WO2008151500A1 - Procédé de séparation gaz-liquide et évaporateur de type à séparation gaz-liquide - Google Patents

Procédé de séparation gaz-liquide et évaporateur de type à séparation gaz-liquide Download PDF

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Publication number
WO2008151500A1
WO2008151500A1 PCT/CN2008/000611 CN2008000611W WO2008151500A1 WO 2008151500 A1 WO2008151500 A1 WO 2008151500A1 CN 2008000611 W CN2008000611 W CN 2008000611W WO 2008151500 A1 WO2008151500 A1 WO 2008151500A1
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WO
WIPO (PCT)
Prior art keywords
liquid
gas
pipe
liquid separation
evaporated
Prior art date
Application number
PCT/CN2008/000611
Other languages
English (en)
French (fr)
Inventor
Xiaofeng Peng
Di Wu
Gui Lu
Zhen Wang
Yang Zhang
Original Assignee
Tsinghua University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CNB2007101189631A external-priority patent/CN100491870C/zh
Priority claimed from CNB200710119262XA external-priority patent/CN100491886C/zh
Application filed by Tsinghua University filed Critical Tsinghua University
Priority to US12/595,602 priority Critical patent/US20100126213A1/en
Publication of WO2008151500A1 publication Critical patent/WO2008151500A1/zh

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
    • F28D7/14—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically both tubes being bent
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
    • B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
    • B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/30—Accessories for evaporators ; Constructional details thereof
    • B01D1/305—Demister (vapour-liquid separation)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/022—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of two or more media in heat-exchange relationship being helically coiled, the coils having a cylindrical configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/08—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being otherwise bent, e.g. in a serpentine or zig-zag
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/02—Evaporators with heating coils
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0068—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for refrigerant cycles
    • F28D2021/0071—Evaporators

Definitions

  • the present invention relates to an evaporator, and more particularly to a gas-liquid separation method and apparatus in a gas-liquid separation evaporator.
  • Evaporator is a kind of thermal equipment, which is widely used in power, chemical, air conditioning engineering and refrigeration engineering.
  • evaporators There are two main types of evaporators, one is liquid heating type, such as common casing evaporator; It is air-heated, such as household air conditioners, large-scale refrigeration, chemical and power plants, etc., and is generally in-pipe evaporation type.
  • a general household split type air conditioner evaporator belongs to an air heating type evaporator, and a conventional vertical serpentine type evaporator 9 is a heat exchange tube 91 and a tube disposed between each heat exchange tube 91.
  • the outer fins 92 are composed, and the evaporated liquid (generally referred to as the refrigerant of the air conditioning refrigeration system) enters from the inlet 93 of the heat exchange tube 91, and is exchanged by the heat exchange tube 91 and the outer fins 92 and the air flowing through the evaporator 9.
  • the heat causes the refrigerant in the heat exchange tube 91 to be evaporated and boiled by heat, thereby achieving complete vaporization, and the gas is discharged from the outlet 94 of the heat exchange tube 91.
  • the conventional spiral sleeve type evaporator 10 is composed of an outer sleeve 101 and an inner tube 102.
  • the inner tube may be a single tube or a tube bundle, and heat source liquids are respectively disposed at both ends of the outer sleeve 101 (cooled)
  • the liquid inlet port 103 and the outlet port 104 are provided with an evaporating liquid inlet 105 and an outlet 106, respectively, at both ends of the inner tube 102.
  • This coiled-tube evaporator 10 exchanges heat with the evaporated liquid in the inner tube 102 through the heat source liquid (cooled liquid) between the outer sleeve 101 and the inner tube 102, so that the evaporated liquid is in the inner tube 102.
  • the tubular shape of the conventional convoluted casing evaporator 10 can also be arranged in a serpentine tube shape (as shown in Fig. 1), but it has no fin structure outside the tube and is replaced by the structure of the outer casing and the inner tube.
  • Such an evaporator may sometimes be a liquid evaporating liquid at both ends of the outer casing, and the inner tube is taken away from the heat source liquid, and the structure and principle are similar, but only in practical applications.
  • the above-described prior art tubular evaporator which is entered as pure liquid by the vaporized liquid inlets 93, 105, is substantially pure gas emerging from the vapor outlets 94, 106 of the vaporized liquid after a full length of vaporization process.
  • the heat exchange tubes are mostly subjected to surface strengthening measures, such as setting internal threads, inner groove tubes, inner surface micro-ribbed tubes, etc., while increasing the heat exchange area while strengthening.
  • surface strengthening measures such as setting internal threads, inner groove tubes, inner surface micro-ribbed tubes, etc.
  • the phase flow is not conducive to achieving and forming a better heat exchange pattern.
  • the casing type evaporator adopts a horizontal spiral tube structure, although there is a secondary flow disturbance inside the tube, but the phenomenon of stratified flow is still inevitable.
  • the stratified flow will cause local drying in the tube, and the liquid phase will gather in the tube.
  • the inner bottom layer can not be spread well to every surface of the inner wall of the tube, forming a non-optimal boiling or surface evaporation state, which greatly weakens the effect of surface strengthening measures and greatly reduces the heat exchange effect.
  • the annular flow and the thin liquid film evaporation flow pattern have good heat transfer performance, 'the proportion in the whole process is small, and the contribution to the overall system heat transfer is very limited.
  • an object of the present invention is to provide an evaporator capable of achieving automatic gas-liquid separation and improving heat exchange capability.
  • a gas-liquid separation method in a gas-liquid separation evaporator which is: (1) a separation is provided in a gas-liquid separator flowing through an upper portion of a pipe to be evaporated.
  • a device dividing the pipeline into a superheating section and an evaporation section of the evaporated liquid; (2) connecting a gas-liquid separation pipe adjacent to the superheating section of the partitioning device, and connecting an evaporated liquid into the evaporation section adjacent to the separating device a liquid pipe, a plurality of steam guiding pipes are arranged in sections on the pipeline of the evaporation section, and the steam guiding pipes respectively communicate with the gas-liquid separation pipe; the gas evaporated by the entire pipeline can be discharged in sections, and After the gas-liquid separation in the gas-liquid separation pipe, the superheating section is superheated; the hot steam is discharged from the vapor outlet; (3) the residual liquid separated from the gas-liquid separation pipe is passed along with the residual liquid which is not evaporated in the evaporation section.
