CN104501643B - Tube and shell heat exchanger - Google Patents
Tube and shell heat exchanger Download PDFInfo
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- CN104501643B CN104501643B CN201410826717.1A CN201410826717A CN104501643B CN 104501643 B CN104501643 B CN 104501643B CN 201410826717 A CN201410826717 A CN 201410826717A CN 104501643 B CN104501643 B CN 104501643B
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Abstract
The invention discloses a tube and shell heat exchanger, relates to the technical field of heat exchange, and can solve the technical problem that a solid medium has high possibility of sedimentation in a heat exchanger. According to the heat exchanger, at least two arch-shaped whirl plates are obliquely arranged inside a shell of the heat exchanger; the inclined angles of the arch-shaped whirl plates range from 10 degrees to 30 degrees; the adjacent arch-shaped whirl plates are arranged in a staggered manner. The heat exchanger can reduce the dead volume of a shell pass, and reduces the risk of shell pass blockage caused by solid sedimentation.
Description
Technical field
The present invention relates to technical field of heat exchangers, more particularly, to a kind of shell-and-tube heat exchanger.
Background technology
With economic and industry fast development, countries in the world are faced with energy starved problem, so how efficiently profit
It is the focus of various countries' people's growing interest with the existing energy.Wherein, heat exchanger be a kind of in different temperatures two kinds or two kinds with
The energy-saving equipment of heat transfer between material is realized between upper fluid, will be relatively low to temperature for the heat transfer of fluid higher for temperature
Fluid, is to improve one of capital equipment of energy utilization rate.At present, the wide heat exchanger of application is shell-and-tube heat exchanger, with
Close the wall restrained in the housing as the dividing wall type heat exchanger of heat-transfer area.
Shell-and-tube heat exchanger is typically made up of parts such as housing, heating surface bank, tube sheet, deflection plate (baffle plate) and bobbin carriages.Shell
Body mostly is cylindrical shape, and tube bank is placed in enclosure interior, and tube bank two ends are fixed on tube sheet.Deflection plate is placed in housing, for carrying
The individual heat transfer coefficient of high extratubal fluid, improves shell-side fluid speed, forces fluid by regulation distance repeatedly laterally across tube bank, increases
High current body turbulence level.Wherein, the fluid carrying out heat exchange has two kinds, and one kind is in heat exchange Bottomhole pressure, referred to as tube side fluid；Separately
One kind is flowing, referred to as shell-side fluid outside heat exchanger tube.Fluid often passes through tube bank and is once referred to as a tube side, often passes through housing one
A secondary referred to as shell side.And in traditional shell-and-tube heat exchanger, when entering the fluid solid content in medium in heat exchanger and being higher,
Heat exchanger long-play easily makes solid dielectric form local deposits in heat exchanger, and fluid-pressure drop increases, thus causing
Heat exchange efficiency declines, and can blocking heat exchanger when solid dielectric deposition is serious, leading to whole equipment to be scrapped, thus losing heat exchange
Ability.
Content of the invention
Embodiments of the invention provide a kind of shell-and-tube heat exchanger, can solve the problem that solid dielectric is susceptible in heat exchanger
The technical problem of deposition.
For reaching above-mentioned purpose, embodiments of the invention adopt the following technical scheme that：
A kind of shell-and-tube heat exchanger, the housing of described heat exchanger is tilted to be provided with least two segmental baffles, described
The inclination angle scope of segmental baffle is 10～30 °, adjacent described segmental baffle interlaced arrangement.
Further, described segmental baffle at least includes single segmental baffle, double segmental baffle or three arch bafflings
One of plate form.
Further, be provided with dividing plate at the linear edge of described segmental baffle, along shell-side fluid flow direction, described every
Plate extends back and protrudes from the rear end face of described segmental baffle.
Further, described dividing plate is rectangle, trapezoidal or triangular structure.
Further, in described housing, the edge of the described dividing plate that shell-side fluid is flowed through is set to smooth flat, ripple
Shape wave curved surface or zigzag curved-surface structure.
Further, described dividing plate is provided with through hole.
Further, described dividing plate and the angular range of described segmental baffle are 90～150 °.
Further, the right height of weir of described dividing plate and the ratio range of the left height of weir of described dividing plate are 0～2.
Further, the meansigma methodss of described left and right height of weir and the ratio range of described housing interior diameter are 0.02～0.15.
