CN106595378B - High-efficient heat exchanger of tubular - Google Patents
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- CN106595378B CN106595378B CN201510671967.7A CN201510671967A CN106595378B CN 106595378 B CN106595378 B CN 106595378B CN 201510671967 A CN201510671967 A CN 201510671967A CN 106595378 B CN106595378 B CN 106595378B
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Abstract
The invention provides a simple modification method of a high-efficiency heat exchanger, which is characterized in that a tube type heat exchange tube is filled with a novel filler, and the heat transfer efficiency is obviously improved. The novel spherical wire mesh packing and the inner tongue arch ring packing are developed and verified to be efficient packing with the greatest development potential for heat exchanger reinforcement transmission, and the convection heat transfer coefficient and the heat exchange quantity of the novel spherical wire mesh packing and the inner tongue arch ring packing can be improved by about 200% compared with those of an empty pipe under the optimized process condition. According to the evaluation criteria (PEC) comprehensive evaluation result of the enhanced heat transfer performance, when the Reynolds number is less than 7000, the combination of the inner 20mm inner-diameter inner-tongue-arch annular filler and the inner 25mm inner-tongue-arch annular filler filled in the 25mm inner-diameter monotube and the 25mm inner-diameter spherical wire mesh filler is remarkably superior to the coil insert in comprehensive heat transfer performance. The invention has important guiding significance and application value for research and development of the high-efficiency heat exchanger and improvement of the heat exchange efficiency of the existing tubular heat exchanger, and meets the application requirements of simplicity, convenience, economy and high efficiency.
Description
Technical Field
The invention relates to development of efficient energy-saving equipment for strengthening heat transfer performance by combining a novel turbulence element and a tube type heat exchanger, is suitable for single-phase or multi-phase fluid convection heat transfer and steam condensation convection heat transfer, and belongs to the technical field of heat exchange.
Background
The heat exchanger occupies a large proportion in chemical investment, and the improvement of the heat performance of the heat exchanger is beneficial to reducing equipment investment, fully utilizing and recycling waste heat, saving energy, reducing consumption, saving space and bearing weight of buildings. According to statistics, if a boiler is also used as heat exchange equipment in a thermal power plant, the investment of a heat exchanger accounts for about 70% of the total investment of the whole power plant, the investment of the heat exchanger accounts for 40% -50% of the total investment in general petrochemical enterprises, the investment of the heat exchanger accounts for 30% -40% of the total investment in modern petrochemical enterprises, and two heat exchangers are arranged in four parts of a refrigeration and air-conditioning system. The tubular heat exchanger is common equipment for industrial heat exchange, has the advantages of wide material selection range, convenient cleaning of heat exchange surface, strong adaptability, large processing capacity, high temperature resistance, high pressure resistance and the like, and occupies a dominant position in heat exchange equipment. The strengthening of the heat exchange process is one of the main directions of the development of high-efficiency energy-saving equipment. In the reactive strengthening technology, fins are added on the inner tube and the outer tube of the tube heat exchanger to improve the heat exchange effect, but the heat exchange tube with the fins is complex to process, easy to scale and influence the heat exchange efficiency, and difficult to clean. To overcome these disadvantages, there are many fin-like inserts built into the heat exchange tubes instead of the fins. The heat exchanger is provided with a plurality of interpolators such as a disc-shaped sheet, a spiral line, a twisted spiral sheet, a metal net, a spiral brush, a static mixer, a crossed sawtooth belt, a trapezoidal belt, a twisted wire, a flat iron, a twisted iron, a star and the like to improve the heat exchange efficiency. However, industrial heat exchangers incorporating inserts have little practical application.
Disclosure of Invention
In order to overcome the defects, the invention provides a high-efficiency energy-saving heat exchanger device which is formed by filling a porous hollow spherical metal wire mesh filler and an inner tongue ring-shaped filler which are patented products into an inner tube of a tubular heat exchanger as novel turbulence elements (the outer diameter of an insert in the filled material is smaller than the inner diameter of the heat exchange tube) and improving the heat exchange efficiency of a common tubular heat exchanger.
