CN206638065U - Double-dryness split-flow heat-exchanging evaporator - Google Patents
Double-dryness split-flow heat-exchanging evaporator Download PDFInfo
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- CN206638065U CN206638065U CN201720340024.0U CN201720340024U CN206638065U CN 206638065 U CN206638065 U CN 206638065U CN 201720340024 U CN201720340024 U CN 201720340024U CN 206638065 U CN206638065 U CN 206638065U
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- 239000000411 inducer Substances 0.000 claims description 8
- 238000001704 evaporation Methods 0.000 abstract description 22
- 230000008020 evaporation Effects 0.000 abstract description 22
- 239000012530 fluid Substances 0.000 abstract description 9
- 238000000034 method Methods 0.000 abstract description 6
- 230000008569 process Effects 0.000 abstract description 6
- 230000008676 import Effects 0.000 abstract description 3
- 239000012071 phase Substances 0.000 description 36
- 239000000126 substance Substances 0.000 description 15
- 239000007788 liquid Substances 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 230000001965 increasing effect Effects 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The utility model relates to a two dryness fraction reposition of redundant personnel heat transfer evaporimeters, there is the first header of import pipe including the intercommunication, the intercommunication has the second header of outlet pipe, and feed through between first header and second header and parallel arrangement's a plurality of heat exchange tubes, all be equipped with interval arrangement's porose baffle and sclausura baffle in proper order in first header and the second header, porose baffle and sclausura baffle divide equally into a plurality of shunting chambers with the inside of first header and second header, and the heat exchange tube that the porose baffle of next-door neighbour was arranged and is close to import pipe one side is the reposition of redundant personnel heat exchange tube of low dryness fraction, the inlet section of the reposition of redundant personnel heat exchange tube of low dryness fraction stretches into the reposition of redundant personnel intracavity, and with shunt chamber exist the clearance between the inner wall. The evaporation of the two-phase fluid by 'high and low dryness fraction separated flow-dividing heat exchange' is realized in the heat exchange process of the multi-tube pass evaporator, the high dryness fraction obviously enhances heat transfer, the flow resistance can be greatly reduced, and the dryness fraction of the two-phase working medium entering the high dryness fraction flow-dividing heat exchange tube can be automatically adjusted to a certain degree according to the flow.
Description
Technical field
Evaporator shunting technical field of heat exchange is the utility model is related to, more particularly to a kind of double-dryness shunting heat exchange evaporation
Device.
Background technology
Existing heat exchange tubular evaparator, put down substantially with coiled pipe flow arrangement or with some non-porous separator plates structure multitube distance
Row streaming is arranged.Simultaneously because in low mass dryness fraction evaporation process heat exchange efficiency to be present not high for heat exchanger tube, and coiled pipe heat exchange arrangement
When, the evaporation later stage is big with gas-phase working medium ratio, and flow velocity is fast, and evaporator has the shortcomings of overpressure loss is serious.Multitube distance
Parallel flow evaporators, due to deeply suitably the increasing with evaporation process of the heat exchanger tube number in its tube side, therefore pipe internal pressure
Power loss is smaller, but be based on evaporation and heat-exchange rule, parallel flow evaporators still exist when low mass dryness fraction is evaporated heat exchange efficiency compared with
Low, due to using parallel flow arrangement when high mass dryness fraction is evaporated, heat exchange efficiency declines the shortcomings of obvious.Finally because evaporation and heat-exchange is in height
The nucleate boiling area heat exchange efficiency highest of mass dryness fraction, therefore coiled and parallel flow evaporators changing in the evaporation and heat-exchange later stage
Thermal effect is significantly increased, and so as to cause overall heat exchange between evaporator tube side substantially uneven, evaporator heat exchange effect is thus limited
System
Utility model content
The purpose of this utility model is to provide a kind of double-dryness shunting heat exchanging evaporator, can improve resistance pressure drop and change
Hot property.
