CN105157459B - It is a kind of that the right angle plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture - Google Patents
It is a kind of that the right angle plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture Download PDFInfo
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- CN105157459B CN105157459B CN201510657872.XA CN201510657872A CN105157459B CN 105157459 B CN105157459 B CN 105157459B CN 201510657872 A CN201510657872 A CN 201510657872A CN 105157459 B CN105157459 B CN 105157459B
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- 239000000203 mixture Substances 0.000 title claims abstract description 38
- 239000012530 fluid Substances 0.000 claims abstract description 19
- 238000009833 condensation Methods 0.000 claims abstract description 15
- 230000005494 condensation Effects 0.000 claims abstract description 15
- 230000000694 effects Effects 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 238000009835 boiling Methods 0.000 abstract description 10
- 238000002156 mixing Methods 0.000 abstract description 8
- 238000002474 experimental method Methods 0.000 description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 238000004080 punching Methods 0.000 description 9
- 230000008859 change Effects 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 7
- 239000007788 liquid Substances 0.000 description 7
- 238000012546 transfer Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 5
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- 239000003345 natural gas Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004804 winding Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 208000012868 Overgrowth Diseases 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
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- 239000000463 material Substances 0.000 description 1
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- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
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- 238000011160 research Methods 0.000 description 1
- 230000008261 resistance mechanism Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention provides a kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, the plate-fin heat exchanger includes plate parallel to each other, between the plate, fin is set, the fin includes the vertical component perpendicular to plate, bur is processed by impact style on vertical component, so that the hole connection that the fluid of vertical component both sides is formed by impact style on vertical component；The bur stretches out from vertical component along mixture flow direction.The invention provides it is a kind of new suitable for the plate-fin heat exchanger used in the condensation of non-azeotrope multicomponent mixture, so as to solve the condensation of the different multicomponent blending agent of boiling point, to improve heat exchange efficiency, reduce fluid flow resistance.
Description
Technical field
The invention belongs to field of heat exchangers, more particularly to the heat exchanger that a kind of condensation of different boiling blending agent is used, category
In the field of heat exchangers of F28D.
Background technology
The condensation of different boiling blending agent is that (main component is -162 DEG C of methane of boiling point, -88 DEG C of boiling point for natural gas liquefaction
Ethane, -42 DEG C of propane of boiling point etc.), air separate, azeotrope refrigeration, oil or cracking waste plastics, the row such as biogas production
The main processes of industry.To reduce technical processLoss, such production technology are wished to be cooled down according to temperature level step by step
The component of different boiling is separated out, heat exchange itself is also carried out in different temperatures interval with one cold-producing medium or product, therefore will
Condensing plant is asked conveniently to realize multiply medium while heat exchange.Multiply medium can conveniently be realized at present while the equipment of heat exchange is mainly
Two kinds of spiral winding heat exchange of heat pipe and plate-fin heat exchanger.Spiral winding heat exchange of heat pipe is shell structure, and pressure-bearing is higher, application compared with
Extensively, but it is difficult to take enhanced heat transfer measure, the coefficient of heat transfer is relatively low, and volume and weight is difficult to reduce.Plate-fin heat exchanger with
In recent years the improvement of manufacturing process, bearing capacity are gradually stepped up.With the advantage that its heat transfer coefficient is higher, more compact, weight is lighter,
There is the trend for replacing winding heat exchange of heat pipe in many occasions such as natural gas liquefaction.
Although plate-fin heat exchanger is in boiling, and similarly hereinafter sample can provide the higher coefficient of heat transfer with the variable working condition of condensation phase, existing
The fin configuration for having plate-fin heat exchanger is primarily directed to the mechanismic design that single-phase medium (it is important that gas phase media) exchanges heat：It is flat
Straight fins are to extend heat exchange area and reduce hydraulic diameter；Corrugated fin, saw tooth fin, louvered fin are in expanding surface
The thinning boundary layer of fluid is disturbed on the basis of product；Be recognized the fin with apertures of phase-change heat-exchange, piece band fin are applicable to for cold
The continuity of liquid film can be destroyed during solidifying heat exchange, but is also proved that effect has excellent unlike plain fin in high reynolds number operating mode
Gesture.
