CN204923592U - Forced recirculation formula evaporimeter - Google Patents
Forced recirculation formula evaporimeter Download PDFInfo
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- CN204923592U CN204923592U CN201520674046.1U CN201520674046U CN204923592U CN 204923592 U CN204923592 U CN 204923592U CN 201520674046 U CN201520674046 U CN 201520674046U CN 204923592 U CN204923592 U CN 204923592U
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Abstract
The utility model discloses a forced recirculation formula evaporimeter, including heat exchanger and gas -liquid separation recycling bin, the heat exchanger with gas -liquid separation recycling bin's inner space is through the circulating pipe that rises, decline circulating pipe intercommunication, rise the circulating pipe the lower extreme with the refrigerant of heat exchanger export intercommunication, the upper end with the gaseous phase space intercommunication on gas -liquid separation recycling bin upper portion, the upper end of decline circulating pipe with the liquid phase space intercommunication of gas -liquid separation recycling bin lower part, the lower extreme is in with the setting the circulating pump import intercommunication of heat exchanger bottom, the export of circulating pump with the refrigerant import intercommunication of heat exchanger, the lower extreme of decline circulating pipe still through the bypass valve with the refrigerant import of heat exchanger directly communicates. The utility model discloses having had the characteristics of gravity circulation formula evaporimeter concurrently, having solved the problem that is short of power at some occasion gravity circulation again, the evaporimeter of more traditional form has reduced the heat transfer difference in temperature, and its heat exchange efficiency obviously promotes.
Description
Technical field
The present invention relates to one and relate to refrigerating field, be specifically related to a kind of forced recirculation formula evaporimeter.
Background technology
At present, in industrial refrigeration field, due to the cooling mode that the reasons such as technique often adopt refrigerating medium indirectly to cool, generally adopt shell and tube evaporator as the heat-exchanger rig between cold-producing medium and refrigerating medium, so the heat exchange efficiency of evaporimeter directly determines the operational efficiency of whole refrigeration system.
Conventional refrigerating medium is water, inorganic salt solution, organic liquor or the organic aqueous solution, and in industrial refrigeration system, refrigerating medium requires that temperature is below 0 DEG C usually, so the aqueous solution such as calcium chloride, ethylene glycol, sodium chloride, buck are commonly used in industrial cold-carrying agent.Low temperature, mass concentration and the kinematic viscosity of refrigerating medium are larger, coolant fluid reynolds number Re is declined to a great extent, flow resistance increases, and flow boundary layer and thermal boundary layer thicken, the coefficient of heat transfer of refrigerating medium single-phase flow is significantly declined, thus the heat transfer efficiency of whole heat exchanger is declined to a great extent.
In order to improve the heat transfer effect of refrigerating medium, generally take two kinds of ways: a kind of is the flow velocity improving coolant fluid, and namely the way of enlargement discharge is to strengthen heat exchange; Another kind of then be increase the heat exchange area of heat exchanger; The former will the flow resistance of larger fluid, adds the driving arrangement of fluid and the power consumption of pump, the latter be increase device fabrication cost for cost is in order to make up the decline of heat transfer efficiency, obviously these two kinds of methods are all very uneconomic.Common shell and tube evaporator mainly contains dry evaporator and flooded evaporator two kinds.Dry evaporator cold-producing medium is at heat exchange in-tube evaporation and absorb heat, and refrigerating medium flows outward and release heat at heat exchanger tube; Flooded evaporator is then contrary, and cold-producing medium evaporates outward at heat exchanger tube and absorbs heat, and refrigerating medium is at heat exchange Bottomhole pressure and release heat.In cryogenic refrigerating system, the dynamic and heat transfer conditions analysis from refrigerating medium effluent, adopts refrigerating medium comparatively reasonable at the dry evaporator of heat exchange heat transfer outside a tube, and safe and reliable also compared with full-liquid type of evaporimeter inner refrigerant side oil return.