The experiment of single-phase convection enhanced heat transfer and steam condensation convection enhanced heat transfer proves that the enhanced heat transfer effect of the two novel turbulence elements, namely the spherical wire mesh filler and the inner tongue arch annular filler, is remarkable, and the heat exchange coefficient can be improved to about three times of that of a hollow pipe to the maximum. The porous hollow body spherical structure of spherical silk screen filler, multidirectional the same sex, disturbance fluid that can be obvious also can shunt the liquid film heat transfer resistance that condensate to a great extent had avoided leading to through the sphere surface, can improve heat transfer coefficient by a wide margin, packs simultaneously and can increase heat transfer area through the fine contact heat transfer with the pipe wall. The single tube experiment result shows that the spherical silk screen packing has a remarkable heat exchange enhancement effect in a laminar flow area; the special inner tongue structure of the inner tongue-shaped bow annular packing can greatly increase the heat exchange area, greatly strengthen turbulence and split condensate to reduce the wall flow liquid film thickness, and has more obvious heat exchange strengthening effect under various conditions.
Spherical wire mesh packing exhibits more significant heat transfer enhancement in the laminar flow region than coil inserts, while intra-lingual arch ring packing enhances heat transfer more significantly throughout fluid flow conditions. Experiments show that the fluid resistance brought by the spherical wire mesh packing is larger (can be optimized by adjusting the diameter of the holes or the balls or mixing and assembling), and the fluid resistance of the inner tongue arch annular packing is similar to that of the coil insert. Therefore, the single spherical wire mesh filler or the inner tongue arch annular filler or the mixed filler thereof can obviously improve the comprehensive heat exchange coefficient, and has better application effect than the inner inserts of coils and the like. The porous hollow metal spherical silk screen and the inner tongue bow annular filler can be respectively and directly placed in the tube, or can be connected in series by one metal wire; the porous hollow metal spherical and the inner tongue arch annular packing are respectively and continuously strung together or strung together at intervals, and the interval distance ranges from 0 to 5 times of the outer diameters of the porous hollow metal spherical and the inner tongue arch annular packing; in addition, the porous hollow metal spherical and inner tongue arch annular fillers can be directly assembled in the same pipe body at the same time, and can also be placed together in a stringing mode by using metal wires, the ratio range of the number of the adjacent porous hollow metal spherical and inner tongue arch annular fillers is 5: 1-1: 5, and the assembling and mixed assembling modes have the effect of remarkably improving the heat exchange efficiency.
The invention provides a simple modification method of a high-efficiency heat exchanger, which is characterized in that a tube type heat exchange tube is filled with a novel filler to obviously improve the heat transfer efficiency. The novel spherical wire mesh packing and the inner tongue ring packing are developed and verified to be efficient packing which has the greatest development potential and is used for enhancing heat transfer of the heat exchanger, the convection heat transfer coefficient and the heat exchange quantity of the novel spherical wire mesh packing and the inner tongue ring packing can be improved by about 200 percent compared with those of an empty pipe under the optimized process condition, and the inner diameter ratio of the porous hollow metal spherical packing and the inner tongue ring packing to the heat exchange pipe is 0.1-1, preferably 0.50-0.95. According to the evaluation criteria (PEC) comprehensive evaluation result of the enhanced heat transfer performance, when the Reynolds number is less than 7000, the combination of the inner 20mm inner-diameter inner-tongue-arch annular filler and the inner 25mm inner-tongue-arch annular filler filled in the 25mm inner-diameter monotube and the 25mm inner-diameter spherical wire mesh filler is remarkably superior to the coil insert in comprehensive heat transfer performance. The invention has important guiding significance and application value for research and development of the high-efficiency heat exchanger and improvement of the heat exchange efficiency of the existing tubular heat exchanger, and meets the application requirements of simplicity, convenience, economy and high efficiency.