In natural gas liquefaction, the thermal resistance mechanism of non-azeotrope multicomponent blending agent condensation is had substantially with pure component material condensation
Difference, theory analysis and experiment are proved the coefficient of heat transfer substantially to be reduced than pure component condensation.It is existing cold to non-azeotrope blending agent
The research of solidifying heat exchange is focusing more on containing a kind of operating mode of on-condensible gas, is subtracted using measures such as low groove, Artificial roughness surfaces
Little average thickness of liquid film is proved the measure that effect is projected when pure component is condensed, containing effect in the case of on-condensible gas sometimes not
Substantially., and natural gas liquefaction, the condensing heat-exchange process of petroleum cracking industry and mechanism are increasingly complex, condensation process is generally comprised
Two or more on-condensible gases, heat exchange situation are more complicated.
For the problems referred to above, the invention provides a kind of new plate-fin heat exchanger, so as to solve different multigroup of boiling point
Divide the condensation of blending agent.
The content of the invention
The invention provides a kind of new plate-fin heat exchanger, so as to solve the cold of the different multicomponent blending agent of boiling point
It is solidifying, to improve heat exchange efficiency, reduce fluid flow resistance.
To achieve these goals, technical scheme is as follows：
A kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, the plate-fin heat exchanger include mutually
Parallel plate, arranges fin between the plate, the fin includes the vertical component perpendicular to plate, it is characterised in that
Bur is processed by impact style on vertical component, so that the fluid of vertical component both sides is by punching press side on vertical component
The hole connection that formula is formed；The bur stretches out from vertical component along mixture flow direction.
Preferably, the fin includes horizontal component and vertical component, the horizontal component it is parallel with plate and with
Plate is sticked together, and the vertical component is connected with horizontal component.
Preferably, the bur is isosceles triangle, the base of the isosceles triangle is arranged on vertical component, and
And perpendicular to plate, the distance of adjacent plate is H, and the length on isosceles triangle base is h, the distance of adjacent vertical component
For w, the drift angle of isosceles triangle is b, and the bearing of trend of the bur is a with the angle of the flow direction of mixture, and L is isosceles
Vertex of a triangle meets equation below to the distance at base midpoint：
7*h/H=c1*Ln (L*sin (a)/w)+c2,
Sin (b/2)=c3+c4*sin (a)-c5* (sin (a))2,
Wherein Ln is logarithmic function, and c1, c2, c3, c4, c5 are coefficients,
0.24<c1<0.25,0.68<c2<0.70,0.87<c3<0.88,0.68<c4<0.70,1.14<c5<1.15；
19°<a<71 °, 55 °<b<165°；
10mm<w<15mm, 6mm<H<14mm；
0.19<L*sin(a)/w<0.41,0.29<7*h/H<0.47；
H is that, with the distance between relative face of adjacent plate, W is with the distance in the relative face of adjacent vertical component.
Preferably, c1=0.2461, c2=0.691,
C3=0.875, c4=0,6987, c5=1.1439.
Preferably, the bearing of trend of the bur is a with the angle of the flow direction of mixture, same vertical component
Multiple burs are set, and along the flow direction of mixture, described angle a is less and less.
Preferably, same vertical component arranges multiple burs, multiple burs interlock from two epitaxial lateral overgrowth of vertical component
Stretch.
Preferably, the length that the bur extends is L, same vertical component arranges multiple burs, along mixture
Flow direction, described length L is less and less.
Preferably, the bur is isosceles triangle, the base of the isosceles triangle is arranged on vertical component, and
And perpendicular to plate, the drift angle of the isosceles triangle is b, and same vertical component arranges multiple burs, along mixture
Flow direction, described drift angle b are increasing.
Preferably, the bur is isosceles triangle, the base of the isosceles triangle is arranged on vertical component, and
And perpendicular to plate, the base of the isosceles triangle is S1, and same vertical component arranges multiple burs, along mixture
Flow direction, described S1 are less and less.
Preferably, same vertical component arranges multiple burs, the distance of adjacent bur is S2, along the stream of mixture
Dynamic direction, described S2 are increasing.
Compared with prior art, plate type heat exchanger and its heat exchange plate of the invention have the following advantages：
1) bur of punching press is applied to the present invention plate-fin heat exchanger of azeotropic multicomponent mixture condensation first, is overcome
Plate-fin heat exchanger heat exchange efficiency low problem for a long time, it will be apparent that improve heat exchange efficiency.