But also there are some problems when worst cold case uses in conventional dry evaporimeter, as dry evaporator generally adopts segmental baffle, its flow regime of the diverse location of refrigerating medium between deflection plate is very uneven, and there is flow dead, and there is gap between deflection plate and inner walls, cause coolant fluid bypass amount comparatively large, particularly high concentration, high viscosity fluid are then particularly evident, cause heat exchanger heat exchange efficiency to be had a greatly reduced quality; Conventional refrigerant system dry evaporator porch is also had to be not exclusively liquid refrigerant, but there is the gas-liquid two-phase fluid of certain mass dryness fraction, the problem of separatory inequality is there is in evaporimeter, along with constantly carrying out of evaporation, the area that heat exchanger tube inwall can infiltrate liquid refrigerant accounts for that the ratio regular meeting of total heat exchange area is continuous to be reduced, and heat exchange area cannot be fully used.Flooded evaporator heat exchanger tube is immersed in refrigerant liquid completely, in addition the application of full-liquid type high-efficiency evaporating organ pipe, heat exchanger tube surface is made more easily to produce gasification core, the coefficient of heat transfer of managing outer refrigerant side is higher than the coefficient of heat transfer of dry evaporator tube refrigerant side, so refrigeration unit adopts its heat transfer temperature difference of evaporimeter of full-liquid type more obviously than dry evaporator to reduce under normal temperature operating mode, energy-saving effect is obvious; But refrigerating medium is at heat exchange Bottomhole pressure under worst cold case, due to the mass concentration of cryogen and kinematic viscosity all larger, flow boundary layer and thermal boundary layer thicker, the coefficient of heat transfer of refrigerating medium side can be had a strong impact on, thus greatly reduce the heat-transfer effect of flooded evaporator.
Also has a kind of heat siphon type evaporimeter relying on gravity circulation now, it is made up of heat exchanger and gas-liquid separating cycle bucket, gas-liquid separation circulation barrel is positioned at the top of heat exchanger, circulation power is decided by the difference in height between them, very little in the difference in height of some occasion heat exchanger and gas-liquid separating cycle bucket, thus cause its circulation power not enough, greatly reduce the heat exchange efficiency of evaporimeter.
In sum, it is no matter the heat siphon type evaporimeter of dry evaporator, flooded evaporator or gravity circulation, if the heat transfer decay being made up refrigerating medium side or refrigerant side by raising rate of flow of fluid or increase heat exchange area is all uneconomic, so the heat transfer efficiency of evaporimeter under how improving worst cold case, thus promote whole refrigeration system efficiency and the object that can realize economize energy and resource has become a technical barrier.
Summary of the invention
Goal of the invention: the object of the invention is for the deficiencies in the prior art, the forced recirculation formula evaporimeter providing a kind of heat transfer efficiency high.
Technical scheme: forced recirculation formula evaporimeter of the present invention, comprise heat exchanger, with the gas-liquid separation circulation barrel be arranged on above described heat exchanger, described heat exchanger is communicated with by rising circulation pipe, decline circulation pipe with the inner space of described gas-liquid separation circulation barrel, the lower end of described rising circulation pipe is connected with the refrigerant outlet of described heat exchanger, and upper end is communicated with the gas-phase space on described gas-liquid separation circulation barrel top; The upper end of described decline circulation pipe is communicated with the liquid Space of described gas-liquid separation circulation barrel bottom, and lower end is communicated with the pump inlet being arranged on described exchanger base, and described circulation delivery side of pump is communicated with the refrigerant inlet of described heat exchanger; The lower end of described decline circulation pipe is also directly communicated with by the refrigerant inlet of by-passing valve with described heat exchanger.
The present invention further preferably technical scheme is, described gas-liquid separation circulation barrel comprises staving, and be arranged on the adapter of cold-producing medium inlet and the adapter of cold-producing medium gas returning port on described staving top, 3 liquid barriers are also provided with in described staving, wherein the first liquid barrier and the second liquid barrier are separately positioned on the both sides of described cold-producing medium inlet adapter, by the spaced apart of described cold-producing medium inlet adapter with its both sides, third gear liquid plate arranges the below of described cold-producing medium gas returning port, described cold-producing medium gas returning port adapter is separated with the refrigerant liquid be positioned at below described third gear liquid plate.First liquid barrier being set and the second liquid barrier is to block the liquid carried in fluid, avoiding the gas-phase space to top to splash, to realize the effect of gas-liquid separation; The effect that third gear liquid plate is set be in order to when preventing return-air by liquid refrigerant take away.