To realize the purpose of this utility model, adopt the technical scheme that：
A kind of double-dryness shunts heat exchanging evaporator, including is communicated with the first header of inlet tube, is communicated with the of outlet
Two headers and it is communicated between the first header and the second header and some heat exchanger tubes of parallel arrangement, the first header and second
Be equipped with case it is spaced apart successively have hole dividing plate and non-porous separator plate, have hole dividing plate and non-porous separator plate by the first header and second
The inside of header is separated into some branch chambers, and is low mass dryness fraction point close to having hole dividing plate and the heat exchanger tube of close inlet tube side
Heat exchanger tube is flowed, the inducer of low mass dryness fraction shunting heat exchanger tube stretches into branch chamber and gap between the inwall of branch chamber be present.
Liquid refrigerant or low mass dryness fraction working medium enter evaporator from inlet tube, and are repeated in by the first header and second
After header heat exchange, discharged from the outlet of the second header.During evaporation and heat-exchange, working medium is often changed by the heat exchanger tube of a tube side
Heat, the relatively low two-phase working substance of mass dryness fraction can be all formed, subsequently into one of header, incoming two-phase working substance enters one of connection
After the branch chamber of case, flow velocity reduces rapidly, and because working medium gas, liquid density variation is obvious, two-phase working substance in branch chamber is by one
Determine degree to occur to be separated and be mutually layered, wherein gas phase is main up, and liquid phase is mainly in lower section.By non-porous separator plate and there is hole
The double dividing plate tube side structures of dividing plate composition, because the inducer of low mass dryness fraction shunting heat exchanger tube is put in branch chamber, it can effectively hinder gas
Phase working medium is discharged because motional inertia directly shunts heat exchanger tube by low mass dryness fraction, and the low mass dryness fraction shunt heat exchanger tube close to have hole every
Plate arranges and close to inlet tube side, and have hole dividing plate adjacent with this and the non-porous separator plate close to outlet side and this have hole every
Heat exchanger tube between plate then shunts heat exchanger tube for high mass dryness fraction, most of by the pressure differential of two neighboring branch chamber in the header
Mixing portion liquid phase by there is hole dividing plate to enter in adjacent branch chamber, is then entered back into and connected with adjacent branch chamber by gas phase
High mass dryness fraction shunting heat exchanger tube in continue evaporation and heat-exchange, low mass dryness fraction working medium, which enters in low mass dryness fraction shunting heat exchanger tube, to be continued evaporation and changes
Heat, incoming working medium is set to complete the shunting of high mass dryness fraction stream and low mass dryness fraction stream in the header, after a tube side exchanges heat, low mass dryness fraction
Stream and high mass dryness fraction stream are entered in the branch chamber of another header and mixed by heat exchanger tube, continue the double dry of next tube side
Degree shunting heat exchange.Because gas-phase working medium is on the increase in evaporation process, liquid phase working fluid is constantly reduced, therefore streamwise, when
When number of tube passes is incremented by, high mass dryness fraction shunting heat exchange tube number tends to increase in tube side, and low mass dryness fraction isocon pipe number tends in tube side
Reduce, it is remote using high mass dryness fraction nucleate boiling high efficient heat exchanging, strengthen the overall heat exchange that enhancing is initiated, and exchange heat using concurrent flow more
Pipe shunting arrangement, improves the mobile performance of evaporator, improves the working medium distributing uniformity of multitube distance evaporator, stream is greatly lowered
Dynamic resistance, improve evaporator resistance pressure drop and heat exchange property.
Technical scheme is further illustrated below：
It is further to have hole dividing plate to be provided with through hole, regulation pipe is socketed with through hole, regulation pipe is changed towards the shunting of low mass dryness fraction
One end of heat pipe is stretched into branch chamber.By controlling to adjust the length of pipe, the two-phase working substance of different mass dryness fractions is set to drain into next point
Intracavitary is flowed, the two-phase working substance mass dryness fraction that regulation enters in high mass dryness fraction shunting heat exchanger tube, improves shunting heat transfer effect.