  • the pipeline is sent to the evaporating liquid inlet pipe and returned to the evaporative heat transfer process of the evaporated liquid.
  • the pipeline flowing through the liquid to be evaporated is a pipeline between an outer sleeve and an inner tube
  • the partitioning device is an annular partition plate disposed between the outer sleeve and the inner tube, the inner portion
  • the tube flows through the heat source liquid.
  • the pipe flowing through the liquid to be evaporated is a single-layer inner pipe, and the inner pipe is provided with outer fins, and the inner pipe flows outside the heat source gas.
  • the pipeline flowing through the liquid to be evaporated is an inner tube, and an outer sleeve is disposed outside the inner tube, and the heat source liquid flows between the two tubes.
  • a gas-liquid separation type evaporator comprising a first-class vaporized liquid line, a first-stage heat source liquid line or a first-class heat source gas space, characterized by: on the line flowing through the evaporated liquid Providing a partitioning device for separating the pipeline for evaporating liquid into a superheating section and an evaporation section; connecting a gas-liquid separation pipe near the superheating section of the partitioning device, and connecting an evaporated liquid to the evaporation section of the separating device a plurality of vapor guiding tubes are arranged in the pipeline of the evaporation section, the steam guiding tubes are respectively connected to the gas-liquid separation tube; the bottom of the gas-liquid separation tube is connected by a pipeline The evaporated liquid is introduced into the inlet end of the liquid pipe.
  • the pipeline flowing through the liquid to be evaporated is a pipeline between an outer sleeve and an inner tube
  • the partitioning device is an annular partition plate disposed between the outer sleeve and the inner tube, the inner portion
  • the bottom port of the tube is the heat source liquid inlet
  • the top port of the inner tube is the heat source outlet.
  • the outer sleeve and the inner tube are respectively provided in the shape of one of a spiral tubular shape and a vertical serpentine tubular shape.
  • the pipe flowing through the liquid to be evaporated is a single inner pipe, and the inner pipe is provided with outer fins.
  • the pipeline flowing through the liquid to be evaporated is an inner tube, and an outer sleeve is disposed outside the inner tube, the partitioning device is a circular partition plate disposed in the inner tube, and the bottom of the outer sleeve
  • the port is a heat source liquid inlet, and the top port of the outer sleeve is a heat source outlet.
  • the outer sleeve and the inner tube are respectively provided in the shape of one of a spiral tubular shape and a vertical serpentine tubular shape.
  • the inner tube is an inner tube bundle which is distributed in a spiral twist shape by a plurality of tubes.
  • the inner tube is a single tube.
  • the inner wall of the inner tube is provided with an internal thread or a micro-groove, and the surface of the internal thread or the micro-groove is coated with a porous layer formed by sintering a multi-layered wire mesh with metal or non-metal particles.
  • the inner wall of the outer sleeve is provided with a porous layer formed by sintering a multi-layered wire mesh with metal or non-metal particles.
  • the invention adopts a separating device to separate the heat exchange tube into a liquid evaporation section and a steam superheating section, which can prevent the inlet liquid phase from directly entering the superheating section and affecting evaporation.
  • the normal operation of the device can realize the control of the outlet superheat which is difficult to be achieved in the conventional evaporator.
  • the length of the superheating section can be adjusted according to the actual overheating requirement to ensure the superheat temperature of the outlet.
  • the arrangement of the partitioning device of the present invention has the characteristics of reducing the consumption of materials, improving the energy conversion and utilization efficiency, and increasing the power of the compressor in the refrigeration system, as compared with the conventional techniques for increasing the length of the pipe. 2.
  • the invention adopts the residual liquid phase reflux tube of the evaporated liquid, is filled with the porous core body, and utilizes the dual functions of the capillary absorbing liquid and the liquid blocking liquid, so that the residual liquid flows out and flows into the mainstream of the evaporating liquid flow of the inlet, thereby realizing the remaining.
  • the recirculation of the liquid has the functions of automatic liquid return and circulation evaporation, which solves the problem of accumulation and elimination of the tail residual liquid which may occur after the gas-liquid separation in the middle of the evaporation process. At the same time, it blocks the mainstream liquid from entering the main evaporating heat transfer pipe section, causing the evaporator function to fail. Improve the working efficiency and adaptability of the evaporator. 3.
  • the invention has a novel gas-liquid separation setting, so that the vaporized gas phase can be quickly discharged through the exhaust pipe, which reduces the pressure loss inside the system and is beneficial to the realization of the high-efficiency evaporation process.
  • the invention can adopt an inner tube bundle structure, and the evaporated liquid liquid (refrigerant) is placed between the outer sleeve and the inner tube, and the complicated structure in the gap is utilized, which not only enhances the disturbance of the liquid phase flow, but also The gas phase is continuously taken away, and the evaporated liquid is gradually less, which is more conducive to the spreading of the liquid film, and the formation of a thin liquid film which has a better heat exchange effect, thereby enhancing the heat exchange. 5.
  • the evaporated liquid liquid refrigerant
  • the evaporation surface is provided with micro-threads, grooves or a porous layer. It is also possible to add a porous layer to the micro-threads or grooves. It can be sintered from a multi-layer mesh with metal or non-metal particles.
  • the capillary suction force of the porous structure can be used to uniformly spread the liquid phase on the inner tube wall to form a thin liquid film evaporation with better heat exchange effect, thereby further enhancing the surface strengthening effect, and the porous liner can promote and A benign self-circulation process that enhances the gas phase discharge in the inner surface area of the tube and the liquid phase is continuously replenished; similar surface structures and coating layers can be added for evaporation outside the heat exchange tube to achieve a completely similar effect.
  • the invention has the characteristics of high gasification capacity, high heat transfer coefficient, small heat exchanger volume and low metal consumption, saves more than 20% of materials compared with the conventional evaporator, has reduced production and running costs, and is simple to process. advantage.
  • Figure 1 is a schematic view of the structure of a conventional air-heated evaporator
  • Figure 2 is a conventional spiral casing type evaporator
  • Figure 3 is a side view of Figure 2
  • FIG. 4 is a schematic view showing the structure of a gas-liquid separation type casing evaporator outside a spiral pipe according to an embodiment of the present invention
  • Figure 5 is a schematic view showing the inner tube of the present invention in a tube bundle type and having a helical torsion distribution
  • FIG. 6 is a schematic structural view of a gas-liquid separation type casing evaporator of a vertical serpentine tube according to an embodiment of the present invention
  • FIG. 7 is a schematic structural view of a gas-liquid separation type evaporator of an air-heated vertical serpentine tube according to a third embodiment of the present invention
  • Figure 9 is a cross-sectional view of Figure 8.
