CN105180690A - Trapezoidal plate fin type heat exchanger provided with stabs and used for condensation of non-azeotropic multi-component mixture - Google Patents
Trapezoidal plate fin type heat exchanger provided with stabs and used for condensation of non-azeotropic multi-component mixture Download PDFInfo
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- CN105180690A CN105180690A CN201510658090.8A CN201510658090A CN105180690A CN 105180690 A CN105180690 A CN 105180690A CN 201510658090 A CN201510658090 A CN 201510658090A CN 105180690 A CN105180690 A CN 105180690A
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Abstract
The invention provides a trapezoidal plate fin type heat exchanger provided with stabs and used for condensation of a non-azeotropic multi-component mixture. The trapezoidal plate fin type heat exchanger comprises mutually parallel sheet plates; fins are arranged between the sheet plates and are trapezoidal fines; each trapezoidal fin comprises inclined parts inclining towards the corresponding sheet plate and horizontal parts; the inclined parts of each trapezoidal fin form the two legs of the trapezoid and are provided with the stabs in a punching mode, so that fluid on the two sides of the inclined parts is communicated through the holes formed in the inclined parts in the punching mode; the stabs extend outwards from the inclined parts in the flowing direction of the mixture. The novel trapezoidal plate fin type heat exchanger provided with the stabs and used for condensation of the non-azeotropic multi-component mixture achieves condensation of the non-azeotropic multi-component mixture so as to improve the heat exchange efficiency and reduce flowing resistance of the fluid.
Description
Technical field
The invention belongs to field of heat exchangers, particularly relate to the heat exchanger that a kind of different boiling blending agent condensation uses, belong to the field of heat exchangers of F28D.
Background technology
The condensation of different boiling blending agent is the main processes of natural gas liquefaction (main component is boiling point-162 DEG C of methane, boiling point-88 DEG C of ethane, boiling point-42 DEG C of propane etc.), air separation, azeotrope refrigeration, oil or the industry such as cracking waste plastics, biogas production.For reducing technical process
loss, this type of production technology wishes to cool according to temperature rank the component separating out different boiling step by step, self also carries out exchange heat with one cold-producing medium or product in different temperatures interval, therefore requires that condensing plant conveniently realizes the heat exchange simultaneously of multiply medium.Conveniently can realize equipment mainly spiral winding heat exchange of heat pipe and the plate-fin heat exchanger two kinds of multiply medium heat exchange simultaneously at present.Spiral winding heat exchange of heat pipe is shell structure, and pressure-bearing is higher, and application is comparatively extensive, but is difficult to take enhanced heat transfer measure, and the coefficient of heat transfer is lower, and volume and weight is difficult to reduction.Plate-fin heat exchanger is along with the improvement of manufacturing process in recent years, and bearing capacity improves gradually., there is in a lot of occasions such as natural gas liquefactions the trend replacing winding pipe heat exchanger in the advantage higher, compacter with its heat transfer coefficient, weight is lighter.
Although plate-fin heat exchanger can provide the higher coefficient of heat transfer equally with under the variable working condition of condensation phase in boiling, the fin configuration of existing plate-fin heat exchanger is mainly for the mechanismic design of single-phase medium (emphasis is gas phase media) heat exchange: plain fin extends heat exchange area and reduces hydraulic diameter; Corrugated fin, saw tooth fin, louvered fin are the thinning boundary layers of disturbance fluid on expanding area basis; Be recognized the fin with apertures, the sheet band fin that are applicable to phase-change heat-exchange in the continuity for liquid film can be destroyed during condensing heat-exchange, but to be also proved effect in high reynolds number operating mode and to have superiority unlike plain fin.
The thermal resistance mechanism of non-azeotrope multicomponent blending agent condensation in natural gas liquefaction has obvious difference with pure component material condensation, and theory analysis and experiment have proved that the coefficient of heat transfer obviously reduces than pure component condensation.The existing research to non-azeotrope blending agent condensing heat-exchange is focusing more on the operating mode containing a kind of on-condensible gas, adopt the measures such as low groove, Artificial roughness surface to reduce average thickness of liquid film and be proved remarkably productive measure when pure component condensation, sometimes not obvious containing effect in on-condensible gas situation., and the condensing heat-exchange process of natural gas liquefaction, petroleum cracking industry and mechanism more complicated, condensation process comprises two or more on-condensible gases usually, and heat exchange situation is more complicated.
