CN103075846B - Condenser for forcibly transferring heat by reboiling - Google Patents
Condenser for forcibly transferring heat by reboiling Download PDFInfo
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- CN103075846B CN103075846B CN201310013226.0A CN201310013226A CN103075846B CN 103075846 B CN103075846 B CN 103075846B CN 201310013226 A CN201310013226 A CN 201310013226A CN 103075846 B CN103075846 B CN 103075846B
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Abstract
The invention relates to a condenser for forcibly transferring heat by reboiling. The condenser is characterized by comprising a connecting pipe, a current divider, a heat exchanger, a first current dividing pipe and a second current dividing pipe, wherein one end of the connecting pipe is communicated with the air outlet of a compressor; one end of the current divider is communicated with the other end of the connecting pipe; one end of the first current dividing pipe and one end of the second current dividing pipe are communicated with the other end of the current divider respectively; the other end of the first current dividing pipe is communicated with the inlet of the heat exchanger; the other end of the second current dividing pipe is communicated with the heat exchanger; and the distance between a position where the second current dividing pipe is communicated with the heat exchanger and the inlet of the heat exchanger is 0.3-0.62 times of the total length. According to the condenser, heat exchange of a refrigerant is mostly performed in a gas-liquid two-phase region with a large heat exchange coefficient; and meanwhile, condensation heat exchange in the gas-liquid two-phase region is reinforced in a focused way, so that the heat exchange coefficient of the condenser is increased on the whole.
Description
Technical field
The present invention relates to a kind of condenser heat transfer enhancement technology, especially a kind of condenser of boiling enhanced heat transfer again.
Background technology
Condenser is the vitals in refrigeration system, improves condenser thermal transfer coefficient and has important function to raising performance of refrigerant systems, reduction refrigeration plant volume and cost.In middle-size and small-size refrigeration plant, interior logical cold-producing medium generally managed by condenser, and pipe is outer is cooling medium.
At present, in condenser tube, the method for augmentation of heat transfer mainly designs for condensation heat transfer in refrigerant pipe, and the method for employing is mainly extended surface method and fluid rotary method.In fact in refrigeration system, cold-producing medium is cooled through three processes in condenser tube, first process is superheated steam cooling procedure, the heat exchange mode of this process is gas forced convection, second process is gas-liquid two-phase condensation process, this process heat exchange mode is condensation heat transfer, 3rd process is liquid subcooling process, and this process heat exchange mode is liquid forced convertion.In these three processes, the heat exchange amount of superheated steam cooling procedure accounts for 1/3 of the total heat exchange amount of condenser, and heat exchange area accounts for 1/2 of total heat exchange area, and this process intraductal heat exchange coefficient is less, is only 1/10 ~ 1/50 of condensation heat transfer coefficient; Gas-liquid two-phase condensation process heat exchange amount accounts for 2/3 of the total heat exchange amount of condenser, and heat exchange area accounts for 1/2 of total heat exchange area, and this process intraductal heat exchange coefficient is maximum; Liquid subcooling process heat exchange amount is less.Obviously, improve the heat transfer coefficient of condenser, its emphasis is not only the coefficient of heat transfer improving gas-liquid two-phase condensation process, also needs to take effective Improving Measurements to superheated steam cooling procedure.
Summary of the invention
The object of the invention is to overcome the condenser that the deficiencies in the prior art provide a kind of boiling enhanced heat transfer again, refrigerant heat exchanger can be made more to carry out at the Gas-liquid phase region that the coefficient of heat transfer is larger, emphasis is strengthened Gas-liquid phase region condensation heat transfer simultaneously, improves the condenser coefficient of heat transfer on the whole.
In order to achieve the above object, a kind of technology of the present invention is achieved in that it is a kind of condenser of boiling enhanced heat transfer again, it is characterized in that comprising:
Tube connector, one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider, one end of described current divider and the other end UNICOM of described tube connector;
First isocon and the second isocon, one end of described first isocon and the second isocon respectively with the other end UNICOM of current divider; With
Heat exchanger, the other end of described first isocon and the entrance UNICOM of heat exchanger, the other end of described second isocon and heat exchanger UNICOM, the UNICOM position of the second isocon and heat exchanger be 0.3-0.62 times of the total length of heat exchanger from the entrance distance of heat exchanger.