  • FIG. 10 is a schematic structural view of a gas-liquid separation type casing evaporator in a four-spindle tube according to an embodiment of the present invention
  • FIG. 11 is a schematic structural view of a gas-liquid separation type casing evaporator in a five-spiral tube according to an embodiment of the present invention.
  • Embodiment 1 A spiral-tube external gas-liquid separation type casing evaporator
  • the embodiment includes a spiral tubular outer sleeve 1, an inner tube 2 disposed in the outer sleeve 1, and the inner tube 2 of the present embodiment refers to an inner tube bundle distributed in a spiral twist shape (as shown in the figure). 5)), which can effectively enhance the spreading and disturbance of the liquid during evaporation, and at the same time maintain the thin liquid film to enhance the evaporation heat transfer.
  • a spiral tubular outer sleeve 1 an inner tube 2 disposed in the outer sleeve 1
  • the inner tube 2 of the present embodiment refers to an inner tube bundle distributed in a spiral twist shape (as shown in the figure). 5)
  • both end portions of the outer sleeve 1 are sealingly connected to the outer wall surface of the inner tube 2, the bottom port of the inner tube 2 serves as the inlet 21 of the heat source medium, and the top port of the inner tube 2 serves as the outlet 22 of the heat source medium, and the outer sleeve
  • the vapor outlet 11 of 1 is disposed on the wall of the top port of the outer casing 1.
  • An annular partition is provided as a partitioning means 3 between the outer casing 1 and the inner pipe 2 of the uppermost layer, and the partitioning means 3 divides the outer casing 1 into a superheating section 12 and an evaporation section 13.
  • a gas-liquid separation pipe 4 is disposed in the superheating section 12 adjacent to the partitioning device 3, and a vapor guiding pipe 5 is respectively disposed on each outer casing 1 of the evaporation section 13, and the other end of each vapor guiding pipe 5 is connected Ventilation separation tube 4.
  • An evaporation liquid is placed downwardly adjacent to the evaporation section 13 of the partitioning device 3.
  • the liquid pipe 6, the bottommost outer casing 1 is connected to the evaporating liquid inlet pipe 6 through a residual evaporated liquid liquid phase return pipe 14 near the end, so that the unvaporized evaporated liquid is re-sent to the top of the evaporation section 13.
  • the partitioning means 3 may also be disposed on the second or third outer casing 1, i.e., the superheating section 12 may be flexibly adjusted to meet the overheating requirements as needed.
  • the vapor guiding tube 5 connected to the gas-liquid separation pipe 4 on the outer casing 1 may not be disposed in each layer, but may be provided in one or two layers, and is flexibly optimized.
  • the heat source medium spirals upward from the bottom of the inner tube 2, and the evaporated liquid passes through the evaporation liquid inlet pipe 6 to enter the evaporation section 13 between the outer casing 1 and the inner tube 2 of the uppermost layer.
  • the spiral outer sleeve 1 is spirally flowed downward, and the heat radiated from the heat source medium in the inner tube 2 is continuously absorbed, and the vapor of each layer of the evaporated liquid enters the gas-liquid separation tube 4 through the vapor guiding tube 5, in the gas-liquid In the separation pipe 4, the gas flows upward, flows from the uppermost superheating section 12 to the vapor outlet 11, and the liquid flows downward by the action of gravity, and flows into the bottom of the evaporation section 13 together with the residual liquid which is not evaporated in the evaporation section 13 together.
  • the liquid inlet pipe 6 only needs to continuously replenish the liquid to be evaporated.
  • the vapor in the pipeline is discharged in sections, so that the gas-liquid flow is unimpeded, the liquid is effectively spread and the thin liquid film is evaporated, and the cooling effect is particularly good.
  • Example 2 - Vertical gas-liquid separation type casing evaporator
  • the partitioning device 3 between the first layer and the second layer.
  • the first outer sleeve 1 is formed into a superheating section 12, and the second outer sleeve 1 is below the evaporation section 13.
  • the partitioning device 3 can also be disposed between the third layer and the fourth layer, and the specific position can be flexibly determined according to the degree of superheat.
  • a gas-liquid separation pipe 4 is connected to the superheating section 12 adjacent to the partitioning device 3, and a vapor guiding pipe 5 communicating with the gas-liquid separation pipe 4 is taken out from the outer casing 1 of each layer of the evaporation section 13.
  • An evaporating liquid inlet pipe 6 is connected to the evaporation section 13 adjacent to the partitioning means 3.
  • the outermost casing 1 of the lowermost layer is connected to the evaporating liquid inlet pipe 6 through a residual liquid phase return pipe 14 of the evaporating liquid near the end portion, so that the evaporated liquid which is not evaporated is re-sent to the top of the evaporation section 13, and the bottom port of the inner pipe 2 is
  • the heat source medium inlet 21 and the top port are heat source medium outlets 22.
  • a porous layer 15 may be disposed on the inner wall of the outer sleeve 1.
  • the porous layer 15 may be formed by sintering a multi-layered wire mesh with metal or non-metal particles, and is pulverized by a porous structure.
  • the suction force spreads the liquid phase evenly on the inner tube wall to form and maintain a thin liquid film evaporation with better heat exchange effect, further enhancing the surface strengthening effect.
  • the working principle of this embodiment is basically the same as that of Embodiment 1, and therefore will not be described again.
  • Example 3 An air-heated vertical serpentine gas-liquid separation evaporator As shown in Fig. 7, this embodiment is similar to the embodiment 2 in that it is a vertical serpentine tube, but since the heating medium is hot air, there is only a single layer tube, which is referred to as the inner tube 2 in the present invention.
  • a plurality of outer tube fins 7 are disposed between the inner tubes 2 of the layers, and the partitioning device 3 divides the outer sleeve 2 into a superheating section 23 and an evaporating section 24.
  • the specific position of the partitioning device 3 can be flexibly determined according to the superheat requirement. .