It is further through hole at least two, regulation pipe is socketed with each through hole, each regulation pipe is done towards low
The length that one end of degree shunting heat exchanger tube is stretched into branch chamber is different.The two-phase work of different mass dryness fractions is discharged by different regulation pipes
In matter to next branch chamber, further regulation shunts the two-phase working substance mass dryness fraction in heat exchanger tube into high mass dryness fraction.
It is further that the aperture of each through hole is different.The working medium flow that the through hole of different pore size passes through is different, different holes
The through hole in footpath, the length stretched into branch chamber one end of heat exchanger tube is shunted towards low mass dryness fraction plus regulation pipe corresponding to each through hole
Difference, can according to flow to a certain degree automatically adjust into high mass dryness fraction shunting heat exchanger tube in two-phase working substance mass dryness fraction, with reach by
Most gas-phase working medium and small part liquid phase working fluid are diverted into high mass dryness fraction shunting heat exchange pipeline section.
It is further that low mass dryness fraction shunting heat exchanger tube stretches into one end of branch chamber and regulation pipe adjacent thereto is adjusted on edge
The projection of tube hub axis direction is not overlapping.Due to the obstruction below through hole without heat exchanger tube, be easy to through hole aperture and its
The length of upper regulation pipe can carry out large-scale optimization design.
It is further that each heat exchanger tube is close to the first side of the first header with the position that first header connects
Wall, the through hole in the first header are close to the second sidewall of the first header, the first side wall cloth relative with second sidewall
Put, each heat exchanger tube is close to the 3rd side wall of the second header with the position that the second header connects, logical in the second header
Hole is close to the 4th side wall of the second header, and the 3rd side wall and the 4th side wall are positioned opposite.Heat exchanger tube is arranged with inclined side mounting means,
It is connected with header inner chamber at side, has the through hole on the dividing plate of hole to dig in the close opposite side without connection heat exchanger tube,
The regulation pipe run through is connected on through hole, is further ensured that below through hole without the obstruction of heat exchanger tube, be easy to through hole aperture and
The length of regulation pipe can carry out large-scale optimization design thereon.
It is further that each heat exchanger tube is respectively positioned on the first inwall of the first header with the position that the first header connects,
First header is additionally provided with the second inwall being be arranged in parallel with the first inwall, and the spacing between the first inwall and the second inwall is H, low
The length that mass dryness fraction shunting heat exchanger tube stretches into the first header is h, wherein, 2H/3≤h ＜ H；Each heat exchanger tube connects with the second header
Position be respectively positioned on the 3rd inwall of the second header, the second header is additionally provided with the 4th inwall being be arranged in parallel with the 3rd inwall,
Spacing between 3rd inwall and the 4th inwall is T, and the length that low mass dryness fraction shunting heat exchanger tube stretches into the second header is t, wherein,
2T/3≤t ＜ T.Ensuring that incoming working medium can be evaporated heat exchange into low mass dryness fraction isocon, preferably hinder gas-phase working medium by
Directly heat exchanger tube is shunted in motional inertia by low mass dryness fraction to discharge.
It is further the both ends of every heat exchanger tube respectively the first mounting surface with the first header, the of the second header
Two mounting surfaces connect, and the first mounting surface and the second mounting surface are plane.Using plane as heat exchanger tube mounting surface, it is easy to produce
Installation positioning, simplifies production technology.
It is further to have that the periphery of hole dividing plate and non-porous separator plate is rectangular, and has the four of hole dividing plate and non-porous separator plate
Individual corner is fillet.Working fluid flow in header is may advantageously facilitate, prevents the stagnant liquid in corner.
It is further that the first header is communicated with inlet tube close to the side of bottom, and the second header is close to the side at top
It is communicated with outlet.The gas-phase working medium being diverted into high mass dryness fraction shunting heat exchange pipeline section is further improved, improves heat exchange efficiency.