Further, it is provided with guide shell in the described housing at the shell side inlet of described heat exchanger or/and shell-side outlet, institute
State and in guide shell, be provided with the first helical baffles.
Further, the inclination angle scope of described first spiral flow plate is 15～20 °.
Further, between the annular space sectional area between described guide shell and described housing and described guide shell inner section are amassed
Ratio range be 0.3～3.
Further, the outer wall of described housing is provided with ultrasonic transducer, and the operating frequency of described ultrasonic transducer is
20～30kHz, amplitude is 20～40 μm.
Further, it is additionally provided with the second helical baffles being in tilted layout, described second helical baffles in described housing
Inclination angle scope is 10～30 °.
Further, described second helical baffles and described segmental baffle are alternative expression interval setting.
It is provided with arch hydraulic barrier in the housing of shell-and-tube heat exchanger provided in an embodiment of the present invention, so that shell-side fluid is existed
Flowing in the passage of segmental baffle institute arrangement form in housing, when shell-side fluid flows through every piece of segmental baffle, shell-side fluid
Need to bypass this segmental baffle and just can flow to next block segmental baffle, in the process, because segmental baffle is to shell side
The barrier effect of fluid, makes shell-side fluid turbulence level strengthen；Due to adjacent segmental deflection plate interlaced arrangement, shell-side fluid along by
In the passage that the segmental baffle of multiple interlaced arrangement is formed during flowing, shell-side fluid will become wave flow forward, enter one
Step strengthens the turbulence level of shell-side fluid, thus reducing the risk of the shell side blocking causing due to solid deposition it is ensured that heat exchange
The heat exchange efficiency of device.
Brief description
Fig. 1 is the overall structure diagram of the shell-and-tube heat exchanger described in the embodiment of the present invention one；
Fig. 2 is the partial structural diagram of shell-and-tube heat exchanger described in Fig. 1；
Fig. 3 is the perspective view of the segmental baffle being provided with dividing plate in Fig. 1；
Fig. 4 is the vertical section attachment structure schematic diagram of Fig. 3 median septum and segmental baffle；
Fig. 5 is the partial structural diagram of the shell-and-tube heat exchanger described in the embodiment of the present invention two；
Fig. 6 is the overall structure diagram of the shell-and-tube heat exchanger described in the embodiment of the present invention three.
Reference：
1st, housing, 2, segmental baffle, 3, tube sheet, 4, shell side inlet, 5, shell-side outlet,
6th, heat exchanger tube installing hole, 7, dividing plate, 8, guide shell, the 9, first helical baffles,
10th, ultrasonic transducer, the 11, second helical baffles, 12, anticollision hole.
The left height of weir of a dividing plate；
The right height of weir of b dividing plate；
Angle between θ segmental baffle and dividing plate；
The flow direction of F shell-side fluid.
Specific embodiment
In the embodiment of the present invention, explanatory notes is as described below.
The angle of inclination of segmental baffle：Refer to the acute angle between segmental baffle plane and housing axis, and its openings
To contrary with the flow direction of shell-side fluid.
The angle of inclination of helical baffles：Refer to helical baffles along after the rotation of its radius, between its plane and housing axis
Angle.
Left and right height of weir：Refer to the height at dividing plate both sides of the edge.
Below in conjunction with the accompanying drawings the shell-and-tube heat exchanger described in the embodiment of the present invention is described in detail.
Embodiment one
The present embodiment is a kind of shell-and-tube heat exchanger, and the housing 1 of this heat exchanger is tilted to be provided with least two arch foldings
Stream plate 2, the inclination angle scope of segmental baffle 2 is chosen as 10～30 °, adjacent segmental deflection plate 2 interlaced arrangement.
It is provided with arch hydraulic barrier 2 in the housing 1 of shell-and-tube heat exchanger provided in an embodiment of the present invention, make shell-side fluid
Flow in the formed passage of segmental baffle 2 arrangement, when shell-side fluid flows through every piece of segmental baffle 2, shell-side fluid needs
Bypass this segmental baffle 2 and just can flow to next block segmental baffle 2, in the process, because segmental baffle 2 is to shell side
The barrier effect of fluid, makes shell-side fluid turbulence level strengthen；Due to adjacent segmental deflection plate interlaced arrangement, shell-side fluid along by
In the passage that the segmental baffle 2 of multiple interlaced arrangement is formed during flowing, shell-side fluid will become wave flow forward, enter one
Step strengthens the turbulence level of shell-side fluid, thus reducing the risk of the shell side blocking causing due to solid deposition it is ensured that heat exchange
The heat exchange efficiency of device, as Figure 1-Figure 4.