For the problems referred to above, the invention provides a kind of new plate-fin heat exchanger, thus solve the condensation of the different multicomponent blending agent of boiling point.
Summary of the invention
The invention provides a kind of new plate-fin heat exchanger, thus solve the condensation of the different multicomponent blending agent of boiling point, to improve heat exchange efficiency, reduce fluid flow resistance.
To achieve these goals, technical scheme of the present invention is as follows:
A kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, described plate-fin heat exchanger comprises plate parallel to each other, between described plate, fin is set, described fin is trapezoidal fin, described trapezoidal fin comprises the sloping portion and horizontal component that favour plate, and sloping portion forms two trapezoidal waists, it is characterized in that, sloping portion processes bur by impact style, thus the hole that the fluid of sloping portion both sides is formed by impact style on sloping portion is communicated with; Described bur stretches out from sloping portion along mixture flow direction.
As preferably, described fin comprises horizontal component, and described horizontal component is parallel with plate and stick together with plate, and described sloping portion is connected with horizontal component.
As preferably, described trapezoidal be isosceles trapezoid, described bur is isosceles triangle, the base of described isosceles triangle is arranged on sloping portion, and the distance of adjacent plate is H, and the length on isosceles triangle base is h, the distance of adjacent sloping portion is w, the drift angle of isosceles triangle is b, and the angle of the bearing of trend of described bur and the flow direction of mixture is a, meets following formula:
6.58*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<6.58*h/H<0.47；
H be with the relative face of adjacent plate between distance, W is being parallel to plate direction and is extending to the distance of another waist of isosceles trapezoid with the mid point on isosceles triangle base selecting on isosceles trapezoid waist, and L is the distance of summit to base mid point of isosceles triangle;
The acute angle on isosceles trapezoid base is c, 90 ° of <c<74 °
As preferably, c1=0.2432, c2=0.689,
c3＝0.872，c4＝0,698，c5＝1.143。
As preferably, the angle of the bearing of trend of described bur and the flow direction of mixture is a, and same sloping portion arranges multiple bur, and along the flow direction of mixture, described angle a is more and more less.
As preferably, same sloping portion arranges multiple bur, and multiple bur is staggered to stretch out from sloping portion both sides.
As preferably, the direction that the long limit along trapezoidal fin extends towards minor face, the bur length L extended in trapezoidal runner is increasing.
As preferably, the direction that the long limit along trapezoidal fin extends towards minor face, the amplitude that L increases is increasing.
As preferably, the angle of the bearing of trend of described bur and the flow direction of mixture is a, and same sloping portion arranges multiple bur, and along the flow direction of mixture, described angle a is more and more less.
As preferably, same sloping portion arranges multiple bur, and multiple bur is staggered to stretch out from sloping portion both sides.
As preferably, the length that described bur extends is L, and same sloping portion arranges multiple bur, and along the flow direction of mixture, described length L is more and more less.
As preferably, described bur is isosceles triangle, and the base of described isosceles triangle is arranged on sloping portion, and favour plate, the drift angle of described isosceles triangle is b, and same sloping portion arranges multiple bur, along the flow direction of mixture, described drift angle b is increasing.
As preferably, described bur is isosceles triangle, and the base of described isosceles triangle is arranged on sloping portion, and favour plate, the base of described isosceles triangle is S1, and same sloping portion arranges multiple bur, along the flow direction of mixture, described S1 is more and more less.
As preferably, same sloping portion arranges multiple bur, and the distance of adjacent bur is S2, and along the flow direction of mixture, described S2 is increasing.
Compared with prior art, plate type heat exchanger of the present invention and heat exchange plate thereof have following advantage:
1) bur of punching press is applied to the plate-fin heat exchanger of azeotropic multicomponent mixture condensation by the present invention first, overcomes the problem that plate-fin heat exchanger heat exchange efficiency is low for a long time, significantly improves heat exchange efficiency.