Preferably, the top of described first liquid barrier, the second liquid barrier is provided with passage near the position at described inner wall of barrel top; The longitudinal length of described third gear liquid plate is 2 ~ 4 times of described cold-producing medium gas returning port tube diameter, and the distance at surface to inner wall of barrel top is at least 1 times of described cold-producing medium gas returning port tube diameter.
Preferably, the outside of described gas-liquid separation circulation barrel is also provided with fluid level control device, for monitoring the liquid level in described gas-liquid separation circulation barrel.
Limit further, the top of described gas-liquid separation circulation barrel is provided with the gas phase tube connector that gas-phase space inner with it is communicated with, bottom is provided with the liquid phase tube connector be communicated with its internal liquid phase space, and described gas phase tube connector is connected with described fluid level control device respectively with liquid phase tube connector.
Preferably, described gas-liquid separation circulation barrel is provided with at least two oil return pipes.
Limit further, the position, lower middle of described gas-liquid separation circulation barrel is provided with the oil return pipe of three differing heights.Owing to being dissolved with a certain amount of refrigeration oil in liquid refrigerant, the mixing material of drawing part of refrigerant and refrigeration oil by oil return pipe gets back to the suction end of compressor, thus the oil return realized in evaporimeter, make the trapped fuel amount in evaporimeter remain on low concentration, reduce the adverse effect because of the higher heat exchanging of refrigeration oil concentration.
Preferably, described heat exchanger comprises housing, be arranged on first tube sheet at described housing two ends, the second tube sheet, and be sealed in described first tube sheet, the first end cap of the second tube sheet side and the second end cap, wherein the inner space of the first end cap is the refrigerant inlet of heat exchanger, and the inner space of the second end cap is the refrigerant outlet of heat exchanger; Be connected with some heat exchanger tubes between described first tube sheet and described second tube sheet, described heat exchanger tube is communicated with the inner space of described first end cap and the second end cap.
Preferably, also deflection plate is provided with in the housing of described heat exchanger, described deflection plate is continuous helical shape flow-guiding structure, and peripheral circumferential is provided with shirt rim, described deflection plate has pore corresponding with described heat exchanger tube, described deflection plate, through described pore, is positioned at its periphery, to the secondary refrigerant liquid water conservancy diversion flowing through its outside by described heat exchanger tube; Described deflection plate also offers tie rod hole, described first tube sheet offers the blind hole corresponding with described tie rod hole, described deflection plate is connected into a black box through described tie rod hole by pull bar, and is fixed on described first tube sheet.
Preferably, the heat exchanger tube entirety arrangement in described heat exchanger shell, in the equal cloth-like of four-quadrant, is arranged in equilateral triangle between any heat exchanger tube and adjacent non-same layer two heat exchanger tube.
Specific works process of the present invention is: in refrigeration systems through throttling refrigerant liquid and enter into gas-liquid separation circulation barrel with certain gas from the adapter of the cold-producing medium inlet on gas-liquid separation circulation barrel top, under the centrifugation of gas-liquid separation circulation barrel inner space, gas is present in the gas-phase space on gas-liquid separation circulation barrel top, refrigerant liquid is stored in the liquid Space of gas-liquid separation circulation barrel bottom, and maintain certain liquid level, refrigerant liquid enters in the refrigerant inlet (i.e. the first end cap) of heat exchanger through decline circulation pipe, enter into again in heat exchanger tube, and carry out heat exchange with the refrigerating medium that heat exchanger tube flows outward, refrigerant liquid in pipe is constantly evaporated to gas and absorbs heat, the cooled cooling of refrigerating medium heat release outside pipe, cold-producing medium becomes the cold-producing medium of gas-liquid mixture phase after heat exchanger tube, and enter in refrigerant outlet (i.e. the second end cap), get back in gas-liquid separation circulation barrel by rising circulation pipe again, the cold-producing medium having flashed to gaseous state flows out from the adapter of cold-producing medium gas returning port, unevaporated refrigerant liquid with constantly take over from cold-producing medium inlet the liquid refrigerant entered and continue to supply in heat exchanger, constantly move in circles, thus realize continuous print kind of refrigeration cycle.
