not making a contrary explanation, these orientation words do not indicate and imply that the device or element referred to must have a specific orientation or be constructed and operated in a specific orientation, and therefore, should not be construed as limiting the scope of the present invention; similarly, the terms "inner and outer" refer to the inner and outer contours of the respective component itself.

For the purpose of facilitating understanding of the embodiments of the present invention, the following description will be given by way of example with reference to the accompanying drawings, and the drawings do not limit the embodiments of the present invention.

For better understanding, as shown in fig. 1 to 3, a heat exchanger includes,

a housing 2;

a first inlet 6 provided at a first side of the housing 2 to introduce a first fluid,

a first outlet 7 provided at a second side of the housing 2 different from the first side for conducting a first fluid out,

a first tube sheet 8 having one end connected to the first inlet 6 and the other end connected to the plurality of heat transfer tubes 11 to introduce the first fluid into the plurality of heat transfer tubes 11,

a second tube plate 9 having one end connected to the plurality of heat transfer tubes 11 and the other end connected to the first outlet 7 to lead out the first fluid in the heat transfer tubes 11,

a plurality of heat transfer tubes 11 including at least one swirl flow tube 10 that generates a swirl flow, wherein,

the vortex flow pipe 10 comprises a structure body 1 and an inner pipe wall arranged on the structure body 1, wherein one end of the structure body 1 inputs fluid, the other end outputs vortex flow fluid, the inner pipe wall comprises,

a first transition section 3, which is located at a first end of the inner pipe wall close to the input fluid, and which has a first length in the longitudinal direction of the vortex flow pipe 10 and a first cross section, which smoothly transitions from a circular shape with a radius R to a vane shape while the first transition section 3 is twisted by a first predetermined angle in the longitudinal direction, the first cross section being twisted by a first predetermined angle in a non-linear transition in the longitudinal direction with the first transition section 3, the vane shape comprising a square with a side length of 2R and a semicircle with a radius R extending on each side of the square, further, the cross-sectional area of the first cross section is kept constant,

a swirling flow section 4 connecting the first transition section 3, the swirling flow section 4 having a second length in the longitudinal direction of the swirling flow tube 10 and a second cross section which is the shape of the vane as the swirling flow section 4 twists by a second predetermined angle in the longitudinal direction,

a second transition section 5 connecting the swirling flow section 4 and located at a second end of the inner tube wall opposite to the first end, the second transition section 5 having a third length in the longitudinal direction of the swirling flow tube 10 and a third cross section, the third cross section smoothly changing from the vane shape to a circle with a radius R while the second transition section 5 is twisted by a third predetermined angle in the longitudinal direction, the third cross section being twisted by the third predetermined angle in a non-linear gradual manner in the longitudinal direction as the second transition section 5, further, a cross sectional area of the third cross section is kept constant;

a second inlet 12 provided on said shell 2 between the first tube sheet 8 and the second tube sheet 9 for introducing a second fluid,

and a second outlet 13 provided in the casing 2 and arranged opposite to the second inlet 12 to lead out the second fluid flowing through the heat transfer pipe 11.

In a preferred embodiment of the heat exchanger, the first cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

In a preferred embodiment of the heat exchanger, the third cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

In a preferred embodiment of the heat exchanger, the first cross-sectional torsion angle and/or the third cross-sectional torsion angle is/are gradually changed based on a victorissis curve or a cosine function.

In a preferred embodiment of the heat exchanger, the second side and the first side are oppositely arranged left and right or up and down.

In the preferred embodiment of the heat exchanger, the first predetermined length is one fourth of the length of the structural body 1, the second predetermined length is one half of the length of the structural body 1, and the third predetermined length is one fourth of the length of the structural body 1.

In a preferred embodiment of the heat exchanger, the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees, the third predetermined angle is 90 degrees, and a ratio of the first length or the third length to the second length is equal to a ratio of the first predetermined angle or the third predetermined angle to the second predetermined angle.

In a preferred embodiment of the heat exchanger, the heat transfer pipe 11 includes a plurality of straight pipes or bent pipes, and a plurality of vortex pipes 10, two ends of the vortex pipes 10 are respectively connected to the straight pipes or the bent pipes, and the first fluid is in a gas state or a liquid state.

