CN101194137A - Plate heat exchanger with exchanging structure forming several channels in a passage - Google Patents
Plate heat exchanger with exchanging structure forming several channels in a passage Download PDFInfo
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- CN101194137A CN101194137A CNA2006800202420A CN200680020242A CN101194137A CN 101194137 A CN101194137 A CN 101194137A CN A2006800202420 A CNA2006800202420 A CN A2006800202420A CN 200680020242 A CN200680020242 A CN 200680020242A CN 101194137 A CN101194137 A CN 101194137A
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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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04975—Construction and layout of air fractionation equipments, e.g. valves, machines adapted for special use of the air fractionation unit, e.g. transportable devices by truck or small scale use
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
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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
- F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
- F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
- F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
- F28F3/025—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being corrugated, plate-like elements
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
-
- 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
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/20—Particular dimensions; Small scale or microdevices
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F2260/00—Heat exchangers or heat exchange elements having special size, e.g. microstructures
- F28F2260/02—Heat exchangers or heat exchange elements having special size, e.g. microstructures having microchannels
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention concerns a heat exchanger with brazed plates comprising a stack of parallel plates defining a plurality of generally flat fluid circulating passages, closure bars which delimit said passages and distributing means for distributing a fluid to each passage of a first series of passages and means for conveying another fluid to a second series of passages wherein at least one passage contains organized exchanging structures (15) which form a plurality of channels (19) in the width of the passage and also at least three channels (19) in the height of the passage. The invention is useful for air separation by cryogenic distillation.
Description
Technical field
The present invention relates to a kind of plate-fin heat exchanger (é changeur de chaleur à plaques etailettes).
Background technology
Have various types of plate-fin heat exchangers, each is applicable to the application in the specific area.Particularly, the present invention advantageously is applied to a kind of being used for by separating air by cryogenic distillation or H
2The heat exchanger of the unit of/CO (hydrogen/carbon monoxide).
Described heat exchanger can be main heat exchange pipe, subcooler or the evaporative condenser of air-separating plant, and this main heat exchange pipe cools off the incoming flow air by carrying out heat exchange indirectly with the cryogenic product that is derived from destilling tower.
Common technology in these heat exchangers is an aluminum brazing sheet fin heat exchanger technology, the feasible very compact parts that can obtain to have big heat exchange area of this technology.
These heat exchangers are made up of the plate that is inserted with corrugated sheet or fin betwixt, thereby form the path that a pile is called as " cold " path and is called as " heat " path.
Normally used heat-exchange fin is straight fins, perforation fin and serrated fin.
The following parameter characterization of these corrugated fins:
H (mm): the height of corrugated fin (3-10mm)
E (mm): the thickness of corrugated fin (0.2-0.6mm)
N (m
-1Or inch
-1): the quantity of the corrugated fin on the unit length (every meter 177-1102 ripple)
Perf (%): puncture degree (for the perforation fin is 5%)
l
s(mm): profile length (with regard to serrated fin)
Like this, the scope of the hydraulic diameter of normally used fin (Dh) is 1 to 6mm in the brazing sheet fin heat exchanger.At present, these corrugated heat-exchange fins are stamping forming.
The method that has various increase heat exchange areas.
The heat exchange area of separating two fluids is made of area that is called as " interarea is long-pending " and the area that is called as " second area ", " interarea is long-pending " is corresponding to the area of plane between two fluids, " second area " is made up of fin usually, thereby described fin amasss and form corrugated heat-exchange fin perpendicular to interarea.The height of quantity of the fin that is inserted (fin density) and fin makes heat exchange area increase.
Fins set is close more, and then heat exchange area is big more.But, there is the restriction of manufacture view, and the existence constraint relevant with method.Being used to make the maximal density that the stamping tool of corrugated fin group can realize is every meter of 1023-1102 ripple.When being partial to limits pressure drops, selected fin density can be lower.In addition, under certain operating condition, for example in the immersion evaporative condenser, with security-related constraint with every meter ripple restricted number far below the peaked numerical value that can reach in the mill.
