CN103615843A - Novel dry-type evaporator and application method thereof - Google Patents
Novel dry-type evaporator and application method thereof Download PDFInfo
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- CN103615843A CN103615843A CN201310597426.5A CN201310597426A CN103615843A CN 103615843 A CN103615843 A CN 103615843A CN 201310597426 A CN201310597426 A CN 201310597426A CN 103615843 A CN103615843 A CN 103615843A
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Abstract
The invention relates to a novel dry-type evaporator and an application method thereof, and overcomes the defects that refrigerant in an existing dry-type evaporator has multiple processes, number of heat-exchanging tubes is basically the same in each process, the heat-exchanging tubes in each process are the same in type, the refrigerant is evaporated with flow velocity and resistance increased during flowing, and adopting of identical flow area and resistance characteristics leads to the situation that the total pressure drop is increased, evaporating temperature is low and heat-exchanging effect is poor. In the application method, special treatment is performed on each process including that number of flow paths is increased and the flow resistance characteristics are lowered along the evaporation flow direction of the evaporator; the number of the heat-exchanging tubes is increased with the increasing number of the flow paths once the same exchanging tubes are adopted, an upper flow path and a lower flow path are in the preferential proportion of 2:3; the diameter of the heat-exchanging tubes is increased by one grade with the increasing number of the flow paths once the heat-exchanging tubes different in diameter are adopted, wherein heat-exchanging areas of the upper flow path and the lower flow path can be the same or adopt the proportion of 5:6. By the design, the flow resistance characteristics and the flow velocity of a heat exchanger can be well matched, heat-exchanging coefficient can be increased by 15%, energy efficiency is improved, consumable materials are saved, and the novel dry-type evaporator is energy saving and efficient.
Description
Technical field
The present invention relates to refrigeration air-conditioner design of heat exchanger, more particularly, particularly relate to the dry evaporator in a kind of refrigerated air-conditioning system, adopt special cold-producing medium flow scheme design, optimize velocity flow profile, reduce along journey pressure drop, belong to field of heat exchangers.
Background technology
Existing dry evaporator has two schemes: the dry evaporator of basic model and U-shaped tube dry type evaporator.Basic model dry evaporator has comprised several flow processs, and by separating every liquid muscle, the heat exchanger tube number of each flow process is the same, heat exchanger tube is the same.U-shaped tube dry type evaporator has comprised two flow processs, and upper flow process and lower flow process, by U-shaped curved connection, have adopted same heat exchanger tube, and heat exchanger tube number too.Whole circulation area is all the same along journey.But the flow velocity of cold-producing medium is but different, and difference is very large, the cold-producing medium mass dryness fraction approximately 20% of evaporator, the mass dryness fraction 100% of outlet.The flow velocity of outlet is 5 times of import, along with evaporating along journey of cold-producing medium, the flow velocity of cold-producing medium is approximately linear to be increased, but the pressure drop that speed produces is to be but 3 power relations to increase, the increase of resistance, evaporating temperature difference before and after causing is large, and the evaporating temperature of leading portion is high, and heat transfer effect can not finely show.What the pressure drop of a whole heat exchanger had can reach 1.5bar, and the evaporating temperature of leading portion can be than high 2 ~ 4 degree of the evaporating temperature in exit, and particularly the heat exchange area of leading portion is large, and overall heat transfer effect loss is serious.
Summary of the invention
For above-mentioned problem: cold-producing medium evaporation gasification flow velocity rises, and cold-producing medium increases along journey pressure drop, causes heat transfer effect to reduce.Propose design of the present invention, optimize the flow pressure drop of cold-producing medium in heat exchanger and distribute: the flowing velocity of each flow process is as far as possible consistent, avoids back segment pressure drop to be greater than leading portion pressure drop.By adjusting on rational heat exchanger tube model collocation and heat exchanger tube number.