Compared with prior art, the utility model has the advantages that：
The utility model improves heat transfer and the mobile performance of evaporator, and original two is realized during multitube distance evaporator heat exchange
" high and low mass dryness fraction separation shunting heat exchange " evaporation of phase fluid, maintains heat exchange efficiency, high mass dryness fraction stream is significantly strengthened by low mass dryness fraction stream
Heat transfer, and flow resistance can be greatly lowered；The inducer of low mass dryness fraction shunting heat exchanger tube deeply puts in header shunting intracavitary, hinders
Gas phase in header largely enters low mass dryness fraction shunting heat exchanger tube with inertia；By installed in the regulation pipe range having on the bulkhead through-hole of hole
Degree and caliber, it can be automatically adjusted to a certain degree into the two-phase working substance mass dryness fraction in high mass dryness fraction shunting heat exchanger tube according to flow.
Brief description of the drawings
Fig. 1 is the structural representation of the utility model embodiment double-dryness shunting heat exchanging evaporator；
Fig. 2 is enlarged drawing at Fig. 1 I；
Fig. 3 is Fig. 2 A direction views；
Fig. 4 is the partial structural diagram of the utility model embodiment double-dryness shunting heat exchanging evaporator.
Description of reference numerals：
10. inlet tube, 20. first headers, 210. first inwalls, 220. second inwalls, 230. the first side walls, 240. second
Side wall, 30. outlets, 40. second headers, 410. the 3rd inwalls, 420. the 4th inwalls, 430. the 3rd side walls, 440. the 4th sides
Wall, 50. heat exchanger tubes, 510. low mass dryness fractions shunting heat exchanger tubes, 511. inducers, 520. high mass dryness fractions shunting heat exchanger tubes, 60. have hole every
Plate, 610. through holes, 70. non-porous separator plates, 80. branch chambers, 90. regulation pipes.
Embodiment
Embodiment of the present utility model is described in detail below in conjunction with the accompanying drawings：
As shown in figure 1, a kind of double-dryness shunting heat exchanging evaporator, including be communicated with the first header 20 of inlet tube 10, connect
It is connected with the second header 40 of outlet 30 and is communicated between the first header 20 and the second header 40 and some of parallel arrangement change
Be equipped with heat pipe 50, the first header 20 and the second header 40 it is spaced apart successively have hole dividing plate 60 and non-porous separator plate 70, have
The inside of first header 20 and the second header 40 is separated into some branch chambers 80 by hole dividing plate 60 and non-porous separator plate 70, and close to
There is the arrangement of hole dividing plate 60 and the heat exchanger tube 50 close to the side of inlet tube 10 shunts heat exchanger tube 510 for low mass dryness fraction, low mass dryness fraction shunting is changed
The inducer 511 of heat pipe 510 stretches into branch chamber 80 and gap be present between the inwall of branch chamber 80, has hole dividing plate 60 to pacify
It is placed in the front of the non-porous separator plate 70 according to direction of flow.
Liquid refrigerant or low mass dryness fraction working medium enter evaporator from inlet tube 10, and are repeated in by the He of the first header 20
After the heat exchange of second header 40, discharged from the outlet 30 of the second header 40, when import working medium is single-phase liquid, the institute of inlet tube 10
It is only non-porous separator plate 70 in first group of dividing plate of the first header 20, in addition, follow-up each tube side non-porous separator plate 70 and has
Hole dividing plate 60 is applied in combination.During evaporation and heat-exchange, working medium often exchanges heat by the heat exchanger tube 50 of a tube side, can all be formed dry
Relatively low two-phase working substance is spent, subsequently into one of header, incoming two-phase working substance enters the branch chamber 80 of one of header
Afterwards, flow velocity is reduced rapidly, and because working medium gas, liquid density variation is obvious, the two-phase working substance in branch chamber 80 will be sent out to a certain degree
Raw to be separated and be mutually layered, wherein gas phase is main up, and liquid phase is mainly in lower section.By non-porous separator plate 70 and there is hole dividing plate 60