Can circulating pump be closed when cooling load is lower and open by-passing valve, allowing evaporimeter be in gravity circulation state; Can ON cycle pump close by-passing valve when causing when load is larger or because installing space is limited that between gas-liquid separation circulation barrel and heat exchanger, difference in height is less, thus allow evaporimeter be in forced circulation state.
The action principle of gravity circulation state is thermosiphon principle: the cold-producing medium after throttling enters in gas-liquid separation circulation barrel, keep certain liquid column hydrostatic pressure within it, by means of gravity to heat exchanger feed flow, liquid refrigerant absorbs heat in heat exchanger, partial gasification makes heat exchanger two ends import and export liquid and produces density contrast (potential energy is poor), the power that this pressure reduction produces makes cold-producing medium between gas-liquid separation circulation barrel and heat exchanger, realize migration, thus the self-loopa process that realization causes density to change by phase transformation.
When gravity circulation is short of power, by the driving of circulating pump, the mass flowrate of heat exchanger tube inner refrigerant and circulating ratio is improved, thus realize forced circulation state, substantially increase the heat exchange efficiency of evaporimeter.
Beneficial effect: (1) the present invention has had the feature of gravity circulation formula evaporimeter concurrently, solve again the problem be short of power at some occasion gravity circulation, compared with the evaporimeter of traditional form, reduce heat transfer temperature difference, its heat exchange efficiency obviously promotes, under the prerequisite not increasing heat exchanger tube quantity, achieve the raising of heat exchange efficiency, thus the Energy Efficiency Ratio that refrigeration unit is run is improved, realizes energy-conservation object; Also reduce the use amount of heat exchanger tube under can realizing keeping the poor condition of original efficiency, thus realize the object of cost declining, be specially adapted to cryogenic refrigeration occasion;
(2) in heat exchanger of the present invention, deflection plate is helical form guiding device, and the coolant fluid under the guiding of helical baffles outside heat exchanger tube flows in the shape of a spiral, everywhere flow velocity and flow regime even; And be provided with shirt rim in the peripheral circumferential of deflection plate, refrigerating medium can be prevented in the bypass of shell side, the flow resistance of refrigerating medium and bypass amount are reduced greatly, be conducive to the raising of refrigerating medium flow velocity, thus improve the coefficient of heat transfer of refrigerating medium side, be specially adapted to mass concentration and the larger cryogenic liquid of kinematic viscosity;
(3) evaporimeter of the present invention is adopted, its inner refrigerant liquid is far longer than dry evaporator at the contact area ratio of tube side and heat exchanging pipe wall, suitable with full-liquid type, the mass flowrate of heat exchanger tube inner refrigerant and circulating ratio, higher than other forms of evaporimeter, make the coefficient of heat transfer of evaporator refrigerant side significantly improve.
Accompanying drawing explanation
Fig. 1 is the structural representation of forced recirculation formula evaporimeter of the present invention;
Fig. 2 is that the A of Fig. 1 is to side view;
Fig. 3 is that the B of Fig. 1 is to side view;
Fig. 4 is the tube sheet cloth hole pattern of heat exchanger of the present invention;
Wherein 1-first end cap, 2-first bolt, 3-first end cap flange, 4-first sealing gasket, 5-first tube sheet, 6-refrigerating medium suction flange, 7-refrigerating medium entrance sleeve, 8-housing, 9-heat exchanger tube, 10-deflection plate, the emptying valve seat of 11-, 12-refrigerating medium discharge connection, 13-refrigerating medium outlet(discharge) flange, 14-second tube sheet, 15-second sealing gasket, 16-second end cap flange, 17-second bolt, 18-second end cap, 19-bearing, 20-blowdown valve seat, 21-pull bar, 22-decline circulation pipe, 23-first end socket, 24-staving, 25-cold-producing medium gas returning port is taken over, 26-gas phase tube connector, 27-first liquid barrier, 28-cold-producing medium inlet is taken over, 29-second liquid barrier, 30-second end socket, 31-rising circulation pipe, 32-connection bracket, 33-liquid phase tube connector, 34-first oil return pipe, 35-second oil return pipe, 36-the 3rd oil return pipe, 37-pore, 38-tie rod hole, 40-third gear liquid plate, 41-first end cap lower linking tube, 42-circulating pump, 43-by-passing valve, 44-Foundation of steel frame seat.
