CN100491886C - Canal evaporator - Google Patents
Canal evaporator Download PDFInfo
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- CN100491886C CN100491886C CNB200710119262XA CN200710119262A CN100491886C CN 100491886 C CN100491886 C CN 100491886C CN B200710119262X A CNB200710119262X A CN B200710119262XA CN 200710119262 A CN200710119262 A CN 200710119262A CN 100491886 C CN100491886 C CN 100491886C
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- 239000007788 liquid Substances 0.000 claims abstract description 169
- 238000001704 evaporation Methods 0.000 claims abstract description 42
- 239000012530 fluid Substances 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims description 33
- 239000010410 layer Substances 0.000 claims description 31
- 239000012792 core layer Substances 0.000 claims description 4
- 239000013528 metallic particle Substances 0.000 claims description 4
- 238000005245 sintering Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 abstract description 26
- 238000000034 method Methods 0.000 abstract description 17
- 230000008676 import Effects 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 11
- 241000270295 Serpentes Species 0.000 abstract 5
- 238000013021 overheating Methods 0.000 abstract 3
- 238000000926 separation method Methods 0.000 description 12
- 238000005728 strengthening Methods 0.000 description 12
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- 238000005516 engineering process Methods 0.000 description 9
- 238000010992 reflux Methods 0.000 description 8
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- 238000009835 boiling Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000007599 discharging Methods 0.000 description 6
- 238000002309 gasification Methods 0.000 description 6
- 238000005057 refrigeration Methods 0.000 description 5
- 238000002156 mixing Methods 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
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- 230000007480 spreading Effects 0.000 description 1
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Abstract
The invention relates to a tube evaporator, belongs to the thermal equipment technical area. The air heating tube evaporator includes the evaporator export of the liquid vapor (1), fin (2), overheating segment (3), gas collection and exhaust port (5), the evaporator import of liquid (6), snake heat exchange segment( 9), snake heat tube (10), divider (11). The one end of the snake heat tube (10) is sealed by another end of the evaporator export of liquid vapor (1), it is divided into overheating segment (3) and the snake heat exchange segment (9) by the divider (11), and in the tube has the porous layer; the top pf the exhaust-gas tube and the gas collection tube (4) in the snake tube connect the top of the divider (11) which is located in the overheating segment (3). The remaining liquid of the evaporation returns to the evaporator import of liquid (6) and cycles evaporation; the invention also provides a fluid heat-pipe evaporator. The invention has high- heat exchange performance, is conducive to maintain the efficient evaporation process; simple processing, enhanced the work efficiency and the adapt ability of the evaporator.
Description
Technical field
The present invention relates to a kind of new and effective canal evaporator, belong to the Thermal Equipment technical field.
Background technology
Canal evaporator is a class Thermal Equipment, uses very extensively in power, chemical industry, Air-conditioning Engineering and Refrigeration Engineering, as refrigerator, and refrigerator, in the air-conditioning system, chemical industry and petrochemical processing evaporimeter etc.Mainly contain two kinds of forms, one, the liquid heated type is such as common casing tube evaporator; Its two, the air heat formula is such as domestic air conditioning, large-scale refrigerating plant etc.
Fig. 1 is a family expenses split-type air conditioner evaporimeter, is made up of evaporation tube and the outer fin of pipe.Wherein, 100-be evaporated liquid (is cold-producing medium to air-conditioning refrigeration system) vapor outlet port, 200-be evaporated liquid (is cold-producing medium to air-conditioning refrigeration system) inlet, the outer fin of 300-pipe.The many employings of A/C evaporator are horizontally disposed, and the dependence air is horizontal slightly to be restrained and go up fin and carry out heat exchange, heat to be evaporated liquid, and evaporating liquid is in in-tube evaporation and boiling realization complete gasification process.