The double dividing plate tube side structures of composition, as shown in Fig. 2 because the inducer 511 of low mass dryness fraction shunting heat exchanger tube 510 puts in branch chamber 80
It is interior, it can effectively hinder gas-phase working medium to be discharged because motional inertia directly shunts heat exchanger tube 510 by low mass dryness fraction, and the low mass dryness fraction point
Stream heat exchanger tube 510 has hole dividing plate 60 adjacent and close to going out close to there is hole dividing plate 60 to arrange and close to the side of inlet tube 10 with this
The non-porous separator plate 70 of mouthful pipe 30 side and this there is the heat exchanger tube 50 between hole dividing plate 60 then to shunt heat exchanger tube 520 for high mass dryness fraction, lead to
Cross the pressure differential of two neighboring branch chamber 80 in the header, most of gas phase is by mixing portion liquid phase, by there is hole dividing plate 60 to enter
Enter in adjacent branch chamber 80, then enter back into the high mass dryness fraction shunting heat exchanger tube 520 connected with adjacent branch chamber 80 and continue to steam
Hair heat exchange, low mass dryness fraction working medium, which enters in low mass dryness fraction shunting heat exchanger tube 510, continues evaporation and heat-exchange, makes incoming working medium complete in the header
Into the shunting of high mass dryness fraction stream and low mass dryness fraction stream, after a tube side exchanges heat, low mass dryness fraction stream and high mass dryness fraction stream pass through heat exchanger tube 50
In into the branch chamber 80 of another header and mix, continue the double-dryness shunting heat exchange of next tube side.Due to evaporation
During gas-phase working medium be on the increase, liquid phase working fluid is constantly reduced, therefore streamwise, when number of tube passes is incremented by, in tube side
The high mass dryness fraction shunting pipe number of heat exchanger tube 520 tends to increase, and low mass dryness fraction isocon pipe number tends to reduce in tube side, utilizes high mass dryness fraction core
State boiling high efficient heat exchanging is remote, strengthens the overall heat exchange that enhancing is initiated, and using the more shunting of heat exchanger tube 50 arrangements of concurrent flow, improve
The mobile performance of evaporator, the working medium distributing uniformity of multitube distance evaporator is improved, flow resistance is greatly lowered, improve evaporation
Device resistance pressure drop and heat exchange property.
In the present embodiment, the first header 20 is communicated with inlet tube 10 close to the side of bottom, and the second header 40 is close to top
The side in portion is communicated with outlet 30, further improves the gas-phase working medium being diverted into high 520 sections of heat exchanger tube of mass dryness fraction shunting, improves
Heat exchange efficiency.
As shown in figure 4, the first header 20 and the second header 40 are designed using big cross-sectional area, make the fluid entered in header
Noticeable deceleration, realize that gas, liquid separates, be constraint with Reynolds number≤10000 in pipe；And the both ends of every heat exchanger tube 50 are respectively
The first mounting surface, the second mounting surface of the second header 70 with the first header 20 connect, and the first mounting surface and the second mounting surface are equal
For plane, using plane as heat exchanger tube mounting surface, it is easy to production installation positioning, simplifies production technology.In the present embodiment,
The cross section of one header 20 and the second header 40 is rectangular, and the cross section of the first header 20 and the second header 40 can also be according to reality
Border is needed using the shape such as cylinder, D types, trapezoidal.
As shown in figure 4, there is the periphery of hole dividing plate 60 and non-porous separator plate 70 and the cross section of header to coordinate, it is also rectangular, and
It is fillet to have four corners of hole dividing plate 60 and non-porous separator plate 70, four of the cross section of the first header 20 and the second header 40
Corner is also fillet, may advantageously facilitate Working fluid flow in header, prevents the stagnant liquid in corner.
