CN105571209A - Heat exchanger provided with area-varying communication holes - Google Patents
Heat exchanger provided with area-varying communication holes Download PDFInfo
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- CN105571209A CN105571209A CN201511008864.9A CN201511008864A CN105571209A CN 105571209 A CN105571209 A CN 105571209A CN 201511008864 A CN201511008864 A CN 201511008864A CN 105571209 A CN105571209 A CN 105571209A
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- 239000012530 fluid Substances 0.000 claims abstract description 70
- 239000011148 porous material Substances 0.000 claims description 103
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- 238000002474 experimental method Methods 0.000 description 16
- 238000010586 diagram Methods 0.000 description 5
- 238000009826 distribution Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000003292 diminished effect Effects 0.000 description 3
- 230000003467 diminishing effect Effects 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000004378 air conditioning Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 238000004904 shortening Methods 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B39/00—Evaporators; Condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/02—Tubular elements of cross-section which is non-circular
- F28F1/022—Tubular elements of cross-section which is non-circular with multiple channels
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B2339/00—Details of evaporators; Details of condensers
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention provides a heat exchanger. The heat exchanger comprises two headers and heat exchanging tubes which are arranged between the two headers; each heat exchanging tube is a flat heat exchanging tube; fins are arranged in each flat tube; each fin comprises an inclined part; the inclined parts are used for isolating fluid passages to form a plurality of small passages; each inclined part is provided with communication holes; the communication holes in different flat heat exchanging tubes are different in area; the farther the distance from each communication hole to an inlet tube is, the larger the area of the communication hole in the flat tube is. According to the heat exchanger provided by the invention, the area of each communication hole is set to vary along with the distance away from the inlet tube, so that a fluid can flow into the heat exchanging tube which is small in flow resistance and far away from the inlet tube; therefore, the fluid can be uniformly distributed in the heat exchanging tubes, the heat exchange efficiency is improved, and the service life is prolonged.
Description
Technical field
The present invention relates to heat exchanger, especially relate to a kind of shell-and-tube heat exchanger.
Background technology
Flat tube was widely used in automotive air conditioning units and house or commercial air-conditioner heat exchanger in recent years.This kind of flat tube inside arranges multiple little passage, and in use, heat exchanging fluid flows through the multiple passages in flat tube.Because flat tube heat exchange area is large, therefore, it is possible to greatly improve heat transfer effect.
In prior art, there is heat exchanger tube because of distance inlet tube near-far problem and cause assignment of traffic problem of non-uniform, such as, distance inlet tube is nearer, and heat exchanger tube inner fluid flow is more, and distance inlet tube is far away, and heat exchanger tube fluid flow is fewer.Prior art is all adopt in header, to be provided with assignment of traffic to lose or pressure distribution parts, makes assignment of traffic in heat exchanger tube even, but causes parts to increase, manufacture difficulty, cost increase by the mode of flow or pressure distribution.The invention provides a kind of new assignment of traffic measure, make assignment of traffic in whole Tube Sheet of Heat Exchanger even.
For the problems referred to above, the invention provides a kind of new shell-and-tube heat exchanger, thus the uneven problem of internal pressure when solving heat exchanger tube heat exchange.
Summary of the invention
The invention provides a kind of new flat tube heat exchanger, thus solve the technical problem occurred above.
To achieve these goals, technical scheme of the present invention is as follows:
A kind of heat exchanger, described heat exchanger comprises lower header and is arranged on the heat exchanger tube between lower header; Described heat exchanger tube is flat heat exchange tube, comprise flat tube and fin, described flat tube comprises sidewall and tube wall parallel to each other, described sidewall connects the end of parallel tube wall, form fluid passage between described sidewall and described parallel tube wall, described fin is arranged between tube wall, and described fin comprises the sloping portion favouring tube wall, described sloping portion is connected with tube wall, and described sloping portion is by the multiple passage aisle of spaced for fluid passage formation; Sloping portion arranges intercommunicating pore, thus adjacent passage aisle is communicated with each other; Described heat exchanger comprises inlet tube, and described inlet tube is arranged on upper header, and the area of the intercommunicating pore in different flat heat exchange tube is different, and along with the distance of distance inlet tube is far away, the area of the intercommunicating pore in described flat tube is larger.