Drawings
FIG. 1 shows a spherical wire mesh packing (5 mm. 5mm holes)
Inner tongue bow ring packing of figure 2 (inner diameter 25mm)
FIG. 3 is a schematic view of a double-pipe single-pipe heat exchanger
1. An inner sleeve outlet; 2. an outer sleeve inlet; 3. a heat-insulating layer; 4. an outer sleeve; 5. an inner sleeve; 6. an outer sleeve outlet; 7. inner sleeve inlet
FIG. 4QaveVariation relationship with Re
FIG. 5 hiVariation relationship with Re
FIG. 6 packing combination QaveVariation relationship with Re
FIG. 7 packing combination hiVariation relationship with Re
FIG. 8QaveVariation relationship with Re
FIG. 9 hiVariation relationship with Re
FIG. 10 ratio of convective heat transfer coefficients of various inserts to empty tubes
FIG. 11 is a view showing a laminar flow state hiVariation relationship with Re
FIG. 12QaveVariation relationship with Re
FIG. 13 hiVariation relationship with Re
FIG. 14Q for the interposer combinationaveVariation relationship with Re
FIG. 15 shows the insert combination hiVariation relationship with Re
FIG. 16QaveVariation relationship with Re
FIG. 17 hiVariation relationship with Re
FIG. 18 ratio of convective heat transfer coefficients of each insert to the empty tube
FIG. 19 Each of the interposers Q/LmAs a function of the amount of steam
FIG. 20 relationship between the friction factor of each insert and the empty tube and Re
FIG. 21 PEC vs. Re curves
Detailed description of the preferred embodiment
The heat transfer experiments of vertically and horizontally placing a single tube are respectively carried out on the lower hollow tube, the coil insert, the spherical silk screen packing and the inner tongue arch annular packing, and the optimal enhanced heat transfer range and the enhanced heat exchange effect of the packing can be well compared and proved by measuring the experimental data under different Reynolds numbers. Compared with series heat exchange effects of spherical silk screen packing and inner tongue arch annular packing with different inner diameters and single tube combinations with different placement conditions, the influence rule of the geometric parameters of the two novel disturbing packings on heat transfer performance and fluid resistance can be better known.
The schematic diagram of the spherical silk screen packing is shown in the attached figure 1, and the specific physical parameters are shown in the table 1. The spherical silk screen filler can be manufactured by stamping a metal silk screen, a metal net, a porous metal plate and the like into a hemisphere and then welding or other simple and convenient methods. The spherical silk screen packing is a porous hollow sphere, and has the characteristics of high porosity, isotropy and wall flow reduction. In single-phase forced convection heat transfer, the turbulence of fluid can be enhanced, the thickness of laminar flow layer fluid is reduced, and heat transfer can be obviously enhanced; in the steam condensation convection heat transfer, the turbulence of the fluid can be enhanced, the thickness of a condensed liquid film is reduced, and the heat transfer can be obviously enhanced.
TABLE 1 physical parameters of spherical wire mesh packing
The phi 25 spherical screen packing 1 represents a hollow spherical screen packing with the inner diameter of 25mm, and the phi 25 spherical screen packing 2 represents an inner filling screen packing with the inner diameter of 25 mm.
The inner tongue bow annular packing is as shown in figure 2, a rectangular metal sheet is punched to form tongue-shaped sheet bodies at intervals, the tongue-shaped sheet bodies are inwards concave, and then the rectangular metal sheet is rolled into a circle, so that the tongue-shaped annular packing with the structure that fins are additionally arranged in the tube is manufactured.
TABLE 2 inner tongue arch Ring Filler physical parameters
Detailed Description
In order to observe the effect of the novel filler on enhancing heat transfer more simply and visually, a double-pipe single-pipe heat exchanger is designed, as shown in the attached figure 3, and specific geometric parameters of the double-pipe single-pipe heat exchanger are shown in a table 3. The first heat exchanger is made of carbon steel, the diameter of an inner pipe is large, fillers with different diameters are placed, and the enhanced heat transfer condition of the stacked filling fillers is inspected. The second heat exchanger is made of stainless steel (S30210), the diameter of the inner tube is small, and the enhanced heat transfer condition of the serial filling filler is examined.
TABLE 3 geometric parameters of shell-type single-tube heat exchanger
The invention is further illustrated by the following non-limiting examples. The following embodiments reflect the rule of influence of laminar flow, excessive flow, turbulent flow, horizontal placement, vertical placement, single-phase convection heat transfer, steam condensation convection heat transfer, different pipe diameters and different flow rates on the heat exchange effect, and can provide technical guidance for the design and manufacture of efficient heat exchangers.