Described fin has thermograde.When surpassing certain fin height, near the zone line of fin and do not carry out heat exchange Anywhere.Therefore, existence is corresponding to the best fin height of best fin coefficient.Usually the altitude range of the fin that adopts changes between the 10mm at 3mm.
Also can increase heat exchange coefficient.
Flow disturbance Shaoxing opera is strong, and then heat exchange coefficient is good more.Shape that can be by changing passage or by insert the barrier that generates turbulent flow (as the straight fins of perforation, serrated fin, herringbone fin, the board-like fin of shutter or by the small-sized fin of insertion, hole etc.) generate as described in turbulent flow.
When fluid evaporator, the surface with nucleation position of comparatively high amts demonstrates heat exchange coefficient preferably.These nucleation positions are the micro-cavities with multiple size and dimension (reentrant cavity) that are present in the surface or pass porous layer.
When fluid condenses, thickness of liquid film has adverse effect to heat exchange coefficient.Therefore, it is favourable utilizing groove, perforation or height to rise and fall liquid is discharged.
The heat exchanger that one class is called as the minute yardstick heat exchanger has appearred recently.
This is the heat exchanger of a kind of hydraulic diameter less than 1 millimeter passage.The size that reduces passage makes and might increase heat exchange area (making this device compactness more).So in fact heat exchange coefficient is inversely proportional to hydraulic diameter.
S.Kandlikar in first international conference in 2003 about microchannel and small size tunnel in " Extending the applicability of the flow boiling correlation to lowReynolds number flows in microchannels (the flow boiling relational expression is the application in the low reynolds number flow in the microchannel) " hydraulic diameter based on passage following classification is proposed:
The small size tunnel of zero 1mm＜Dh＜3mm (corresponding to the Dh value of this paper corrugated fin group)
The small size tunnel of 0 200 μ m＜Dh＜1mm
The microchannel of zero Dh＜200 μ m
(200 μ m＜Dh＜3mm), the hydrodynamics law that is used for conventional pipe stands good for small size tunnel.
For microchannel (Dh＜200 μ m), skin effect is quite important, and conventional hydrodynamics law is no longer suitable.
EP-A-1008826 has described a kind of plate type heat exchanger, and wherein, at least one path comprises the auxiliary channel of the sealing of tubulose, and its Breadth Maximum is greater than 50% of the distance between the two adjacent plates.
(heat) flux by the heat exchanger exchange is provided by following formula:
φ＝k×S×ΔT
For given Δ T, only by increasing heat exchange coefficient (k) and/or just can improving (heat) exchange by increasing heat exchange area (S).
Under the situation of brazing sheet fin heat exchanger,, utilize so-called " second " area to increase heat exchange area and reach its limit owing to make and/or the constraint relevant with method.It is favourable increasing heat exchange coefficient by turbulization, but has two main defectives:
● increase turbulent flow and can increase pressure drop;
● owing to the complexity of relevant geometry increases manufacturing cost.
Therefore, the corrugated fin group of creating a kind of new shape can not make heat exchange coefficient significantly be increased to exceed the level that existing fins set can reach.Discharge the position as for producing nucleation position and liquid, these two kinds of methods only relate to the heat exchange of particular type, mainly are evaporation or condensation.
Therefore, according to continuing exploitation, it seems to make the brazing sheet fin heat exchanger that substantial improvement be arranged with being difficult to identical route mentioned above.
In addition, the technology of microchannel type very expensive (the miniature processing of passage), and still keep to some extent for small-sized heat exchanger is current: it is not suitable for the application such as the very big air separation of flow and the temperature difference at present.
Summary of the invention
The scheme that is proposed is intended to increase heat exchange area by combination in (" master " and " the second ") area that has existed with the 3rd heat exchange area that is called as " the 3rd area ".
The present invention proposes and make that increasing " the 3rd " area to the current ripple heat-exchange fin group that is used for the brazing sheet fin heat exchanger becomes three kinds of possible designs:
● " multistage corrugated fin group " switching path;
● " small size tunnel " heat-exchange fin group, the fins set that extrudes;
● " small size tunnel " heat-exchange fin group, capillary.