As preferably, along with the distance of distance inlet tube is far away, it is more and more higher that the area of the intercommunicating pore in described flat heat exchange tube becomes large amplitude.
As preferably, the area of the intercommunicating pore in the flat heat exchange tube of distance inlet tube farthest be the 1.4-1.6 of the area of the intercommunicating pore in distance inlet tube flat heat exchange tube the most nearby doubly.
As preferably, the area of the intercommunicating pore in the flat heat exchange tube of distance inlet tube farthest is 1.5 times of the area of the intercommunicating pore in distance inlet tube flat heat exchange tube the most nearby.
As preferably, the quantity of the intercommunicating pore in every root flat heat exchange tube is identical.
As preferably, the shape of described intercommunicating pore is the first isosceles triangle; Adjacent sloping portion connects on tube wall, forms triangle between adjacent sloping portion and tube wall, and forming triangle between adjacent sloping portion and tube wall is the second isosceles triangle, and adjacent sloping portion is the waist of the second isosceles triangle; The drift angle of the first isosceles triangle is B, and the drift angle of the second isosceles triangle is A, then meet following formula:
Sin(B)=a+b*sin(A/2)-c*sin(A/2)
2；
Wherein a, b, c are parameters, wherein 0.58<a<0.59,1.65<b<1.75,1.78<c<1.85;
50°<A<150°；30°<B<80°。
As preferably, a=0.5849, b=1.6953, c=1.8244;
80°<A<120°；50°<B<60°。
As preferably, the length on the first isosceles triangle base is h, meets following formula:
0.25<d*(h/H) <0.38; Wherein d is parameter, 0.5<d<1.8;
H be with the relative face of adjacent tube wall between distance.
H be with the relative face of adjacent tube wall between distance.
As preferably, 0.8<d<1.2.
As preferably, along with drift angle is the increase of A, described d diminishes.
As preferably, along with the increase of H, described d diminishes.
Compared with prior art, flat heat exchange tube of the present invention has following advantage:
1) the present invention is by arranging the change of intercommunicating pore area along with distance inlet tube, makes fluid to the distance inlet tube that flow resistance is little heat exchange Bottomhole pressure far away, thus makes fluid distributed uniform in heat exchanger tube.
2) the present invention by arranging intercommunicating pore on the fin of flat tube, ensures the connection between adjacent passage aisle, the problem that internal pressure when solving flat tube heat exchange is uneven, improves heat exchange efficiency, improve service life.
3) the present invention is by reasonably determining the change of the size of intercommunicating pore along flowing, namely ensures rational pressure in heat exchanger tube, ensures again to reach abundant heat exchange.
4) the present invention is by a large amount of experiments, determines the physical dimension of best flat heat exchange tube, thus when making to ensure heat exchange resistance, makes heat transfer effect reach best.
Accompanying drawing explanation
Fig. 1 is the structural representation of heat exchanger of the present invention;
Fig. 2 is flat tube cross-sectional structure schematic diagram of the present invention;
Fig. 3 is the structural representation of the flat tube cross section of outer setting fin of the present invention;
Fig. 4 is the cross section structural representation that the present invention's flat tube inner fin arranges intercommunicating pore position;
Fig. 5 is the modified node method schematic diagram of the outer fin flat tube cross section of outer setting of the present invention;
Fig. 6 is the schematic diagram that the present invention arranges intercommunicating pore structure sloping portion plane;
Fig. 7 is another schematic diagram that the present invention arranges intercommunicating pore structure sloping portion plane;
Fig. 8 is triangle intercommunicating pore structure schematic diagram of the present invention.
Reference numeral is as follows:
1 flat tube, 2 fluid passages, 3 tube walls, 4 sloping portions, 5 summits, 6 intercommunicating pores, 7 fins, 8 upper collecting chambers, 9 lower headers, 10 passage aisles, 11 outside fin, 12 sidewalls, 13 inlet tubes, 14 outlets.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.
Herein, if do not have specified otherwise, relate to formula, "/" represents division, "×", " * " represent multiplication.
