CN208313109U - A kind of outer siphon plate-fin heat exchanger of multi-stag - Google Patents
A kind of outer siphon plate-fin heat exchanger of multi-stag Download PDFInfo
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- CN208313109U CN208313109U CN201820759196.6U CN201820759196U CN208313109U CN 208313109 U CN208313109 U CN 208313109U CN 201820759196 U CN201820759196 U CN 201820759196U CN 208313109 U CN208313109 U CN 208313109U
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Abstract
The utility model discloses siphon plate-fin heat exchangers outside a kind of multi-stag, belong to field of chemical equipment.In the heat exchanger, the propylene stream for being used to provide cooling capacity is continually entered in multistage Siphon pot from inlet tube, propylene stream is set to fill the liquid bath at top, then the indentation, there from the liquid bath head slab is overflowed, into the liquid bath of lower section, and the liquid bath in multistage Siphon pot at different height and bottom liquid bath lower space are filled one by one.The heat exchanging segment that mutually level logistics passes through same pipeline caliber and the connecting tube input heat exchanger body interior different height of equivalent length in liquid bath at different height.Then in the fin of heat exchanging segment, propylene stream carries out heat exchange condensation to ethylene cryogen, and the gas-liquid mixture for the evaporation that exchanges heat is exported from gas-liquid two-phase to be discharged.Special tectonic in above-mentioned heat exchanger apparatus ensure that the import hydrostatic head of the heat exchanging segment of input different height and levels pressure are equal, therefore heat transfer temperature difference in each heat exchanging segment and siphon condition are also identical.
Description
Technical field
The utility model belongs to field of chemical equipment, and in particular to a kind of outer siphon plate-fin heat exchanger of multi-stag.
Background technique
Dehydrogenating propane device, ethylene unit in the process of part, ethylene are the important cryogen of entire engineering.Low temperature ethylene compression
Afterwards it is generally necessary to condense between -33~-34 DEG C, then throttling is provided for multiple temperature gradient cryogens for various heat exchange device cold
Amount.Compressed ethylene generallys use low pressure propylene and provides cooling capacity.The pressure of low pressure propylene usually control for gauge pressure 50~
70kpa, boiling point are usually -37 DEG C or so.The integral temperature difference of ethylene condensing heat exchanger is about 3 DEG C, and the liquid level of propylene increases, and leads
The surface pressing for entering heat exchanger liquid propene is caused to increase, so as to cause the rising of propylene boiling point.The rising of propylene boiling point will lead to this
The heat exchanger integral temperature difference is decreased obviously, and is increased so as to cause heat-transfer surface needed for heat exchanger.And in the prior art, to reduce high liquid
Influence of the position to the temperature difference, heat exchanger height is relatively low in design, and number of units is more, and occupied area is larger.Therefore, for such condensation work
Skill, how in the case where guaranteeing temperature difference of heat exchanger, solve the problems, such as condensing heat exchanger number of units is more, manufacturing cost take up an area it is big,
It is a technical problem urgently to be resolved.
Summary of the invention
Utility model aims to solve problems of the prior art, and provide a kind of outer siphon plate of multi-stag
Fin heat exchanger.
Specific technical solution used by the utility model is as follows:
The outer siphon plate-fin heat exchanger of multi-stag comprising multistage plate-fin heat exchanger and multistage Siphon pot；Described is more
The heat exchanger body of grade plate-fin heat exchanger is in the form of a column, and is vertically being in different height equipped with several segments inside heat exchanger body
Heat exchanging segment, every section of heat exchange segment structure is identical, and be equipped with heat exchanger stream inlet and gas-liquid two-phase outlet；The multistage rainbow
Also is provided with several liquid baths for being in different height in the Siphon pot ontology of cucurbitula, each liquid bath by base platform, inclined plate and
Head slab is constituted, base platform and head slab be in it is horizontally disposed, be connected between the two by inclined plate, base platform, tiltedly
Plate, head slab and heat exchanger body inner wall constitute one and provide the groove profile space of the logistics of cooling capacity, the bottom for accommodating
Stream outlet is offered on portion's plate, and the notch of perforation plate body is offered on head slab；The base platform of each liquid bath and top
The difference in height of portion's plate is equal, but the notch upright projection position opened up on the head slab of two neighboring liquid bath is not overlapped；Rainbow
Inlet tube is provided with above the liquid bath at top on cucurbitula ontology；Logistics on the multistage Siphon pot in different height liquid bath
Outlet is connected by connecting tube with the heat exchanger stream inlet of heat exchanging segment at different height on the multistage plate-fin heat exchanger, and
The two is connected in one-to-one correspondence mode；In the effective fin and coupled liquid bath of various heat exchange section between head slab
Difference in height is equal, and the pipe diameter of each connecting tube is identical with equivalent length.