  • the upper port of the inner tube 2 is a vapor outlet 25, and the lower port is closed, and is connected to the lower portion of the evaporative liquid inlet pipe 6 through a residual liquid phase return pipe 1 of the evaporating liquid disposed on the wall of the port, evaporating the liquid inlet pipe 6
  • the top is connected to the evaporation section 24 of the separator 3.
  • the top end of the gas-liquid separation pipe 4 is connected to the superheating section 23 of the partitioning device, and the respective vapor guiding pipes 5 connected to the evaporation section 24 are respectively connected to the gas-liquid separation pipe 4, and the bottom end inner pipe 2 is connected to the bottom of the gas-liquid separation pipe 4.
  • the inner wall of the inner tube 2 may be provided with an internal thread or a micro-groove 16 , and a surface of the internal thread or the micro-groove 16 is coated with a porous layer 15 for ensuring the inner portion.
  • the inner wall of the tube 2 forms and maintains a very thin, thin film layer that maintains the best thin film evaporation in the tube.
  • the heating heat source is air, and the air exchanges heat with the inner tube 2 and the outer tube fin 7.
  • the evaporated liquid is sent to the evaporation section 24 to evaporate or boil through the evaporating liquid inlet pipe 6, and the generated gas is continuously passed through.
  • the vapor guiding tube 5 and the gas-liquid separating tube 4 are introduced into the superheating section 23 of the inner tube 2 to be superheated, and then discharged through the vapor outlet 25 of the inner tube 2.
  • the residual liquid of the unvaporized liquid separated by the gas-liquid separation pipe 4 and the remaining unvaporized liquid in the evaporation section 24 are flowed into the inner tube 2 of the bottom layer together with the evaporated liquid, and are evaporated to the bottom by the liquid phase liquid return pipe 14 remaining by the evaporation liquid.
  • the liquid inlet pipe 6, under the action of the power source of the evaporating liquid inlet pipe 6, is sent back to the evaporation section 24 at the upper portion of the inner pipe 2 to continue the heat exchange cycle.
  • Example 4 A vertical gas-liquid separation type casing evaporator in a serpentine tube
  • this embodiment includes a vertical serpentine tubular inner tube 2, and the inner tube of this embodiment is a single tube.
  • the upper port of the inner tube 2 is a vapor outlet 25, and the lower port of the inner tube 2 is closed.
  • An outer sleeve 1 is disposed on the outer surface of the inner tube 2, and the outer sleeve 1 is only sealed in the horizontal section of the inner tube 2 of each layer, and the outer sleeves 1 of the horizontal sections of each layer are respectively passed through the separate vertical joint tubes 8 and the next outer layer.
  • Tube 1 is connected.
  • a heat source medium inlet 17 is provided at the end of the outermost outer casing 1
  • a heat source medium outlet 18 is provided at the end of the outermost outer casing 1.
  • the partitioning device 3 is a circular partition disposed at a bend between the first layer and the second inner tube 2 (not limited thereto, can be flexibly adjusted according to design), and the inner tube 2 is divided into a superheating section 23 and evaporation.
  • the gas-liquid separation pipe 4 is connected to the superheating section 23 of the partitioning device 3, and the vapor guiding pipes 5 of each layer are respectively connected to the inner pipe 2 of the evaporation section 24 and the gas-liquid separation pipe 4, and the gas-liquid separation pipe 4 is connected to the inner pipe.
  • the evaporative liquid inlet pipe 6 is connected to the evaporative liquid liquid return pipe 14, and the top outlet of the evaporative liquid inlet pipe 6 is connected to the evaporation section 24 of the inner pipe 2 adjacent to the partitioning device 3.
  • the heat source medium enters from the inlet 17 of the outer casing 1, passes through the inner tubes 2 of each layer, and then flows out from the outlet 18, and the evaporated liquid entering from the evaporation liquid inlet pipe 6 is sent to the upper portion close to the partitioning device.
  • the inner tube 2 of the third tube 2 is evaporated to the section 24, and then exchanges heat with the heat source liquid in the outer sleeve 1 through the inner tube 2 of each layer, and the vapor enters the gas-liquid separation tube 4 through the vapor guiding tube 5, and the vapor passes through the superheating section of the inner tube 2
  • the vapor outlet 25 flows out, and the residual liquid flows into the bottom end of the inner tube 2 together with the evaporation portion 24 without evaporating the complete residual liquid, and flows into the upper portion of the inner tube 2 through the remaining liquid phase return pipe 14 of the evaporated liquid. Evaporation section 24.
  • Example 5 A spiral-in-tube gas-liquid separation type casing evaporator
  • the structural form of this embodiment is similar to that of the embodiment 4, and is also an in-pipe evaporation type, but the piping structure is in the form of a spiral. It comprises a spiral inner tube 2, the inner tube of this embodiment being a single tube. The upper port of the inner tube 2 is a vapor outlet 25, and the lower port of the inner tube 2 is closed. An outer sleeve 1 is provided outside the inner tube 2. A heat source medium inlet 17 is provided at the bottom end of the outermost outer casing 1, and a heat source medium outlet 18 is provided at the end of the outermost outer casing 1.
  • the partitioning device 3 is a circular partition disposed at a bend between the first layer and the second inner tube 2 (not limited thereto, and can be flexibly adjusted according to design), and the inner tube 2 is divided into a superheating section and an evaporation section.
  • a gas-liquid separation pipe 4 is connected to the superheating section of the partitioning device 3 through the outer casing 1, and the vapor guiding pipes 5 of each layer are connected to the inner pipe 2 and the gas-liquid separation pipe 4 of the evaporation section through the outer casing 1, respectively, and the gas-liquid
  • the separation pipe 4 is connected to the lowermost port of the inner pipe 2 through the outer casing 1, and is connected to the evaporative liquid inlet pipe 6 through the remaining liquid phase liquid return pipe 14 of the evaporating liquid, and the top outlet of the evaporating liquid inlet pipe 6 passes through the outer casing.
  • 1 is connected to the evaporation section of the inner tube 2 adjacent to the partitioning device 3.
  • the gas-liquid separation method in the gas-liquid separation evaporator of the present invention comprises the following contents:
  • a partitioning device is disposed in the upper portion of the pipeline through which the liquid to be evaporated flows in the gas-liquid separator, and the pipeline is separated into a superheating section and an evaporation section of the evaporated liquid.