A kind of heat exchanger, as shown in Figure 1, described heat exchanger comprises upper collecting chamber 8 and lower header 9 and is arranged on lower header 8, the heat exchanger tube between 9.Fin 11 is set between described heat exchanger tube.Described heat exchanger can be widely use such as automotive heat exchanger, air-condition heat exchanger etc.
As shown in Figure 2, described heat exchanger tube is flat heat exchange tube, comprise flat tube 1 and fin 7, described flat tube 1 comprises tube wall 3 parallel to each other and sidewall 12, described sidewall 12 connects the end of parallel tube wall 2, fluid passage 2 is formed between described sidewall 12 and described parallel tube wall 3, described fin 7 is arranged between tube wall 3, described fin 7 comprises the sloping portion 4 favouring tube wall, described sloping portion 4 connects with parallel tube wall 3, described sloping portion 4 is by multiple for spaced for fluid passage 2 formation passage aisle 10, adjacent sloping portion 4 connects on tube wall, triangle is formed between described adjacent sloping portion 4 and tube wall 3, sloping portion 4 arranges intercommunicating pore 6, thus adjacent passage aisle 10 is communicated with each other.
As preferably, described sidewall 2 is arc-shaped.
By arranging intercommunicating pore 6, ensure the connection between adjacent passage aisle 10, thus the fluid in the passage aisle making pressure large can flow in the passage aisle little to contiguous pressure, solve the problem that internal pressure is uneven and local pressure is excessive when flat tube heat exchange, thus facilitate the abundant flowing of fluid in heat exchanger channels, improve heat exchange efficiency, also improve the service life of heat exchanger tube simultaneously.
As preferably, same sloping portion 4 arranges multiple intercommunicating pore 6, and along the flow direction of fluid, the area of described intercommunicating pore 6 is increasing.
Found through experiments, large by the change gradually of area, compared with identical with area, flow resistance can be reduced further, the flow resistance of about about 10% can be reduced, but heat exchange efficiency obviously not reduce.
As preferably, along the flow direction of fluid, it is increasing that the area of intercommunicating pore 6 becomes large amplitude.Found through experiments, the amplitude that the change of the area of intercommunicating pore 6 is large is increasing, when can ensure heat exchange efficiency, reduces flow resistance further, approximately can reduce the flow resistance of about 5%.
As preferably, along the centre centre position of tube wall 3 (namely in Fig. 2 cross sectional representation) of the tube wall 3 of flat tube cross section, to both sides sidewall 12 direction, described intercommunicating pore 6 area on different sloping portion 4 constantly diminishes.Wherein, be positioned at the centre position of flat tube 1, i.e. the centre position of tube wall 3 in Fig. 2 cross sectional representation, the area of intercommunicating pore 6 is maximum.Main cause found through experiments, because fluid maldistribution, intermediate pressure is maximum, reduces gradually from centre to pressure at both sides.Therefore the distribution of intercommunicating pore area, the fluid at middle part is flowed to both sides as far as possible, reduce the flow resistance at middle part, cause the minimizing of heat exchange area in order to avoid perforated area is excessive simultaneously, perforated area is changed according to pressure, while reduction resistance, improve heat exchange efficiency further.
The most preferred, along the centre of flat tube cross section to sidewall 12 direction, the amplitude that described intercommunicating pore 6 area on different sloping portion 4 constantly diminishes is increasing.By setting like this, be also the Changing Pattern meeting flowing pressure, while reducing flow resistance further, improve heat exchange efficiency.
As preferably, the shape of described intercommunicating pore 6 is isosceles triangle, and the mid point on the base of described isosceles triangle is identical with the flow direction of fluid to the direction of drift angle.That is, the drift angle direction of isosceles triangle is fluid flow direction.Found through experiments, drift angle direction is set to be consistent with flow direction, can heat exchange efficiency be improved, reduce flow resistance simultaneously.By setting like this, the heat exchange efficiency of about 10% can be improved, reduce the resistance of about 9% simultaneously.
As preferably, forming triangle between described adjacent sloping portion and tube wall is isosceles triangle, is called for short the second isosceles triangle later.By being set to isosceles triangle, fluid flowing can being ensured evenly, improving heat transfer effect.