A theme of the present invention relates to a kind of brazing plate type heat exchanger (é changeur de chaleur à plaques bras é es), and this heat exchanger types comprises that a pile limits a plurality of parallel-plate parts with fluid peripheral passage of flat overall shape, defines the sealing lath of these paths and be used for to the distributor of each path distributing fluids of first series of passages and be used for carrying to the second series path device of another fluid; In this heat exchanger, at least one path comprises at least one structurized (heat) switching fabric, this heat exchange structure forms a plurality of passages on the width of path, each passage or contact with at least two other passages or contact with a plate with at least one other passage, this heat exchanger is characterised in that, described structure also forms at least three passages, at least five passages preferably on the height of path.
Preferably, each passage contacts with two other passages with at least three other passages or a plate.Described plate can be the plate that limits path, or is arranged in second plate of path.
According to other optional aspect:
-described structure is made of a plurality of cylinders;
-at inner at least one second plate that exists of path, this second plate has flat overall shape and parallel with the plate that limits path;
-described structure is by stacked formation of ripple heat-exchange fin group, and each can be separated by second plate adjacent ripple heat-exchange fin group;
-described structure is formed by the monolithic entity that comprises a plurality of passages;
-passage has the hydraulic diameter of 1-6mm;
-passage has the hydraulic diameter of 200 μ m-1mm;
-passage has the hydraulic diameter less than 200 μ m;
-path has the height of 3-18mm;
-described passage has the cross section of circle, ellipse, square, rectangle, triangle or rhombus.
Another theme of the present invention is a kind of cryogenic separation that comprises at least one aforesaid heat exchanger.
Another theme of the present invention is a kind of air separation equipment, and wherein, main heat exchange pipe and/or evaporative condenser and/or subcooler are aforesaid heat exchangers.
Description of drawings
The present invention is described below with reference to the accompanying drawings in further detail, wherein:
The perspective view of the partly cut-away of an example of Fig. 2 illustrates that the present invention is suitable for this heat exchanger with conventional structure;
The path according to the heat exchanger of prior art that Fig. 3 A, 4A and 5A have described that longshore current body flow direction looks, Fig. 3 B, 4B, 4C and 5B described the path according to heat exchanger of the present invention that longshore current body flow direction is looked.
The specific embodiment
In Fig. 2, shown in heat exchanger 1 comprise the identical parallel rectangle plate 2 of a pile, these plates 2 are limited with a plurality of paths that are used to make fluid to be in the indirect heat exchange relation betwixt.In the example shown, these paths are to be used for the path 3 of first fluid, the path 5 that is used for the path 4 of second fluid and is used for the 3rd fluid in succession and circularly.It will be appreciated that the present invention is contained the heat exchanger that includes only two kinds of fluids or comprised the heat exchanger of the fluid of any kind of number.
The side of each path 3-5 is provided with the sealing lath 6 that defines this path, and inlet/outlet 7 is opened wide for corresponding fluid.In each path, have at interval ripple or corrugated fin 8, its as hot fin, particularly when the soldering as the distance piece between the described plate and when using compression fluid as the method for any distortion that prevents plate and the guiding piece that flows as the guiding fluid.
Plate heap, sealing lath and interval ripple are made by aluminum or aluminum alloy usually, and assemble in single operation by furnace brazing.
Fluid intake/the downstream chamber 9 that with overall shape is semicylinder then is welded to the heat exchanger body, like this, inlet/outlet chamber 9 is assembled on the inlet/outlet hole of respective row, and is connected on the pipe 10 of supply and discharge fluid.
---for example those technology of being described in " Micro é changeurs thermiques " by Anton GRUSS in " Techniques de l ' Ing é nieur, 06-2002 "---forms passage can to use various technology.
The scheme use pattern of Fig. 3 B is identical but a plurality of ripple heat-exchange fin groups 13 that fin height is shorter replace traditional ripple heat-exchange fin group of using among Fig. 3 A.These insert a path of heat exchanger and are that the thin plate that the new fins set utilization in the same path is coated with brazing metal 13 is assembled.These thin plates that are called as " the 3rd area plate " constitute so-called " the 3rd " additional area.In this example, have three separated two thin plates of fins set.