In the preferred embodiment of the heat exchanger, the structural body 1 is a straight pipe or an elbow pipe.

In the preferred embodiment of the heat exchanger, the heat exchanger further comprises a temperature measuring unit, a sealing head and a control unit, wherein the first inlet 6 and the second inlet 12 are respectively provided with a control valve, the control unit is connected with the temperature measuring unit and the control valves, and the on-off and opening degree of the control valves are controlled in response to the measured temperature data of the temperature measuring unit.

In the preferred embodiment of the heat exchanger, the structural body 11 is a straight pipe, the radius R is 0.01m to 100m, and the ratio of the sum of the first length, the second length and the third length to the radius R is 8: 1.

In one embodiment, as shown in fig. 4 to 5, in the process of gradually changing the cross-sectional shape of the inner wall of the tube of the first gradual change section 3 and the second gradual change section 5 from a circular shape to a blade-shaped cross-section, the cross-section is axially rotated clockwise or counterclockwise by a predetermined angle. The cross section of the inner wall of the pipe in a transition stage in the gradual change region is shown in fig. 4, and the cross section of the complete blade shape after the gradual change is shown in fig. 5, wherein Rcs is the diameter of the inner square circumscribed circle after the gradual change is completed. And R is the diameter of the internal square circumscribed circle in the gradual change process. rf is the radius of the blade-shaped fan after the gradual change is finished, and r is the radius of the blade-shaped fan in the gradual change process. A is the center of the blade-shaped fan, O is the center of the circumscribed circle of the inner square after the gradual change is finished, BDEF is four vertexes of the inner square after the gradual change is finished, and C is used for representing the circular arc BCD. y is the distance from A to the center O of the square circumscribed circle. Gamma is the angle formed by the radius of the leaf-shaped sector and the square vertical side (FB). γ is 45 ° when the cross section is circular and 90 ° when the cross section is the shape of a complete blade. A series of transition sections may be formed as the gamma angle gradually increases from 45 deg. to 90 deg.. These sections are turned clockwise (or counterclockwise) through a predetermined angle in the course of the axial progression, and are twisted 90 ° clockwise in the illustration. If the change of the spacing between the sections is uniform during the clockwise rotation of the sections in the axial direction, the transition is a linear transition.

As shown in fig. 6, where x is the cross-sectional location coordinate from the circular cross-section in the transition tube, L is the length of the transition tube, and γ is the angle formed by the radius of the lobed sector and the square vertical side FB. When x is located at the circular cross-section, x is 0, so x/L is 0, where γ is 45 °; when x is in the shape of a complete blade, x is L, so x/L is 1, where γ is 90 °, γ is 45 ° when the cross-section is circular, and γ is 90 ° when the cross-section is in the shape of a complete blade. A series of transition sections may be formed as the gamma angle gradually increases from 45 deg. to 90 deg.. These sections are turned clockwise or counterclockwise through a predetermined angle during the axial progression, for example, by 90 ° clockwise in the illustration. The utility model discloses a produce bigger vortex intensity and reduce along the journey loss of pressure, can be at the originated section of gradual change district section and the smooth transition mode that ends section design transition more, the angle of turning over in the unit distance is littleer promptly. Such as an alpha transition curve based on a cosine function, or using a vitoscinski curve (Vitosinski curve). Wherein the content of the first and second substances,

in the vortex flow tube 10, the ratio of the sum of the first length, the second length and the third length to the radius R is 8: 1, which is based on the ratio of the strength of the vortex generated by the vortex flow tube 1010 to the pressure loss caused by the vortex flow tube. I.e. the maximum intensity of the vortex flow is generated with the minimum pressure loss.

In one embodiment, as shown in fig. 7, the heat exchanger is a shell and tube heat exchanger comprising a shell 2, a tube bundle and a head. The shell 2 is cylindrical and houses heat transfer tubes 11, such as a bundle of parallel tubes, fixed to a tube sheet. Two fluids that exchange heat in a shell and tube heat exchanger, one flowing within the tube bundle, have a stroke called the tube side. The other flows within the tube housing, referred to as the shell side. The wall surface of the tube bundle is the heat transfer surface. In order to improve the shell pass, asymmetric baffles 14 are arranged in the shell 2 up and down to make the flow outside the tube in a snake shape, so that the indirect heat exchange between the fluid outside the tube and the fluid inside the tube is improved. The utility model discloses be applied to the tube bank with vortex flow tube 10, make the interior furthest's of flowing increase torrent effect of tube bank, increase heat exchange efficiency. Meanwhile, the wall surface or the pipe wall is reduced in scaling and heat resistance by the self-cleaning function of the vortex flow.