Preferably, each stream outlet is connected to Siphon pot body exterior, and the connection by outlet tube
Pipe one end connects the stream outlet by outlet tube；The pipe diameter and equivalent length phase for the outlet tube that different liquid baths are connected
Together.
Preferably, the length of every section of heat exchanging segment is identical in the multistage plate-fin heat exchanger.
Preferably, effective fin height and heat exchanger in the multistage plate-fin heat exchanger, in every section of heat exchanging segment
The height of stream inlet is identical.
Preferably, the structure of each liquid bath is identical in the multistage Siphon pot.
Preferably, the logistics height of each liquid bath kind storage is identical in the multistage Siphon pot.
Preferably, the notch is opened up in the side of head slab close to heat exchanger body inner wall, and but adjacent two
The notch of a liquid bath opens up not ipsilateral with head slab.
Preferably, the inlet tube height is not less than the head slab height of Siphon pot ontology inner top liquid bath.
The utility model, by special baffle arrangement, forms multiple liquid baths, provides the liquids of cooling capacity in Siphon pot
Flow point multistage enters the heat exchange of heat exchanger different height heat exchanging segment, guarantees that the logistics head height for entering every section of heat exchanging segment is identical, because
Heat transfer temperature difference in this its surface pressing and fin is also able to maintain identical.For heat exchanger in compared with the existing technology, this reality
With novel heat exchange area can be made to increase in short transverse, reduced in the case where guaranteeing that various heat exchange section heat transfer temperature difference is constant
The heat exchanger number of units needed in project reduces field device land occupation, reduces manufacturing cost.
Detailed description of the invention
Fig. 1 is the overall structure diagram of the outer siphon plate-fin heat exchanger of multi-stag；
Fig. 2 is the structural schematic diagram of multistage plate-fin heat exchanger；
Fig. 3 is the structural schematic diagram of multistage Siphon pot；
Fig. 4 is the liquid trough structure schematic diagram in multistage Siphon pot under the visual angle A；
In figure: multistage plate-fin heat exchanger 1, multistage Siphon pot 2, connecting tube 3；
Heat exchanger body 1-1, heat exchanger stream inlet 1-2, gas-liquid two-phase export 1-3, A sections of siphon logistics heat exchange 1-A, B
1-B, C sections of section siphon logistics heat exchange 1-D, E sections of siphon logistics heat exchange of 1-C, D sections of siphon logistics heat exchange siphon logistics heat exchange 1-E；
Siphon pot ontology 2-1, liquid bath 2-2, inlet 2-3, outlet tube 2-4, base platform 2-2-1, inclined plate 2-2-2, top
Portion plate 2-2-3, notch 2-2-4, A outlet tube 2-4-A, B outlet tube 2-4-B, C outlet tube 2-4-C, D outlet tube 2-4-D, E go out
Liquid pipe 2-4-E.
Specific embodiment
The utility model is further elaborated and is illustrated with reference to the accompanying drawings and detailed description.In the utility model
The technical characteristic of each embodiment can carry out the corresponding combination under the premise of not conflicting with each other.
In the present embodiment, part requirements of process is usually required after low temperature ethylene compression -33 using ethylene as cryogen
It is condensed between~-34 DEG C, then throttle and provides cooling capacity for the heat exchanger heat exchanging segment of multiple gradients.Compressed ethylene then uses
Low pressure propylene provides cooling capacity, and the pressure control of low pressure propylene is 50~70kpa of gauge pressure, and boiling point is usually -37 DEG C or so, therefore second
The integral temperature difference of alkene condensing heat exchanger is about 3 DEG C.The characteristics of process ethylene condensation process is propylene boiling temperature and ethylene cold
The temperature difference of solidifying temperature is smaller, and the load that exchanges heat is very big.