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Description

一种气液分离式蒸发器中的气液分离方法及装置 技术领域
本发明涉及一种蒸发器， 特别是关于一种气液分离式蒸发器中的气液分离方 法及装置。
背景技术
蒸发器是一类热工设备， 在动力、 化工、 空调工程和制冷工程中应用得非常 广泛， 蒸发器主要有两种形式， 其一是液体加热式， 比如常见的套管蒸发器； 其 二是空气加热式， 比如家用空调、 大型制冷、 化工和动力装置等， 一般都为管内 蒸发型。
如图 1所示， 一般的家用分体式空调蒸发器属于空气加热式蒸发器， 传统的 立式蛇形管式蒸发器 9是由换热管 91和设置在各换热管 91之间的管外翅片 92组 成， 被蒸发液体（一般指空调制冷系统的制冷剂） 由换热管 91的入口 93进入， 依靠换热管 91和管外翅片 92与流经蒸发器 9的空气进行换热，使换热管 91内的 制冷剂受热蒸发和沸腾， 进而实现完全汽化， 气体则由换热管 91的出口 94排出。
如图 2、 图 3所示， 传统的盘旋套管式蒸发器 10是由外套管 101和内管 102， 内管可为单管或管束， 在外套管 101两端分别设置热源液体（被冷却的液体）入 口 103和出口 104， 在内管 102两端分别设置被蒸发液体入口 105和出口 106。这 种盘旋套管式蒸发器 10通过位于外套管 101和内管 102之间的热源液体（被冷却 的液体） 与内管 102中的被蒸发液体进行换热， 使被蒸发液体在内管 102中蒸发 和沸腾， 进而实现完全汽化。传统盘旋套管式蒸发器 10的管型也可以采用蛇形管 形布置（如图 1所示），但是它没有管外的翅片结构，代之为外套管和内管的结构。 这种蒸发器有时也可以是外套管两端走被蒸发液体， 内管走热源液体， 结构和原 理类似， 只是实际应用中较少。
上述现有技术的管式蒸发器， 被蒸发液体入口 93、 105进入的为纯液体， 经 过全管程长的汽化过程后， 从被蒸发液体的蒸气出口 94、 106出来的基本为纯气 体。 为提高换热效果， 换热管多采用表面强化措施， 比如设置内螺纹、 内槽管、 内表面微肋管等， 在强化的同时增大换热面积。 被蒸发液体在换热管里的汽化换 热过程中， 虽然会随着干度的增大其换热效果能有所提高， 但幅度不大， 且采用 管内蒸发， 会形成更为复杂的两相流动， 不利于达到和形成更好的换热形态。 同 时， 套管式蒸发器采用水平螺旋管式结构， 管内部虽存在二次流的扰动作用， 但 分层流动的现象仍不可避免。 分层流动将导致管内局部干涸， 液相大量聚集于管 内底层， 不能很好地铺展到管内壁每一处表面， 形成很不均勾的处于非最佳的沸 腾或表面蒸发状态， 极大削弱了表面强化措施的功效， 大大降低了换热效果。 环 状流和薄液膜蒸发流型虽然具有很好的换热性能， 但'在整个流程中所占的比例很 小， 对整体系统传热贡献非常有限。 另一方面， 单一管内流程蒸发及沸腾过程也 导致了复杂的气液两相流， 当管内出现两相流动时， 气液会依干度大小处于泡状、 气塞状、 环状或分层流等流型， 大大增加流动阻力和运行不稳定性， 对系统运行 的稳定性、 流动阻力和系统的调控等， 都带来很不利的影响。
发明内容
针对上述问题， 本发明的目的是提供一种能够实现自动气液分离， 提高换热 能力的蒸发器。
为实现上述目的， 本发明采取以下技术方案： 一种气液分离式蒸发器中的气 液分离方法， 其是： （1 ) 在气液分离器中流经被蒸发液体的管路上部设置一分隔 装置， 将管路分隔为被蒸发液体的过热段和蒸发段； （2 ) 在靠近所述分隔装置的 过热段连接一气液分离管， 在靠近所述分隔装置的蒸发段连接一被蒸发液体进液 管， 在所述蒸发段的管路上分段设置多个蒸气导流管， 所述各蒸气导流管分别连 通所述气液分离管； 使整个管路蒸发的气体能够分段排出， 并在气液分离管中进 行气液分离后进入过热段过热； 经过热的蒸气从蒸气出口排出； ( 3 ) 将从气液分 离管分离后的残液与蒸发段未蒸发完全的残液一同通过管路送至被蒸发液体进液 管， 重新回到被蒸发液体的蒸发换热过程中。
所述流经被蒸发液体的管路为一外套管和一内管之间的管路， 所述分隔装置 为一设置在所述外套管和内管之间的环形分隔板， 所述内管流经热源液体。
所述流经被蒸发液体的管路为一单层内管， 内管上设置有管外翅片， 内管外 流经热源气体。
所述流经被蒸发液体的管路为一内管， 所述内管外面设置一外套管， 二管路 之间流经热源液体。
一种气液分离式蒸发器， 它包括一流经被蒸发液体的管路， 一流经热源液体 的管路或一流经热源气体的空间， 其特征在于： 在所述流经被蒸发液体的管路上 部设置一分隔装置， 将被蒸发液体的管路分隔为过热段和蒸发段； 在靠近所述分 隔装置的过热段连接一气液分离管， 在靠近所述分隔装置的蒸发段连接一被蒸发 液体进液管， 在所述蒸发段的管路上分段设置多个蒸气导流管， 所述各蒸气导流 管分别连通所述气液分离管； 所述气液分离管的底部通过管路连接所述被蒸发液 体进液管进口端。 所述流经被蒸发液体的管路为一外套管和一内管之间的管路， 所述分隔装置 为一设置在所述外套管和内管之间的环形分隔板， 所述内管的底部端口为热源液 体进口， 所述内管的顶部端口为热源出口。
相应设置的所述外套管和内管的形状呈螺旋管状和立式蛇形管状之一。