As preferably, described sloping portion summit 5 is plane, and the fixed point 5 of described two adjacent sloping portions 4 is connected, and described summit 5 is connected with tube wall 3.Because arrange fixed point 5 for plane, therefore make sloping portion 4 large with tube wall contact area, thus tube wall and sloping portion are more fully better contacted.Installation is more prone to, avoids sliding.
As preferably, form in triangle between adjacent sloping portion 4 and tube wall, the inner surface that sloping portion 4 is relative forms vertex of a triangle, and described vertex of a triangle is positioned on tube wall.
In Fig. 6, the flow direction of fluid is from left to right.But left and right herein just illustrates the flow direction of fluid along intercommunicating pore, do not represent actual certain left and right flowing.
As preferably, described isosceles triangle base mid point is L to the length of drift angle.
As shown in Figure 9, the drift angle of described isosceles triangle is B, and as shown in Figure 6, along the flow direction of fluid, same sloping portion 4 arranges multiple triangle intercommunicating pore 6.As preferably, along the flow direction of fluid, same sloping portion 4 arranges multiple intercommunicating pore 6, and along the flow direction of fluid, when base length remains unchanged, described intercommunicating pore drift angle B is more and more less.Found through experiments, by diminishing gradually of intercommunicating pore drift angle B, compared with identical with drift angle B, when can ensure heat exchange efficiency, reduce flow resistance further, approximately can reduce the flow resistance of about 7%.
As preferably, along the flow direction of fluid, the amplitude that drift angle B diminishes is increasing.Found through experiments, the amplitude that drift angle B diminishes is increasing, when can ensure heat exchange efficiency, reduces flow resistance further, approximately can reduce the flow resistance of about 4%.
As preferably, along the flow direction of fluid, same sloping portion arranges many row's intercommunicating pores 6, and as shown in Figures 6 and 7, often the distance of arranging between intercommunicating pore is S2, and described S2 is for calculating distance with the base of the intercommunicating pore of adjacent row.
As preferably, as shown in Figure 7, many row's intercommunicating pores 6 are shifted structure.
Find in an experiment, the area of intercommunicating pore can not be excessive, excessive words can cause the loss of heat exchange area, reduce heat exchange efficiency, too small, cause local pressure to distribute still uneven, in like manner, the distance of adjacent tube wall 3 can not be excessive, and cross the reduction that conference causes heat exchange efficiency, too small meeting causes flow resistance excessive.Experimentally find, the drift angle of the first isosceles triangle and the drift angle of the second isosceles triangle are the change of certain rule, such as the second isosceles triangle drift angle becomes large, thus cause the passage aisle area of heat exchanger channels to increase, corresponding flow resistance diminishes, and therefore now the circulation area of the second isosceles triangle will diminish, and can reduce the area of intercommunicating pore 6 like this, when ensureing flow resistance, improve heat exchange efficiency simultaneously.Therefore there is following relation between the first isosceles triangle and the second isosceles triangle drift angle:
The drift angle of the first isosceles triangle is B, and the drift angle of the second isosceles triangle is A, then meet following formula:
Sin(B)=a+b*sin(A/2)-c*sin(A/2)
2；
Wherein a, b, c are parameters, wherein 0.58<a<0.59,1.65<b<1.75,1.78<c<1.85;
50°<A<150°；30°<B<80°。
As preferably, a=0.5849, b=1.6953, c=1.8244;
80°<A<120°；50°<B<60°；
By above-mentioned formula, the best relation between the first isosceles triangle and the second isosceles triangle drift angle can being determined, can ensureing when meeting flow resistance under this relation, reach best heat exchange efficiency.
As preferably, H=7-15mm.Be further used as preferably, 9<H<12mm.
As preferably, the length on the first isosceles triangle base is h, meets following formula:
0.25<d*(h/H) <0.38; Wherein d is parameter, 0.5<d<1.8;
H be with the relative face of adjacent tube wall between distance.
As preferably, 0.8<d<1.2.
As preferably, along with drift angle is the increase of A, described d diminishes.
As preferably, along with the increase of H, described d diminishes.