Figure 2 shows that traditional liquid or steam heated bushing type evaporimeter, form by concentric interior pipe and outer tube.As Fig. 2, figure (a) is a conventional disc rotation set tubular evaparator vertical view; Figure (b) is a conventional disc rotation set tubular evaparator side view.Wherein, 100-heat source fluid (liquid or steam are cooled) inlet, 200-be evaporated liquid (is cold-producing medium to air-conditioning refrigeration system) vapor outlet port, 300-be evaporated fluid intake, the 400-fluid issuing that is cooled, 500-outer tube.Conventional disc rotation set tubular evaparator adopts screw type to arrange for saving the space more, relies on the heat convection of water in sleeve pipe and interior ligament, and evaporating liquid is realized gasification at in-tube evaporation and boiling.The cylinder structure of similar Fig. 1, liquid or steam heated formula evaporimeter also can be that the hosepipe type is arranged, just the fin among Fig. 1 this moment has become outer tube (referring to Fig. 4).
Still be liquid or steam condensation heated evaporator for existing air heat no matter, entering the mouth is neat liquid, and through full pipe range gasification, outlet is a pure gas substantially.In the gasification heat transfer process, though can be improved along with the increase heat exchange effect of mass dryness fraction, amplitude is little in the pipe.For improving the heat exchange effect, interior pipe adopts the surface peening measure more, such as internal thread, interior barrel, inner surface micro-rib pipe etc., increases heat exchange area when strengthening.Simultaneously, this single tube side evaporation and boiling process must cause complicated biphase gas and liquid flow.When two-phase flow occurring in the pipe, gas-liquid can be in blister, vent plug shape, ring-type or stratified flow equal flow type according to the mass dryness fraction size, increases flow resistance and fluctuation of service greatly, to the regulation and control of system operation etc., all brings very adverse influence.Though annular flow and thin liquid film evaporation flow pattern have good heat exchange property, proportion is very little in whole flow process, very limited to total system heat transfer contribution, and because of existing the layering factor will cause managing interior local dry, liquid phase is gathered in bottom in the pipe in a large number, can not well spread into surface, everywhere in the pipe, form the very strong liquid film convective boiling state of heat exchange effect, greatly weaken the effect of surface peening measure.
Summary of the invention
Goal of the invention: the invention provides the efficient canal evaporator of a class, comprise the concrete technology contents and the measure of structural design, middle gas-liquid separation, in-tube evaporation intensifying method, outlet steam superheating and the recirculation of surplus liquid.Central principle is: (1) guarantees to be evaporated in the pipe in the whole flow process liquid and realizes ring-type or thin liquid film evaporation form substantially from the middle gas-liquid separation of flowage structure realization two phase flow, is in the high-efficiency evaporating heat-transfer behavior; (2) in pipe, insert a suitable porous lining and cover former optical surface or strengthening surface, utilize the loose structure capillary suction force on the measure basis in the above, with liquid phase in the inner tubal wall uniform spreading, form the better thin liquid film evaporation of heat exchange effect, further strengthen the surface peening effect, and the porous lining can promote to discharge with reinforced pipe inner surface section gas phase, liquid phase is constantly by the optimum self-loopa process of replenishing; (3) introduce the surplus liquid recirculation of evaporation and separate the independent thermal technology of crossing with steam.Be that example illustrates this scheme implementation mode with the screw thread enhanced tube below.
A kind of new and effective air heat formula canal evaporator, as shown in Figure 3, comprise 1. be evaporated liquid (or cold-producing medium, down with.) vapor outlet port, 2. fin, 4. the gas collection blast pipe, 5. the gas collection exhaust outlet, 6. be evaporated liquid-inlet, 7. remainingly be evaporated liquid liquid phase recirculation return duct, 8. be evaporated liquid inlet tube, 10. snakelike heat exchange tube, 11. separating devices.
New and effective air heat formula evaporimeter, whole snakelike heat exchange tube (10) heat exchanging part is divided into snakelike heat exchanging segment (9) and superheat section (3) by separating device (11), topmost is to be evaporated liquid vapors outlet (1), and the other end is shut.The outside expanded joint fin of snakelike heat exchange tube (10) (2).Tube interior tightens on the basis of primary tube inwall internal thread (Fig. 5 (2)) (or light pipe or other strengthening surfaces) and sticks an annular porous layer (Fig. 5 (1)), this porous layer can be to be made by porous core layer of multi-layer silk screen or metallic particles sintering etc., its thickness and porosity need according to the service condition specific design, sprawl good liquid film layer to guarantee that inside pipe wall forms, be in best thin liquid film evaporating state in the holding tube.Be evaporated the connection of liquid inlet tube (8) one ends and be evaporated liquid-inlet (6), an end and snakelike heat exchange tube (10) upper end joins, and interface is apart from being evaporated liquid vapors outlet (1) preceding about straight length position (also can determine this segment length according to actual needs).All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, be communicated with gas collection blast pipe (4).Exhaust outlet (5) topmost is positioned at the upstream that is evaporated liquid inlet tube (8) and snakelike heat exchange tube (10) interface.The remaining liquid liquid phase recirculation refluxing opening pipe (7) that is evaporated in bottom communicates with being evaporated liquid-inlet (6), the surplus liquid that does not evaporate is carried be back to evaporating liquid import (6), continues evaporation.