Can use getable on the market all types of corrugated fin group, and only need revise and change the height of fin.Therefore, can adjust all parameters (perforation of thickness, density, fin etc.) of the geometry that constitutes the corrugated fin set type.Other parameter comprises:
● passage in height;
● the quantity of heat exchanger fin in each path;
● the thickness of the 3rd area plate (equaling the thickness of corrugated fin group in theory);
● the shape of the 3rd area plate: be solid or have the perforation of meticulous location.
For this " multistage corrugated fin group " technology, its hydraulic diameter has the identical order of magnitude (1/n-e) with the width of channel of traditional corrugated fin.
Following table provides the increase of comparing with traditional fins set of equal densities of both n for the heat exchange area of multiple fin height:
| Traditional configuration | n *＝2 |
| H path (mm) | E fin (mm) | n (m -1) | w (mm) | H passage (mm) | H fin (mm) | H passage (mm) | The increase of area |
| 5.1 | 0.2 | 551.18 | 1.61 | 4.9 | 2.45 | 2.25 | 19％ |
| 5.1 | 0.3 | 393.7 | 2.26 | 4.8 | 2.45 | 2.15 | 25％ |
| Traditional configuration | n *＝3 | ||||||
| H path (mm) | E fin (mm) | n (m -1) | w (mm) | H passage (mm) | H fin (mm) | H passage (mm) | The increase of area |
| 7.13 | 0.2 | 944.88 | 0.86 | 6.93 | 2.24 | 2.04 | 12％ |
| 7.13 | 0.2 | 629.92 | 1.39 | 6.93 | 2.24 | 2.04 | 24％ |
| Traditional configuration | n *＝4 | ||||||
| H path (mm) | E fin (mm) | n (m -1) | w (mm) | H passage (mm) | H fin (mm) | H passage (mm) | The increase of area |
| 9.63 | 0.2 | 944.88 | 0.86 | 9.43 | 2.26 | 2.06 | 13％ |
| 9.63 | 0.2 | 629.92 | 1.39 | 9.43 | 2.26 | 2.06 | 27％ |
n
*The quantity of the fin of the short transverse of=path (thickness of the 3rd area plate is 0.2mm)
The w=width of channel
The height of h passage=passage
Herein, the height of passage (h passage) is constrained to the minimum 2mm (owing to the reason of soldering) that is.
For identical volume, increase the quantity that is stacked in the fin in the heat exchanger and can increase its manufacturing cost.But installation cost remains unchanged.
The structurized corrugated fin group 17 that the scheme utilization of Fig. 4 B comprises the small size tunnel 19 of a large amount of square cross sections replaces traditional ripple heat-exchange fin group of using among Fig. 4 A.This corrugated fin group can make by extruding.
Described extruding method for making means can imagine channel cross-section (rectangle, triangle, circle, rhombus etc.) arbitrarily.Fig. 4 C illustrates the passage of triangular cross section.
Major parameter comprises the quantity of passage of the height of path, the number of channels of unit passage in height, per 1 meter wide path and all parameters (channel height, width, diameter etc.) relevant with the geometry of employed passage.
This manufacture method also makes can be at passage interpolation fin or small-sized fin in a subtle way, with further increase heat exchange area and/or to discharge liquid.
Passage length (fluid thermal exchange length) can be divided into several corrugated fin pack modules that are crushed to, and each module separates several millimeters far to allow interchannel connection.
The channel geometry that exists three classes to distinguish according to the hydraulic diameter (Dh) of passage:
-Dh and the channel width of traditional corrugated fin group have the passage (w=1/n-e) of the identical order of magnitude;
The scope of-Dh is 200 microns to 1 millimeter a passage (small size tunnel);
-Dh is less than 200 microns passage (microchannel).