The hydrostatic head that propylene liquid level, i.e. head height generate, which will cause propylene boiling point, to be significantly affected, and propylene liquid level increases
When, the boiling temperature of propylene rises, and will lead to the heat exchanger heat transfer temperature difference and is obviously reduced.Temperature difference diminution leads to heat exchange needed for heat exchanger
Device area increases in proportion.Heat exchanger usually height can reach 10m or so, and width and thickness is 1.5m or so.If
Heat exchange area can be made to increase in short transverse, it is possible to reduce the heat exchanger number of units needed in project reduces manufacturing cost.Therefore
Problem to be solved in this project when how to keep the propylene head height of various heat exchange section in heat exchanger.
As shown in Figure 1, main structure includes multistage plate fin heat-exchanging for a kind of multi-stag outer siphon plate-fin heat exchanger
2 two parts of device 1 and multistage Siphon pot.
As shown in Fig. 2, the heat exchanger body 1-1 of multistage plate-fin heat exchanger 1 is in the form of a column, and inside heat exchanger body 1-1
5 sections of heat exchanging segments for being in different height, 1-A, B sections of siphon logistics heat exchange 1- of respectively A sections of siphon logistics heat exchange are equipped with vertical
B, C sections of 1-C, D sections of siphon logistics heat exchange 1-D, E sections of siphon logistics heat exchange siphon logistics heat exchange 1-E, height gradually mention from bottom to up
It rises.Heat exchange fin is equipped with inside every section of heat exchanging segment, internal structure is identical, and heat exchange segment length is identical.Multistage plate fin heat-exchanging
In device 1, effective fin height in every section of heat exchanging segment is identical as the height of heat exchanger stream inlet 1-2.Every section of heat exchanging segment is all provided with
There are heat exchanger stream inlet 1-2 and gas-liquid two-phase outlet 1-3.
As shown in figure 3, the main body of multistage Siphon pot 2 is the Siphon pot ontology 2-1 being in the form of a column, set in Siphon pot ontology 2-1
There are 4 liquid bath 2-2 for being in different height.As shown in figure 4, each liquid bath 2-2 by base platform 2-2-1, inclined plate 2-2-2 and
Head slab 2-2-3 is constituted, base platform 2-2-1 and head slab 2-2-3 be in it is horizontally disposed, pass through inclined plate 2- between the two
2-2 is closed to be connected, and base platform 2-2-1, inclined plate 2-2-2, head slab 2-2-3 and heat exchanger body 1-1 inner wall constitute one
A groove profile space for being used to accommodate propylene stream.The groove profile space bottom is closed, only offers logistics on base platform 2-2-1
Outlet.Each stream outlet is connected to outside Siphon pot ontology 2-1 by the outlet tube 2-4 of identical size, is followed successively by A under upper
Outlet tube 2-4-A, B outlet tube 2-4-B, C outlet tube 2-4-C, D outlet tube 2-4-D.
In addition, offering the notch 2-2-4 of perforation plate body on head slab 2-2-3, enable propylene stream from notch
It flows down.The structure and size of 4 liquid bath 2-2 are all the same, and the difference in height of base platform 2-2-1 and head slab 2-2-3 also phase
Deng.Notch 2-2-4 on head slab 2-2-3 is opened up in the side of head slab 2-2-3, and close in heat exchanger body 1-1
Wall, and but two neighboring liquid bath 2-2 notch 2-2-4 open up it is not ipsilateral with head slab 2-2-3 so that notch 2-2- up and down
4 upright projection position in the horizontal plane is not overlapped.From top notch overflow and under propylene stream will not fall directly into lower section
Notch, but the liquid bath 2-2 of lower section is filled under the water conservancy diversion of lower section head slab 2-2-3.As shown in figure 3, in first liquid bath
From the opening overflow on the left of top flap to second liquid bath, second liquid bath top flap opening setting is protected on right side for logistics
It demonstrate,proves after liquid flooding expires second liquid bath in first liquid bath, is flowed downward out from second liquid bath right hand top plate, to protect
Card liquid stream fills each liquid bath one by one from top to bottom.Liquid bath in multistage Siphon pot controls liquid level by plate and inclined plate,
Its highest liquid level is at the notch 2-2-4 of head slab 2-2-3, therefore the logistics height of each liquid bath 2-2 kind storage is identical.And
And since upper and lower liquid bath is by notch connection, the liquid surface air pressure of each liquid bath is identical.Also ethylene streams fill each liquid bath
Afterwards, into Siphon pot ontology 2-1 bottom space, which also is provided with E outlet tube 2-4-E, and for the bottom space
Its height, which should be controlled, enables its liquid level when filling liquid identical as liquid level in each liquid bath of top.Siphon pot sheet
Inlet tube 2-3 is provided on body 2-1 above the liquid bath 2-2 at top, inlet tube 2-3 height is not less than Siphon pot ontology 2-1
The head slab 2-2-3 height of interior top liquid bath 2-2 enables ethylene streams to flow automatically into each liquid bath.