Be evaporated liquid and enter by being evaporated liquid-inlet (6), be delivered to heat exchanger top by being evaporated liquid inlet tube (8), phase-change heat-exchange from top to bottom flows in the snakelike heat exchange tube (10) of snakelike heat exchanging segment (9).Whenever, flow through one section, all can carry out a gas-liquid separation by gas collection exhaust outlet (5), being evaporated liquid vapors can be evaporated liquid and can continue flow further downstream by gas collection exhaust outlet (5) discharge.The steam of discharging by gas collection exhaust outlet (5) can enter superheat section (3) by gas collection blast pipe (4) and carry out overheated (can simultaneously the liquid phase droplet that carries out the evaporation, to guarantee that vapor outlet port is pure superheated vapor), finally discharge via being evaporated liquid vapors outlet (1).Being evaporated liquid and can constantly carrying out heat exchange of flow further downstream at snakelike heat exchanging segment (9), produce steam, discharge by gas collection exhaust outlet (5) gas-liquid separation once more, until arriving the heat exchanger bottom, be evaporated liquid liquid-phase reflux mouth pipe (7) and be evaporated liquid by remaining, reenter the evaporimeter heat exchange in inlet mixing mutually.Add horizontal slightly snakelike heat exchange tube (10) of hot-air and last fin (2) thereof and carry out heat exchange, heating is evaporated liquid.
The present invention also provides a kind of canal evaporator.
A kind of new and effective fluid heated type canal evaporator, as shown in Figure 4, comprise 1. add hot fluid (liquid or steam) import, 2. be evaporated liquid vapors outlet, 4. the gas collection blast pipe, 5. the gas collection exhaust outlet, 6. add hot fluid (liquid or steam) outlet, 7. be evaporated liquid-inlet, 8. remainingly be evaporated liquid liquid phase recirculation return duct, 9. be evaporated liquid inlet tube, 11. outer tubes, 12. tube connectors, 13. snakelike heat exchange tubes, 14. separating devices.
New and effective liquid heated evaporator, outer tube (11) is wrapped in the outside of every section snakelike heat exchange tube (13) horizontal segment, relies on tube connector (12) to communicate between outer tube.The superiors' outer tube (11) one ends are for adding hot fluid (liquid or steam) import (1), and lowermost layer outer tube (11) one ends are the heating fluid issuing.
Whole snakelike heat exchange tube (13) heat exchanging part is divided into snakelike heat exchanging segment (10) and superheat section (3) by separating device (14), topmost is to be evaporated liquid vapors outlet (2), and the other end is shut.Snakelike heat exchange tube (13) tube interior tightens on the basis of primary tube inwall internal thread (Fig. 5 (2)) (or light pipe or other strengthening surfaces) and sticks an annular porous layer (Fig. 5 (1)), this porous layer can be to be made by porous core layer of multi-layer silk screen or metallic particles sintering etc., its thickness and porosity need according to the service condition specific design, sprawl good liquid film layer to guarantee that inside pipe wall forms, be in best thin liquid film evaporating state in the holding tube.Be evaporated the connection of liquid inlet tube (9) one ends and be evaporated liquid-inlet (7), an end and snakelike heat exchange tube (13) upper end joins, and interface is apart from being evaporated liquid vapors outlet (2) preceding about straight length position (also can determine this segment length according to actual needs).All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, be communicated with gas collection blast pipe (4).Exhaust outlet (5) topmost is positioned at the upstream that is evaporated liquid inlet tube (9) and snakelike heat exchange tube (13) interface.The remaining liquid liquid phase recirculation refluxing opening pipe (8) that is evaporated in bottom communicates with being evaporated liquid-inlet (7), the surplus liquid that does not evaporate is carried be back to evaporating liquid import (7), continues evaporation.