This dry evaporator, has comprised end plate, cylindrical shell, heat-exchanging tube bundle, water inlet, delivery port, deflection plate, deflection plate backstay, liquid islocation plate; Wherein heat-exchanging tube bundle carries out subregion by liquid islocation plate, cold-producing medium is subregion from inlet enters, then flow to lower subregion, if any more subregion, flow down successively, finally pass through gas outlet, the heat exchanger tube number of getting subregion is that X, heat exchanger tube diameter are that D1, circulation area are A1, the heat exchanger tube number of lower subregion is that Y, heat exchanger tube diameter are that D2, circulation area are A2,, it is characterized in that: lower subregion flow resistance characteristics is lower than the flow resistance characteristics of upper subregion; The circulation area A1 of upper subregion is less than or equal to the circulation area A2 of lower subregion; The heat exchanger tube diameter D1 of upper subregion is less than or equal to the heat exchanger tube diameter D2 of lower subregion; If any multi partition more, the like.The average flow process of cold-producing medium that guarantees front flow process is close to rear flow process.
Described dry evaporator, it is further characterized in that the heat exchanger tube diameter D1 of described upper subregion equals the heat exchanger tube diameter D2 of lower subregion, the heat exchanger tube of upper subregion is counted the heat exchanger tube that X is less than lower subregion and is counted Y.
Described dry evaporator, is further characterized in that described Y equals 1.2 ~ 2 times of X.
Described heat exchanger tube is counted X and Y, and further feature is that Y is preferably 1.5 times of X.
Described dry evaporator, is further characterized in that the heat exchanger tube diameter D1 of described upper subregion is less than the heat exchanger tube diameter D2 of lower subregion.
Described heat exchanger tube diameter D1 and D2, the heat exchanger tube diameter D1 that is further characterized in that described upper subregion is less than mono-grade of the heat exchanger tube diameter D2 of lower subregion.Heat exchanger tube roughly has following several grades: 6.35mm, 7mm, 7.94mm, 9.52mm, 12.56mm, 15.88mm, 19mm.
Described heat exchanger tube diameter D1 and D2, the heat exchanger tube diameter D1 that is further characterized in that described upper subregion is less than two grades of the heat exchanger tube diameter D2 of lower subregion.Heat exchanger tube roughly has following several grades: 6.35mm, 7mm, 7.94mm, 9.52mm, 12.56mm, 15.88mm, 19mm.
Described dry evaporator, is further characterized in that the cold-producing medium mean flow rate of described upper subregion equals the cold-producing medium flow velocity of lower subregion, error 10%.
The refrigerant managing of this device and oil management are achieved in that two-phase low-pressure low-temperature cold-producing medium and oily mixture enter into first pass by inlet and restrain, cold-producing medium and oily mixture flow to the other end from one end, in flow process, constantly gasification, flow velocity increases; After entering next flow process, because circulation area increases suddenly, the initial flow rate of next flow process is the same with the initial flow rate of a upper flow process, cold-producing medium and oily mixture flow to the other end from one end, constantly gasification, and flow velocity increases, last flowing velocity is the same with the flowing velocity of upper flow process end, refrigerant gas pressure drop before and after having guaranteed is like this almost consistent, and pressure drop minimizes, and the evaporating temperature of cold-producing medium leading portion is unlikely to exceed the too many of back segment; The cold-producing medium being gasified totally flows out from gas outlet, and oil, along with flow of refrigerant, is finally taken out of system by gaseous refrigerant, and in whole process, the variation of the evaporating temperature of cold-producing medium is controlled at 0.5 ° of C left and right.
This programme is with respect to basic model dry evaporator and U-shaped pipe evaporator, according to cold-producing medium, along journey, evaporate, accelerate characteristic mobile, resistance increment, different flow processs, increase along with flow process number, adopted the arrangement mode of heat exchanger tube number increase or adopted large diameter heat exchanger tube, in order to reduce back segment pressure drop, there is original advantage.In whole process, the variation of the evaporating temperature of cold-producing medium is controlled at 0.5 ° of C left and right, can improve heat transfer effect more than 15%.This programme can be used the dry evaporator of dual system equally, and every dry evaporator that utilizes the design philosophy of this programme, all belongs to the scope of protection of the invention.