2) on the one hand can breakable layer laminar sublayer, on the other hand compared with " punching " fin, not because heat exchange area is lost in punching, and " thorn " and " hole " can disturbance fluid on differing heights respectively, strengthens different thermal resistance links;
3) aperture that punching press " aculea " is formed, by the impact of " aculea " downstream pressure field, can realize pressure and the mass exchange of fin media of both sides, damage, enhanced heat exchange to the stability of viscous sublayer and liquid film;
4) for the fluid of non-azeotrope multicomponent mixture, can the contact area of expansion gas-liquid interface and gas phase boundary and cooling wall be realized by " aculea " and strengthen disturbance;
5) easily process realization, manufacture difficulty and cost can not obviously rise;
6) by a large amount of experiments, the physical dimension of best plate-fin heat exchanger is determined;
7) be H by the distance of the adjacent plate of design, the length on isosceles triangle base is h, the distance of adjacent sloping portion is w, the drift angle of isosceles triangle is b, the angle of the bearing of trend of described bur and the flow direction of mixture is the change of the parameters such as a along fluid flow direction, improves heat exchange efficiency or reduces fluid pressure.
8) solve the problem that heat exchange efficiency containing on-condensible gas is low, save the energy greatly.
Accompanying drawing explanation
Fig. 1 is a kind of plate-fin heat exchanger heat exchange plate of the present invention structural representation;
Fig. 2 is the structural representation of the present invention's plate wing unit;
Fig. 3 is the schematic diagram that the present invention arranges bur structures slope part planar;
Fig. 4 is another schematic diagram that the present invention arranges bur structures slope part planar;
Fig. 5 is 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 bur of the present invention extends to sloping portion both sides;
Fig. 8 sloping portion bur, hole affect schematic diagram to pressure and mass exchange.
Reference numeral is as follows:
1 seal, 2 fluid passages, 3 plates, 4 sloping portions, 5 horizontal components, 6 burs, 7 fins.
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.
As shown in Figure 1, a kind of plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, described plate-fin heat exchanger comprises plate 3 parallel to each other, forms fluid passage 2 between described adjacent plate 3, arranges fin 7 between described adjacent plate 3.Described fin 7 comprises tilting the sloping portion 4 with plate 3, by impact style processing bur 6 on sloping portion 4, thus the fluid of sloping portion 4 both sides is communicated with by the hole that sloping portion 4 is formed by impact style; Described bur 6 stretches out from sloping portion 4.
Described fin is trapezoidal fin, and described trapezoidal fin comprises the sloping portion and horizontal component that favour plate, and sloping portion forms two trapezoidal waists.
By arranging bur 6, there is following advantage:
1) on the one hand can breakable layer laminar sublayer, on the other hand compared with " punching " fin, not because heat exchange area is lost in punching, and " thorn " and " hole " can disturbance fluid on differing heights respectively, strengthens different thermal resistance links;
2) aperture that punching press " aculea " is formed, by the impact of " aculea " downstream pressure field, can realize pressure and the mass exchange of fin media of both sides, damage, enhanced heat exchange, see Fig. 8 to the stability of viscous sublayer and liquid film
3) for the fluid of non-azeotrope multicomponent mixture, can the contact area of expansion gas-liquid interface and gas phase boundary and cooling wall be realized by " aculea " and strengthen disturbance;
4) easily process realization, manufacture difficulty and cost can not obviously rise.
In plate-fin heat exchanger, take above-mentioned measure, the simple and easy effective technology again of non-azeotrope blending agent condensing heat-exchange can greatly be improve.With take compared with " punching " fin, the heat exchange efficiency of 20-30% can be improved.
As preferably, the angle that described bur 6 and the flow direction of mixture are formed is acute angle, as shown in Figure 8.
As preferably, as shown in Figure 2, described fin 7 is perpendicular type fin, and described fin 7 comprises horizontal component 5 and sloping portion 4, and described horizontal component 5 is parallel with plate 3 and stick together with plate 3, and described sloping portion 4 is connected with horizontal component 5.