Be evaporated liquid and enter by being evaporated liquid-inlet (7), be delivered to heat exchanger top by being evaporated liquid inlet tube (9), phase-change heat-exchange from top to bottom flows in the snakelike heat exchange tube (13) of snakelike heat exchanging segment (10).Whenever, flow through one section, all can carry out a gas-liquid separation by gas collection exhaust outlet (5), being evaporated liquid vapors can be evaporated liquid and can continue flow further downstream by gas collection exhaust outlet (5) discharge.The steam of discharging by gas collection exhaust outlet (5) can enter superheat section (3) by gas collection blast pipe (4) and carry out overheated (can simultaneously the liquid phase droplet that carries out the evaporation, to guarantee that vapor outlet port is pure superheated vapor), finally discharge via being evaporated liquid vapors outlet (2).Being evaporated liquid and can constantly carrying out heat exchange of flow further downstream at snakelike heat exchanging segment (10), produce steam, discharge by gas collection exhaust outlet (5) gas-liquid separation once more, until arriving the heat exchanger bottom, be evaporated liquid liquid phase recirculation return duct (8) and be evaporated liquid by remaining, reenter the evaporimeter heat exchange in inlet mixing mutually.Add hot fluid (liquid or steam) and enter outer tube (11) via heating fluid inlet (1), between snakelike heat exchange tube (13) straight length and outer tube (11), flow and wash away snakelike heat exchange tube (13) and be evaporated liquid with heating and make its gasification, and by tube connector (12) importing lower floor's outer tube (11), until discharging through heating liquid outlet (6).
The technology used in the present invention characteristics have following several respects: (1) structural design, middle gas-liquid separation, in-tube evaporation intensifying method, outlet steam superheating and the recirculation of surplus liquid.(2) novel enhanced heat exchange technology is used, and more helps sprawling of liquid film on the tube wall face, forms the better thin liquid film evaporation of heat exchange effect, thereby has strengthened heat exchange; (3) novel enhanced heat exchange technology is used, and makes liquid phase to be evaporated can pass through capillary force, constantly fast via porous layer attached on the inside pipe wall, help keeping of high-efficiency evaporating process; (4) utilize this reinforcement technique to change traditional strengthening surface enhanced water evaporation, the disadvantageous situation of boiling heat transfer, the design by innovation makes that original wall enhancements is more effective.Finally, improved the performance of integral cannula evaporating heat exchanger, made full use of each cun strengthening surface by above-mentioned technical characterstic.The present invention processes simply, and comparing with conventional evaporator to increase any special processing technology.
The present invention also has two local techniques inventive points:
(1) the sleeve pipe evaporator section adopts separating device to separate with the steam superheat section.This invention and measure are very crucial characteristic of the present invention and technology, both in case the import liquid phase is evaporated liquid mixes mutually with steam and enter the other side's heat exchanging segment, influence the evaporimeter operate as normal, can realize the outlet degree of superheat control that is difficult to accomplish in the present evaporimeter again.Generally all be to realize in the routine techniques by increasing pipe range, more than one consumable material, two reduce energy conversion and utilization ratio, also increase compressor horsepower in refrigeration system.
(2) residual liquid outlet (pipe).This invention and measure are another local techniques keys of the present invention, have solved in the middle of the employing evaporation process after the gas-liquid separation, and afterbody residual liquid accumulative total that may occur and the problem of getting rid of have also improved the working efficiency and the adaptive capacity of evaporimeter simultaneously.This inventive point key problem in technology is, adopt the attract deposits dual-use function of liquid and blocking solution of capillary, allow residual liquid flow out to import the import evaporating liquid and flow main flow, realize the recirculation of remaining liquid, simultaneously hinder main flow liquid again and enter evaporator main heat exchange pipeline section from here, cause evaporator function to lose efficacy.
To being applied to the bushing type evaporimeter under the big heat exchange power situation, can design according to this principle, adopt that the parallel connection of liquid division type double-pipe evaporimeter reaches shown in many Fig. 2.