Detailed description of the invention
Below by accompanying drawing, technical solution of the present invention is described in detail, but protection scope of the present invention is not limited to described embodiment.
embodiment 1:a kind of high efficiency gravity type recirculation-type evaporator, as shown in the figure, comprising: heat exchanger, gas-liquid separation circulation barrel, circulating pump 42 3 part.
Wherein, heat exchanger section comprises: the first end cap 1, first end cap flange 3, first sealing gasket 4, first tube sheet 5, heat exchanger shell 8, refrigerating medium entrance sleeve 7, refrigerating medium suction flange 6, refrigerating medium discharge connection 12, refrigerating medium outlet(discharge) flange 13, heat exchanger tube 9, helical baffles 10, pull bar 21, emptying valve seat 11, blowdown valve seat 20, second tube sheet 14, second end cap 18, second end cap flange 16, second sealing gasket 15.
Gas-liquid separation circulation barrel part comprises: the first end socket 23, second end socket 30, gas-liquid separation circulation barrel staving 24, cold-producing medium gas returning port adapter 25, cold-producing medium inlet adapter 28, first liquid barrier 27, second liquid barrier 29, third gear liquid plate 40, gas phase tube connector 26, liquid phase tube connector 33, first oil return pipe 34, second oil return pipe 35, the 3rd oil return pipe 36.
Be communicated with rising circulation pipe 31 by decline circulation pipe 22, first end cap lower linking tube 41 between heat exchanger with gas-liquid separation circulation barrel; Decline circulation pipe 22 is communicated with circulating pump 42 entrance, the first end cap lower linking tube 41 and circulating pump 42 outlet; Between decline circulation pipe 22 and the first end cap lower linking tube 41, by-passing valve 43 is set and passes through pipeline connection.
Heat exchanger shell 8 two ends are fixedly connected with the first tube sheet 5, second tube sheet 14 respectively, and it is an entirety that the first end cap 1 and the first end cap flange 3 are connected and fixed, and is connected with the first tube sheet 5 by the first bolt 2; It is an entirety that second end cap 18 and the second end cap flange 16 are connected and fixed, and is connected with the second tube sheet 14 by the second bolt 17; The sealing surface that sealing surface between first tube sheet 5 and the first end cap flange 3 is provided with between the first sealing gasket 4, second tube sheet 14 and the second end cap flange 16 is provided with the second sealing gasket 15.Heat exchanger shell 8 outer upper two ends are provided with refrigerating medium entrance sleeve 7 and refrigerating medium discharge connection 12, and one end of refrigerating medium entrance sleeve 7 is communicated with the inside of heat exchanger shell 8, and the other end is provided with refrigerating medium suction flange 6, for the connection with exterior line; One end of refrigerating medium discharge connection 12 is communicated with the inside of heat exchanger shell 8, and the other end is provided with refrigerating medium outlet(discharge) flange 13, for the connection with exterior line.
Heat exchanger shell 8 inside is also provided with helical baffles 10, and helical baffles 10 is provided with the pore 37 corresponding with heat exchanger tube 9, and helical baffles 10 is continuous helical structure, and peripheral circumferential is provided with shirt rim; Heat exchanger tube 9 is internal thread high-efficiency evaporation pipe, and heat exchanger tube 9 is successively through some helical baffles 10, second tube sheet 14 in the first tube sheet 5, heat exchanger shell 8, and the two ends of heat exchanger tube 9 adopt the mode of expanded joint or welding to be connected with the first tube sheet 3, second tube sheet 11; First tube sheet 5 is provided with pull bar retaining thread hole with the joint face of heat exchanger shell 8, helical baffles 10 is provided with the tie rod hole 38 corresponding with pull bar retaining thread hole, pull bar 21 end is provided with external screw thread, deflection plate is connected into a black box through helical baffles 10 by pull bar 21, and is fixed on the first tube sheet 5.
