CN115218557A - Pressure-equalizing spiral shell type falling film evaporator - Google Patents
Pressure-equalizing spiral shell type falling film evaporator Download PDFInfo
- Publication number
- CN115218557A CN115218557A CN202210801615.9A CN202210801615A CN115218557A CN 115218557 A CN115218557 A CN 115218557A CN 202210801615 A CN202210801615 A CN 202210801615A CN 115218557 A CN115218557 A CN 115218557A
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- spiral
- chamber
- pressure equalizing
- film evaporator
- Prior art date
- Legal status (The legal status 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 status listed.)
- Pending
Links
- 239000011552 falling film Substances 0.000 title claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 238000003860 storage Methods 0.000 claims abstract description 34
- 239000007921 spray Substances 0.000 claims abstract description 20
- 238000005192 partition Methods 0.000 claims abstract description 11
- 239000002826 coolant Substances 0.000 claims abstract description 6
- 239000003507 refrigerant Substances 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 8
- 238000004804 winding Methods 0.000 claims description 6
- 239000012159 carrier gas Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 2
- 230000009471 action Effects 0.000 abstract description 9
- 238000012546 transfer Methods 0.000 abstract description 4
- 239000010408 film Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000011295 pitch Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000013072 incoming material Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B39/00—Evaporators; Condensers
- F25B39/02—Evaporators
-
- 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
- F28D7/024—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 only one medium being helically coiled tubes, the coils having a cylindrical configuration
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention discloses a pressure-equalizing spiral tube shell type falling-film evaporator which comprises a tubular shell, wherein two ends of the tubular shell are closed, the tubular shell is respectively divided into a cold medium temporary storage chamber, a heat exchange chamber and an exhaust chamber in sequence along the axial direction through a pressure equalizing plate and a partition plate, a plurality of spiral heat exchange tubes are uniformly distributed in the heat exchange chamber, one ends of the heat exchange tubes penetrate through the partition plate and are communicated with the exhaust chamber, the other ends of the heat exchange tubes are provided with a cyclone spray head, the cyclone spray head is communicated with the cold medium temporary storage chamber through threaded holes in the pressure equalizing plate, the tube wall of the heat exchange chamber is respectively provided with a gaseous heat medium inlet and a liquid discharge port, and the diameter of one side provided with the gaseous heat medium inlet is larger than that of one side provided with the liquid discharge port. The invention enables liquid cooling medium to uniformly enter the spiral heat exchange tube in a fan-shaped fog state in an equivalent manner through the combined action of the pressure equalizing plate and the swirl spray head, and the spiral heat exchange tube is reasonably arranged, so that the full heat exchange between the cooling medium and gaseous heat medium can be realized, and the heat transfer coefficient and the heat exchange efficiency are obviously improved.
Description
Technical Field
The invention belongs to the technical field of shell-and-tube heat exchangers, and particularly relates to a pressure-equalizing spiral tube shell type falling film evaporator.
Background
As is well known, an evaporator is a heat exchange device in a refrigeration system, and is a heat exchanger for absorbing heat of a refrigerant at low temperature, which is an important part of four major components of refrigeration. The evaporator mainly comprises a heating chamber and an evaporation chamber. The heating chamber provides heat required by evaporation to the liquid to promote boiling and vaporization of the liquid, and the evaporation chamber completely separates gas phase from liquid phase.
The shell-and-tube evaporator has the advantages of good heat transfer effect, compact structure, small occupied area, simple manufacture, low maintenance cost, convenient installation and the like, so the shell-and-tube evaporator is widely applied to various refrigeration equipment. The method can be divided into a falling film evaporator and a rising film evaporator according to different positions of feed liquid (liquid cold medium) entering a heating pipe, wherein the biggest difference between the falling film evaporator and the rising film evaporator is that the feed liquid of the rising film evaporator forms a film on the pipe wall and moves upwards under the action of high-speed secondary steam flow and vacuum, the evaporated feed liquid and the secondary steam enter a separator from the top of the evaporator, and the separation of the evaporated feed liquid and the secondary steam is realized; the falling film evaporator distributes the incoming material to each film falling pipe under the action of the material-liquid distributor and flows from top to bottom along the pipe wall in a film state under the action of self gravity and secondary steam flow, and the evaporated material liquid and the secondary steam enter the separator at the bottom of the evaporator to realize the complete separation of the evaporated material liquid and the secondary steam. Because the rising film evaporator requires a large heating temperature difference, the operation is not easy to control, and phenomena such as deflection and the like are easily caused, the rising film evaporator is gradually eliminated by the market in recent years, and the existing falling film evaporator has the following disadvantages: firstly, because the volume of the feed liquid can expand many times when the feed liquid is evaporated, the volume of the feed liquid entering the evaporator is generally small in consideration of the flow velocity after gasification, and the flow distribution entering each heat exchange tube is uneven due to uneven pressure, so that the local heat exchange is uneven;
secondly, the heat exchange tube structure (straight tubes) of the existing evaporator and the layout thereof are unreasonable, so that the retention time of the feed liquid in the evaporator is short, and the feed liquid cannot be in full contact with a heat medium; thirdly, the device is quite sensitive to the fluctuation of the feeding load, and when the design or the operation is not proper, the film is not easy to form, and at the moment, the convection heat transfer coefficient is obviously reduced; based on the reasons, the whole heat exchange efficiency of the existing falling film evaporator is not high, and the feed liquid cannot be fully utilized.