所述流经被蒸发液体的管路为一单层内管， 所述内管上设置有管外翅片。 所述流经被蒸发液体的管路为一内管， 所述内管外面设置一外套管， 所述分 隔装置为一设置在所述内管内的圆形分隔板， 所述外套管的底部端口为热源液体 进口， 所述外套管的顶部端口为热源出口。
相应设置的所述外套管和内管的形状呈螺旋管状和立式蛇形管状之一。
所述内管为由多根管呈螺旋扭转状分布的内管束。
所述内管为一单管。
所述内管内壁设置有内螺紋或微型沟槽， 所述内螺紋或微型沟槽表面敷有一 层由多层丝网与金属或非金属颗粒烧结而成的多孔层。
所述外套管内壁上设置有一由多层丝网与金属或非金属颗粒烧结而成的多孔 层。
由于采用了以上技术方案， 本发明具有以下优点： 1、 本发明采用分隔装置将 换热管非密封式分隔为液体蒸发段与蒸气过热段， 既能防止进口液相直接进入过 热段， 影响蒸发器正常工作， 又能实现传统蒸发器中很难做到的出口过热度的控 制， 可根据实际过热要求自行调整过热段长短以保证出口的过热温度。 相对于常 规技术中一般采用增加管长的措施， 本发明分隔装置的设置， 具有减少消耗材料、 提高能源转换和利用效率、 增加制冷系统中压缩机功率的特点。 2、 本发明由于釆 用了残存被蒸发液体液相回流管， 内填有多孔芯体， 利用毛细吸存液与阻液的双 重功能， 让残存液流出汇入进口蒸发液体流主流， 实现残存液体的再循环， 具有 自动回液、 循环蒸发的功能， 解决了蒸发过程中间气液分离后， 可能出现的尾部 残存液累计和排除的问题。 同时又阻碍主流液体从此处进入主蒸发换热管段， 造 成蒸发器功能失效。 提高了蒸发器的工作效益和适应能力。 3、 本发明具有新颖的 气液分离设置， 使得蒸发的气相能够快速经由排气管排出， 减小了系统内部的压 力损失， 有利于高效蒸发过程的实现。 4、 本发明可采用内管束结构， 将被蒸发液 体液.（制冷剂） 置于外套管与内管之间流动， 利用间隙内复杂的结构， 不仅增强 了液相流动的扰动， 同时随着气相不断被带走， 被蒸发液体逐渐较少， 更有利于 液膜的铺展， 形成换热效果更佳的薄液膜蒸发， 从而强化了换热。 5、 蒸发表面设 置有微型螺纹、 沟槽或一多孔层， 也可在微型螺紋或沟槽上再加多孔层， 多孔层 可由多层丝网与金属或非金属颗粒烧结而成。 可在上面措施基础上利用多孔结构 毛细抽吸力， 将液相在内管壁均匀铺展， 形成换热效果更佳的薄液膜蒸发， 进一 步增强表面强化效果， 而且， 多孔衬层可促进和增强管内表面区气相排出、 液相 不断被补充的良性自循环过程； 对于换热管外蒸发也可增加类似的表面结构和覆 盖层， 以达到完全类似的效果。 6、 本发明具有高效气化能力， 高传热系数， 小换 热器体积和金属消耗量低的特点，与传统蒸发器相比节省材料 20%以上， 具有降低 制作和运行成本、 加工简单的优点。
附图说明
图 1是传统空气加热式蒸发器的结构示意图
图 2是传统盘旋套管式蒸发器
图 3是图 2的侧视示意图
图 4是本发明实施例一螺旋管外气液分离式套管蒸发器结构示意图
图 5是本发明内管为管束式且呈螺旋扭转分布示意图
图 6是本发明实施例二立式蛇形管外气液分离式套管蒸发器结构示意图 图 7是本发明实施例三空气加热立式蛇形管内气液分离式蒸发器结构示意图 图 8是图 7中的蛇形管内壁的结构示意图
图 9是图 8的剖视示意图
图 10是本发明实施例四立式蛇形管内气液分离式套管蒸发器结构示意图 图 11是本发明实施例五螺旋形管内气液分离式套管蒸发器结构示意图 具体实施方式
下面结合附图和实施例对本发明进行详细的描述。
实施例 1 : 一种螺旋管外气液分离式套管蒸发器
如图 4所示，本实施例包括一螺旋管状的外套管 1，一设置在外套管 1内的内 管 2， 本实施例的内管 2是指呈螺旋扭转状分布的内管束 （如图 5所示）， 这样可 以有效增强蒸发时液体的铺展和扰动， 同时能很好地维持薄液膜增强蒸发换热。 如图 4所示， 外套管 1的两端部与内管 2的外壁面密封连接， 内管 2的底部端口 作为热源介质的进口 21， 内管 2顶部端口作为热源介质的出口 22， 外套管 1的蒸 气出口 11设置在外套管 1顶部端口的管壁上。在最上一层的外套管 1与内管 2之 间设置有一作为分隔装置 3的环形隔板， 分隔装置 3将外套管 1分隔成一过热段 12和一蒸发段 13。在靠近分隔装置 3的过热段 12设置有一气液分离管 4，在蒸发 段 13的每层外套管 1上分别设置一根蒸气导流管 5， 并将各蒸气导流管 5的另一 端连通气液分离管 4。 在靠近分隔装置 3的蒸发段 13向下设置有一被蒸发液体进 液管 6， 最底层的外套管 1靠近端部通过一残存被蒸发液体液相回流管 14连通蒸 发液体进液管 6， 使未被蒸发的被蒸发液体重新送入蒸发段 13顶部。
上述实施例中， 分隔装置 3也可以设置在第二层或第三层外套管 1上， 即过 热段 12可以根据需要灵活调整长度以满足过热要求。 另外， 外套管 1上连接气液 分离管 4的蒸气导流管 5也可以不是每层设置， 而可以是隔一、 两层设置一根， 灵活进行优化设计。
本实施例使用时， 如图 4所示， 热源介质从内管 2底部盘旋向上流动， 被蒸 发液体通过蒸发液体进液管 6进入最上层的外套管 1与内管 2之间的蒸发段 13， 然后围绕螺旋状外套管 1 向下盘旋流动， 并不断吸收内管 2内热源介质散发的热 量，各层被蒸发液体的蒸气会通过蒸气导流管 5进入气液分离管 4，在气液分离管 4中， 气体向上流动， 从最上层的过热段 12过热后流向蒸气出口 11， 液体在重力 的作用向下流动， 与蒸发段 13中未蒸发完全的残余液体一同流入蒸发段 13底部， 并通过最下层的外套管 1上的残存被蒸发液体液相回流管 14流入蒸发液体进液管 6， 并被重新送入外套管 1上部的蒸发段 13进行蒸发换热， 这时连接被蒸发液体 进液管 6只需要不断补充被蒸发液体即可。 在被蒸发液的不断循环、 补充流动中， 管路中的蒸气被分段排出， 因此气液流动畅通无阻， 液体得以有效铺展形成和维 持薄液膜蒸发， 制冷效果特别好。