In order to achieve the above object, another kind of technology of the present invention is achieved in that it is a kind of condenser of boiling enhanced heat transfer again, it is characterized in that comprising:
Tube connector, one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider, one end of described current divider and the other end UNICOM of described tube connector;
First isocon, the second isocon and the 3rd isocon, described first isocon, the second isocon
And the 3rd isocon one end respectively with the other end UNICOM of current divider; With
Heat exchanger, the other end of described first isocon and the entrance UNICOM of heat exchanger; The other end of described second isocon and heat exchanger UNICOM, the UNICOM position of the second isocon and heat exchanger be 0.2-0.5 times of the total length of heat exchanger from the entrance distance of heat exchanger; The other end of described 3rd isocon and heat exchanger UNICOM, the UNICOM position of the 3rd isocon and heat exchanger be 0.5-0.8 times of the total length of heat exchanger from the entrance distance of heat exchanger.
Hinge structure of the present invention has the following advantages:
1) the superheated steam heat of cooling load of desuperheating zone reduces, most of superheated steam heat of cooling load transfer plan to the higher Gas-liquid phase region of the coefficient of heat transfer, average heat transfer coefficient raising;
2) add refrigerant superheat steam in gas-liquid two-phase condensation heat transfer process, some liquid refrigerant is seethed with excitement again, and condensation heat transfer is strengthened, and the coefficient of heat transfer improves further;
3) gas-liquid two-phase condensation heat transfer process major part is carried out in the mass dryness fraction scope of heat exchange the best, and the coefficient of heat transfer is improved.
Accompanying drawing explanation
Fig. 1 is the structural representation of the embodiment of the present invention one;
Fig. 2 is the structural representation of the invention process two.
Detailed description of the invention
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and in figure, same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Being exemplary below by the embodiment be described with reference to the drawings, only for explaining invention, and can not limitation of the present invention being interpreted as.
In describing the invention, term " first ", " second " and " the 3rd " only for describing object, and can not be interpreted as instruction or hint relative importance.
Embodiment one
As shown in Figure 1, it is a kind of condenser of boiling enhanced heat transfer again, comprising:
Tube connector 1, one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider 2, one end of described current divider 2 and the other end UNICOM of described tube connector 1;
First isocon 3 and the second isocon 4, one end of described first isocon 3 and the second isocon 4 respectively with the other end UNICOM of current divider 2; With
Heat exchanger 5, the described other end of the first isocon 3 and the entrance UNICOM of heat exchanger 5, the other end of described second isocon 4 and heat exchanger 5 UNICOM, the UNICOM position of the second isocon 4 and heat exchanger 5 be 0.3-0.62 times of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5.In the present embodiment, the UNICOM position of the second isocon 4 and heat exchanger 5 be 0.52 times of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5, also can calculate according to heat exchanger 5 inner refrigerant mass dryness fraction and the UNICOM position of the second isocon 4 and heat exchanger 5 is determined in the change of delivery temperature and pressure at expulsion.
During work, the high temperature refrigerant superheated steam that refrigeration system compressor is discharged enters current divider 2 through tube connector 1 and is divided into two-way, one tunnel first isocon 3 enters in heat exchanger tube from the entrance of heat exchanger 5, forced-convection heat transfer is carried out at superheated steam zone, this part high temperature refrigerant is progressively cooled to dry saturated steam saturation temperature and is entered gas-liquid two-phase condensing zone in superheated steam zone, carry out condensation heat transfer, along with the carrying out of condensation heat transfer, gas-liquid two-phase cold-producing medium mass dryness fraction declines gradually and enters the mass dryness fraction scope of heat exchange the best from tube connector 1, along with the further decline of mass dryness fraction, start off-target heat exchange mass dryness fraction district, now, another road high temperature refrigerant superheated steam through the second isocon 4 the heat exchange tube inlet distance of distance heat exchanger 5 for 0.52 times of total length within the scope of enter the two-phase condensing zone of heat exchanger 5, mix with the cold-producing medium in two-phase section, some liquid refrigerant in two-phase section seethes with excitement again, condensation heat transfer is further strengthened, flowed out after eventually passing cold-zone.