The width of tube wall is W, is preferably 7.4<W/H<4.6, further preferably, and 6.8<W/H<5.6.
One by above-mentioned optimal design, can improve the heat exchange property of heat exchanger tube further, reduce flow resistance simultaneously.
The present invention is thousands of numerical simulations by the heat exchanger tube of multiple different size and test data, meeting in industrial requirements pressure-bearing situation (below 10MPa), when realizing maximum heat exchange amount, the dimensionally-optimised relation of the flat tube tube wall of the best summed up.
For intercommunicating pore size along fluid flow direction or along the centre from heat exchanger tube cross section tube wall in the changing situation of sidewall 2, be also still applicable to above-mentioned formula, or other intercommunicating pore sizes can be selected to meet by regulation coefficient.
As preferably, the base of the adjacent isosceles triangle intercommunicating pore of described same row all on one wire, the intercommunicating pore distance that same row is adjacent is S1, described 2.9 × h<S1<3.3 × h, wherein S1 is with the distance of the mid point on the base of adjacent two isosceles triangle intercommunicating pores.Be preferably 3.2 × h=S1.
As preferably, the base of the isosceles triangle of the intercommunicating pore of adjacent row is parallel to each other, and the summit of isosceles triangle is L to the distance of base mid point, and the distance S2 of adjacent row is 3.8*L<S2<4.8*L.Be preferably S2=4.4*L
When the base of the isosceles triangle of adjacent row is different, take the weighted average on two bases to calculate.
As preferably, the angle of the isosceles triangle of same row is identical with base.Namely shape is identical, is equal shape.
For formula above, for the intercommunicating pore that front and rear row size is different, be also still suitable for.
As preferably, the wall thickness of fin is 0.6-1.1mm; As preferably, 0.8-1.0mm.
For the concrete dimensional parameters do not mentioned, design according to normal heat exchanger.
As preferably, as shown in Figure 2, at the outer setting fin 11 of the tube wall 3 of flat tube 1.
As preferably, described fin is straight tabular, the bearing of trend of fin along the flow direction of fluid, namely as shown in Figure 2, along the direction perpendicular to paper.
As preferably, along the flow direction of fluid, outside fin 11 highly constantly increases, and the amplitude highly increased is increasing.By increasing fin height, thus increase the heat exchange area of fin.Experiment finds, by setting like this, compared with identical with fin height, can improve the heat exchange efficiency of about 5%.
As preferably, as shown in Figure 5, along the centre of flat tube 1 cross section to both sides, the height of described fin 11 constantly reduces.Wherein, be positioned at the centre position of flat tube 1, the height of fin is the highest.
Because found by test, flat tube is maximum in middle part heat radiation, from middle part to both sides, heat radiation diminishes gradually, therefore by arranging the outside fin height change of flat tube, make the area of dissipation of flat tube maximum at middle part like this, minimum in both sides, make middle part heat-sinking capability maximum, meet the heat dissipation law of flat tube heat like this, make flat tube heat radiation on the whole evenly, avoid flat tube local temperature overheated, cause radiating effect excessively poor, cause the shortening in flat tube life-span.
Preferably, described heat exchanging fluid is water.
As preferably, described heat exchanger comprises inlet tube 13 and outlet 14, and described inlet tube 13 is arranged on upper header 8, and outlet 14 is arranged in lower collector pipe 9.As preferably, described inlet tube 13 and outlet 14 are arranged on the same side of heat exchanger, such as, are all arranged on as shown in Figure 1 on the left of heat exchanger.
As preferably, inlet tube 13 is arranged on the upper position of the side of upper header 8, and outlet 14 is arranged on the lower position of lower collector pipe 9 side.
As preferably, the area of the intercommunicating pore 6 in different flat tubes is different, and along with the distance of distance inlet tube 13 is far away, the area of the intercommunicating pore 6 in described flat tube is larger.By setting like this, make distance inlet tube 13 nearer, then because the area of intercommunicating pore 6 is less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance apart from inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, such as, pipe a in Fig. 1, more and more far, it is more and more higher that the area of the intercommunicating pore 6 in described flat tube becomes large amplitude to b, c, d, e, f distance inlet tube 13.Found through experiments, become the increase of large amplitude by area, fluid can be made to distribute more even.The i.e. area of the area < pipe d intercommunicating pore 6 of the area < pipe c intercommunicating pore 6 of the area < pipe b intercommunicating pore 6 of pipe a intercommunicating pore 6 ..., the rest may be inferred.