In view of the above, the present inventors have designed a pressure equalizing spiral shell type falling film evaporator to solve the above technical problems.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a pressure-equalizing spiral shell type falling-film evaporator which firstly depressurizes liquid cold medium entering a cold medium temporary storage chamber through a throttling device, then enables the liquid cold medium to be uniformly filled in the cold medium temporary storage chamber through the combined action of a pressure equalizing plate and a rotational flow nozzle, and then enables the liquid cold medium to be uniformly sprayed into a spiral heat exchange tube under the action of the rotational flow nozzle, so that the liquid cold medium and gaseous heat medium can fully exchange heat in the heat exchange chamber, and the spiral heat exchange tube is reasonable in layout, thereby achieving the purpose of high-efficiency heat exchange.
The purpose of the invention is solved by the following technical scheme:
a pressure-equalizing spiral shell-and-tube falling-film evaporator comprises a tubular shell with two closed ends, wherein a cavity of the tubular shell is axially divided into a cold medium temporary storage cavity, a heat exchange cavity and an exhaust cavity through a pressure equalizing plate and a partition plate respectively, and the heat exchange cavity is positioned between the cold medium temporary storage cavity and the exhaust cavity;
the cold medium temporary storage chamber is communicated with a refrigerant liquid inlet pipe and is used for temporarily storing liquid cold medium;
a plurality of spiral heat exchange tubes are uniformly distributed in the heat exchange cavity along the axial direction of the tubular shell, one end of each spiral heat exchange tube penetrates through the partition plate and then is communicated with the exhaust cavity, a spiral flow nozzle is mounted at the other end of each spiral heat exchange tube and is positioned between the two pressure equalizing plates, each pressure equalizing plate is provided with a threaded hole, the spiral flow nozzle is mounted on each pressure equalizing plate and is communicated with the cold medium temporary storage cavity through the threaded hole, the tube wall of the heat exchange cavity is respectively provided with a gaseous heat medium inlet and a liquid discharge port, the gaseous heat medium inlet is formed at one side close to the cold medium temporary storage cavity and is connected with a carrier gas pipeline, and the liquid discharge port is formed at one side close to the exhaust cavity and is used for discharging liquid after the gaseous heat medium is liquefied by the heat exchange cavity;
the exhaust chamber is provided with an exhaust port for exhausting gas generated by vaporizing the liquid cold medium through the heat exchange chamber.
Further, the heat exchange chamber is composed of a first chamber and a second chamber which are coaxial, the diameter of the first chamber is larger than that of the second chamber, and the gaseous heat medium inlet is arranged on the pipe wall of the first chamber and is used for enabling the gaseous heat medium which just enters the heat exchange chamber to be in contact with the spiral heat exchange pipe fully and uniformly.
Furthermore, the spiral heat exchange tubes are arranged in the heat exchange cavity in a multilayer mode and are wound in a staggered mode according to the spiral line shape, the distance between any two adjacent layers of spiral heat exchange tubes is the same, and the spiral winding directions are opposite.
Furthermore, each layer of spiral heat exchange tubes are distributed in an annular array by taking the axial lead of the tubular shell as the center, the number of the spiral heat exchange tubes of each layer is increased from the inner layer to the outer layer in sequence, and the thread pitch, the spiral radius and the spiral direction of the spiral heat exchange tubes positioned on the same layer are the same.
Further, the whirl shower nozzle includes that nozzle and cover establish the outside shell that spouts of nozzle, spout shell entry department and can dismantle and be connected with the filter screen panel, exit port department has seted up the efflux hole, the nozzle is located one side annular equipartition in efflux hole and has three spiral guiding gutter.
Furthermore, the connection part of the rotational flow nozzle and the pressure equalizing plate, the connection part of the rotational flow nozzle and the spiral heat exchange tube and the connection part of the spiral heat exchange tube and the partition plate are in sealing connection, so that gas or liquid leakage is prevented.
Further, the falling film evaporator is arranged in a vertical or horizontal arrangement mode, and when the falling film evaporator is arranged vertically, the cold medium temporary storage chamber is positioned at the top end of the tubular shell.