Since multistage plate-fin heat exchanger 1 and multistage Siphon pot 2 are provided with multilevel structure in the height direction, two
Person, which can cooperate, realizes that vertical heat exchange area increases.Specifically, the object on multistage Siphon pot 2 in different height liquid bath 2-2
The heat exchanger stream inlet 1-2 phase that outflux passes through connecting tube 3 and heat exchanging segment at different height on multistage plate-fin heat exchanger 1
Even, and the two is connected in one-to-one correspondence mode.1-A, B sections of siphon logistics 1-B, C sections of siphon objects of heat exchange of A sections of siphon logistics heat exchange
The heat exchanger stream inlet 1-2 of 1-C, D sections of stream heat exchange 1-D, E sections of siphon logistics heat exchange siphon logistics heat exchange 1-E goes out liquid with A respectively
Pipe 2-4-A, B outlet tube 2-4-B, C outlet tube 2-4-C, D outlet tube 2-4-D, E outlet tube 2-4-E is connected.While in order to guarantee
The logistics head height of various heat exchange section is identical, should ensure that the pipe diameter for the outlet tube 2-4 that different liquid bath 2-2 are connected and works as
Measure the difference in height that length is identical, in effective fin of various heat exchange section and coupled liquid bath 2-2 between head slab 2-2-3
It is equal, and the pipe diameter of each connecting tube 3 and equivalent length are also identical.
Based on the siphon heat-exchange method of siphon plate-fin heat exchanger outside above-mentioned multi-stag, its step are as follows:
The propylene stream for being used to provide cooling capacity is continually entered in multistage Siphon pot 2 from inlet tube 2-3, infuses propylene stream
The liquid bath 2-2 at full top, then overflows at the notch 2-2-4 from liquid bath 2-2 head slab 2-2-3, into the liquid of lower section
Slot 2-2, and the liquid bath 2-2 in multistage Siphon pot 2 at different height and bottom liquid bath lower space are filled one by one.Different height
Mutually level logistics passes through the 3 input heat exchanger ontology of connecting tube of same pipeline caliber and equivalent length in the liquid bath 2-2 at place
The heat exchanging segment of different height inside 1-1.Then in the fin of heat exchanging segment, propylene stream carries out heat exchange condensation to ethylene cryogen,
Gas-liquid mixture after heat exchange evaporation is discharged from gas-liquid two-phase outlet 1-3.Special tectonic in above-mentioned heat exchanger apparatus, ensure that
The import hydrostatic head and surface pressing for inputting the heat exchanging segment of different height are equal, therefore the heat transfer temperature difference in each heat exchanging segment
Also identical.
Embodiment described above is a kind of preferable scheme of the utility model, and so it is not practical to limit
It is novel.Those of ordinary skill in related technical field can be in the case where not departing from the spirit and scope of the utility model
It makes a variety of changes and modification.Therefore all mode technical solutions obtained for taking equivalent substitution or equivalent transformation, all fall within
In the protection scope of the utility model.