The area of the intercommunicating pore 6 in the heat exchanger tube of distance inlet tube 13 farthest is 1.4-1.6 times of the area of the intercommunicating pore 6 in distance inlet tube 13 heat exchanger tube the most nearby, is preferably 1.5 times.
As preferably, the quantity of the intercommunicating pore 6 in every root heat exchanger tube is identical.
As preferably, the quantity of the intercommunicating pore 6 on each sloping portion is identical.The area employing of the intercommunicating pore 6 of a flat tube changes all intercommunicating pore gross areas on flat tube and calculates.
As preferably, the distributed quantity of the intercommunicating pore 6 in different flat tubes is different, and along with the distance of distance inlet tube 13 is far away, the distributed quantity of the intercommunicating pore 6 in described flat tube is more and more.By setting like this, make distance inlet tube 13 nearer, then because the distributed quantity of intercommunicating pore 6 is few, circulation area between passage aisle is less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, the amplitude that the distribution number quantitative change of the intercommunicating pore 6 in described flat tube is many is more and more higher.Found through experiments, become the increase of large amplitude by area, fluid can be made to distribute more even.
The area of the intercommunicating pore 6 in the heat exchanger tube of distance inlet tube 13 farthest is 1.4-1.6 times of the distributed quantity of the intercommunicating pore 6 in distance inlet tube 13 heat exchanger tube the most nearby, is preferably 1.5 times.
Preferably, the area of each intercommunicating pore 6 is identical.
As preferably, varying in size of the included angle A in different flat tubes.Along with the distance of distance inlet tube 13 is far away, the included angle A that the sloping portion 4 in described flat tube is formed is increasing.By setting like this, make distance inlet tube 13 nearer, diminishing then because of included angle A, cause the circulation area of passage aisle less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, it is more and more higher that the included angle A of sloping portion 4 formation in described flat tube becomes large amplitude.Found through experiments, become the increase of large amplitude by A, fluid can be made to distribute more even.
Preferably, the included angle A of the intercommunicating pore 6 of same flat tube adopts average angle to calculate, and is namely calculated by the weighted average of multiple angle.
Preferably, the included angle A of all intercommunicating pores 6 of same flat tube is equal.
As preferably, the base length h of the isosceles triangle intercommunicating pore 6 of all heat exchanger tubes is equal, and the drift angle B in different flat tubes varies in size.Along with the distance of distance inlet tube 13 is far away, in described flat tube, the drift angle B of isosceles triangle intercommunicating pore is more and more less.By setting like this, make distance inlet tube 13 nearer, then because the change of drift angle B is large, cause the circulation area of intercommunicating pore 6 less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, the amplitude that in described flat tube, the drift angle B of isosceles triangle intercommunicating pore is more and more less is more and more higher.Found through experiments, the increase of the amplitude diminished by drift angle B, fluid can be made to distribute more even.
Preferably, the drift angle B of the intercommunicating pore 6 of same flat tube adopts average drift angle to calculate, and is namely calculated by the weighted average of multiple drift angle.
Preferably, the drift angle B of all intercommunicating pores 6 in same flat tube is equal.
As preferably, the L of the isosceles triangle intercommunicating pore 6 of all heat exchanger tubes is equal, base length h in different flat tubes varies in size, and along with the distance of distance inlet tube 13 is far away, in described flat tube, the base length h of isosceles triangle intercommunicating pore is increasing.By setting like this, make distance inlet tube 13 nearer, diminishing then because of base length h, cause the circulation area of intercommunicating pore 6 less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, the amplitude that in described flat tube, the base length h of isosceles triangle intercommunicating pore is increasing is more and more higher.Found through experiments, become the increase of large amplitude by base length h, fluid can be made to distribute more even.
Preferably, the base length h of the intercommunicating pore 6 of same flat tube adopts average drift angle to calculate, and is namely calculated by the weighted average of multiple base length h.