As shown in Figure 1 and Figure 4, the first header 20 is provided with the first inwall 210 and the first inwall 210 being connected with heat exchanger tube
The second inwall 220 be arrangeding in parallel, the spacing between the first inwall 210 and the second inwall 220 are H, low mass dryness fraction shunting heat exchange
The length that pipe 510 stretches into the first header 20 is h, wherein, 2H/3≤h ＜ H；Second header 40 is provided with the 3rd be connected with heat exchanger tube
Inwall 410, the 4th inwall 420 being be arranged in parallel with the 3rd inwall 410, the position that each heat exchanger tube connects with the second header 40 are equal
On the 3rd inwall 410 of the second header 40, the second header 40 is additionally provided with the 4th inwall being be arranged in parallel with the 3rd inwall 410
420, the spacing between the 3rd inwall 410 and the 4th inwall 420 is T, and low mass dryness fraction shunting heat exchanger tube 510 stretches into the second header 40
Length is t, wherein, 2T/3≤t ＜ T.Ensuring that incoming working medium can be evaporated heat exchange, more preferable ground resistance into low mass dryness fraction isocon
Gas-phase working medium is hindered to be discharged because motional inertia directly shunts heat exchanger tube 510 by low mass dryness fraction.Low mass dryness fraction shunting heat exchanger tube 510 stretches into
The length of branch chamber 80 can also be arranged to other values according to being actually needed.
As shown in Figure 2 and Figure 4, there is hole dividing plate 60 to be provided with through hole 610, regulation pipe 90, regulation pipe 90 are socketed with through hole 610
Stretched into towards one end of low mass dryness fraction shunting heat exchanger tube 510 in branch chamber 80.By controlling to adjust the length of pipe 90, make different mass dryness fractions
Two-phase working substance drain into next branch chamber 80, regulation enter high mass dryness fraction shunting heat exchanger tube 520 in two-phase working substance mass dryness fraction, carry
Height shunting heat transfer effect.
In the present embodiment, through hole 610 has three, and regulation pipe 90, each regulation pipe 90 are socketed with each through hole 610
The length stretched into towards one end of low mass dryness fraction shunting heat exchanger tube 510 in branch chamber 80 is different, and the aperture of each through hole 610 is not
Together, the aperture of through hole 610 can the optimum organization in the range of 3-10mm.The two-phase of different mass dryness fractions is discharged by different regulation pipes 90
In working medium to next branch chamber 80, the working medium flow that the through hole 610 of different pore size passes through is different, the through hole 610 of different pore size,
The length stretched into plus regulation pipe 90 corresponding to each through hole 610 towards one end of low mass dryness fraction shunting heat exchanger tube 510 in branch chamber 80
Degree is different, can be automatically adjusted to a certain degree according to flow into the two-phase working substance mass dryness fraction in high mass dryness fraction shunting heat exchanger tube 520, with up to
It is diverted into by most gas-phase working medium and small part liquid phase working fluid in high 520 sections of heat exchanger tube of mass dryness fraction shunting.Through hole 610 is also
More than one can be set according to being actually needed, aperture can also be arranged to other values according to being actually needed, the aperture of through hole 610
And the length of regulation pipe 90 can be designed to other combining forms according to the design discharge and load optimal of evaporator.
Low mass dryness fraction shunting heat exchanger tube 510 stretch into branch chamber 80 one end and regulation pipe 90 adjacent thereto along regulation pipe 90
The projection of central axial direction is not overlapping, because the lower section of through hole 610 is without the obstruction of heat exchanger tube, be easy to the aperture of through hole 610 with
And the length of regulation pipe 90 can carry out large-scale optimization design thereon.
In the present embodiment, as shown in Figure 3 and Figure 4, the first header 20 also includes being located at the first inwall 210 and the second inwall
The first side wall 230 and second sidewall 240 between 220, each heat exchanger tube 50 are close to the position that the first header 20 connects
The first side wall 230 of one header 20, the through hole 610 in the first header 20 are close to the second sidewall of the first header 20
240, the first side wall 230 and second sidewall 240 are positioned opposite；With reference to heat exchanger tube, the arrangement side of through hole 610 in the first header 20
Formula, the second header 40 are also included located at the 3rd side wall 430 and the 4th side wall between the 3rd inwall 410 and the 4th inwall 420
440, each heat exchanger tube is close to the 3rd side wall 430 of the second header 40 with the position that the second header 40 connects, positioned at second
Through hole 610 in case 40 is close to the 4th side wall 440 of the second header 40,440 relative cloth of the 3rd side wall 430 and the 4th side wall
Put.Heat exchanger tube row is connected at side with header inner chamber with inclined side mounting means, is had the through hole 610 on hole dividing plate 60 to open
Dig and connecting the regulation pipe 90 run through on the opposite side without connection heat exchanger tube, through hole 610, further ensure that through hole 610
Lower section does not have the obstruction of heat exchanger tube, be easy to through hole 610 aperture and thereon the length of regulation pipe 90 can carry out on a large scale it is excellent
Change design.Heat exchanger tube row can also ensure that low mass dryness fraction shunting heat exchanger tube 510 stretches into according to being actually needed using other mounting means
One end of branch chamber 80 and regulation pipe 90 adjacent thereto are staggeredly arranged in the projection along the central axial direction of regulation pipe 90.