Specifically, segmental baffle 2 is at least included in single segmental baffle, double segmental baffle or triple segmental baffle
A kind of form.For example, segmental baffle 2 can be chosen as single segmental baffle, double segmental baffle, in triple segmental baffle
Any one, any two kinds of combination, or three kinds of deflection plates are located in housing 1 simultaneously；When there being at least two segmental baffles
When, different types of segmental baffle can be alternately arranged in housing, detailed in Example two, or can combine cloth with subregion
Put.
In the present embodiment, segmental baffle 2 is single segmental baffle, and is provided with the linear edge of segmental baffle 2
Dividing plate 7, along shell-side fluid flow direction, dividing plate 7 extends back and protrudes from the rear end face of segmental baffle 2.When fluid flows through
During dividing plate 7, dividing plate 7 to come to flow shell-side fluid play strengthening disturbance, strengthen fluid turbulence degree effect, thus effectively reducing shell
Journey system dead volume, is reduced the risk of the shell side blocking being caused due to solid deposition, improves process heat transfer and heat exchange efficiency, such as
Shown in Fig. 1-Fig. 4.
Specifically, each segmental baffle 2 can arrange one or more dividing plates 7.Wherein, the shape of dividing plate 7 is permissible
It is chosen as rectangle, trapezoidal or triangular structure, it is of course also possible to the dividing plate 7 using other non-regular shape structures.Dividing plate 7
Setting can reduce or even eliminate the gap between adjacent segmental deflection plate 2, thus reduce being made due to this gap containing rheid
The incidence rate that deposition occurs in housing 1 becoming.
The edge on dividing plate 7 that shell-side fluid is flowed through could be arranged to smooth flat, waveform curved surface or zigzag
Curved-surface structure or other non-regular shape structures.Especially, when this edge is zigzag curved-surface structure, can make
Fluid is not in leakage current and causes solid to deposit, and when flowing through the segmental baffle 2 in dividing plate 7 front, can roll over this arch
Heat exchanger tube on stream plate 2 is fully contacted, and carries out sufficient heat exchange；And laciniation can also destroy the surface tension of fluid,
Reduce local resistance, reduce shell-side pressure drop, so that the nowed forming of fluid is more tended to rule, stablize, be more beneficial for flow of fluid
And heat exchange.
Certain impulsive force can be applied when shell-side fluid flows through dividing plate 7 to this dividing plate 7, flow velocity this impulsive force bigger is more
Greatly, the pressure drop making whole shell side increases, and so that heat exchanger is vibrated in the course of the work, therefore in order to reduce this impact
Power, it is to avoid heat exchanger produces vibration, in the present embodiment, along the thickness direction of dividing plate 7, is provided with several (at least one on dividing plate 7
Individual) through hole, i.e. anticollision hole 12, as shown in Figure 3 and Figure 4, when shell-side fluid flows through dividing plate 7, there is segment fluid flow to pass through anticollision hole
12 flow forward, thus reduce this impulsive force.
Specifically, on dividing plate 7, anticollision hole 12 can be circular hole, square opening or other shapes through hole.Anticollision hole 12 is multiple
When, anticollision hole 12 can be located at the centre of dividing plate 7 height or upper middle position in regular array it is also possible in interlocking up and down
Setting or the arrangement of other irregular forms.
In shell-side fluid flow process, in order to reduce the risk of solids particles precipitate, the heat improving heat transfer process is handed over
Change, and reduce system pressure drop, dividing plate 7 is chosen as 90～150 ° with the angle theta scope of segmental baffle 2, preferably 90～120 °.
In the present embodiment, the right height of weir of dividing plate 7 and the ratio range of left height of weir are 0～2, preferably 0.6～1.2.Work as b/a
When=0, represent right height of weir be highly zero, that is, dividing plate 7 be shaped as triangle.Additionally, by the meansigma methodss of left and right height of weir and housing
The ratio range of 1 internal diameter is chosen as 0.02～0.15, preferably 0.05～0.1.