2) laminar sublayer on the one hand can be destroyed, on the other hand compared with " punching " fin, not because of punching loss heat-transfer surface
Product, and " thorn " and " hole " can disturb fluid respectively on differing heights, strengthen different thermal resistance links；
3) aperture that punching press " aculea " is formed, by the impact of " aculea " downstream pressure field, is capable of achieving fin media of both sides
Pressure and mass exchange, the stability of viscous sublayer and liquid film is damaged, enhanced heat exchange；
4) for the fluid of non-azeotrope multicomponent mixture, can realize expanding gas-liquid interface and gas phase by " aculea "
The contact area of boundary layer and cooling wall simultaneously strengthens disturbance；
5) easy processing realizes that manufacture difficulty and cost substantially will not rise；
6) by substantial amounts of experiment, it is determined that the physical dimension of optimal plate-fin heat exchanger；
7) distance by designing adjacent plate is H, and the length on isosceles triangle base is h, adjacent sloping portion
Distance be w, the drift angle of isosceles triangle is b, and the bearing of trend of the bur is a etc. with the angle of the flow direction of mixture
Change of the parameter along fluid flow direction, improves heat exchange efficiency or reduces Fluid pressure.
8) solve the problems, such as that the heat exchange efficiency containing on-condensible gas is low, greatly saved the energy.
Description of the drawings
Fig. 1 is a kind of plate-fin heat exchanger heat exchange plate structural representation of the invention；
Fig. 2 is the structural representation of a plate wing unit of the invention；
Fig. 3 is the schematic diagram that the present invention arranges bur structure vertical part planar；
Fig. 4 is another schematic diagram that the present invention arranges bur structure vertical part planar；
Fig. 5 is the triangle bur structural representation of the present invention；
Fig. 6 is the tangent plane structural representation in triangle bur runner of the present invention；
The structural representation that Fig. 7 burs of the present invention extend to vertical component both sides；
The impact schematic diagram of Fig. 8 vertical component burs, hole to pressure and mass exchange.
Reference is as follows：
1 seal, 2 fluid passages, 3 plates, 4 vertical components, 5 horizontal components, 6 burs, 7 fins.
Specific embodiment
Below in conjunction with the accompanying drawings the specific embodiment of the present invention is described in detail.
Herein, if no specified otherwise, it is related to formula, "/" represents division, and "×", " * " represent multiplication.
As shown in figure 1, a kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, the plate fin heat-exchanging
Device includes plate 3 parallel to each other, forms fluid passage 2, set between the adjacent plate 3 between the adjacent plate 3
Put fin 7.The fin 7 includes vertical component 4 vertically with plate 3, on vertical component 4 processes bur by impact style
6, so that the fluid of 4 both sides of vertical component is by being connected by the hole that impact style is formed on vertical component 4；The bur 6
Stretch out from vertical component 4.
By arranging bur 6, have the following advantages：
1) laminar sublayer on the one hand can be destroyed, on the other hand compared with " punching " fin, not because of punching loss heat-transfer surface
Product, and " thorn " and " hole " can disturb fluid respectively on differing heights, strengthen different thermal resistance links；
2) aperture that punching press " aculea " is formed, by the impact of " aculea " downstream pressure field, is capable of achieving fin media of both sides
Pressure and mass exchange, the stability of viscous sublayer and liquid film is damaged, enhanced heat exchange is shown in Fig. 8
3) for the fluid of non-azeotrope multicomponent mixture, can realize expanding gas-liquid interface and gas phase by " aculea "
The contact area of boundary layer and cooling wall simultaneously strengthens disturbance；
4) easy processing realizes that manufacture difficulty and cost substantially will not rise.
Above-mentioned measure is taken in plate-fin heat exchanger, the letter of non-azeotrope blending agent condensing heat-exchange can greatly be improve
Easy and effective technology.Compared with " punching " fin is taken, it is possible to increase the heat exchange efficiency of 20-30%.
Preferably, the angle formed by the flow direction of described bur 6 and mixture is acute angle, as shown in Figure 8.
Preferably, as shown in Fig. 2 described fin 7 is perpendicular type fin, the fin 7 includes horizontal component 5 and hangs down
Straight part 4, the horizontal component 5 is parallel with plate 3 and sticks together with plate 3, the vertical component 4 and horizontal component 5
Connection is simultaneously disposed mutually.
As shown in fig. 6, the bearing of trend of the bur 6 is a with the angle of the flow direction of mixture, as shown in figure 3, edge
The flow direction of mixture, same vertical component 4 arranges multiple burs 6, along the flow direction of mixture, described folder
Angle a is increasing.
It is found through experiments, by becoming larger for angle a, compared with angle a is identical, it is possible to achieve higher changes
The thermal efficiency, can about improve 10% or so heat exchange efficiency.
Preferably, along the flow direction of mixture, the amplitude that angle a becomes big is less and less.It is found through experiments, becomes
Change the big amplitude of the change of angle a, it is ensured that in the case of heat exchange efficiency, further reduce flow resistance, about can reduce
5% or so flow resistance.