As shown in Figure 2, it is a kind of condenser of boiling enhanced heat transfer again, comprising: tube connector 1, one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider 2, one end of described current divider 2 and the other end UNICOM of described tube connector 1; First isocon 3, second isocon 4 and the 3rd isocon 6, one end of described first isocon 3, second isocon 4 and the 3rd isocon 6 respectively with the other end UNICOM of current divider 2; With heat exchanger 5, the described other end of the first isocon 3 and the entrance UNICOM of heat exchanger 5;
The other end of described second isocon 4 and heat exchanger 5 UNICOM, the UNICOM position of the second isocon 4 and heat exchanger 5 be 0.2-0.5 times of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5, in the present embodiment, the UNICOM position of the second isocon 4 and heat exchanger 5 be 0.48 of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5, also can calculate according to heat exchanger 5 inner refrigerant mass dryness fraction and the UNICOM position of the second isocon 4 and heat exchanger 5 is determined in the change of delivery temperature and pressure at expulsion; The other end of described 3rd isocon 6 and heat exchanger 5 UNICOM, the UNICOM position of the 3rd isocon 6 and heat exchanger 5 be 0.5-0.8 times of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5, in the present embodiment, the UNICOM position of the 3rd isocon 6 and heat exchanger 5 be 0.7 times of the total length of heat exchanger 5 from the entrance distance of heat exchanger 5, also can calculate according to heat exchanger 5 inner refrigerant mass dryness fraction and the UNICOM position of the 3rd isocon 6 and heat exchanger 5 is determined in the change of delivery temperature and pressure at expulsion.
During work, the high temperature refrigerant superheated steam that refrigeration system compressor is discharged enters current divider 2 through tube connector 1 and is divided into two-way, one tunnel first isocon 3 enters in heat exchanger tube from the entrance of heat exchanger 5, forced-convection heat transfer is carried out at superheated steam zone, this part high temperature refrigerant is progressively cooled to dry saturated steam saturation temperature and is entered gas-liquid two-phase condensing zone in superheated steam zone, carry out condensation heat transfer, along with the carrying out of condensation heat transfer, gas-liquid two-phase cold-producing medium mass dryness fraction declines gradually and enters the mass dryness fraction scope of heat exchange the best from tube connector 1, along with the further decline of mass dryness fraction, start off-target heat exchange mass dryness fraction district, now, another road high temperature refrigerant superheated steam is through the two-phase condensing zone of the second isocon 4 at the heat exchange tube inlet distance of distance heat exchanger 5 to be heat exchanger 5 enter within the scope of 0.48 times of total length heat exchanger 5, mix with the cold-producing medium in two-phase section, some liquid refrigerant in two-phase section seethes with excitement again, condensation heat transfer is further strengthened, mass dryness fraction declines again thereupon, now another road high temperature refrigerant superheated steam is through the two-phase condensing zone of the 3rd isocon 6 at the heat exchange tube inlet distance of distance heat exchanger 5 to be heat exchanger 5 enter within the scope of 0.7 times of total length again heat exchanger 5, condensation heat transfer is strengthened, thus reach best mass dryness fraction, flowed out after eventually passing cold-zone.
Although illustrate and describe embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple change, amendment, replacement and distortion to these embodiments when not departing from principle of the present invention and aim, scope of the present invention is by claim and equivalents thereof.