In one embodiment, the swirl tubes 10 replace a straight section of each inner tube in the tube bundle in the inlet direction, and then the swirl tubes 10 are placed at intervals to maintain the fluid turbulence intensity and self-cleaning capability of the application. The spacing between the swirl tubes 10 depends on the diameter of the tubes, the flow rate of the fluid, and the smoothness of the walls. In specific implementation, the optimal spacing parameters can be obtained through Computational Fluid Dynamics (CFD) simulation.

In one embodiment, as shown in fig. 8, if additional tube passes are desired, the cold fluid inlet and outlet can be mounted on the same side of the tube sheet, with the head divided into two chambers by a partition 15. Each tube is bent into a U-shape. The U-shaped pipe can double the pipe pass, and the heat transfer efficiency of the fluid in the pipe and the fluid outside the pipe is increased. The swirl tubes 10 are then arranged at a distance from the inlet end on each tube. The distance of separation can be optimized by computational fluid dynamics CFD simulation.

In one embodiment, because the U type pipe is difficult to dismantle the replacement, and the tube side is difficult to wash, although vortex flow tube 10 can slow down the scale deposit, to unclean or the fluid of easy scale deposit, still need regularly to wash, also can partly remove U type pipe, the intraductal fluid mixes the back in opposite side head, reentrant upper end inner tube forms shell and tube type heat exchanger.

In one embodiment, as shown in fig. 9, the heat exchanger is a double pipe heat exchanger, which includes two straight pipes with different diameters assembled concentrically and a U-shaped bent pipe connected to the inner pipe, and the two fluids for heat exchange enter the inner pipe and the annular channel between the inner pipe and the outer pipe respectively, and exchange heat with the inner pipe wall. Adopts a counter-current mode. The inner pipe and the outer pipe are both provided with vortex pipes 10 in a countercurrent (or concurrent) heat exchange mode. Place vortex tube 10 at hot-fluid entrance point (outer tube), place vortex tube 10 again at the initial section of next journey outer tube behind the intertube connecting piece, so reciprocal, guarantee that every layer of outer tube all has at least one outer tube vortex tube 10, place the position at the initiating terminal of the direction that the fluid flows to ensure that its low reaches have abundant vortex flow.

The inner tube fluid flow direction is opposite to the outer tube fluid flow direction. Place whirlpool vortex pipe 10 at cold fluid inducer (inner tube), place whirlpool vortex pipe 10 again at the next journey inner tube initiating terminal behind the U-shaped pipe, so reciprocal, guarantee that every layer of outer tube all has at least one inner tube vortex pipe 10, place the initiating terminal of position in the direction that the fluid flows to ensure that its low reaches have abundant vortex. Because the pipe diameter of inner tube is less than the outer tube pipe diameter, the effect scope of inner tube vortex flow tube 10 is less under the same velocity of flow, therefore the inner tube can set up more vortex flow tube 10 each journey. In specific implementation, the optimal spacing parameters of the inner pipe and the outer pipe can be obtained through Computational Fluid Dynamics (CFD) simulation. The inner pipe spiral pipe and the outer pipe spiral pipe can adopt anticlockwise spiral; or the inner (outer) tube spiral tube adopts clockwise spiral, and the outer (inner) tube spiral tube adopts anticlockwise spiral.