Example 1 constant hot water flow rate of 0.0493kg/s for outer sleeve
FIG. 4 and FIG. 5 show the average heat transfer rate Q of the hollow pipe, the coil insert, the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue ring packing, respectively, for a shell-type single-pipe heat exchanger with 27mm inner pipe diameter, with hot water inlet temperature of about 60 ℃, cold water inlet temperature of about 20 ℃, constant outer sleeve hot water flow of 0.0493kg/s, hollow pipe, coil insert, phi 25 spherical wire mesh packing 2 and phi 25 inner tongue ring packingaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. The Reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the double-tube single-tube heat exchanger, and the Reynolds number and the flow are in a direct proportion relation.
From the figure we conclude that:
(1) the average heat transfer rate and convective heat transfer coefficient generally rise as the cold water reynolds number rises. The more the cold water flow is increased, the more heat is taken away in unit time, so that the average heat transfer rate and the convection heat transfer coefficient can be increased;
(2) when the Reynolds number of cold water is lower than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 2 are obviously higher than those of an empty pipe; and when the cold water Reynolds number is higher than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 2 have small changes compared with those of an empty pipe. Therefore, the phi 25 spherical wire mesh packing 2 can obviously enhance heat transfer in the fluid laminar flow and transition flow states;
(3) when the Reynolds number of cold water is lower than 4000, the average heat transfer rate and the convection heat transfer coefficient of the coil insert are not greatly changed compared with those of the hollow pipe, and the average heat transfer rate and the convection heat transfer coefficient of the tongue bow annular packing in the phi 25 are reduced to some extent; and when the Reynolds number of cold water is higher than 4000, the average heat transfer rate and the convection heat transfer coefficient of the coil insert and the tongue bow annular packing in the phi 25 are higher than those of the hollow pipe. Therefore, the coil insert and the hyoid annular packing in phi 25 can obviously enhance heat transfer under the condition of fluid turbulence.
EXAMPLE 2 Effect of Single Filler in combination with Filler
FIG. 6 and FIG. 7 show the average heat transfer rate Q of the combination of phi 25 spherical wire mesh packing 1, phi 20 inner tongue arch ring packing and coil insert, and phi 25 spherical wire mesh packing 2 and phi 25 inner tongue arch ring packing respectively, wherein the pipe in the shell-type single-pipe heat exchanger with the inner pipe diameter of 27mm is filled with cold water and the outer sleeve is filled with hot water (horizontally arranged), the hot water inlet temperature is about 60 ℃, the cold water inlet temperature is about 20 ℃, the constant outer sleeve hot water flow rate is 0.0493kg/s, and the phi 25 spherical wire mesh packing 1, the phi 20 inner tongue arch ring packing, the phiaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. Wherein the Reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger.
From the figure we conclude that:
(1) under various flow states, the average heat transfer rate and the convection heat transfer coefficient of the phi 20 inner tongue arch annular packing, the phi 20 inner tongue arch annular packing and the coil insert combination are obviously higher than those of the phi 25 spherical wire mesh packing 1, the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing combination, so that the phi 20 inner tongue arch annular packing has a better enhanced heat transfer effect;
(2) under various flow states, compared with the combination of the phi 20 inner tongue arch annular packing and the coil insert, the phi 20 inner tongue arch annular packing has higher average heat transfer rate and convection heat transfer coefficient, and has better enhanced heat transfer effect;
(3) compared with the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 1, the combination of the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing has little change.
Example 3 the hot water flow rate of the outer sleeve is increased to 0.230kg/s
FIG. 8 and FIG. 9 show the average heat transfer rate Q of the hollow tube, the coil insert, the phi 25 spherical wire mesh packing 2 and the phi 25 inner lingual ring packing, respectively, for a shell-type single-tube heat exchanger with 27mm inner tube diameter, with hot water inlet temperature of about 60 deg.C, cold water inlet temperature of about 20 deg.C, constant outer sleeve hot water flow of 0.230kg/s, hollow tube, coil insert, phi 25 spherical wire mesh packing 2 and phi 25 inner lingual ring packingaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. Wherein the Reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger.