In industrial practical application engineering, the setting of heat exchanger needs to follow the relevant specification of country, and shell side inlet 4 and shell side go out
Mouth 5 has a certain distance apart from tube sheet 3, and especially when this heat exchanger is in high-temperature and high-pressure conditions, this kind of structure setting is necessary
, but, the region that this structure easily causes shell side inlet 4 and shell-side outlet 5 arrives between corresponding adjacent tube sheet 3 respectively is formed
Dead volume, so that the heat exchanger tube in this region does not have the effect of heat exchange.In order to avoid the generation of this region dead volume phenomenon,
It is provided with guide shell 8 in the housing 1 at shell side inlet 4, be provided with the first helical baffles 9 in guide shell 8, as shown in Figure 1.
Equally, it is provided with guide shell 8 in the housing 1 at shell-side outlet 5, in guide shell 8, be provided with the first helical baffles 9,
First helical baffles 9 form the first helical duct, and wherein, this first helical baffles 9 can be suitable by multiple segmental baffles
Secondary overlap joint forms, as shown in Figure 1.Now, between fluid is flowed through herein between guide shell 8 and housing 1 by shell side inlet 4 first
Gap, then passes sequentially through passage between the first helical duct in the guide shell 8 at shell side inlet 4, two guide shells 8, shell side
Export the first helical duct in the guide shell 8 at 5, finally flow through guide shell 8 at shell-side outlet 5 and at this between housing 1
Gap, housing 1 is flowed out by shell-side outlet 5.
Specifically, the inclination angle scope of the first spiral flow plate 9 can be chosen as 15～20 °.Between guide shell 8 and housing 1
Ratio range between annular space sectional area and guide shell 8 inner section are amassed can be chosen as 0.3～3, preferably 1:1.This ratio model
Enclose the flow velocity that can reasonably control fluid flow in heat exchanger it is ensured that the uniformity of rate of flow of fluid, it is to avoid fluid is going out in local
The risk that existing momentum deviation is larger and causes vibration equipment.
Shell-side fluid in flow process in heat exchanger, in order to effectively reduce the system pressure drop of heat exchanger and blocking further
Risk, heat exchanger also can be changed to vertically place by horizontal positioned.Shell-side fluid can flow from the bottom up or flow from top to down.
But, when fluid flows from top to bottom, flow of fluid can be more beneficial for by the effect of solid particle gravity.
In order to improve the level of disruption of the shell-side fluid of this heat exchanger further, strengthen Turbulence Flow, can also be in housing 1
Outer wall be provided with ultrasonic transducer, as shown in Figure 1.This ultrasonic transducer 10 may be mounted at the bottom of housing 1 outer wall, top
Portion or side etc., with right angle setting or can tilt certain angle.This is the characteristic that make use of ultrasound wave itself, and ultrasound wave is one
Plant the sound wave of altofrequency (under normal circumstances, higher than 20kHZ), its good directionality, penetration capacity is by force it is easy to obtain relatively concentration
Acoustic energy, remote in water transmission distance, can be used for finding range, test the speed, clean, welding, rubble, sterilizing etc..In the present embodiment, surpass
The operating frequency of acoustic wave transducer is 20～30kHz, and amplitude is 20～40 μm.
Depth due to ultrasound wave transmission can be for delivery to fluid media (medium) inside, and direction ecto-entad radially and axially
Propagate, produce the inner walls not only only acting upon with ultrasonic transducer directly contact of ultrasonic disturbance, also can be delivered to shell
In heat exchanger tube tube bank within body 1, therefore, ultrasound wave not only can effectively prevent housing 1 inwall to be difficult deposition of solid particle, changes
The same perturbation action because of ultrasound wave of heat exchange tube fluid (i.e. tube side fluid) within hot device vibrates in radial direction,
And the momentum with shell-side fluid flow direction and axially move, supersonic vibration equally be may also function as to tube side fluid
Effect, and can strengthening process heat transfer, be particularly suited for the situation that heat exchange tube fluid is also containing rheid, now beneficial effect
Fruit becomes apparent from, as shown in Figure 1.
Embodiment two
The present embodiment is that the difference of heat exchanger in another kind of shell-and-tube heat exchanger, with above-described embodiment one is mainly bow
The arrangement mode of shape deflection plate 2 is different.Segmental baffle 2 in shell-and-tube heat exchanger in embodiment one is arranged for monolayer, this
Segmental baffle 2 in shell-and-tube heat exchanger in embodiment is bilayer arrangement, as shown in Figure 5.Certainly, arch folding in the present invention
The arrangement mode of stream plate 2 is not limited to both arrangement forms, can also adopt three layers etc., or the row of other irregular forms
The deflection plate combination arrangement of different structure in mode for cloth, such as embodiment three.