Accompanying drawing explanation
The left view of Fig. 1, drytype evaporator;
The meaning that in accompanying drawing, each legend mark is expressed as follows:
1----end plate, 2----cylindrical shell, 3----heat-exchanging tube bundle, 4----deflection plate locating hole, 5----liquid islocation plate, 101----bolt hole,
Subregion heat exchanger tube number under subregion, the upper subregion heat exchanger tube of X----number, Y----under the upper subregion of 301----, 302----,
Subregion heat exchanger tube diameter under the upper subregion heat exchanger tube of D1----diameter, D2----
the specific embodiment:
Below in conjunction with accompanying drawing, 1 couple of the present invention is introduced.
On end plate 1, open hole, heat-exchanging tube bundle 3 passes, and both have carried out rising and have connect or weld, the effect of end plate 1 is to cut off cold-producing medium and water, cylindrical shell 2 and end plate 1 welding, be used for cutting off extraneous and inner water, plays pressure-bearing effect, top has a water inlet and a delivery port, water is subject to the effect of deflection plate, washes away heat exchanger tube, enhanced heat exchange, deflection plate locating hole 4 is used for locating the spacing of deflection plate, guarantees that whole process current evenly wash away.Heat-exchanging tube bundle 3 is separated into Liang Ge district by liquid islocation plate 5: upper subregion 301 and lower subregion 302, liquid islocation plate 5 cuts off upper flow process and lower flow process, present case is two flow processs, liquid islocation plate 5 has cut off feed liquor and has given vent to anger, cold-producing medium is subregion 301 from inlet enters, to baffling after the other end to lower subregion 302, from lower subregion 302, flow out mass dryness fraction 100%.
Cold-producing medium and oily management are achieved in that two-phase low-pressure low-temperature cold-producing medium and oily mixture enter into first pass by inlet and restrain, and cold-producing medium and oily mixture flow to the other end from one end, in flow process, and constantly gasification, flow velocity increases; After entering next flow process, because circulation area increases suddenly, the initial flow rate of next flow process is the same with the initial flow rate of a upper flow process, cold-producing medium and oily mixture flow to the other end from one end, constantly gasification, and flow velocity increases, last flowing velocity is the same with the flowing velocity of upper flow process end, refrigerant gas pressure drop before and after having guaranteed is like this almost consistent, and pressure drop minimizes, and the evaporating temperature of cold-producing medium leading portion is unlikely to exceed the too many of back segment; The cold-producing medium being gasified totally flows out from gas outlet, and oil, along with flow of refrigerant, is finally taken out of system by gaseous refrigerant, and in whole process, the variation of the evaporating temperature of cold-producing medium is controlled at 0.5 ° of C left and right.
On the unit of a 60kW, three kinds of designs have been adopted; In the first design, heat exchanger tube has adopted 9.52mm, and the heat exchanger tube number of upper subregion 301 is 52, and the heat exchanger tube number of lower subregion 302 is 78, is 1.5 times of heat exchanger tube number of upper subregion 301.This unit is the cold module machine of a typhoon, the in the situation that of environment temperature 35oC, test, unit inflow temperature 12oC, leaving water temperature 7oC, the mass dryness fraction of dry evaporator import is 18%, and after upper subregion 301, mass dryness fraction is 50%, obtains 3 superheated vapors of spending temperature in the exit of lower subregion 302, the evaporating temperature of upper subregion 301 entrances is that the evaporating temperature of 4.5oC, 302 outlets of upper subregion is 4.3oC, and the evaporating temperature of lower subregion 302 outlets is 4.0oC; The efficiency of whole unit is 3.25, reaches national secondary efficiency.In the second design, heat exchanger tube has adopted different heat exchanger tubes, upper subregion 301 has adopted the heat exchanger tube of 7.94mm, heat exchanger tube number is 60, lower subregion 302 has adopted the heat exchanger tube of 9.52mm, heat exchanger tube number 78, be placed on the air cooling module machine of a 60kW and test, environment temperature 35oC, inflow temperature 12oC, leaving water temperature 7oC, the mass dryness fraction of dry evaporator import is 18%, after upper subregion 301, mass dryness fraction is 51%, in the outlet of lower subregion 302, obtain the superheated vapor of the 3oC degree of superheat, the evaporating temperature of upper subregion 301 entrances is 4.6oC, the evaporating temperature of upper subregion 302 outlets is 4.4oC, the evaporating temperature of lower subregion 302 outlets is 4.2oC, the efficiency of whole unit is 3.29, reaches national secondary efficiency.In the third design, heat exchanger tube has adopted different heat exchanger tubes, upper subregion 301 has adopted the heat exchanger tube of 7.94mm, heat exchanger tube number is 65, lower subregion 302 has adopted the heat exchanger tube of 12.56mm, heat exchanger tube number 65, be placed on the air cooling module machine of a 60kW and test, environment temperature 35oC, inflow temperature 12oC, leaving water temperature 7oC, the mass dryness fraction of dry evaporator import is 18%, after upper subregion 301, mass dryness fraction is 52%, in the outlet of lower subregion 302, obtain the superheated vapor of the 3oC degree of superheat, the evaporating temperature of upper subregion 301 entrances is 4.5oC, the evaporating temperature of upper subregion 302 outlets is 4.3oC, the evaporating temperature of lower subregion 302 outlets is 4.1oC, the efficiency of whole unit is 3.27, reaches national secondary efficiency.