From the figure we conclude that:
(1) the average heat transfer rate and the convection heat transfer coefficient also rise along with the rising of the Reynolds number of the cold water;
(2) under the whole fluid flowing state, the average heat transfer rate fluctuates after the Reynolds number is larger than 2000, and the change of the average heat transfer rate of the heat exchanger containing the coil insert is relatively stable;
(3) after the thermal fluid flux is increased to five times, under various flow states, the phi 25 inner tongue arch annular packing, the phi 25 spherical silk screen packing 2 and the coil inner insert have better heat transfer effects compared with a hollow pipe, wherein the phi 25 inner tongue arch annular packing has the best enhanced heat transfer effect.
EXAMPLE 4 Effect of Single Filler in combination with Filler
FIG. 10 shows that the inner pipe of the sleeve-type single-pipe heat exchanger with the inner pipe diameter of 27mm is communicated with cold water and the outer sleeve is communicated with hot water (horizontally arranged), the temperature of a hot water inlet is about 60 ℃, and cold water enters the heat exchangerThe mouth temperature is about 20 ℃, the hot water flow of the outer sleeve is constant and is 0.0493kg/s, the coil insert, the phi 25 spherical silk screen packing 1, the phi 25 inner tongue arch annular packing, the phi 25 spherical silk screen packing 2, the phi 20 inner tongue arch annular packing and the coil insert are combined, the phi 25 spherical silk screen packing 2 and the phi 25 inner tongue arch annular packing are combined, and the convection heat transfer coefficient h of the hollow pipe isiAnd (4) proportion. Wherein the reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger, and we can draw the following conclusions from the figure:
(1) under various flowing states, the filler and the insert can obviously enhance heat transfer;
(2) under various flowing states, the enhanced heat transfer effect of the tongue bow annular packing in the phi 20 is the best, and the highest enhanced heat transfer effect can be more than twice;
(3) the enhanced heat transfer effect of the turbulence element is firstly increased and then decreased along with the Reynolds number of cold water, and when the Reynolds number of the cold water is about 4000, the enhanced heat transfer effect of the turbulence element is the best.
Example 5
In the attached figure 11, the relationship between the convection heat transfer coefficient hi and the reynolds number Re of a sleeve type single-tube heat exchanger with an inner tube of 67mm in diameter and an outer tube of hot water passing cold water (horizontally placed), the hot fluid flowing is in a laminar state, the hot water inlet temperature is about 60 ℃, the cold water inlet temperature is about 20 ℃, the hot water flow rate of the inner tube is 0.0570kg/s constantly, and a phi 25 inner tongue-bow annular filler, a phi 25 spherical wire mesh filler 2, a phi 40 spherical wire mesh filler, a phi 50 spherical wire mesh filler and a hollow tube are randomly filled in the inner tube of the heat exchanger. Wherein the reynolds number Re on the abscissa represents the flow of cold water passing through the outer sleeve of the shell-type single-tube heat exchanger, and the following conclusion is obtained from the figure:
(1) under the fluid laminar flow motion state, the convection heat transfer coefficient is reduced along with the rising of the Reynolds number of cold water;
(2) under the fluid laminar flow motion state, the irregular filling filler obviously has the enhanced heat transfer effect, and the enhanced effect is weakened along with the rising of the cold water Reynolds number;
(3) the reinforced heat transfer effect of the tongue bow annular packing in the phi 25 and the phi 40 spherical wire mesh packing is the best, and the convection heat transfer coefficient of the fillers is more than 2 times that of a hollow pipe.
Example 6
FIG. 12 and FIG. 13 show the average heat transfer rate Q of the cold water outer sleeve hot water (vertically placed) passing through the inner tube and the outer sleeve of the shell-type single-tube heat exchanger with the inner tube diameter of 27mm, the hot water inlet temperature of about 60 ℃, the cold water inlet temperature of about 20 ℃, the constant outer sleeve hot water flow of 0.0493kg/s, the hollow tube, the coil insert, the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue ring packingaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. Wherein the reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger, and we can draw the following conclusions from the figure:
(1) when the Reynolds number of cold water is lower than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing are obviously higher than those of a hollow pipe; and when the Reynolds number of cold water is higher than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing are lower than those of an empty pipe. Therefore, when the heat exchanger is vertically placed, the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing can obviously enhance heat transfer in a fluid laminar flow and transition flow state;
(2) the average heat transfer rate and convective heat transfer coefficient of the coil insert varied steadily under various flow conditions, but were lower than the empty tube. It can be seen that the coil insert does not enhance heat transfer when the heat exchanger is placed vertically.