As shown in Figure 6, the angle of the described bearing of trend of bur 6 and the flow direction of mixture is a, and as shown in Figure 3, along the flow direction of mixture, same sloping portion 4 arranges multiple bur 6, and along the flow direction of mixture, described angle a is increasing.
Found through experiments, large by the change gradually of angle a, compared with identical with angle a, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 10%.
As preferably, along the flow direction of mixture, it is more and more less that angle a becomes large amplitude.Found through experiments, change the amplitude that the change of angle a is large, when can ensure heat exchange efficiency, reduce flow resistance further, approximately can reduce the flow resistance of about 5%.
As preferably, the length that described bur 6 extends is L, and along the flow direction of mixture, same sloping portion 4 arranges multiple bur 6, and along the flow direction of mixture, described length L is increasing.Found through experiments, large by the change gradually of length L, compared with identical with length L, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 9%.
As preferably, along the flow direction of mixture, it is more and more less that length L becomes large amplitude.Found through experiments, the amplitude that the change of length L is large is more and more less, when can ensure heat exchange efficiency, reduces flow resistance further, approximately can reduce the flow resistance of about 5%.
As preferably, described bur 6 is isosceles triangle, the base of described isosceles triangle is arranged on sloping portion 4, and as preferably, base is identical with the angle of inclination of sloping portion, the drift angle of described isosceles triangle is b, along the flow direction of mixture, same sloping portion 4 arranges multiple bur 6, along the flow direction of mixture, when base length remains unchanged, described bur drift angle b is more and more less.Found through experiments, by diminishing gradually of bur drift angle b, compared with identical with drift angle b, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 8%.
As preferably, along the flow direction of mixture, the amplitude that drift angle b diminishes is more and more less.Found through experiments, the amplitude that drift angle b diminishes is more and more less, when can ensure heat exchange efficiency, reduces flow resistance further, approximately can reduce the flow resistance of about 4%.
As preferably, described bur 6 is isosceles triangle, and the base of described isosceles triangle is arranged on sloping portion, as preferably, base is identical with the angle of inclination of sloping portion, and the base length of described isosceles triangle is h, along the flow direction of mixture, same sloping portion 4 arranges multiple bur 6, along the flow direction of mixture, same sloping portion 4 arranges multiple bur, when drift angle remains unchanged, along the flow direction of mixture, described h is increasing.Found through experiments, large by the change gradually of h, compared with identical with h, higher heat exchange efficiency can be realized, approximately can improve the heat exchange efficiency of about 7%.
As preferably, along the flow direction of mixture, it is more and more less that h becomes large amplitude.Found through experiments, it is more and more less that h becomes large amplitude, when can ensure heat exchange efficiency, reduces flow resistance further, approximately can reduce the flow resistance of about 5%.
As preferably, along the flow direction of fluid, same sloping portion arranges many row's burs 6, and as shown in Figures 3 and 4, often the distance of arranging between bur is S2, and along the flow direction of mixture, described S2 is increasing.Why so arrange, main purpose is large by the change of S2, realizes, when ensureing heat exchange efficiency, reducing flow resistance further.Found through experiments, flow resistance reduces about 10%.
Described S2 is for calculating distance with the base of the bur of adjacent row.
As preferably, as shown in Figure 4, many row's burs 6 are shifted structure.
Find in an experiment, the distance of adjacent plate 3 can not be excessive, cross the reduction that conference causes heat exchange efficiency, too small meeting causes flow resistance excessive, in like manner, for the base length of isosceles triangle, drift angle, bur, the distance of fin sloping portion and the angle of fluid flow direction all can not be excessive or too small, excessive or too smallly the change of the reduction of heat exchange efficiency or flow resistance all can be caused large, therefore in the distance of adjacent plate 3, the base length of isosceles triangle, drift angle, bur, an optimized size relationship is met between fin sloping portion and the angle of fluid flow direction.
Therefore, the present invention is thousands of numerical simulations by the heat exchanger 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 heat exchange plate of the best summed up.