Above-mentioned is the scheme of two flow processs, when flow of refrigerant needs more multipaths, the pressure drop Managed Solution of cold-producing medium remains flow process pressure drop and equals lower flow process, lower flow process employing is more managed number or adopts the more heat exchanger tube of Large Diameter Pipeline, offsets cold-producing medium evaporation and produces flow velocity increase, pressure drop increase.Flow process is more, means that the heat exchanger tube length of each flow process is short, can obtain lower pressure drop like this.
Claims (9)
1. a drytype evaporator, has comprised end plate (1), cylindrical shell (2), heat-exchanging tube bundle (3), water inlet, delivery port, deflection plate, deflection plate backstay (4), liquid islocation plate (5); Wherein heat-exchanging tube bundle (3) carries out subregion by liquid islocation plate (5), cold-producing medium is subregion (301) from inlet enters, then flow to lower subregion (302), if any more subregion, flow down successively, finally pass through gas outlet, the heat exchanger tube number of upper subregion (301) is that X, heat exchanger tube diameter are that D1, circulation area are A1, the heat exchanger tube number of lower subregion (302) is that Y, heat exchanger tube diameter are that D2, circulation area are A2,, it is characterized in that:
1), lower subregion (301) flow resistance characteristics is lower than the flow resistance characteristics of upper subregion (302);
2), the circulation area A1 of upper subregion (301) is less than or equal to the circulation area A2 of lower subregion (302);
3), the heat exchanger tube diameter D1 of upper subregion (301) is less than or equal to the heat exchanger tube diameter D2 of lower subregion (302);
4), if any multi partition more, the like.
2. dry evaporator according to claim 1, it is characterized in that the heat exchanger tube diameter D1 of described upper subregion (301) equals the heat exchanger tube diameter D2 of lower subregion, the heat exchanger tube of upper subregion (301) is counted the heat exchanger tube that X is less than lower subregion (302) and is counted Y.
3. dry evaporator according to claim 2, is characterized in that described Y equals 1.2 ~ 2 times of X.
4. dry evaporator according to claim 3, is characterized in that described Y is preferably 1.5 times of X.
5. dry evaporator according to claim 1, is characterized in that the heat exchanger tube diameter D1 of described upper subregion (301) is less than the heat exchanger tube diameter D2 of lower subregion (302).
6. dry evaporator according to claim 5, the heat exchanger tube diameter D1 that it is characterized in that described upper subregion (301) is less than mono-grade of the heat exchanger tube diameter D2 of lower subregion (302).
7. dry evaporator according to claim 5, the heat exchanger tube diameter D1 that it is characterized in that described upper subregion (301) is less than two grades of the heat exchanger tube diameter D2 of lower subregion (302).
8. dry evaporator according to claim 1, is characterized in that the cold-producing medium mean flow rate of described upper subregion (301) equals the cold-producing medium flow velocity of lower subregion (302), error 10%.