Example 7
FIG. 13 and FIG. 14 show the average heat transfer rate Q of the combination of the phi 25 spherical wire mesh packing 1, the phi 20 inner tongue arch annular packing, the phi 25 inner tongue arch annular packing, the phi 20 inner tongue arch annular packing and the coil insert, and the phi 25 spherical wire mesh packing 2 and the phi 25 inner tongue arch annular packing, respectively, where the pipe in the shell-type single-tube heat exchanger with the inner pipe diameter of 27mm is filled with cold water and the outer sleeve is filled with hot water (placed vertically), the hot water inlet temperature is about 60 ℃, the cold water inlet temperature is about 20 ℃, the constant outer sleeve hot water flow rate is 0.0493kg/s, the phi 25 spherical wire mesh packing 1, the phi 20 inner tongueaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. Wherein the Reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the heat exchanger, we can conclude that:
(1) when the Reynolds number of cold water is less than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 1, the phi 20 internal tongue arch annular packing, the phi 25 internal tongue arch annular packing, the phi 20 internal tongue arch annular packing and coil insert combination and the phi 25 spherical wire mesh packing 2 and the phi 25 internal tongue arch annular packing combination rise along with the rising of the Reynolds number of the cold water; when the cold water Reynolds number is greater than 4000, the average heat transfer rate and the convection heat transfer coefficient of the phi 25 spherical wire mesh packing 1, the phi 20 internal tongue arch annular packing, the phi 25 internal tongue arch annular packing, the phi 20 internal tongue arch annular packing and coil insert combination and the phi 25 spherical wire mesh packing 2 and the phi 25 internal tongue arch annular packing combination slowly decrease along with the increase of the cold water Reynolds number;
(2) the heat transfer performance of the phi 25 inner tongue arch annular packing is the best and better than that of the phi 20 inner tongue arch annular packing, and the phi 25 spherical wire mesh packing 1 has the worst heat transfer performance. The heat transfer performance of the combination of the phi 20 internal tongue ring packing and the coil insert and the combination of the phi 25 spherical silk screen packing 2 and the phi 25 internal tongue ring packing is between the phi 20 internal tongue ring packing and the phi 25 spherical silk screen packing 1.
Example 8
FIG. 16 and FIG. 17 show the average heat transfer rate Q of the hollow tube, the coil insert, the phi 25 spherical wire mesh packing 2 and the phi 25 inner lingual ring packing, respectively, for a shell-type single-tube heat exchanger with 27mm inner tube diameter, with hot water inlet temperature of about 60 deg.C, cold water inlet temperature of about 20 deg.C, constant outer sleeve hot water flow of 0.230kg/s, hollow tube, phi 25 spherical wire mesh packing, and phi 25 inner lingual ring packingaveAnd convective heat transfer coefficient hiIn relation to the reynolds number Re. Wherein the reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger, and we can draw the following conclusions from the figure:
the average heat transfer rate and the convective heat transfer coefficient of the packing (insert) are lower than those of the empty tube in the entire fluid flow state, and therefore the coil insert, the Φ 25 spherical wire mesh packing 2, and the Φ 25 intra-lingual arch ring packing do not have the enhanced heat transfer effect.