Preferably, the length that the bur 6 extends is L, along the flow direction of mixture, same vertical component 4
Multiple burs 6 are set, and along the flow direction of mixture, described length L is increasing.It is found through experiments, by length L
Become larger, compared with length L is identical, it is possible to achieve higher heat exchange efficiency, can about improve 9% or so and change
The thermal efficiency.
Preferably, along the flow direction of mixture, the amplitude that length L becomes big is less and less.It is found through experiments, it is long
The amplitude that the change of degree L is big is less and less, it is ensured that in the case of heat exchange efficiency, further reduce flow resistance, can be about
Reduce by 5% or so flow resistance.
Preferably, the bur 6 is isosceles triangle, the base of the isosceles triangle is arranged on vertical component 4,
And perpendicular to plate 3, the drift angle of the isosceles triangle is b, along the flow direction of mixture, same vertical component 4
Multiple burs 6 are set, along the flow direction of mixture, in the case where base length keeps constant, described bur drift angle b
It is less and less.It is found through experiments, by tapering into for bur drift angle b, compared with drift angle b is identical, it is possible to achieve more
High heat exchange efficiency, can about improve 8% or so heat exchange efficiency.
Preferably, along the flow direction of mixture, the amplitude that drift angle b diminishes is less and less.It is found through experiments, pushes up
The amplitude that angle b diminishes is less and less, it is ensured that in the case of heat exchange efficiency, further reduces flow resistance, about can drop
Low 4% or so flow resistance.
Preferably, the bur 6 is isosceles triangle, the base of the isosceles triangle is arranged on vertical component,
And perpendicular to plate, the base length of the isosceles triangle is h, along the flow direction of mixture, same vertical component effect
Divide 4 multiple burs 6 are set, along the flow direction of mixture, same vertical component 4 arranges multiple burs, keep in drift angle
In the case of constant, along the flow direction of mixture, described h is increasing.It is found through experiments, by the gradually change of h
Greatly, 7% or so heat exchange efficiency compared with h is identical, it is possible to achieve higher heat exchange efficiency, can about be improved.
Preferably, along the flow direction of mixture, the amplitude that h becomes big is less and less.It is found through experiments, h becomes big
Amplitude it is less and less, it is ensured that in the case of heat exchange efficiency, further reduce flow resistance, can about reduce by 5% left
Right flow resistance.
Preferably, along the flow direction of fluid, same vertical component arranges multiple rows of bur 6, as shown in Figures 3 and 4, often
The distance between row's bur is S2, and along the flow direction of mixture, described S2 is increasing.Why it is arranged such, it is main
Syllabus be it is big by the change of S2, realize, in the case where heat exchange efficiency is ensured, further reducing flow resistance.Sent out by experiment
Existing, flow resistance reduces by 10% or so.
The S2 is the base of the bur with adjacent row to calculate distance.
Preferably, as shown in figure 4, multiple rows of bur 6 is shifted structure.
Find in an experiment, the distance of adjacent plate 3 can not be excessive, crossing conference causes the reduction of heat exchange efficiency, too small meeting
Cause flow resistance excessive, in the same manner, base length, drift angle, bur, the distance of fin vertical component for isosceles triangle with
The angle of fluid flow direction all can not be excessive or too small, the excessive or too small reduction or flowing that can all cause heat exchange efficiency
The change of resistance is big, therefore the base length of the distance in adjacent plate 3, isosceles triangle, drift angle, bur, fin vertical component
An optimized size relationship is met and the angle of fluid flow direction between.
Therefore, the present invention is the thousands of numerical simulations and test data by multiple various sizes of heat exchangers,
Meet in the case of industrial requirements pressure-bearing (below 10MPa), in the case where maximum heat exchange amount is realized, the optimal heat exchange for summing up
The dimensionally-optimised relation of plate.
The distance of adjacent plate is H (i.e. the height of vertical component is also H), and the length on isosceles triangle base is h, phase
The distance of adjacent vertical component is w,
7*h/H=c1*Ln (L*sin (a)/w)+c2,
Sin (b/2)=c3+c4*sin (a)-c5* (sin (a))2,
Wherein Ln is logarithmic function, and c1, c2, c3, c4, c5 are coefficients,
0.24<c1<0.25,0.68<c2<0.70,0.87<c3<0.88,0.68<c4<0.70,1.14<c5<1.15；
19°<a<71 °, 55 °<b<165°；
10mm<w<15mm, 6mm<H<14mm；
0.19<L*sin(a)/w<0.41,0.29<7*h/H<0.47；
H is that, with the distance between relative face of adjacent plate, W is that, with the distance in the relative face of adjacent vertical component, L is
Distance of the summit of isosceles triangle to base midpoint；
Preferably, c1=0.2461, c2=0.691；
C3=0.875, C4=0,6987, C5=1.1439.