Gas-liquid separation circulation barrel housing 24 two ends are respectively by the first end socket 23, second end socket 30 is sealed, staving 24 top of gas-liquid separation circulation barrel is provided with cold-producing medium gas returning port adapter 25 and cold-producing medium inlet adapter 28, first liquid barrier 27, second liquid barrier 29 lays respectively at cold-producing medium inlet adapter 28 two ends, first liquid barrier 27 and the second liquid barrier 29 are cambered plate, the staving 24 upper contact position of its top edge and gas-liquid separation circulation barrel is welded to connect, first liquid barrier 27 and the second liquid barrier 29 top are provided with passage near the position at gas-liquid separation circulation barrel staving 24 inwall top, third gear liquid plate 40 is positioned at immediately below cold-producing medium gas returning port adapter 25, its longitudinal edge and gas-liquid separation circulation barrel staving 24 contact site are welded to connect, longitudinal length is 3 times of cold-producing medium gas returning port adapter 25 diameter, and the distance at surface to staving 24 inwall top is at least 1 times of cold-producing medium gas returning port adapter 25 diameter, the top of gas-liquid separation circulation barrel staving 24 is provided with the gas phase tube connector 26 be communicated with inner gas-phase space, bottom is provided with the liquid phase tube connector 33 be communicated with internal liquid phase space, and gas phase tube connector 26 is connected with the fluid level control device of outside respectively with liquid phase tube connector 33, the position, lower middle of gas-liquid separation circulation barrel housing 24 is provided with the oil return pipe of three differing heights, is respectively the first oil return pipe 34, second oil return pipe 35, the 3rd oil return pipe 36.
The upper end of decline circulation pipe 22 is communicated with gas-liquid separation circulation barrel staving 24 bottom, and the lower end of decline circulation pipe 22 is communicated with circulating pump 42 entrance, the first end cap lower linking tube 41 and circulating pump 42 outlet; First end cap lower linking tube 41 is communicated with the bottom of the first end cap 1; Between decline circulation pipe 22 and the first end cap lower linking tube 41, by-passing valve 43 is set and passes through pipeline connection; The upper end of rising circulation pipe 31 is communicated with the top of the second end socket 30, and the lower end of rising circulation pipe 31 is communicated with the top of the second end cap 18.Heat exchanger, gas-liquid separation circulation barrel are fixed together by two pairs of connection brackets 32, and the bearing 19 bottom heat exchanger shell 8, circulating pump base are connected with the Foundation of steel frame seat 44 of whole device.
As mentioned above, although represented with reference to specific preferred embodiment and described the present invention, it shall not be construed as the restriction to the present invention self.Under the spirit and scope of the present invention prerequisite not departing from claims definition, various change can be made in the form and details to it.
Claims (10)
1. a forced recirculation formula evaporimeter, comprise heat exchanger, with the gas-liquid separation circulation barrel be arranged on above described heat exchanger, described heat exchanger is communicated with by rising circulation pipe (31), decline circulation pipe (22) with the inner space of described gas-liquid separation circulation barrel, it is characterized in that, the lower end of described rising circulation pipe (31) is communicated with the refrigerant outlet of described heat exchanger, and upper end is communicated with the gas-phase space on described gas-liquid separation circulation barrel top; The upper end of described decline circulation pipe (22) is communicated with the liquid Space of described gas-liquid separation circulation barrel bottom, lower end and circulating pump (42) inlet communication being arranged on described exchanger base, the outlet of described circulating pump (42) is communicated with the refrigerant inlet of described heat exchanger; The lower end of described decline circulation pipe (22) is also directly communicated with the refrigerant inlet of described heat exchanger by by-passing valve (43).
2. forced recirculation formula evaporimeter according to claim 1, it is characterized in that, described gas-liquid separation circulation barrel comprises staving (24), and be arranged on cold-producing medium inlet adapter (28) and cold-producing medium gas returning port adapter (25) on described staving (24) top, 3 liquid barriers are also provided with in described staving (24), wherein the first liquid barrier (27) and the second liquid barrier (29) are separately positioned on the both sides of described cold-producing medium inlet adapter (28), by the spaced apart of described cold-producing medium inlet adapter (28) with its both sides, third gear liquid plate (40) arranges the below of described cold-producing medium gas returning port (25), described cold-producing medium gas returning port adapter (25) and the refrigerant liquid being positioned at described third gear liquid plate (40) below are separated.
3. forced recirculation formula evaporimeter according to claim 2, is characterized in that, the top of described first liquid barrier (27), the second liquid barrier (29) is provided with passage near the position at described staving (24) inwall top; The longitudinal length of described third gear liquid plate (40) is 2 ~ 4 times of described cold-producing medium gas returning port adapter (25) diameter, and the distance at surface to staving (24) inwall top is at least 1 times of described cold-producing medium gas returning port adapter (25) diameter.