实施例 2: —种立式蛇形管外气液分离式套管蒸发器
如图 6所示， 本实施例与实施例 1主要区别是采用立式蛇形管状的外套管 1 和与其形状相应的内管 2，作为分隔装置 3设置在第一层与第二层之间，使第一层 外套管 1形成一过热段 12， 第二层外套管 1以下成为蒸发段 13。 分隔装置 3也可 设置在第三层与第四层之间， 具体位置可根据过热度要求灵活确定。 在靠近分隔 装置 3的过热段 12连接一气液分离管 4，在蒸发段 13每层的外套管 1上分别引出 一连通气液分离管 4的蒸气导流管 5。 在靠近分隔装置 3的蒸发段 13连接一被蒸 发液体进液管 6。 最底层的外套管 1靠近端部通过一残存被蒸发液体液相回流管 14连通蒸发液体进液管 6， 使未被蒸发的被蒸发液体重新送入蒸发段 13顶部， 内 管 2底部端口为热源介质进口 21， 顶部端口为热源介质出口 22。
上述实施例 1、 2中， 外套管 1内壁上可以设置有一多孔层 15 (如图 5所示)， 多孔层 15可由多层丝网与金属或非金属颗粒烧结而成，利用多孔结构毛细抽吸力， 将液相在内管壁均匀铺展， 形成和维持换热效果更佳的薄液膜蒸发， 进一步增强 表面强化效果。 本实施例的工作原理与实施例 1基本相同， 故不再赘述。
实施例 3: —种空气加热立式蛇形管内气液分离式蒸发器 如图 7所示， 本实施例与实施例 2类似也是一立式蛇形管状， 但是其由于加 热介质是热空气， 故只有单层管， 本发明将其称为内管 2。在各层内管 2之间采用 胀接设置有若干管外翅片 7，分隔装置 3将外套管 2分隔成过热段 23和蒸发段 24, 分隔装置 3具体设置位置可以根据过热度要求灵活确定。 内管 2的上端口是蒸气 出口 25， 下端口封闭， 并通过一设置在端口壁面上的残存被蒸发液体液相回流管 1 连接蒸发液体进液管 6的下部， 蒸发液体进液管 6的顶部连接靠近分隔装置 3 的蒸发段 24。 气液分离管 4顶端连接靠近分隔装置的过热段 23， 连接蒸发段 24 的各蒸气导流管 5分别连通气液分离管 4，最底端的内管 2连接气液分离管 4底部。
如图 8、 图 9所示， 本实施例中， 内管 2的内壁上可以设置有内螺紋或微型沟 槽 16， 内螺紋或微型沟槽 16表面敷有一层多孔层 15， 用以保证内管 2内壁形成 和维持铺展很好的薄液膜层， 保持管内处于最好的薄液膜蒸发状态。
本实施例使用时， 加热热源是空气， 空气与内管 2和管外翅片 7换热， 被蒸 发液体通过蒸发液体进液管 6被送入蒸发段 24蒸发或沸腾， 产生的气体不断经蒸 气导流管 5和气液分离管 4引入内管 2的过热段 23过热， 随后通过内管 2的蒸气 出口 25排出。 通过气液分离管 4分离的未蒸发液体的残液与蒸发段 24中未蒸发 完全的残存被蒸发液体一同流入底层的内管 2， 经残存被蒸发液体液相回液管 14 流入底部的蒸发液体进液管 6，在蒸发液体进液管 6—端的动力源作用下，被蒸发 液体又被送回内管 2上部的蒸发段 24， 继续换热循环。
实施例 4: 一种立式蛇形管内气液分离式套管蒸发器
如图 10所示， 本实施例包括一立式蛇形管状内管 2，本实施例的内管是单管。 内管 2的上端口为蒸气出口 25， 内管 2的下端口封闭。 在内管 2的外面设置有外 套管 1，外套管 1只密封设置在每层内管 2的水平段，各层水平段的外套管 1分别 通过单独的垂向联管 8与下一层外套管 1连接。 在最底层的外套管 1端部设置一 热源介质进口 17， 在最顶层的外套管 1的端部设置一热源介质出口 18。 分隔装置 3为一圆形隔板， 设置在第一层与第二层内管 2之间的拐弯处（不限于此， 可根据 设计灵活调整）， 将内管 2分隔成过热段 23和蒸发段 24， 在靠近分隔装置 3的过 热段 23连接气液分离管 4，各层的蒸气导流管 5分别连接蒸发段 24的内管 2和气 液分离管 4，气液分离管 4连接内管 2最下部端口处，再通过残存被蒸发液体液相 回液管 14连接蒸发液体进液管 6， 蒸发液体进液管 6的顶部出口连接在靠近分隔 装置 3的内管 2蒸发段 24。
本实施例使用时， 热源介质从外套管 1的进口 17进入， 经过各层内管 2冷却 后从出口 18流出， 从蒸发液体进液管 6进入的被蒸发液体被送入上部靠近分隔装 置 3的内管 2蒸发段 24， 然后通过各层内管 2与外套管 1内地热源液体换热， 蒸 气通过蒸气导流管 5进入气液分离管 4， 蒸气通过内管 2的过热段从蒸气出口 25 流出， 残液与蒸发段 24未蒸发完全残余液体一同流入内管 2底端， 并通过残存被 蒸发液体液相回流管 14流入被蒸发液体进液管 6回到内管 2上部的蒸发段 24。
实施例 5: —种螺旋形管内气液分离式套管蒸发器