The utility model overcomes coiled pipe flow arrangement or common with common multitube distance parallel flow type arrangement evaporator
Heat exchange efficiency is not high in existing low mass dryness fraction evaporation process, and because evaporation process later stage, heat transfer effect are remarkably reinforced, so as to lead
Between induced evaporation device tube side the shortcomings that overall heat exchange inequality；And coiled pipe flow arrangement evaporator is improved because pipe number is constant
The shortcomings that overpressure loss is serious caused by snakelike flow arrangement；Parallel flow evaporators are improved due to parallel flow arrangement,
Cause to reduce in high mass dryness fraction nucleate boiling region refrigerant flow rate, heat exchange efficiency declines the shortcomings of obvious.Compared with prior art, originally
Utility model does heat exchanger tube mounting surface using plane, is easy to production installation positioning, simplifies production technology；It is double dry using multitube distance
Evaporation and heat-exchange mode is spent, utilizes high mass dryness fraction nucleate boiling high efficient heat exchanging principle, the overall heat exchange of enhanced water evaporation device；Using concurrent flow
More heat exchanger tube shunting arrangements, improve the mobile performance of evaporator, improve the working medium distributing uniformity of multitube distance evaporator, significantly
Reduce flow resistance；Low mass dryness fraction isocon inducer 511 is deeply put in header shunting chamber 80, hinders the gas phase in header with used
Property largely enters low mass dryness fraction stream heat exchanger tube；, can root by installed in the length of regulation pipe 90 and caliber having on the aperture of hole dividing plate 60
According to flow, automatically adjust to a certain degree into the two-phase working substance mass dryness fraction in high mass dryness fraction shunting heat exchanger tube 520, ensure augmentation of heat transfer effect
Fruit.
Each technical characteristic of embodiment described above can be combined arbitrarily, to make description succinct, not to above-mentioned reality
Apply all possible combination of each technical characteristic in example to be all described, as long as however, the combination of these technical characteristics is not deposited
In contradiction, the scope that this specification is recorded all is considered to be.
Embodiment described above only expresses several embodiments of the present utility model, and its description is more specific and detailed,
But therefore it can not be interpreted as the limitation to utility model patent scope.It should be pointed out that the common skill for this area
For art personnel, without departing from the concept of the premise utility, various modifications and improvements can be made, these are belonged to
The scope of protection of the utility model.Therefore, the protection domain of the utility model patent should be determined by the appended claims.
Claims (10)
1. a kind of double-dryness shunts heat exchanging evaporator, it is characterised in that including being communicated with the first header of inlet tube, being communicated with out
Second header of mouthful pipe and it is communicated between first header and second header and some heat exchanger tubes of parallel arrangement,
Be equipped with first header and second header it is spaced apart successively have hole dividing plate and a non-porous separator plate, it is described have hole every
The inside of first header and second header is separated into some branch chambers by plate and the non-porous separator plate, and close to institute
State hole dividing plate and the heat exchanger tube close to the inlet tube side shunts heat exchanger tube for low mass dryness fraction, the low mass dryness fraction shunting is changed
The inducer of heat pipe stretches into the branch chamber and gap be present between the inwall of the branch chamber.
2. double-dryness according to claim 1 shunts heat exchanging evaporator, it is characterised in that described to have hole dividing plate provided with logical
Hole, regulation pipe is socketed with the through hole, and the regulation pipe stretches into described point towards one end of the low mass dryness fraction shunting heat exchanger tube
Flow intracavitary.