Description of drawings
Be family expenses split-type air conditioner air heat evaporimeter or be called the cooling air evaporator shown in Fig. 1.
Shown in Fig. 2 traditional liquid or steam heated evaporimeter.Wherein, figure (a) is traditional liquid or steam heated evaporimeter vertical view; Figure (b) is traditional liquid or steam heated vaporizer side view.
Fig. 3 is the new and effective air heat of the present invention (or cooling air) formula evaporimeter schematic diagram.Wherein, figure (a) is this evaporimeter vertical view; Figure (b) is this vaporizer side view.
Fig. 4 is the new and effective fluid of the present invention (liquid or steam) heated evaporator schematic diagram.Wherein, figure (a) is this evaporimeter vertical view; Figure (b) is this vaporizer side view.
Fig. 5 is pipe schematic diagram in the evaporimeter of the present invention.
The specific embodiment
Further specify the present invention below in conjunction with accompanying drawing.
Fig. 3 is the new and effective air heat of the present invention (or cooling air) formula evaporimeter schematic diagram.Comprise 1. be evaporated liquid (or cold-producing medium, down with.) vapor outlet port, 2. fin, 4. the gas collection blast pipe, 5. the gas collection exhaust outlet, 6. be evaporated liquid-inlet, 7. remainingly be evaporated liquid liquid phase circulating reflux pipe, 8. be evaporated liquid inlet tube, 10. snakelike heat exchange tube, 11. separating devices.New and effective air heat formula evaporimeter, whole snakelike heat exchange tube (10) heat exchanging part is divided into snakelike heat exchanging segment (9) and superheat section (3) by separating device (11), topmost is to be evaporated liquid vapors outlet (1), and the other end is shut.The outside expanded joint fin of snakelike heat exchange tube (10) (2).Tube interior adds a porous layer (Fig. 5 (1)) on the basis of primary tube inwall internal thread (Fig. 5 (2)) (or light pipe or other strengthening surfaces).The assurance inside pipe wall forms sprawls good liquid film layer, is in best thin liquid film evaporating state in the holding tube.Be evaporated the connection of liquid inlet tube (8) one ends and be evaporated liquid-inlet (6), an end and snakelike heat exchange tube (10) upper end joins, and interface is apart from being evaporated liquid vapors outlet (1) preceding about straight length position (also can determine this segment length according to actual needs).All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, be communicated with gas collection blast pipe (4).Exhaust outlet (5) topmost is positioned at the upstream that is evaporated liquid inlet tube (8) and snakelike heat exchange tube (10) interface.The remaining liquid liquid phase recirculation refluxing opening pipe (7) that is evaporated in bottom communicates with being evaporated liquid-inlet (6), the surplus liquid that does not evaporate is carried be back to evaporating liquid import (6), continues evaporation.
Be evaporated liquid and enter by being evaporated liquid-inlet (6), be delivered to heat exchanger top by being evaporated liquid inlet tube (8), phase-change heat-exchange from top to bottom flows in the snakelike heat exchange tube (10) of snakelike heat exchanging segment (9).Whenever, flow through one section, all can carry out a gas-liquid separation by gas collection exhaust outlet (5), being evaporated liquid vapors can be evaporated liquid and can continue flow further downstream by gas collection exhaust outlet (5) discharge.The steam of discharging by gas collection exhaust outlet (5) can enter superheat section (3) by gas collection blast pipe (4) and carry out overheated (can simultaneously the liquid phase droplet that carries out the evaporation, to guarantee that vapor outlet port is pure superheated vapor), finally discharge via being evaporated liquid vapors outlet (1).Being evaporated liquid and can constantly carrying out heat exchange of flow further downstream at snakelike heat exchanging segment (9), produce steam, discharge by gas collection exhaust outlet (5) gas-liquid separation once more, until arriving the heat exchanger bottom, be evaporated liquid liquid-phase reflux mouth pipe (7) and be evaporated liquid by remaining, reenter the evaporimeter heat exchange in inlet mixing mutually.Add horizontal slightly snakelike heat exchange tube (10) of hot-air and last fin (2) thereof and carry out heat exchange, heating is evaporated liquid.