By the optimal geometric scale of " bur " that go out of above-mentioned formula, heat exchange efficiency can be improved, while can be real
Now only to viscous sublayer or comprising liquid film and to the reinforcing comprising gas phase boundary different scale internal thermal resistance, it is to avoid measure
Degree, causes unnecessary drag losses.
Preferably, the base of the adjacent bur of described same row is all on one wire, the adjacent bur of same row
Distance is S1, the 4 × h<S1<6 × h, wherein S1 are with the distance at the midpoint on the base of two neighboring isosceles triangle bur.
Preferably, the base of the isosceles triangle of the bur of adjacent row is parallel to each other, the summit of isosceles triangle is on earth
The distance at side midpoint be L, adjacent row apart from S2 be 4*L<S2<7*L.Preferably S2=5*L
When the base of the isosceles triangle of adjacent row is different, take the weighted average on two bases to calculate.
Preferably, the angle of the isosceles triangle of same row is identical with base.I.e. shape is identical, is equal
Shape.
For formula above, the bur different for front and rear row size, also still it is suitable for.
For the concrete dimensional parameters do not mentioned, it is designed according to normal heat exchanger.
Preferably, as shown in fig. 7, multiple burs 6 are arranged on vertical component, not homonymy of the bur to vertical component
Extend
Preferably, same vertical component arranges multiple rows of bur, at least row's bur is with other row's burs to rake
The extension side divided is different.
Preferably, adjacent bur of often arranging extends to the not homonymy of vertical component.
By being arranged such, fluid can be caused to replace heat exchanging tampering in the passage of vertical component both sides, further carried
High heat exchange efficiency.Compared with the same side, it is possible to increase 8% or so.
Although the present invention is disclosed as above with preferred embodiment, the present invention is not limited to this.Any art technology
Personnel, without departing from the spirit and scope of the present invention, can make various changes or modifications, therefore protection scope of the present invention should
When being defined by claim limited range.
Claims (2)
1. a kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, the plate-fin heat exchanger includes mutually equal
Capable plate, arranges fin between the plate, the fin includes the vertical component perpendicular to plate, it is characterised in that
Bur is processed by impact style on vertical component, so that the fluid of vertical component both sides is by impact style on vertical component
The hole connection of formation；The bur stretches out from vertical component；The fin includes horizontal component and vertical component, the water
Flat part is parallel with plate and sticks together with plate, and the vertical component is connected with horizontal component；
The bearing of trend of the bur is a with the angle of the flow direction of mixture, and same vertical component arranges multiple burs,
Along the flow direction of mixture, described angle a is increasing.
2. plate-fin heat exchanger as claimed in claim 1, it is characterised in that same vertical component effect arranges multiple burs, multiple
Bur staggeredly stretches out from vertical component effect both sides.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510657872.XA CN105157459B (en) | 2015-10-12 | 2015-10-12 | It is a kind of that the right angle plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510657872.XA CN105157459B (en) | 2015-10-12 | 2015-10-12 | It is a kind of that the right angle plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105157459A CN105157459A (en) | 2015-12-16 |
| CN105157459B true CN105157459B (en) | 2017-04-05 |
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| CN201510657872.XA Expired - Fee Related CN105157459B (en) | 2015-10-12 | 2015-10-12 | It is a kind of that the right angle plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture |
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| NL2015996B1 (en) * | 2015-12-21 | 2017-06-30 | Recair Holding B V | Heat exchanger. |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3265127A (en) * | 1963-10-21 | 1966-08-09 | Ford Motor Co | Heat exchange element |
| JP3744432B2 (en) * | 2002-02-06 | 2006-02-08 | 株式会社デンソー | Exhaust heat exchanger |
| JP3784735B2 (en) * | 2002-03-07 | 2006-06-14 | カルソニックカンセイ株式会社 | Louver fin |
| US20070012430A1 (en) * | 2005-07-18 | 2007-01-18 | Duke Brian E | Heat exchangers with corrugated heat exchange elements of improved strength |
| US7913750B2 (en) * | 2008-01-09 | 2011-03-29 | Delphi Technologies, Inc. | Louvered air center with vortex generating extensions for compact heat exchanger |
| IN2012DN00867A (en) * | 2009-09-16 | 2015-07-10 | Carrier Corp |
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