Claims (8)
1. a kind of outer siphon plate-fin heat exchanger of multi-stag, which is characterized in that including multistage plate-fin heat exchanger (1) and multistage rainbow
Cucurbitula (2)；The heat exchanger body (1-1) of the multistage plate-fin heat exchanger (1) is in the form of a column, and in heat exchanger body (1-1)
In the heat exchanging segment for being vertically in different height equipped with several segments, every section of heat exchange segment structure is identical, and is equipped with heat exchanger logistics in portion
Entrance (1-2) and gas-liquid two-phase outlet (1-3)；It also is provided in the Siphon pot ontology (2-1) of the multistage Siphon pot (2) several
A liquid bath (2-2) in different height, each liquid bath (2-2) is by base platform (2-2-1), inclined plate (2-2-2) and top
Plate (2-2-3) is constituted, base platform (2-2-1) and head slab (2-2-3) be in it is horizontally disposed, pass through inclined plate between the two
(2-2-2) is connected, in base platform (2-2-1), inclined plate (2-2-2), head slab (2-2-3) and heat exchanger body (1-1)
Wall constitutes one and provides the groove profile space of the logistics of cooling capacity for accommodating, and offers logistics on the base platform (2-2-1) and goes out
Mouthful, the notch (2-2-4) of perforation plate body is offered on head slab (2-2-3)；Base platform (the 2-2- of each liquid bath (2-2)
1) equal with the difference in height of head slab (2-2-3), but opened up on the head slab (2-2-3) of two neighboring liquid bath (2-2)
Notch (2-2-4) upright projection position is not overlapped；It is provided with above the liquid bath (2-2) at top on Siphon pot ontology (2-1)
Inlet tube (2-3)；Stream outlet on the multistage Siphon pot (2) in different height liquid bath (2-2) passes through connecting tube (3) and institute
The heat exchanger stream inlet (1-2) for stating heat exchanging segment at different height on multistage plate-fin heat exchanger (1) is connected, and the two is in one by one
Corresponded manner is connected；In the effective fin and coupled liquid bath (2-2) of various heat exchange section between head slab (2-2-3)
Difference in height it is equal, and the pipe diameter of each connecting tube (3) is identical with equivalent length.
2. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that each stream outlet
It is external that Siphon pot ontology (2-1) is connected to by outlet tube (2-4), and described connecting tube (3) one end is connected by outlet tube (2-4)
Connect the stream outlet；The pipe diameter for the outlet tube (2-4) that different liquid baths (2-2) are connected is identical with equivalent length.
3. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the multistage plate-fin changes
In hot device (1), the length of every section of heat exchanging segment is identical.
4. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the multistage plate-fin changes
In hot device (1), effective fin height in every section of heat exchanging segment is identical as the height of heat exchanger stream inlet (1-2).
5. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the multistage Siphon pot
(2) in, the structure of each liquid bath (2-2) is identical.
6. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the multistage Siphon pot
(2) in, the logistics height of each liquid bath (2-2) kind storage is identical.
7. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the notch (2-2-4)
Opened up in the side of head slab (2-2-3) close to heat exchanger body (1-1) inner wall, and but two neighboring liquid bath (2-2) lack
Mouth (2-2-4) opens up not ipsilateral with head slab (2-2-3).
8. the outer siphon plate-fin heat exchanger of multi-stag as described in claim 1, which is characterized in that the inlet tube (2-3)
Head slab (2-2-3) height of the height not less than Siphon pot ontology (2-1) inner top liquid bath (2-2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820759196.6U CN208313109U (en) | 2018-05-21 | 2018-05-21 | A kind of outer siphon plate-fin heat exchanger of multi-stag |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820759196.6U CN208313109U (en) | 2018-05-21 | 2018-05-21 | A kind of outer siphon plate-fin heat exchanger of multi-stag |
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| CN208313109U true CN208313109U (en) | 2019-01-01 |
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ID=64716195
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| CN201820759196.6U Active CN208313109U (en) | 2018-05-21 | 2018-05-21 | A kind of outer siphon plate-fin heat exchanger of multi-stag |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108592678A (en) * | 2018-05-21 | 2018-09-28 | 杭州中泰深冷技术股份有限公司 | A kind of outer siphon plate-fin heat exchanger of multi-stag and its method |
| CN110627289A (en) * | 2019-10-28 | 2019-12-31 | 中国华电科工集团有限公司 | Low-temperature flue gas heating wastewater concentration system |
-
2018
- 2018-05-21 CN CN201820759196.6U patent/CN208313109U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108592678A (en) * | 2018-05-21 | 2018-09-28 | 杭州中泰深冷技术股份有限公司 | A kind of outer siphon plate-fin heat exchanger of multi-stag and its method |
| CN108592678B (en) * | 2018-05-21 | 2023-09-01 | 杭州中泰深冷技术股份有限公司 | Multistage type outer siphon plate-fin heat exchanger and method thereof |
| CN110627289A (en) * | 2019-10-28 | 2019-12-31 | 中国华电科工集团有限公司 | Low-temperature flue gas heating wastewater concentration system |
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