The distance of adjacent plate is H (namely the distance of the long limit of isosceles trapezoid and minor face is also H), and the length on isosceles triangle base is h, and the distance of adjacent sloping portion is w,
Described trapezoidal be isosceles trapezoid, described bur is isosceles triangle, the base of described isosceles triangle is arranged on sloping portion, the distance of adjacent plate is H, the length on isosceles triangle base is h, and the distance of adjacent sloping portion is w, and the drift angle of isosceles triangle is b, the angle of the bearing of trend of described bur and the flow direction of mixture is a, meets following formula:
6.58*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<6.58*h/H<0.47；
H be with the relative face of adjacent plate between distance, W is being parallel to plate direction (being namely parallel to trapezoidal long limit or short side direction) and is extending to the distance of another waist of isosceles trapezoid with the mid point on isosceles triangle base selecting on isosceles trapezoid waist, and L is the distance of summit to base mid point of isosceles triangle;
As preferably, the acute angle on isosceles trapezoid base is c, 90 ° of <c<74 °
As preferably, c1=0.2432, c2=0.689,
c3＝0.872，c4＝0,698，c5＝1.143。
By the geometric scale of the best of " bur " that go out of above-mentioned formula, heat exchange efficiency can be improved, can realize only to viscous sublayer or comprise liquid film and to the strengthening comprising gas phase boundary different scale internal thermal resistance, avoiding measures is excessive, causes unnecessary drag losses simultaneously.
As preferably, the base of the adjacent bur of described same row all on one wire, the bur distance that same row is adjacent is S1, and described 4 × h<S1<6 × h, wherein S1 is with the distance of the mid point on the base of adjacent two isosceles triangle burs.
As preferably, the base of the isosceles triangle of the bur 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 4*L<S2<7*L.Be 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.
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 bur that front and rear row size is different, be also still suitable for.
For the concrete dimensional parameters do not mentioned, design according to normal heat exchanger.
Minor face along trapezoidal fin extends towards trapezoidal long limit, and the angle a of the bur extended in trapezoidal runner is increasing.Mainly by the continuous change of angle, while guarantee improves heat exchange efficiency, flow resistance can be reduced.Because in trapezoidal shape runner, the circulation area on section bank is minimum, the circulation area on long limit is maximum, therefore, the angle a arranged by the position that circulation area is little is little, can reduce flow resistance, avoids again corner position place to cause short circuit phenomenon to occur because flow resistance is excessive simultaneously.
As preferably, the minor face along trapezoidal fin extends towards trapezoidal long limit, and the amplitude that angle a increases is increasing.Found through experiments, by increasing the amplitude of angle a, the heat exchange efficiency of about about 10% can be improved, and resistance increases relatively only increase about 1%.Therefore heat exchange efficiency is greatly improved.
Minor face along trapezoidal fin extends towards trapezoidal long limit, and the L extended in trapezoidal runner is increasing.Mainly by the continuous change of L, while guarantee improves heat exchange efficiency, flow resistance can be reduced.Because in trapezoidal runner, the circulation area of drift angle is minimum, and the circulation area on base is maximum, therefore, the L arranged by the position that circulation area is little is little, can reduce flow resistance, avoids again minor face position to cause short circuit phenomenon to occur because flow resistance is excessive simultaneously.
As preferably, the minor face along trapezoidal fin extends towards long limit, and the amplitude that L increases is increasing.Found through experiments, by increasing the amplitude of L, the heat exchange efficiency of about about 10% can be improved, and resistance increases relatively only increase about 0.8%.Therefore heat exchange efficiency is greatly improved.
As preferably, as shown in Figure 7, sloping portion is arranged multiple bur 6, described bur extends to the not homonymy of sloping portion
As preferably, same sloping portion is arranged arranges bur more, and to arrange bur different to the extension side of sloping portion from other at least one row's bur.
As preferably, adjacent bur of often arranging extends to the not homonymy of sloping portion.
By setting like this, fluid can be made in the passage of sloping portion both sides to replace heat exchanging tampering, improve heat exchange efficiency further.With compared with the same side, can about 8% be improved.