4. forced recirculation formula evaporimeter according to claim 2, is characterized in that, the outside of described gas-liquid separation circulation barrel is also provided with fluid level control device, for monitoring the liquid level in described gas-liquid separation circulation barrel.
5. forced recirculation formula evaporimeter according to claim 4, it is characterized in that, the top of described gas-liquid separation circulation barrel is provided with the gas phase tube connector (26) that gas-phase space inner with it is communicated with, bottom is provided with the liquid phase tube connector (33) be communicated with its internal liquid phase space, and described gas phase tube connector (26) is connected with described fluid level control device respectively with liquid phase tube connector (33).
6. forced recirculation formula evaporimeter according to claim 2, is characterized in that, described gas-liquid separation circulation barrel is provided with at least two oil return pipes.
7. forced recirculation formula evaporimeter according to claim 6, is characterized in that, the position, lower middle of described gas-liquid separation circulation barrel is provided with the oil return pipe of three differing heights.
8. forced recirculation formula evaporimeter according to claim 1, it is characterized in that, described heat exchanger comprises housing (8), be arranged on first tube sheet (5) at described housing (8) two ends, the second tube sheet (14), and be sealed in described first tube sheet (5), first end cap (1) of the second tube sheet (14) side and the second end cap (18), wherein the inner space of the first end cap (1) is the refrigerant inlet of heat exchanger, and the inner space of the second end cap (18) is the refrigerant outlet of heat exchanger; Be connected with some heat exchanger tubes (9) between described first tube sheet (5) and described second tube sheet (14), described heat exchanger tube (9) is communicated with the inner space of described first end cap (1) and the second end cap (18).
9. forced recirculation formula evaporimeter according to claim 8, it is characterized in that, deflection plate (10) is also provided with in the housing (8) of described heat exchanger, described deflection plate (10) is continuous helical shape flow-guiding structure, and peripheral circumferential is provided with shirt rim, described deflection plate (10) has the pore (37) corresponding with described heat exchanger tube (9), described heat exchanger tube (9) is through described pore (37), described deflection plate (10) is positioned at its periphery, to the secondary refrigerant liquid water conservancy diversion flowing through its outside; Described deflection plate (10) also offers tie rod hole (38), described first tube sheet (5) offers the blind hole corresponding with described tie rod hole (38), described deflection plate (10) is connected into a black box through described tie rod hole (38) by pull bar (21), and is fixed on described first tube sheet (5).
10. forced recirculation formula evaporimeter according to claim 8, it is characterized in that, heat exchanger tube (9) entirety arrangement in described heat exchanger shell (8), in the equal cloth-like of four-quadrant, is arranged in equilateral triangle between any heat exchanger tube and adjacent non-same layer two heat exchanger tube.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520674046.1U CN204923592U (en) | 2015-09-01 | 2015-09-01 | Forced recirculation formula evaporimeter |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520674046.1U CN204923592U (en) | 2015-09-01 | 2015-09-01 | Forced recirculation formula evaporimeter |
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| CN204923592U true CN204923592U (en) | 2015-12-30 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105066520A (en) * | 2015-09-01 | 2015-11-18 | 南京冷德节能科技有限公司 | Forced recirculation-type evaporator |
| CN108844775A (en) * | 2018-05-24 | 2018-11-20 | 江西怡杉科技有限公司 | A kind of water sample distribution unit and water quality sampling equipment |
| WO2021209111A1 (en) * | 2020-04-15 | 2021-10-21 | Mayekawa Europe N.V. | Heat exchanger system |
-
2015
- 2015-09-01 CN CN201520674046.1U patent/CN204923592U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105066520A (en) * | 2015-09-01 | 2015-11-18 | 南京冷德节能科技有限公司 | Forced recirculation-type evaporator |
| CN108844775A (en) * | 2018-05-24 | 2018-11-20 | 江西怡杉科技有限公司 | A kind of water sample distribution unit and water quality sampling equipment |
| WO2021209111A1 (en) * | 2020-04-15 | 2021-10-21 | Mayekawa Europe N.V. | Heat exchanger system |
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