Example 9
FIG. 18 shows the temperature of hot water inlet at about 60 deg.C and the temperature of cold water inlet at 2 deg.C in a shell-type single-tube heat exchanger with hot water (placed vertically) introduced from inner tube to cold water and outer sleeve to hot waterAbout 0 ℃, the hot water flow of the outer sleeve is 0.0493kg/s constantly, the coil is inserted, the phi 25 spherical wire mesh packing 2, the phi 25 inner tongue arch annular packing, the phi 25 spherical wire mesh packing 1, the phi 20 inner tongue arch annular packing is combined with the coil inserted, and the phi 25 spherical wire mesh packing 2 is combined with the phi 25 inner tongue arch annular packing and the convection heat transfer coefficient h of the hollow pipeiAnd (4) proportion. Wherein the reynolds number Re on the abscissa represents the flow of cold water in the inner tube of the shell-type single-tube heat exchanger, and we can draw the following conclusions from the figure:
(1) when the Reynolds number of cold water is less than 5000, the heat transfer can be obviously enhanced by other fillers (inserts) except the coil inserts; when the Reynolds number of cold water is more than 5000, the filler has no enhanced heat transfer effect;
(2) under the whole fluid flowing state, the enhanced heat transfer effect of the tongue bow annular packing in the phi 25 is the best, and the highest enhanced heat transfer effect can be more than twice;
(3) from the distribution of the whole scattering points, the filler enhanced heat transfer effect is reduced along with the rising of the Reynolds number of the cold water, and the filler enhanced heat transfer effect is best when the fluid is in laminar flow.
Example 10
In the accompanying drawings, two diagrams (a) and (b) show the relationship between the heat transfer quantity and the condensation quantity (Lm) of the coil insert, the phi 25 spherical silk screen packing 2, the phi 25 inner lingual ring packing and the hollow pipe and the steam quantity, wherein the inner pipe of the sleeve type single-pipe heat exchanger with the pipe diameter of 27mm is communicated with the steam outer sleeve and is communicated with cold water (vertically arranged), the steam inlet temperature is about 100 ℃, the cold water inlet temperature is about 20 ℃, the cold water flow rate of the outer sleeve is constant, and the relationship between the heat transfer quantity and the condensation quantity (Lm) of. From the figure we conclude that:
(1) when the steam amount is large, the filler does not enhance the condensation heat transfer effect of the steam;
(2) when the steam amount is less than 0.000278kg/s, the condensed water amount is more than 0.0278kg/s, the filler has the obvious effect of enhancing the steam condensation heat transfer, and the heat exchange effect of the tongue bow annular filler in the phi 25 is more than twice of that of a hollow pipe.
Example 11
FIG. 19 shows the relationship between the cold water inlet temperature of about 20 ℃, phi 25 spherical wire mesh packing 1, phi 25 spherical wire mesh packing 2, phi 20 inner tongue ring packing, phi 25 inner tongue ring packing, phi 20 inner tongue ring packing and coil insert combination, phi 25 inner tongue ring packing and phi 25 spherical wire mesh packing 2 combination, and the friction factor between the coil insert and the hollow pipe and the Reynolds number of the cooling water in the shell-type single-pipe heat exchanger with the inner pipe diameter of 27 mm. The cold water reynolds number is proportional to the cold water flow, from which we conclude that:
(1) as can be seen from the graph, the friction factor decreases up to a constant value as the reynolds number of the cold water increases;
(2) the friction factor of the inner tube containing the filler (the insert) is obviously larger than that of the empty tube, which shows that the fluid resistance is obviously increased by filling the turbulence element in the tube;
(3) the fluid resistance of the turbulence elements is formed by combining phi 20 internal tongue arch annular packing and a coil insert, phi 25 spherical silk screen packing 1, phi 25 spherical silk screen packing 2, phi 25 internal tongue arch annular packing, phi 20 internal tongue arch annular packing, phi 25 internal tongue arch annular packing and phi 25 spherical silk screen packing 2 and the coil insert in sequence from large to small.
Example 12
FIG. 21 shows a sleeve type single-tube heat exchanger with an inner tube diameter of 25mm, wherein the inner tube is filled with cold water, the outer sleeve is filled with hot water, the constant hot water flow is 0.0493kg/s, the cold water inlet temperature is about 20 ℃, the hot water inlet temperature is about 60 ℃, phi 25 spherical wire mesh packing 1, phi 25 spherical wire mesh packing 2, phi 20 inner tongue arch annular packing, phi 25 inner tongue arch annular packing, phi 20 inner tongue arch annular packing and coil insert combination, phi 25 inner tongue arch annular packing and phi 25 spherical wire mesh packing 2 combination, and the relationship between the evaluation criterion (PEC) of the enhanced heat transfer performance of the coil insert and the Reynolds number of the cooling water. The cold water reynolds number is proportional to the cold water flow, from which we conclude that:
(1) as can be seen from the figure, when the Reynolds number of cold water is larger, the PEC value is relatively higher, and the comprehensive performance of the heat transfer enhancement of the insert is better;
(2) only the coil inserts had PEC greater than 1 at cold water Reynolds numbers around 10000, which represented good heat transfer enhancement elements. In other cases, the PEC of the filler (the interposer) is less than 1;
(3) when the Reynolds number of cold water is less than 7000, the PEC value of the combination of the phi 20 internal tongue bow annular packing 1 and the phi 25 internal tongue bow annular packing and the phi 25 spherical screen packing 2 is larger than that of the coil insert, and the comprehensive enhanced heat transfer performance of the PEC is better than that of the coil insert.