Embodiment three
The present embodiment is also a kind of shell-and-tube heat exchanger, this heat exchanger different from the heat exchanger in above-described embodiment one it
Employ different types of deflection plate, two kinds of deflection plate alternate intervals arrangements or arranged in conjunction in place's mainly housing 1, such as scheme
Shown in 6.
Specifically, it is additionally provided with the second helical baffles 11 being in tilted layout, the second spiral baffling in the housing 1 of this heat exchanger
Plate 11 inclination angle scope is 10～30 °, as shown in fig. 6, this second helical baffles 11 can be by multiple segmental baffles sequentially
Overlap joint forms.
Wherein, the second helical baffles 11 can be alternative expression interval setting with segmental baffle 2, and in figure is not shown.?
Can be to arrange in the form of being combined using two kinds of deflection plate subregions, as shown in Figure 6.
Additionally, segmental baffle 2 can be consistent with the inclination angle of the second helical baffles 11, to ensure shell-side fluid
In flow process fluid momentum in the radial and axial directions keep approximate or consistent it is ensured that the flow stability of fluid.
When both inclination angles are different, the flowing containing rheid can be conducive to, reduce pressure drop, reduce dead volume, thus being conducive to containing solid
The process heat exchange of fluid.
When using arrangement of baffles form as shown in Figure 6, by arranging arcuate deflection plate 2 He in heat exchanger shell 1
The form that second helical baffles 11 combine, gives full play to segmental baffle 1 and the advantage of the second helical baffles 11, strengthening
Flow liquid process disturbance, strengthens turbulence level, effectively reduces the risk of solid deposition, simultaneously strengthening process heat transfer.When arch is rolled over
Stream plate 2 is used alternatingly with the second helical baffles 11 or the benefit that is used in combination also resides in, and shell-side fluid is in the second spiral baffling
The linear velocity in the radial direction of plate 11 is different, fast by antermarginal place flow velocity, low by paracentral place flow velocity, thus holding
Easily cause the inhomogeneities of flow of fluid in helical duct, or bias current, and when with reference to segmental baffle 2, then can be real
The reallocation of existing fluid, enables the fluid of bias current evenly distributed again, effectively prevent the deposition of solid particle.Additionally,
11 two kinds of deflection plates of segmental baffle 2 and the second helical baffles are applied in combination, and can overcome helical baffles to a certain extent
The big problem of pressure drop, for the sensitive technique of pressure drop or fluid, can control fluid-pressure drop in rational scope.
In the description of this specification, specific features, structure, material or feature can be in any one or more realities
Apply in example or example and combine in an appropriate manner.
The above, the only specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, and any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, all should contain
Cover within protection scope of the present invention.Therefore, protection scope of the present invention should described be defined by scope of the claims.
Claims (13)
1. a kind of shell-and-tube heat exchanger is provided with least two arch foldings it is characterised in that the housing of described heat exchanger is tilted
Stream plate, the inclination angle scope of described segmental baffle is 10～30 °, adjacent described segmental baffle interlaced arrangement；Described arch folding
It is provided with dividing plate, along shell-side fluid flow direction, described dividing plate extends back and protrudes from described arch at the linear edge of stream plate
The rear end face of deflection plate；Described dividing plate is provided with through hole.
2. shell-and-tube heat exchanger according to claim 1 is it is characterised in that described segmental baffle at least includes single arch
One of deflection plate, double segmental baffle or triple segmental baffle form.
3. shell-and-tube heat exchanger according to claim 1 is it is characterised in that described dividing plate is rectangle, trapezoidal or triangle
Structure.
4. shell-and-tube heat exchanger according to claim 1 is it is characterised in that institute that in described housing, shell-side fluid is flowed through
The edge stating dividing plate is set to smooth flat, waveform curved surface or zigzag curved-surface structure.
5. shell-and-tube heat exchanger according to claim 1 is it is characterised in that the folder of described dividing plate and described segmental baffle
Angle range is 90～150 °.
6. shell-and-tube heat exchanger according to claim 1 is it is characterised in that the right height of weir of described dividing plate and described dividing plate
The ratio range of left height of weir is 0～2.
7. shell-and-tube heat exchanger according to claim 6 it is characterised in that the meansigma methodss of described left and right height of weir with described
The ratio range of housing inner diameter is 0.02～0.15.