Fig. 4 is the new and effective fluid of the present invention (liquid or steam) heated evaporator schematic diagram.Comprise 1. heating fluid inlets, 2. be evaporated liquid vapors outlet, 4. the gas collection blast pipe, 5. the gas collection exhaust outlet, 6. the heating fluid issuing, 7. be evaporated liquid-inlet, 8. remainingly be evaporated liquid liquid phase circulating reflux pipe, 9. be evaporated liquid inlet tube, 11. outer tubes, 12. tube connectors, 13. snakelike heat exchange tubes, 14. separating devices.New and effective liquid heated evaporator, outer tube (11) is wrapped in the outside of every section snakelike heat exchange tube (13) horizontal segment, relies on tube connector (12) to communicate between outer tube.The superiors' outer tube (11) one ends are for adding hot fluid (liquid or steam) import (1), and lowermost layer outer tube (11) one ends are the heating fluid issuing.
Whole snakelike heat exchange tube (13) heat exchanging part is divided into snakelike heat exchanging segment (10) and superheat section (3) by separating device (14), topmost is to be evaporated liquid vapors outlet (2), and the other end is shut.Snakelike heat exchange tube (13) tube interior adds a porous layer (Fig. 5 (1)) on the basis of primary tube inwall internal thread (Fig. 5 (2)) (or light pipe or other strengthening surfaces).The assurance inside pipe wall forms sprawls good liquid film layer, is in best thin liquid film evaporating state in the holding tube.Be evaporated the connection of liquid inlet tube (9) one ends and be evaporated liquid-inlet (7), an end and snakelike heat exchange tube (13) upper end joins, and interface is apart from being evaporated liquid vapors outlet (2) preceding about straight length position (also can determine this segment length according to actual needs).All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, be communicated with gas collection blast pipe (4).Exhaust outlet (5) topmost is positioned at the upstream that is evaporated liquid inlet tube (9) and snakelike heat exchange tube (13) interface.The remaining liquid liquid phase recirculation refluxing opening pipe (8) that is evaporated in bottom communicates with being evaporated liquid-inlet (7), the surplus liquid that does not evaporate is carried be back to evaporating liquid import (7), continues evaporation.
Be evaporated liquid and enter by being evaporated liquid-inlet (7), be delivered to heat exchanger top by being evaporated liquid inlet tube (9), phase-change heat-exchange from top to bottom flows in the snakelike heat exchange tube (13) of snakelike heat exchanging segment (10).Whenever, flow through one section, all can carry out a gas-liquid separation by gas collection exhaust outlet (5), being evaporated liquid vapors can be evaporated liquid and can continue flow further downstream by gas collection exhaust outlet (5) discharge.The steam of discharging by gas collection exhaust outlet (5) can enter superheat section (3) by gas collection blast pipe (4) and carry out overheated (can simultaneously the liquid phase droplet that carries out the evaporation, to guarantee that vapor outlet port is pure superheated vapor), finally discharge via being evaporated liquid vapors outlet (2).Being evaporated liquid and can constantly carrying out heat exchange of flow further downstream at snakelike heat exchanging segment (10), produce steam, discharge by gas collection exhaust outlet (5) gas-liquid separation once more, until arriving the heat exchanger bottom, be evaporated liquid liquid phase recirculation return duct (8) and be evaporated liquid by remaining, reenter the evaporimeter heat exchange in inlet mixing mutually.Add hot fluid (liquid or steam) and enter outer tube (11) via heating fluid inlet (1), between snakelike heat exchange tube (13) straight length and outer tube (11), flow and wash away snakelike heat exchange tube (13) and be evaporated liquid with heating and make its gasification, and by tube connector (12) importing lower floor's outer tube (11), until discharging through heating liquid outlet (6).