The increase of the heat exchange area that three classes mentioned above (channel geometry) are obtained is as follows:
Have the passage (w=1/n-e) of the identical order of magnitude for Dh and the channel width of traditional corrugated fin group, this paper provides for multiple fin height and with respect to the increase of the heat exchange area (se) of the traditional fins set with equal height and equal densities of both n.
| Traditional corrugated fin group h=5.1mm | The structure that extrudes | |||
| n (m -1) | w (mm) | se (m 2/m 2) | H passage (mm) | Increase |
| 551.18 | 1.61 | 7.18 | 2.25 | 19％ |
| 393.7 | 2.26 | 5.51 | 2.25 | 33％ |
| Traditional corrugated fin group h=7.13mm | The structure that extrudes | |||
| n (m -1) | w (mm) | se (m 2/m 2) | H passage (mm) | Increase |
| 944.88 | 0.86 | 14.73 | 0.96 | 40％ |
| 629.92 | 1.39 | 10.48 | 1.53 | 40％ |
| Traditional corrugated fin group h=9.63mm | The structure that extrudes | |||
| n (m -1) | w (mm) | se (m 2/m 2) | H passage (mm) | Increase |
| 944.88 | 0.86 | 19.44 | 0.97 | 43％ |
| 629.92 | 1.39 | 13.63 | 1.69 | 42％ |
For the scope of Dh is 200 microns to 1 millimeter passage (small size tunnel), and this paper provides for multiple fin height and with respect to the equal height and the increase of heat exchange area (se) with conventional wave corrugated fin group of high density n.
| Traditional corrugated fin group h=5.1mm | The structure that extrudes | ||
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 102.36 | 12.36 | 0.2 | 161％ |
| Traditional corrugated fin group h=7.13mm | The structure that extrudes | ||
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 102.36 | 16.84 | 0.2 | 171％ |
| Traditional corrugated fin group h=9.63mm | The structure that extrudes |
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 123.62 | 20.86 | 0.2 | 197％ |
For the passage (microchannel) of Dh less than 200 microns, this paper provides for multiple fin height and with respect to the increase of equal height with the heat exchange area (se) of the conventional wave corrugated fin group with high density n.
| Traditional corrugated fin group h=5.1mm | The structure that extrudes | ||
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 102.36 | 12.36 | 0.05 | 717％ |
| Traditional corrugated fin group h=7.13mm | The structure that extrudes | ||
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 102.36 | 16.84 | 0.05 | 741％ |
| Traditional corrugated fin group h=9.63mm | The structure that extrudes | ||
| n (m -1) | se (m 2/m 2) | H passage (mm) | |
| 1 123.62 | 20.86 | 0.05 | 818％ |
The scheme of Fig. 5 B utilizes the capillary of suitable quantity to replace traditional ripple heat-exchange fin group of using among Fig. 5 A.These capillaries are owing to its shape is easy to arrange in an orderly way.These capillaries are covered with brazing metal and mechanically are assembled into one.
Adjustable parameter comprises the quantity capillaceous of the height of path, diameter capillaceous, thickness capillaceous or every square metre.
This paper provides for multiple fin height and with respect to the increase of the heat exchange area (se) of the conventional wave corrugated fin group of equal densities of both.D
ExtIt is external diameter capillaceous.
| Traditional corrugated fin group | Scheme: every passage in height 7 capillaries | ||
| H path (mm) | n(m -1) | D ext(mm) | The increase of se |
| 5.1 | 551.18 | 1.4 | 50％ |
| 5.1 | 393.7 | 1.4 | 96％ |
| The corrugated fin group of system | Scheme: every passage in height 7 capillaries | ||
| H path (mm) | n(m -1) | D ext(mm) | The increase of se |
| 7.13 | 944.88 | 1.2 | 23％ |
| 7.13 | 629.72 | 1.2 | 73％ |
| Traditional corrugated fin group | Scheme: every passage in height 7 capillaries | ||
| H path (mm) | n(m -1) | D ext(mm) | The increase of se |
| 9.63 | 944.88 | 1.4 | 10％ |
| 9.63 | 629.72 | 1.4 | 57％ |
In each example, for obtaining the increase with respect to the heat exchange area of traditional scheme, diameter capillaceous equals maximum gauge; Less diameter will make the increase of heat exchange area not nearly enough obviously.