如图 11所示， 本实施例的结构形式与实施例 4类似， 也是管内蒸发型， 但是 管路结构形式采用螺旋形。其包括一螺旋形内管 2， 本实施例的内管是单管。 内管 2的上端口为蒸气出口 25，内管 2的下端口封闭。在内管 2的外面设置有外套管 1。 在最底层的外套管 1底端设置一热源介质进口 17， 在最顶层的外套管 1的端部设 置一热源介质出口 18。 分隔装置 3为一圆形隔板， 设置在第一层与第二层内管 2 之间的拐弯处（不限于此， 可根据设计灵活调整）， 将内管 2分隔成过热段和蒸发 段，在靠近分隔装置 3的过热段穿过外套管 1连接一气液分离管 4，各层的蒸气导 流管 5穿过外套管 1分别连接蒸发段的内管 2和气液分离管 4，气液分离管 4穿过 外套管 1连接内管 2最下部端口处， 再通过残存被蒸发液体液相回液管 14连接蒸 发液体进液管 6，蒸发液体进液管 6的顶部出口穿过外套管 1连接在靠近分隔装置 3的内管 2蒸发段。
本实施例使用时， 与实施例 4相似， 在此不再赘述。
由上述各实施例可以看出， 本发明气液分离式蒸发器中的气液分离方法包括 以下内容：
( 1 )在气液分离器中流经被蒸发液体的管路上部设置一分隔装置， 将管路分 隔为被蒸发液体的过热段和蒸发段，
(2)在靠近所述分隔装置的过热段连接一气液分离管， 在靠近所述分隔装置 的蒸发段连接一被蒸发液体进液管， 在所述蒸发段的管路上分段设置多个蒸气导 流管， 所述各蒸气导流管分别连通所述气液分离管； 使整个管路蒸发的气体能够 分段排出， 并在气液分离管中进行气液分离后进入过热段过热； 经过热的蒸气从 蒸气出口排出；
(3)将从气液分离管分离后的残液与蒸发段未蒸发完全的残液一同通过管路 送至被蒸发液体进液管， 重新回到被蒸发液体的蒸发换热过程中。
上述实施例用以说明本发明的具体结构特征， 但本发明的内容并不局限于上 述各实施例的描述， 任何基于本发明原理和技术方案所表示的结构特征所进行的 等效变换的结构， 均不应排除在本发明 保护范围之外。

Claims

权 力 要 求
1、 一种气液分离式蒸发器中的气液分离方法， 其是：
( 1 )在气液分离器中流经被蒸发液体的管路上部设置一分隔装置， 将管路分 隔为被蒸发液体的过热段和蒸发段；
(2)在靠近所述分隔装置的过热段连接一气液分离管， 在靠近所述分隔装置 的蒸发段连接一被蒸发液体进液管， 在所述蒸发段的管路上分段设置多个蒸气导 流管， 所述各蒸气导流管分别连通所述气液分离管； 使整个管路蒸发的气体能够 分段排出， 并在气液分离管中进行气液分离后进入过热段过热； 经过热的蒸气从 蒸气出口排出；
(3)将从气液分离管分离后的残液与蒸发段未蒸发完全的残液一同通过管路 送至被蒸发液体进液管， 重新回到被蒸发液体的蒸发换热过程中。
2、如权利要求 1所述一种气液分离式蒸发器中的气液分离方法，其特征在于： 所述流经被蒸发液体的管路为一外套管和一内管之间的管路， 所述分隔装置为一 设置在所述外套管和内管之间的环形分隔板， 所述内管流经热源液体。
3、如权利要求 1所述一种气液分离式蒸发器中的气液分离方法，其特征在于： 所述流经被蒸发液体的管路为一单层内管， 内管上设置有管外翅片， 内管外流经 热源气体。
4、如权利要求 1所述一种气液分离式蒸发器中的气液分离方法，其特征在于： 所述流经被蒸发液体的管路为一内管， 所述内管外面设置一外套管， 二管路之间 流经热源液体。
5、 一种实现如权利要求 1〜4所述的气液分离方法的气液分离式蒸发器， 它 包括一流经被蒸发液体的管路，一流经热源液体的管路或一流经热源气体的空间， 其特征在于： 在所述流经被蒸发液体的管路上部设置一分隔装置， 将被蒸发液体 的管路分隔为过热段和蒸发段； 在靠近所述分隔装置的过热段连接一气液分离管， 在靠近所述分隔装置的蒸发段连接一被蒸发液体进液管， 在所述蒸发段的管路上 分段设置多个蒸气导流管， 所述各蒸气导流管分别连通所述气液分离管； 所述气 液分离管的底部通过管路连接所述被蒸发液体进液管进口端。
6、 如权利要求 5所述一种气液分离式蒸发器， 其特征在于： 所述流经被蒸发 液体的管路为一外套管和一内管之间的管路， 所述分隔装置为一设置在所述外套 管和内管之间的环形分隔板， 所述内管的底部端口为热源液体进口， 所述内管的 顶部端口为热源出口。
7、 如权利要求 6所述一种气液分离式蒸发器， 其特征在于： 相应设置的所述 外套管和内管的形状呈螺旋管状和立式蛇形管状之一。
8、 如权利要求 5所述一种气液分离式蒸发器， 其特征在于： 所述流经被蒸发 液体的管路为一单层内管， 所述内管上设置有管外翅片。
9、 如权利要求 5所述一种气液分离式蒸发器， 其特征在于： 所述流经被蒸发 液体的管路为一内管， 所述内管外面设置一外套管， 所述分隔装置为一设置在所 述内管内的圆形分隔板， 所述外套管的底部端口为热源液体进口， 所述外套管的 顶部端口为热源出口。
10、 如权利要求 9所述一种气液分离式蒸发器， 其特征在于： 相应设置的所 述外套管和内管的形状呈螺旋管状和立式蛇形管状之一。
11、 如权利要求 6或 7所述一种气液分离式蒸发装置， 其特征在于： 所述内 管为由多根管呈螺旋扭转状分布的内管束。
12、如权利要求 6或 7或 8或 9或 10所述一种气液分离式蒸发装置， 其特征 在于： 所述内管为一单管。
13、如权利要求 8或 9或 10所述一种气液分离式蒸发装置， 其特征在于： 所 述内管内壁设置有内螺紋或微型沟槽， 所述内螺纹或微型沟槽表面敷有一层由多 层丝网与金属或非金属颗粒烧结而成的多孔层。
14、 如权利要求 6或 7所述一种气液分离式蒸发装置， 其特征在于： 所述外 套管内壁上设置有一由多层丝网与金属或非金属颗粒烧结而成的多孔层。
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