Fig. 5 is pipe schematic diagram in the evaporimeter of the present invention.Pure liquid phase at first enters pipe in the heat exchange, and the carrying out along with evaporation, boiling forms stratified flow gradually.At this moment, a large amount of liquid phases accumulate in the interior mainstream channel of porous layer (1), since the gravity effect, the layering of gas-liquid phase.But it is different with the single use strengthening surface of tradition, partially liq can be because the swabbing action of porous layer (1), cause full annular tube wall face (2) uniformly, spread in the porous layer of being close to tube wall (2) between (1) or porous layer and pipe internal thread or strengthening surface wall in (3) layer, form the better thin liquid film evaporation of heat exchange effect, strengthened heat exchange.Guaranteed that the every place of strengthening surface all contacts with liquid phase in the pipe, fully with its utilization.Along with the phase transformation of liquid phase on the surface, gas phase constantly is expelled to main channel in the pipe by porous layer (1), and liquid phase constantly is pumped to tube wall (2) by porous layer and locates the main channel in, has formed the self-loopa process, constantly makes full use of strengthening surface and carries out thin liquid film and evaporate.
The above is embodiments of the invention, and protection scope of the present invention is not limited to this, anyly all belongs within the effective protection domain of the present invention based on the equivalent transformation on the principle of the invention and the technical scheme.
Claims (6)
1, a kind of air heat formula canal evaporator comprises being evaporated liquid vapors outlet (1), fin (2), gas collection blast pipe (4), gas collection exhaust outlet (5), being evaporated liquid-inlet (6), remainingly be evaporated liquid liquid phase recirculation return duct (7), be evaporated liquid inlet tube (8), snakelike heat exchange tube (10), separating device (11);
Described snakelike heat exchange tube (10) one ends are to be evaporated liquid vapors outlet (1), and the other end is shut; Described snakelike heat exchange tube (10) is divided into superheat section (3) and snakelike heat exchanging segment (9) by separating device (11); The outside expanded joint fin of snakelike heat exchange tube (10) (2); The inner porous layer that on the basis of primary tube inwall internal thread, adds of snakelike heat exchange tube (10);
All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, gas collection exhaust outlet (5) is communicated with gas collection blast pipe (4); Topmost the exhaust outlet of coiled pipe is connected the top that is positioned at superheat section (3) separating device (11) with gas collection blast pipe (4); Gas collection blast pipe (4) connects the remaining liquid liquid phase recirculation return duct (7) that is evaporated, remainingly be evaporated liquid liquid phase recirculation return duct (7) and be evaporated liquid inlet tube (8) and communicate, unevaporated surplus liquid is back to is evaporated liquid-inlet (6), carry out circulating and evaporating;
Be evaporated liquid-inlet (6) and join with snakelike heat exchange tube (10) by being evaporated liquid inlet tube (8), interface is positioned at the below of the snakelike heat exchanging segment of coiled pipe (9) separating device (11).
2, a kind of air heat formula canal evaporator according to claim 1 is characterized in that, described porous layer is an annular.
3, a kind of air heat formula canal evaporator according to claim 2 is characterized in that, described porous layer is the porous core layer of multi-layer silk screen or metallic particles sintering.
4, a kind of fluid heated type canal evaporator comprises heating fluid inlet (1), is evaporated liquid vapors outlet (2), gas collection blast pipe (4), gas collection exhaust outlet (5), heating fluid issuing (6), is evaporated liquid-inlet (7), remainingly is evaporated liquid liquid phase recirculation return duct (8), is evaporated liquid inlet tube (9), outer tube (11), tube connector (12), snakelike heat exchange tube (13), separating device (14);
Described outer tube (11) is wrapped in the outside of every section described snakelike heat exchange tube (13) horizontal segment, relies on tube connector (12) to communicate between the outer tube; The superiors' outer tube (11) upper end is heating fluid inlet (1), and lowermost layer outer tube (11) lower end is the heating fluid issuing;
Described snakelike heat exchange tube (13) one ends are to be evaporated liquid vapors outlet (2), and the other end is shut; Described snakelike heat exchange tube (13) is divided into superheat section (3) and snakelike heat exchanging segment (10) by separating device (14); The inner porous layer that on the basis of primary tube inwall internal thread, adds of snakelike heat exchange tube (13);
All have gas collection exhaust outlet (5) every section snakelike heat exchange tube elbow, gas collection exhaust outlet (5) is communicated with gas collection blast pipe (4); Topmost the exhaust outlet of coiled pipe is connected the top that is positioned at superheat section (3) separating device (14) with gas collection blast pipe (4); Gas collection blast pipe (4) connects the remaining liquid liquid phase recirculation return duct (8) that is evaporated, remainingly be evaporated liquid liquid phase recirculation return duct (8) and be evaporated liquid inlet tube (9) and communicate, unevaporated surplus liquid is back to is evaporated liquid-inlet (7), carry out circulating and evaporating;
Be evaporated liquid-inlet (7) and join with snakelike heat exchange tube (10) by being evaporated liquid inlet tube (9), interface is positioned at the below of the snakelike heat exchanging segment of coiled pipe (9) separating device (11).