9. a using method for dry evaporator described in claim 1, is characterized in that, two-phase low-pressure low-temperature cold-producing medium and oily mixture enter into first pass by inlet and restrain, cold-producing medium and oily mixture flow to the other end from one end, in flow process, constantly gasification, flow velocity increases; After entering next flow process, because circulation area increases suddenly, the initial flow rate of next flow process is the same with the initial flow rate of a upper flow process, cold-producing medium and oily mixture flow to the other end from one end, constantly gasification, and flow velocity increases, last flowing velocity is the same with the flowing velocity of upper flow process end, the refrigerant gas pressure drop of front flow process and rear flow process is almost consistent, minimum pressure drop, and the evaporating temperature of cold-producing medium leading portion exceeds approximately 0.2 ° of the value of back segment; The cold-producing medium being gasified totally flows out from gas outlet, and oil, along with flow of refrigerant, is finally taken out of system by gaseous refrigerant, and in whole process, the variation of the evaporating temperature of cold-producing medium is controlled at 0.5 ° of C left and right.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310597426.5A CN103615843A (en) | 2013-11-22 | 2013-11-22 | Novel dry-type evaporator and application method thereof |
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| CN201310597426.5A CN103615843A (en) | 2013-11-22 | 2013-11-22 | Novel dry-type evaporator and application method thereof |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104819651A (en) * | 2015-04-17 | 2015-08-05 | 广东申菱空调设备有限公司 | Efficient shell tube type heat exchanger and manufacturing method thereof |
| CN105020944A (en) * | 2014-04-25 | 2015-11-04 | 重庆美的通用制冷设备有限公司 | Water chilling unit and heat exchanger thereof |
| CN105202821A (en) * | 2015-11-03 | 2015-12-30 | 维克（天津）有限公司 | Multi-system integrated evaporator |
| CN109489237A (en) * | 2018-11-30 | 2019-03-19 | 青岛海尔空调电子有限公司 | Air conditioner |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2384188Y (en) * | 1999-08-12 | 2000-06-21 | 江苏双良锅炉有限公司 | Reducing flow area heat exchanger |
| JP2002286330A (en) * | 2001-03-28 | 2002-10-03 | Mitsubishi Electric Corp | Condenser |
| CN2594735Y (en) * | 2003-01-06 | 2003-12-24 | 浙江盾安人工环境设备股份有限公司 | Uniform dry evaporator |
| CN201173645Y (en) * | 2008-03-14 | 2008-12-31 | 阿尔西制冷工程技术（北京）有限公司 | Pipe shell type highly effective dry-type evaporator |
| CN103017423A (en) * | 2013-01-08 | 2013-04-03 | 浙江思科国祥制冷设备有限公司 | Dry type evaporator |
-
2013
- 2013-11-22 CN CN201310597426.5A patent/CN103615843A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2384188Y (en) * | 1999-08-12 | 2000-06-21 | 江苏双良锅炉有限公司 | Reducing flow area heat exchanger |
| JP2002286330A (en) * | 2001-03-28 | 2002-10-03 | Mitsubishi Electric Corp | Condenser |
| CN2594735Y (en) * | 2003-01-06 | 2003-12-24 | 浙江盾安人工环境设备股份有限公司 | Uniform dry evaporator |
| CN201173645Y (en) * | 2008-03-14 | 2008-12-31 | 阿尔西制冷工程技术（北京）有限公司 | Pipe shell type highly effective dry-type evaporator |
| CN103017423A (en) * | 2013-01-08 | 2013-04-03 | 浙江思科国祥制冷设备有限公司 | Dry type evaporator |
Non-Patent Citations (1)
| Title |
|---|
| 陈振选: "《空调与制冷系统问答》", 31 July 2007, 化学工业出版社 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105020944A (en) * | 2014-04-25 | 2015-11-04 | 重庆美的通用制冷设备有限公司 | Water chilling unit and heat exchanger thereof |
| CN105020944B (en) * | 2014-04-25 | 2019-08-30 | 重庆美的通用制冷设备有限公司 | Water cooler and its heat exchanger |
| CN104819651A (en) * | 2015-04-17 | 2015-08-05 | 广东申菱空调设备有限公司 | Efficient shell tube type heat exchanger and manufacturing method thereof |
| CN105202821A (en) * | 2015-11-03 | 2015-12-30 | 维克（天津）有限公司 | Multi-system integrated evaporator |
| CN109489237A (en) * | 2018-11-30 | 2019-03-19 | 青岛海尔空调电子有限公司 | Air conditioner |
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Application publication date: 20140305 |