Claims (11)
1. brazing plate type heat exchanger, such heat exchanger comprises: a pile limits a plurality of fluid peripheral passages (3 with flat overall shape, 4,5) parallel-plate part (2), define the sealing lath of these paths, be used for to first series of passages (3, the distributor of each path distributing fluids 5), and the device that is used for carrying another fluid to second series path (4), in this heat exchanger, at least one path (3) comprises at least one structurized heat exchange structure (15,17,21), this heat exchange structure forms a plurality of passages (19) on the width of path, each passage (19) or contact with at least two other passages, or with at least one other passage and a plate (2,13) contact, this heat exchanger is characterised in that described structure also forms at least three passages on the height of path.
2. heat exchanger according to claim 1 is characterized in that, described structure is made of a plurality of cylinders (21).
3. according to the described heat exchanger of one of aforementioned claim, it is characterized in that, comprise at least one second plate (13) in path (3) inside, this second plate has flat overall shape and parallel with the plate (2) that limits path.
4. heat exchanger according to claim 1 is characterized in that, described structure is by stacked formation of ripple heat-exchange fin group (15), and each may be separated by second plate (13) adjacent ripple heat-exchange fin group.
5. heat exchanger according to claim 1 is characterized in that, described structure is formed by the monolithic entity that comprises a plurality of passages (19) (17).
6. according to the described heat exchanger of one of aforementioned claim, it is characterized in that passage (19) has the hydraulic diameter of 1-6mm.
7. according to the described heat exchanger of claim 1 to 5, it is characterized in that passage (19) has the hydraulic diameter of 200 μ m-1mm.
8. according to the described heat exchanger of claim 1 to 5, it is characterized in that passage (19) has the hydraulic diameter less than 200 μ m.
9. according to the described heat exchanger of one of aforementioned claim, it is characterized in that described passage (19) has the cross section of circle, ellipse, square, rectangle, triangle or rhombus.
10. a cryogenic separation comprises that at least one is according to the described heat exchanger of one of aforementioned claim.
11. air separation equipment according to claim 10 is characterized in that, main heat exchange pipe and/or evaporative condenser and/or subcooler are according to the described heat exchanger of one of claim 1 to 9.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0551560 | 2005-06-09 | ||
| FR0551560A FR2887020B1 (en) | 2005-06-09 | 2005-06-09 | PLATE HEAT EXCHANGER WITH EXCHANGE STRUCTURE FORMING MULTIPLE CHANNELS IN A PASSAGE |
| PCT/FR2006/050600 WO2006131685A2 (en) | 2005-06-09 | 2006-06-06 | Plate heat exchanger with exchanging structure forming several channels in a passage |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010154708A Division CN101871744A (en) | 2005-06-09 | 2006-06-06 | Plate heat exchanger with exchanging structure forming several channels in a passage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101194137A true CN101194137A (en) | 2008-06-04 |
| CN101194137B CN101194137B (en) | 2010-11-24 |
Family
ID=36424039
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010154708A Pending CN101871744A (en) | 2005-06-09 | 2006-06-06 | Plate heat exchanger with exchanging structure forming several channels in a passage |
| CN2006800202420A Expired - Fee Related CN101194137B (en) | 2005-06-09 | 2006-06-06 | Plate heat exchanger with exchanging structure forming several channels in a passage |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010154708A Pending CN101871744A (en) | 2005-06-09 | 2006-06-06 | Plate heat exchanger with exchanging structure forming several channels in a passage |