Claims (2)
1. a condenser for boiling enhanced heat transfer again, is characterized in that comprising:
Tube connector (1), one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider (2), one end of described current divider (2) and the other end UNICOM of described tube connector (1); First isocon (3) and the second isocon (4), described first isocon (3) and the second shunting
One end of pipe (4) respectively with the other end UNICOM of current divider (2); With
Heat exchanger (5), the other end of described first isocon (3) and the entrance UNICOM of heat exchanger (5),
The other end of described second isocon (4) and heat exchanger (5) UNICOM, the UNICOM position of the second isocon (4) and heat exchanger (5) be 0.3-0.62 times of the total length of heat exchanger (5) from the entrance distance of heat exchanger (5).
2. a condenser for boiling enhanced heat transfer again, is characterized in that comprising:
Tube connector (1), one end of described tube connector and the exhaust outlet UNICOM of compressor;
Current divider (2), one end of described current divider (2) and the other end UNICOM of described tube connector (1); First isocon (3), the second isocon (4) and the 3rd isocon (6), described first shunting
One end of pipe (3), the second isocon (4) and the 3rd isocon (6) respectively with the other end UNICOM of current divider (2); With
Heat exchanger (5), the other end of described first isocon (3) and the entrance UNICOM of heat exchanger (5);
The other end of described second isocon (4) and heat exchanger (5) UNICOM, the UNICOM position of the second isocon (4) and heat exchanger (5) be 0.2-0.5 times of the total length of heat exchanger (5) from the entrance distance of heat exchanger (5); The other end of described 3rd isocon (6) and heat exchanger (5) UNICOM, the UNICOM position of the 3rd isocon (6) and heat exchanger (5) be 0.5-0.8 times of the total length of heat exchanger (5) from the entrance distance of heat exchanger (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310013226.0A CN103075846B (en) | 2013-01-15 | 2013-01-15 | Condenser for forcibly transferring heat by reboiling |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310013226.0A CN103075846B (en) | 2013-01-15 | 2013-01-15 | Condenser for forcibly transferring heat by reboiling |
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| Publication Number | Publication Date |
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| CN103075846A CN103075846A (en) | 2013-05-01 |
| CN103075846B true CN103075846B (en) | 2015-07-01 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN110094902A (en) * | 2019-05-29 | 2019-08-06 | 珠海格力电器股份有限公司 | Refrigerant flow path and design method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH094941A (en) * | 1995-06-21 | 1997-01-10 | Sanyo Electric Co Ltd | Refrigerating device |
| JPH10103796A (en) * | 1996-09-30 | 1998-04-21 | Sanyo Electric Co Ltd | Steam compression type refrigerating device |
| JPH10111029A (en) * | 1996-10-04 | 1998-04-28 | Sanyo Electric Co Ltd | Vapor compression refrigerator |
| JPH10238894A (en) * | 1997-02-26 | 1998-09-08 | Sanyo Electric Co Ltd | Heat exchanger |
| JP2008256304A (en) * | 2007-04-06 | 2008-10-23 | Daikin Ind Ltd | Refrigerating device |
| JP2010261642A (en) * | 2009-05-01 | 2010-11-18 | Ｓ−Ｓｐｅｃ株式会社 | Condenser and air conditioning device having the same |
-
2013
- 2013-01-15 CN CN201310013226.0A patent/CN103075846B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH094941A (en) * | 1995-06-21 | 1997-01-10 | Sanyo Electric Co Ltd | Refrigerating device |
| JPH10103796A (en) * | 1996-09-30 | 1998-04-21 | Sanyo Electric Co Ltd | Steam compression type refrigerating device |
| JPH10111029A (en) * | 1996-10-04 | 1998-04-28 | Sanyo Electric Co Ltd | Vapor compression refrigerator |
| JPH10238894A (en) * | 1997-02-26 | 1998-09-08 | Sanyo Electric Co Ltd | Heat exchanger |
| JP2008256304A (en) * | 2007-04-06 | 2008-10-23 | Daikin Ind Ltd | Refrigerating device |
| JP2010261642A (en) * | 2009-05-01 | 2010-11-18 | Ｓ−Ｓｐｅｃ株式会社 | Condenser and air conditioning device having the same |
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| CN103075846A (en) | 2013-05-01 |
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