Preferably, the base length h of all intercommunicating pores 6 of same flat tube is equal.
As preferably, arrange intercommunicating pore 6 same sloping portion is arranged, as shown in Figures 3 and 4, often the distance of arranging between intercommunicating pore is S2, and the S2 in different flat tubes varies in size more, and along with the distance of distance inlet tube 13 is far away, described S2 is more and more less.By setting like this, make distance inlet tube 13 nearer, then because S2 is larger, cause the circulation area of intercommunicating pore 6 less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, the amplitude that S2 is more and more less is more and more higher.Found through experiments, the increase of the amplitude diminished by S2, fluid can be made to distribute more even.
Preferably, the S2 of the intercommunicating pore 6 of same flat tube adopts average drift angle to calculate, and is namely calculated by the weighted average of multiple S2.
Preferably, the S2 of all intercommunicating pores 6 of same flat tube is equal.
As preferably, all on one wire, the intercommunicating pore distance that same row is adjacent is S1, and the S1 in different flat tubes varies in size on the base of the adjacent isosceles triangle intercommunicating pore of described same row, along with the distance of distance inlet tube 13 is far away, described S1 is more and more less.By setting like this, make distance inlet tube 13 nearer, then because S1 is larger, cause the circulation area of intercommunicating pore 6 less, the resistance then causing fluid to flow becomes large, thus make fluid to the little heat exchange Bottomhole pressure of flow resistance, make fluid get over the heat exchange Bottomhole pressure of distant positions towards the distance of distance inlet tube 13, thus make fluid distributed uniform.
As preferably, along with the distance of distance inlet tube 13 is far away, the amplitude that S1 is more and more less is more and more higher.Found through experiments, the increase of the amplitude diminished by S1, fluid can be made to distribute more even.
Preferably, the S1 of the intercommunicating pore 6 of same flat tube adopts average drift angle to calculate, and is namely calculated by the weighted average of multiple S1.
Preferably, the S1 of all intercommunicating pores 6 of same flat tube is equal.
Although the present invention discloses as above with preferred embodiment, the present invention is not defined in this.Any those skilled in the art, without departing from the spirit and scope of the present invention, all can make various changes or modifications, and therefore protection scope of the present invention should be as the criterion with claim limited range.
Claims (7)
1. a heat exchanger, described heat exchanger comprises lower header and is arranged on the heat exchanger tube between lower header; Described heat exchanger tube is flat heat exchange tube, comprise flat tube and fin, described flat tube comprises sidewall and tube wall parallel to each other, described sidewall connects the end of parallel tube wall, form fluid passage between described sidewall and described parallel tube wall, described fin is arranged between tube wall, and described fin comprises the sloping portion favouring tube wall, described sloping portion is connected with tube wall, and described sloping portion is by the multiple passage aisle of spaced for fluid passage formation; Sloping portion arranges intercommunicating pore, thus adjacent passage aisle is communicated with each other; Described heat exchanger comprises inlet tube, and described inlet tube is arranged on upper header, it is characterized in that: the area of the intercommunicating pore in different flat heat exchange tube is different, and along with the distance of distance inlet tube is far away, the area of the intercommunicating pore in described flat tube is larger.
2. heat exchanger as claimed in claim 1, is characterized in that, along with the distance of distance inlet tube is far away, it is more and more higher that the area of the intercommunicating pore in described flat heat exchange tube becomes large amplitude.
3. heat exchanger as claimed in claim 1 or 2, is characterized in that, the area of the intercommunicating pore in the flat heat exchange tube of distance inlet tube farthest is 1.4-1.6 times of the area of the intercommunicating pore in distance inlet tube flat heat exchange tube the most nearby.
4. heat exchanger as claimed in claim 3, is characterized in that, the area of the intercommunicating pore in the flat heat exchange tube of distance inlet tube farthest is 1.5 times of the area of the intercommunicating pore in distance inlet tube flat heat exchange tube the most nearby.
5. heat exchanger as claimed in claim 1, it is characterized in that, the quantity of the intercommunicating pore on each sloping portion is identical.