8. the shell-and-tube heat exchanger according to any one of claim 1-7 is it is characterised in that the shell side inlet of described heat exchanger
Or/and it is provided with guide shell in the described housing at shell-side outlet, it is provided with the first helical baffles in described guide shell.
9. shell-and-tube heat exchanger according to claim 8 is it is characterised in that the inclination angle scope of described first helical baffles
For 15～20 °.
10. shell-and-tube heat exchanger according to claim 8 is it is characterised in that between described guide shell and described housing
Ratio range between annular space sectional area and described guide shell inner section are amassed is 0.3～3.
11. shell-and-tube heat exchangers according to any one of claim 1-7 are it is characterised in that the outer wall of described housing is provided with
Ultrasonic transducer, the operating frequency of described ultrasonic transducer is 20～30kHz, and amplitude is 20～40 μm.
12. shell-and-tube heat exchangers according to any one of claim 1-7 incline it is characterised in that being additionally provided with described housing
Tiltedly the second helical baffles of arrangement, described second helical baffles inclination angle scope is 10～30 °.
13. shell-and-tube heat exchangers according to claim 12 are it is characterised in that described second helical baffles and described bow
Shape deflection plate is alternative expression interval setting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410826717.1A CN104501643B (en) | 2014-12-26 | 2014-12-26 | Tube and shell heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410826717.1A CN104501643B (en) | 2014-12-26 | 2014-12-26 | Tube and shell heat exchanger |
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| Publication Number | Publication Date |
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| CN104501643A CN104501643A (en) | 2015-04-08 |
| CN104501643B true CN104501643B (en) | 2017-02-22 |
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| CN201410826717.1A Active CN104501643B (en) | 2014-12-26 | 2014-12-26 | Tube and shell heat exchanger |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106017136B (en) * | 2016-05-13 | 2018-04-24 | 中国海洋石油总公司 | A kind of vertical shell-and-tube heat exchanger |
| CN106440882B (en) * | 2016-11-24 | 2019-01-01 | 郑州大学 | The trapezoidal inclined baffle shell-and-tube heat exchanger of class |
| CN106979716A (en) * | 2017-03-21 | 2017-07-25 | 茂名重力石化装备股份公司 | A kind of three-dimensional deflection plate and shell-and-tube heat exchanger |
| CN107726897A (en) * | 2017-11-17 | 2018-02-23 | 四川沃姆斯科技有限公司 | A kind of shell side formula condenser |
| JP7098512B2 (en) * | 2018-12-03 | 2022-07-11 | 三菱重工業株式会社 | Channel resistor and heat exchanger |
| CN110094995A (en) * | 2019-05-07 | 2019-08-06 | 珠海格力电器股份有限公司 | Case tube heat exchanger and air-conditioner set |
| CN110260687B (en) * | 2019-06-28 | 2024-06-07 | 河南豫氢装备有限公司 | Sheet-shaped series-connection shell-and-tube heat exchanger |
| CN110373315A (en) * | 2019-07-04 | 2019-10-25 | 乐山勤力农业开发有限公司 | A kind of charging heating means of marsh gas fermentation |
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| CN2251431Y (en) * | 1995-12-21 | 1997-04-09 | 山东省沂源县化肥厂 | Column plate for gas-liquid mass transfer |
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| CN103105075A (en) * | 2013-01-24 | 2013-05-15 | 东南大学 | U-shaped tubular condenser of vertical type spiral baffle plate |
| CN103471415A (en) * | 2013-09-23 | 2013-12-25 | 王毓芳 | Parallel-flow low-lying condenser |
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|---|---|---|---|---|
| EP0097587A2 (en) * | 1982-06-17 | 1984-01-04 | Societe Anonyme Des Usines Chausson | Tubular heat exchanger |
| CN2251431Y (en) * | 1995-12-21 | 1997-04-09 | 山东省沂源县化肥厂 | Column plate for gas-liquid mass transfer |
| CN201237459Y (en) * | 2008-06-13 | 2009-05-13 | 路辉 | Assembly type continuous spiral baffle plate heat exchanger |
| CN103105075A (en) * | 2013-01-24 | 2013-05-15 | 东南大学 | U-shaped tubular condenser of vertical type spiral baffle plate |
| CN103471415A (en) * | 2013-09-23 | 2013-12-25 | 王毓芳 | Parallel-flow low-lying condenser |
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| Publication number | Publication date |
|---|---|
| CN104501643A (en) | 2015-04-08 |
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