5, a kind of fluid heated type canal evaporator according to claim 4 is characterized in that, described porous layer is an annular.
6, a kind of fluid heated type canal evaporator according to claim 5 is characterized in that, described porous layer is the porous core layer of multi-layer silk screen or metallic particles sintering.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710119262XA CN100491886C (en) | 2007-07-19 | 2007-07-19 | Canal evaporator |
| PCT/CN2008/000611 WO2008151500A1 (en) | 2007-06-15 | 2008-03-27 | A gas-liquid separating method and a gas-liquid separating type evaporator |
| US12/595,602 US20100126213A1 (en) | 2007-06-15 | 2008-03-27 | Liquid-Vapor Separating Method and a Liquid-Vapor Separating Type Evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200710119262XA CN100491886C (en) | 2007-07-19 | 2007-07-19 | Canal evaporator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101101177A CN101101177A (en) | 2008-01-09 |
| CN100491886C true CN100491886C (en) | 2009-05-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200710119262XA Expired - Fee Related CN100491886C (en) | 2007-06-15 | 2007-07-19 | Canal evaporator |
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| CN (1) | CN100491886C (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008151500A1 (en) * | 2007-06-15 | 2008-12-18 | Tsinghua University | A gas-liquid separating method and a gas-liquid separating type evaporator |
| CN102003844B (en) * | 2010-12-07 | 2012-01-18 | 东南大学 | Efficient full-wet inner surface evaporator |
| CN102692145A (en) * | 2011-03-25 | 2012-09-26 | 江苏煌明能源科技有限公司 | Novel device for absorbing and converting heat energy of waste hot water |
| CN103159176B (en) * | 2011-12-16 | 2014-11-05 | 浙江新安化工集团股份有限公司 | Liquefied chlorine vaporizer |
| CN104236175B (en) * | 2014-09-25 | 2016-06-29 | 天津商业大学 | A kind of bleeder vaporizer |
| CN105258404A (en) * | 2015-11-10 | 2016-01-20 | 南通四方冷链装备股份有限公司 | Finned evaporator |
| KR101676993B1 (en) * | 2016-05-03 | 2016-11-16 | (주)귀뚜라미 | U-bend pipe type heat exchanger |
| CN107328147A (en) * | 2017-08-25 | 2017-11-07 | 天津商业大学 | A kind of tube-in-tube condenser |
| CN107799193B (en) * | 2017-10-25 | 2019-11-05 | 中国核动力研究设计院 | Polycyclic road couples thermally conductive passive residual heat removal system experiment simulator |
| CN108088302A (en) * | 2017-12-07 | 2018-05-29 | 合肥华凌股份有限公司 | Heat-exchanger rig and Cryo Equipment |
| CN107941056A (en) * | 2017-12-20 | 2018-04-20 | 江苏普格机械有限公司 | A kind of air preheater |
| CN108114493B (en) * | 2018-01-22 | 2023-07-07 | 南京工程学院 | Heat source tower solution concentration device and concentration method thereof |
| CN109900004B (en) * | 2019-02-20 | 2024-03-26 | 仲恺农业工程学院 | Two-stage compression adjustable dryness refrigerating system with ejector |
| CN111015139B (en) * | 2019-11-26 | 2021-05-18 | 西安远航真空钎焊技术有限公司 | Preparation method of ground test precooler |
| EP4034495A1 (en) * | 2020-11-25 | 2022-08-03 | Mc 2020 Scpm | Thermal inverter |
-
2007
- 2007-07-19 CN CNB200710119262XA patent/CN100491886C/en not_active Expired - Fee Related
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| CN101101177A (en) | 2008-01-09 |
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