6. heat exchanger as claimed in claim 1, the shape of described intercommunicating pore is the first isosceles triangle; Adjacent sloping portion connects on tube wall, forms triangle between adjacent sloping portion and tube wall, and forming triangle between adjacent sloping portion and tube wall is the second isosceles triangle, and adjacent sloping portion is the waist of the second isosceles triangle; The drift angle of the first isosceles triangle is B, and the drift angle of the second isosceles triangle is A, then meet following formula:
Sin(B)=a+b*sin(A/2)-c*sin(A/2)
2；
Wherein a, b, c are parameters, wherein 0.58<a<0.59,1.65<b<1.75,1.78<c<1.85;
50°<A<150°；30°<B<80°。
7. heat exchanger as claimed in claim 6, is characterized in that, a=0.5849, b=1.6953, c=1.8244;
80°<A<120°；50°<B<60°。
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| CN201511008864.9A CN105571209B (en) | 2015-12-30 | 2015-12-30 | A kind of heat exchanger of intercommunicating pore area change |
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| CN201511008864.9A CN105571209B (en) | 2015-12-30 | 2015-12-30 | A kind of heat exchanger of intercommunicating pore area change |
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| CN105571209A true CN105571209A (en) | 2016-05-11 |
| CN105571209B CN105571209B (en) | 2017-03-08 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109855452A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of shell-and-tube heat exchanger containing on-condensible gas |
| CN109855451A (en) * | 2018-07-20 | 2019-06-07 | 国网山东省电力公司聊城供电公司 | A kind of vapor heat exchanger evenly distributing flow |
| CN109855449A (en) * | 2018-07-20 | 2019-06-07 | 国网山东省电力公司聊城供电公司 | A kind of shell-and-tube heat exchanger generating steam |
| CN109855450A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of design method of on-condensible gas pipe for shell-and-tube exchanger spacing |
| CN109855453A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of vehicle repair major flow tube shell type heat exchanger |
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| CN201028900Y (en) * | 2007-04-24 | 2008-02-27 | 张奡 | Novel flat flowing condenser |
| CN203443450U (en) * | 2013-07-10 | 2014-02-19 | 北京凯德菲冷却器制造有限公司 | Tube bundle of flat tubes with inner fins and outer fins |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20050034848A1 (en) * | 2003-06-20 | 2005-02-17 | Naoki Ueda | Manufacturing method of heat exchanger and structure thereof |
| CN201028900Y (en) * | 2007-04-24 | 2008-02-27 | 张奡 | Novel flat flowing condenser |
| CN203443450U (en) * | 2013-07-10 | 2014-02-19 | 北京凯德菲冷却器制造有限公司 | Tube bundle of flat tubes with inner fins and outer fins |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109855452A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of shell-and-tube heat exchanger containing on-condensible gas |
| CN109855451A (en) * | 2018-07-20 | 2019-06-07 | 国网山东省电力公司聊城供电公司 | A kind of vapor heat exchanger evenly distributing flow |
| CN109855449A (en) * | 2018-07-20 | 2019-06-07 | 国网山东省电力公司聊城供电公司 | A kind of shell-and-tube heat exchanger generating steam |
| CN109855450A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of design method of on-condensible gas pipe for shell-and-tube exchanger spacing |
| CN109855453A (en) * | 2018-07-20 | 2019-06-07 | 国网山东综合能源服务有限公司 | A kind of vehicle repair major flow tube shell type heat exchanger |
| CN109855452B (en) * | 2018-07-20 | 2020-03-17 | 国网山东综合能源服务有限公司 | Shell-and-tube heat exchanger containing non-condensable gas |
| CN109855450B (en) * | 2018-07-20 | 2020-08-18 | 国网山东综合能源服务有限公司 | Design method for tube spacing of non-condensable gas shell-and-tube heat exchanger |
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| CN105571209B (en) | 2017-03-08 |
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Inventor after: Zhao Wei Inventor after: Wang Changyu Inventor after: Fan Lianlei Inventor after: Xue Lu Inventor after: Ma Wenhui Inventor after: Lv Jiping Inventor after: Guo Cuiyun Inventor after: Liu Yunsheng Inventor before: Zhao Wei Inventor before: Chen Yan Inventor before: Wang Qi |
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