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 (8)
1. the plate-fin heat exchanger for the condensation of non-azeotrope multicomponent mixture, described plate-fin heat exchanger comprises plate parallel to each other, between described plate, fin is set, described fin is trapezoidal fin, described trapezoidal fin comprises the sloping portion and horizontal component that favour plate, and sloping portion forms two trapezoidal waists, it is characterized in that, sloping portion processes bur by impact style, thus the hole that the fluid of sloping portion both sides is formed by impact style on sloping portion is communicated with; Described bur stretches out from sloping portion along mixture flow direction.
2. plate-fin heat exchanger as claimed in claim 1, is characterized in that, described horizontal component is parallel with plate and stick together with plate, and described sloping portion is connected with horizontal component.
3. plate-fin heat exchanger as claimed in claim 1 or 2, it is characterized in that, described trapezoidal be isosceles trapezoid, described bur is isosceles triangle, and the base of described isosceles triangle is arranged on sloping portion, the distance of adjacent plate is H, the length on isosceles triangle base is h, and the distance of adjacent sloping portion is w, and the drift angle of isosceles triangle is b, the angle of the bearing of trend of described bur and the flow direction of mixture is a, meets following formula:
6.58*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<6.58*h/H<0.47；
H be with the relative face of adjacent plate between distance, W is being parallel to plate direction and is extending to the distance of another waist of isosceles trapezoid with the mid point on isosceles triangle base selecting on isosceles trapezoid waist, and L is the distance of summit to base mid point of isosceles triangle;
The acute angle on the base of isosceles trapezoid is c, 90 ° of <c<74 °.
4. plate-fin heat exchanger as claimed in claim 3, is characterized in that, c1=0.2432, c2=0.689,
c3＝0.872，c4＝0,698，c5＝1.143。
5. plate-fin heat exchanger as claimed in claim 1, it is characterized in that, the angle of the bearing of trend of described bur and the flow direction of mixture is a, and same sloping portion arranges multiple bur, and along the flow direction of mixture, described angle a is more and more less.
6. plate-fin heat exchanger as claimed in claim 1, it is characterized in that, same sloping portion arranges multiple bur, and multiple bur is stretched from the different epitaxial lateral overgrowth of sloping portion.
7. plate-fin heat exchanger as claimed in claim 1, it is characterized in that, the direction that the long limit along trapezoidal fin extends towards minor face, the bur length L extended in trapezoidal runner is increasing.
8. plate-fin heat exchanger as claimed in claim 7, is characterized in that, the direction that the long limit along trapezoidal fin extends towards minor face, and the amplitude that L increases is increasing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510658090.8A CN105180690B (en) | 2015-10-12 | 2015-10-12 | It is a kind of that the trapezoidal plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510658090.8A CN105180690B (en) | 2015-10-12 | 2015-10-12 | It is a kind of that the trapezoidal plate-fin heat exchanger that bur is set is condensed for non-azeotrope multicomponent mixture |
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| CN105180690A true CN105180690A (en) | 2015-12-23 |
| CN105180690B CN105180690B (en) | 2017-04-05 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3265127A (en) * | 1963-10-21 | 1966-08-09 | Ford Motor Co | Heat exchange element |
| US20040011516A1 (en) * | 2002-03-07 | 2004-01-22 | Calsonic Kansei Corporation | Louver fin and corrugation cutter for forming louver fin |
| JP3744432B2 (en) * | 2002-02-06 | 2006-02-08 | 株式会社デンソー | Exhaust heat exchanger |
| 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 |
| CN102483313A (en) * | 2009-09-16 | 2012-05-30 | 开利公司 | Free-draining finned surface architecture for a heat exchanger |
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2015
- 2015-10-12 CN CN201510658090.8A patent/CN105180690B/en active Active
Patent Citations (6)
| 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 |
| US20040011516A1 (en) * | 2002-03-07 | 2004-01-22 | Calsonic Kansei Corporation | Louver fin and corrugation cutter for forming 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 |
| CN102483313A (en) * | 2009-09-16 | 2012-05-30 | 开利公司 | Free-draining finned surface architecture for a heat exchanger |
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|---|---|
| CN105180690B (en) | 2017-04-05 |
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