Country Status (6)
| Country | Link |
|---|---|
| US (2) | US20080210415A1 (en) |
| EP (1) | EP1899669B1 (en) |
| JP (1) | JP2008545946A (en) |
| CN (2) | CN101871744A (en) |
| FR (1) | FR2887020B1 (en) |
| WO (1) | WO2006131685A2 (en) |
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| CN102015182A (en) * | 2008-04-28 | 2011-04-13 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing a heat exchanger using a spacer piece for holding open the passages of brazed plates and fin exchangers |
| CN102305561A (en) * | 2011-08-16 | 2012-01-04 | 李永堂 | Plate-tube type heat exchanger |
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| CN1080869C (en) * | 1996-04-01 | 2002-03-13 | 缪志先 | Plate type heat exchanger with integral braze-welded structure |
| FR2789165B1 (en) * | 1999-02-01 | 2001-03-09 | Air Liquide | HEAT EXCHANGER, PARTICULARLY PLATE HEAT EXCHANGER OF AN AIR SEPARATION APPARATUS |
| WO2001027552A1 (en) * | 1999-10-08 | 2001-04-19 | Carrier Corporation | A plate-type heat exchanger |
| EP1243886A4 (en) * | 1999-12-27 | 2006-05-03 | Sumitomo Prec Products Company | Plate fin type heat exchanger for high temperature |
| FR2819048B1 (en) * | 2000-12-28 | 2005-08-19 | Air Liquide | WINDED FIN IN HEAT EXCHANGER WITH FLAT PLATES AND CORRESPONDING HEAT EXCHANGER |
| JP3961443B2 (en) * | 2003-04-08 | 2007-08-22 | 本田技研工業株式会社 | Evaporator |
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- 2005-06-09 FR FR0551560A patent/FR2887020B1/en not_active Expired - Fee Related
-
2006
- 2006-06-06 WO PCT/FR2006/050600 patent/WO2006131685A2/en not_active Application Discontinuation
- 2006-06-06 CN CN201010154708A patent/CN101871744A/en active Pending
- 2006-06-06 US US11/916,920 patent/US20080210415A1/en not_active Abandoned
- 2006-06-06 EP EP06778947.9A patent/EP1899669B1/en not_active Not-in-force
- 2006-06-06 CN CN2006800202420A patent/CN101194137B/en not_active Expired - Fee Related
- 2006-06-06 JP JP2008515269A patent/JP2008545946A/en active Pending
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2011
- 2011-10-05 US US13/253,477 patent/US20120090354A1/en not_active Abandoned
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| CN102015182A (en) * | 2008-04-28 | 2011-04-13 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing a heat exchanger using a spacer piece for holding open the passages of brazed plates and fin exchangers |
| CN102015182B (en) * | 2008-04-28 | 2013-06-12 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing a heat exchanger using a spacer piece for holding open the passages of brazed plates and fin exchangers |
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| CN106123484A (en) * | 2015-05-09 | 2016-11-16 | 张周卫 | Cold three stream plate-fin heat exchanger of LNG low-temperature liquefaction three tier structure |
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| CN110214256A (en) * | 2017-02-09 | 2019-09-06 | 斯瓦捷克股份有限公司 | Circular heat exchanger |
| CN109668458A (en) * | 2018-12-20 | 2019-04-23 | 中国航空工业集团公司金城南京机电液压工程研究中心 | A kind of rib of slab declines scale primary surface heat exchanger |
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| CN113474956B (en) * | 2019-02-25 | 2023-01-03 | 乔治洛德方法研究和开发液化空气有限公司 | Device for heat and mass exchange |
| CN114341581A (en) * | 2019-09-13 | 2022-04-12 | 阿法拉伐股份有限公司 | Plate heat exchanger for treating liquid feed |
| CN114341581B (en) * | 2019-09-13 | 2023-11-03 | 阿法拉伐股份有限公司 | Plate heat exchanger for treating liquid feed |
Also Published As
| Publication number | Publication date |
|---|---|
| US20080210415A1 (en) | 2008-09-04 |
| FR2887020B1 (en) | 2007-08-31 |
| EP1899669B1 (en) | 2015-08-12 |
| WO2006131685A3 (en) | 2007-05-18 |
| JP2008545946A (en) | 2008-12-18 |
| WO2006131685A2 (en) | 2006-12-14 |
| CN101194137B (en) | 2010-11-24 |
| FR2887020A1 (en) | 2006-12-15 |
| CN101871744A (en) | 2010-10-27 |
| US20120090354A1 (en) | 2012-04-19 |
| EP1899669A2 (en) | 2008-03-19 |
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