Claims (2)
1. The utility model provides a shell and tube heat exchanger of built-in filler, constitutes including the casing and sets up the heat exchange tube in the casing, its characterized in that: the heat exchange tube is filled with inner tongue arch ring-shaped filler, or filled with porous hollow or filler-filled metal spherical wire mesh filler and inner tongue arch ring-shaped filler, and the outer diameter of the fillers is smaller than the inner diameter of the heat exchange tube;
the inner tongue arch annular filler is prepared by stamping a rectangular metal sheet to form tongue-shaped sheet bodies at intervals, inwards recessing the tongue-shaped sheet bodies and then rolling the rectangular metal sheet into a round shape;
and the number of the first and second electrodes,
the ratio of the inner diameter of the porous hollow metal spherical wire mesh filler to the inner diameter of the heat exchange tube is 0.50-0.95;
the ratio of the inner diameter of the inner tongue arch annular packing to the inner diameter of the heat exchange tube is 0.50-0.95.
2. A shell and tube heat exchanger according to claim 1, characterized in that: the inner tongue arch ring-shaped filler is directly placed or is connected in series by a metal wire;
or the porous hollow metal spherical wire mesh filler and the inner tongue arch ring-shaped filler are directly assembled in the same pipe body at the same time, or are placed by stringing metal wires together, and the ratio range of the number of the adjacent porous hollow metal spherical wire mesh filler and the inner tongue arch ring-shaped filler is 5: 1-1: 5.
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| CN201510671967.7A CN106595378B (en) | 2015-10-16 | 2015-10-16 | High-efficient heat exchanger of tubular |
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| CN201510671967.7A CN106595378B (en) | 2015-10-16 | 2015-10-16 | High-efficient heat exchanger of tubular |
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| CN111359351A (en) * | 2020-03-13 | 2020-07-03 | 重庆德沃木制品加工有限公司 | Manufacturing process of boiler dust collection device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1486735A1 (en) * | 1987-07-13 | 1989-06-15 | Sergej G Kochemasov | Heat exchange tube |
| CN101084409A (en) * | 2004-10-07 | 2007-12-05 | 布鲁克斯自动化有限公司 | Efficient heat exchanger for refrigeration process |
| CN201387255Y (en) * | 2009-04-06 | 2010-01-20 | 周麟 | Internal turbulent type heat exchanger |
| CN201463376U (en) * | 2009-02-24 | 2010-05-12 | 潘戈 | Solar heat collecting tube |
| CN104236377A (en) * | 2014-05-15 | 2014-12-24 | 重庆天瑞化工设备股份有限公司 | Automatic fluid blender |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2079729U (en) * | 1990-08-01 | 1991-06-26 | 朱永全 | Network ball type static mixer |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1486735A1 (en) * | 1987-07-13 | 1989-06-15 | Sergej G Kochemasov | Heat exchange tube |
| CN101084409A (en) * | 2004-10-07 | 2007-12-05 | 布鲁克斯自动化有限公司 | Efficient heat exchanger for refrigeration process |
| CN201463376U (en) * | 2009-02-24 | 2010-05-12 | 潘戈 | Solar heat collecting tube |
| CN201387255Y (en) * | 2009-04-06 | 2010-01-20 | 周麟 | Internal turbulent type heat exchanger |
| CN104236377A (en) * | 2014-05-15 | 2014-12-24 | 重庆天瑞化工设备股份有限公司 | Automatic fluid blender |
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