3. double-dryness according to claim 2 shunts heat exchanging evaporator, it is characterised in that the through hole at least two,
The regulation pipe is socketed with each through hole, each regulation pipe shunts one end of heat exchanger tube towards the low mass dryness fraction
The length stretched into the branch chamber is different.
4. double-dryness according to claim 3 shunts heat exchanging evaporator, it is characterised in that the aperture of each through hole is not
Together.
5. double-dryness according to claim 2 shunts heat exchanging evaporator, it is characterised in that the low mass dryness fraction shunting heat exchanger tube
Stretch into the branch chamber one end and the regulation pipe adjacent thereto in the projection along the regulation pipe central axial direction not
It is overlapping.
6. double-dryness according to claim 5 shunts heat exchanging evaporator, it is characterised in that each heat exchanger tube with it is described
The position of first header connection is close to the first side wall of first header, and the through hole in first header is equal
Close to the second sidewall of first header, the first side wall and the second sidewall are positioned opposite, each heat exchanger tube
The position connected with second header is close to the 3rd side wall of second header, described in second header
Through hole is close to the 4th side wall of second header, and the 3rd side wall and the 4th side wall are positioned opposite.
7. double-dryness according to claim 1 shunts heat exchanging evaporator, it is characterised in that each heat exchanger tube with it is described
The position of first header connection is respectively positioned on the first inwall of first header, and first header is additionally provided with and described first
The second inwall that inwall be arranged in parallel, the spacing between first inwall and second inwall are H, the low mass dryness fraction shunting
The length that heat exchanger tube stretches into first header is h, wherein, 2H/3≤h ＜ H；Each heat exchanger tube and second header
The position of connection is respectively positioned on the 3rd inwall of second header, and second header is additionally provided with parallel with the 3rd inwall
The 4th inwall set, the spacing between the 3rd inwall and the 4th inwall is T, and the low mass dryness fraction shunting heat exchanger tube is stretched
The length for entering second header is t, wherein, 2T/3≤t ＜ T.
8. the double-dryness shunting heat exchanging evaporator according to any one of claim 1 to 7, it is characterised in that changed described in every
Respectively the first mounting surface with first header, the second mounting surface of second header connect at the both ends of heat pipe, described
First mounting surface and second mounting surface are plane.
9. double-dryness according to claim 8 shunts heat exchanging evaporator, it is characterised in that described to have hole dividing plate and the nothing
The periphery of hole dividing plate is rectangular, and four corners for having hole dividing plate and a non-porous separator plate are fillet.
10. the double-dryness shunting heat exchanging evaporator according to any one of claim 1 to 7, it is characterised in that described first
Case is communicated with the inlet tube close to the side of bottom, and second header is communicated with the outlet close to the side at top.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720340024.0U CN206638065U (en) | 2017-03-31 | 2017-03-31 | Double-dryness split-flow heat-exchanging evaporator |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720340024.0U CN206638065U (en) | 2017-03-31 | 2017-03-31 | Double-dryness split-flow heat-exchanging evaporator |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106839829A (en) * | 2017-03-31 | 2017-06-13 | 仲恺农业工程学院 | Double-dryness split-flow heat-exchanging evaporator |
| CN109987349A (en) * | 2017-12-29 | 2019-07-09 | 南通中集罐式储运设备制造有限公司 | Tank case |
| CN110864568A (en) * | 2018-07-20 | 2020-03-06 | 山东大学 | Design method for balanced flow of side length change heat exchanger |
-
2017
- 2017-03-31 CN CN201720340024.0U patent/CN206638065U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106839829A (en) * | 2017-03-31 | 2017-06-13 | 仲恺农业工程学院 | Double-dryness split-flow heat-exchanging evaporator |
| CN109987349A (en) * | 2017-12-29 | 2019-07-09 | 南通中集罐式储运设备制造有限公司 | Tank case |
| CN110864568A (en) * | 2018-07-20 | 2020-03-06 | 山东大学 | Design method for balanced flow of side length change heat exchanger |
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