In one embodiment, as shown in FIG. 10, the heat exchanger is a submerged coil heat exchanger. Coil heat exchangers are formed by bending metal or non-metal tubes into desired shapes, such as round, spiral, and long coils, as desired. The coil heat exchanger can be divided into immersion coil and spray coil according to different use states. When in use, the two fluids are immersed in a container containing heated or cooled media, and the two fluids exchange heat respectively inside and outside the tube. The immersion coil heat exchanger has simple structure, low cost and less operation sensitivity, and the pipe can bear larger fluid medium pressure. However, the flow velocity of the fluid outside the pipe is small, so the heat transfer coefficient is small, the heat transfer efficiency is low, the required heat transfer area is large, and the equipment is heavy. Submerged coil heat exchangers are often used for cooling of high pressure fluids, as well as heat transfer elements of the reactor. According to the bending shape of the metal pipe, the vortex flow pipe 10 is designed into a corresponding bending shape (such as bending 90 degrees or 180 degrees), the vortex flow pipe 10 is installed at the hot fluid inlet end, the vortex flow pipe 10 is installed repeatedly at a proper position in a targeted manner, and the whole tubular reactor is ensured to be in a vortex flow state. Vortex flow that vortex flow tube 10 can form strikes inner tube surface by force, improves heat exchange efficiency. Meanwhile, the vortex flow has the function of self-cleaning of the pipeline, and the deposition of dirt and heat resistance in the pipeline are avoided.

In one embodiment, as shown in fig. 11, the heat exchanger is a trickle heat exchanger. The spray heat exchanger fixes the heat exchange tubes on the steel frame in rows, cooled fluid flows in the tubes, and cooling water is uniformly sprayed by a spray device above the tube rows. Compared with the immersion type, the spray type heat exchanger has the main advantages of large heat transfer coefficient of fluid outside the pipe, and convenient maintenance and cleaning. Its disadvantages are large volume and large consumption of cooling water. The tube rows are connected by U-shaped tubes to save space. The vortex flow pipe 10 is arranged at the inlet end of the cooled fluid, the vortex flow pipe 10 is placed at the starting end of the next heat exchange pipe behind the U-shaped pipe again, and the reciprocating operation ensures that each layer of outer pipe is provided with at least one inner pipe vortex flow pipe 10, and the starting end of the position in the fluid flowing direction is placed to ensure that the downstream of the outer pipe has sufficient vortex flow. In specific implementation, the nearest mounting position of the vortex tube 10 can be obtained through computational fluid dynamics CFD simulation. A water tank is arranged below the heat exchange tube bank, and cooling liquid in the water tank is conveyed to the upper part of the heat exchange tube bank by a water pump and is uniformly sprayed down by a spraying device. The cooling water forms a layer of liquid film with higher turbulence degree outside the heat exchange pipe, and the heat exchange of cold and hot fluids is realized through the wall of the heat exchange pipe.

As shown in fig. 12, the knoop number is an important parameter in the heat transfer phenomenon, and it directly affects the magnitude of the convective heat transfer coefficient, and the evaluation of the knoop number is also an index for evaluating the heat transfer efficiency. The magnitude of the nussel number indicates the degree of enhancement of convective heat transfer relative to the same fluid layer. The larger the Knoop number is, the more obvious the convection heat exchange effect is.

Compared with linear transition, the nonlinear transition mode can provide smoother transition, avoid local eddy and boundary layer separation generated by larger change of the shape of the section of the pipeline, cause larger local pressure loss, and influence the weakening of wall shearing force caused by boundary layer falling when the circular section is transited to the blade section. In order to illustrate the vortex strength of the nonlinear gradual increase of the present invention, different flow rates are simulated as shown in fig. 13, in which a comparison schematic diagram of the nonlinear gradual change and the common linear gradual change of an alpha transition curve based on a cosine function and a victorinsty curve is given, and when three transition modes are used for the transition pipe, the initial tangential velocity value at the outlet of the vortex flow pipeline is obtained. The greater the shear velocity, the greater the eddy current intensity. It can be seen from the figure that as the pipe flow rate increases, the vortex strength increases. At each flow rate, the strength of the generated vortex was induced. The cross section is twisted in a non-linear gradual manner along the longitudinal direction of the gradual change section and is in a preset angle, the Wittonsisky transition mode is superior to the alpha transition mode, and the alpha transition mode is superior to the linear transition mode. There is a significant increase in the vortex flow effect when using a non-linear gradual twist preset angle. The linear transition mode produced cut velocity values 19.1-33.1% lower than the vittonsiki transition. Compared with the Wittonsiki transition, the cutting speed value generated by the alpha transition mode is 6.5 to 18.6 percent lower. Compared with linear transition, the provided non-linear gradual transition of an alpha transition mode, a Wittonsisky curve transition mode and the like generates larger initial tangential velocity, and the stronger vortex effect is also meant. The performance of the vortex tube is obviously improved.

Fig. 14 is a graph showing the comparison between the α transition curve and the wall shear force using the non-linear transition and the normal linear transition of the vitoshib curve according to an embodiment of the present invention, and the CFD simulation of the inlet flow rate of 3m/s proves that the wall shear force behind the non-linear transition is significantly increased when the non-linear transition is used. Compared with linear transition, when an alpha transition mode is used, the shearing force of the wall surface is increased by 2-8%; when the Wittonsiki curve transition mode is used, the wall shearing force is increased by 2% -13%. Fig. 15 is a graph showing the comparison between the α transition curve and the pressure loss using the non-linear transition and the normal linear transition of the vitoshib curve according to an embodiment of the present invention, and at the same time, the pressure loss is reduced by 16% to 28% when the α transition mode is used, compared to the linear transition mode; when the Wittonsiki curve transition mode is used, the pressure loss is reduced by 22 to 38 percent. Therefore, when the nonlinear transition is used, due to the fact that the smooth fluid channel is provided, the adverse effects of local turbulence, wall surface boundary layer separation and the like are caused on the wall surface, the pressure loss can be reduced to the maximum extent, and the energy consumption is reduced. Meanwhile, more energy is used for inducing and generating vortex flow, so that the generated vortex flow is higher in strength, and the effect of improving the wall surface shearing force is more obvious. The nonlinear transition technology can enable the vortex flow tube to play a more remarkable role on the tubular (surface type) heat exchanger, reduce energy consumption and prolong the service life of process equipment. The heat exchanger has high energy consumption ratio in the processing process. Due to the effect improvement brought by the nonlinear transition technology, the cost can be obviously reduced for enterprises, and the overall production efficiency is improved.

The above examples are only intended to illustrate the technical solutions of the present disclosure, not to limit them; although the present disclosure has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present disclosure.

Claims

1. A heat exchanger, characterized in that it comprises,

a housing;

2. The heat exchanger of claim 1, wherein the first cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

3. The heat exchanger of claim 1, wherein the third cross-sectional twist angle is gradual based on an alpha transition curve, wherein,

4. The heat exchanger of claim 1, wherein the first cross-sectional twist angle and/or the third cross-sectional twist angle is graded based on a Vitossby curve or a cosine function.

5. The heat exchanger of claim 1, wherein the second side is disposed opposite the first side from the left to the right or from the top to the bottom.

6. The heat exchanger of claim 1, wherein a plurality of baffles are disposed in a staggered arrangement within the housing between the second inlet and the second outlet, the baffles forming an S-shaped channel therebetween.

7. A heat exchanger as claimed in claim 1, wherein the first predetermined angle is 90 degrees, the second predetermined angle is 180 degrees and the third predetermined angle is 90 degrees, the ratio of the first or third length to the second length being equal to the ratio of the first or third predetermined angle to the second predetermined angle.

8. The heat exchanger of claim 1, wherein the heat transfer tube comprises a plurality of straight or curved tubes and a plurality of vortex tubes, the vortex tubes are connected at two ends to the straight or curved tubes respectively, and the first fluid is in a gas or liquid state.

9. The heat exchanger of claim 1, wherein the structural body is a straight tube or an elbow tube.

10. The heat exchanger of claim 1, wherein the heat exchanger further comprises a temperature measuring unit, a sealing head and a control unit, the first inlet and the second inlet are respectively provided with a control valve, the control unit is connected with the temperature measuring unit and the control valve, and the on-off and opening degree of the control valve are controlled in response to the measured temperature data of the temperature measuring unit.

11. The heat exchanger of claim 1, wherein the ratio of the sum of the first length, the second length, and the third length to the radius R is from 16: 1 to 4: 1.

12. The heat exchanger of claim 1, wherein the swirl tube comprises a first transition section, n swirl flow sections, and a second transition section, n being a natural number greater than 1.

13. The heat exchanger of claim 12, wherein the first predetermined angle is 90 degrees, the second predetermined angles are n 180 degrees, and the third predetermined angle is 90 degrees.

14. The heat exchanger of claim 12, wherein the first, second and third predetermined angles sum to n +1 180 degrees.