Furthermore, the refrigerant liquid inlet pipe is connected with a throttling device and is used for depressurizing the liquid cold medium flowing into the cold medium temporary storage chamber.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention relates to a pressure-equalizing spiral shell type falling-film evaporator, wherein liquid cold medium entering the falling-film evaporator is throttled and depressurized by a throttling device and then enters a cold medium temporary storage chamber through a refrigerant liquid inlet pipe, the liquid cold medium is uniformly filled in the cold medium temporary storage chamber under the combined action of a pressure equalizing plate and a cyclone spray head, namely, pressure difference is formed between the front and the rear of the cyclone spray head, and the liquid cold medium can uniformly enter a spiral heat exchange pipe at the front end (with a slightly larger diameter) of the heat exchange chamber in a fan-shaped fog state after passing through a spiral diversion trench of the cyclone spray head under the action of the pressure difference and is contacted with the wall of the spiral heat exchange pipe first to exchange heat with gaseous hot medium; in addition, the spiral flow spray heads are uniformly distributed on the pressure equalizing plate in a layered annular array mode according to the layout of the spiral heat exchange tubes, the spiral winding directions of any two adjacent spiral heat exchange tubes are opposite, and the turbulence degree in the heat exchange cavity and the spiral heat exchange tubes is increased. In summary, compared with the traditional evaporator, the falling film evaporator structure has the following advantages: firstly, liquid cold medium can uniformly enter the contact pipe wall of the heat exchange pipe in a fan-shaped fog state under the action of the rotational flow spray head, so that the film is more easily formed, and the heat exchange is facilitated; secondly, the heat exchange tube adopts a spiral type and is reasonable in structural layout, compared with the traditional laminar flow/straight line tube, the heat exchange time of the liquid cold medium and the gaseous heat medium is prolonged, and the turbulence degree is increased by matching with the structure of the heat exchange cavity; thirdly, the structure utilizes the disturbance generated by the spiral heat exchange tube and the larger density and viscosity of the liquid compared with the gas, and the uniform evaporation is realized in the limited descending process, so that the film forming effect of the liquid is greatly enhanced, the heat exchange strength in unit area is enhanced, and the convection heat transfer coefficient is improved; based on the advantages, compared with the traditional technology, the falling film evaporator remarkably improves the heat exchange efficiency, and the heat exchange strength is improved by 2-3 times through actual tests.
2. The pressure-equalizing spiral shell type falling-film evaporator provided by the invention has the advantages that as the liquid cold medium is uniformly evaporated on the tube side almost in an isothermal process (the liquid cold medium is changed into the gaseous cold medium, the temperature is not changed, but the phase state is changed), the evaporator can realize a very small end difference even in a downstream mode (because the phase state is changed, the obtained heat mainly causes the phase change of the medium, namely the latent heat is mainly changed, and the sensible heat is changed very little), so that the falling-film evaporator can be arranged in a vertical or horizontal mode, and the arrangement is convenient according to the field requirement.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description, serve to explain the principles of the invention.
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a schematic view of a tubular housing according to the present invention;
FIG. 2 is a schematic view of the overall structure of the evaporator of the present invention;
FIG. 3 is a schematic view of the pressure equalizing plate according to the present invention;
FIG. 4 is a schematic view of a swirl nozzle of the present invention;
FIG. 5 is a schematic view of a nozzle structure of the swirl nozzle of the present invention; wherein, a is a front view of the nozzle, and b is a side view of the nozzle.
Wherein: 1 is a tubular shell; 2 is a pressure equalizing plate; 3 is a clapboard; 4 is a refrigerant liquid inlet pipe; 5 is a spiral heat exchange tube; 6 is a rotational flow nozzle; 11 is a cold medium temporary storage chamber; 12 is a heat exchange chamber; 12-1 is a first chamber; 12-2 is a second chamber; 13 is an exhaust chamber; 21 is a threaded hole; 61 is a nozzle; spray shell 62; 63 is a filter screen; 121 is a gaseous heat medium inlet; 122 is a liquid outlet; 131 is an exhaust port; 611 is a spiral diversion trench; 621 is an orifice.
Detailed Description
Reference will now be made in detail to the exemplary embodiments, examples of which are illustrated in the accompanying drawings. When the following description refers to the accompanying drawings, like numbers in different drawings represent the same or similar elements unless otherwise indicated. The embodiments described in the following exemplary embodiments do not represent all embodiments consistent with the present invention. Rather, they are merely examples of devices consistent with certain aspects of the invention, as detailed in the appended claims.
In order to make those skilled in the art better understand the technical solutions of the present invention, the present invention is further described in detail below with reference to the accompanying drawings and examples.
Referring to fig. 1 to 5, the present invention provides a pressure equalizing spiral shell type falling film evaporator, which includes a tubular shell 1 with two closed ends, the tubular shell 1 is cylindrical in overall shape, a chamber of the tubular shell 1 is divided into a cold medium temporary storage chamber 11, a heat exchange chamber 12 and an exhaust chamber 13 along an axial direction (length direction) through a pressure equalizing plate 2 and a partition plate 3, the heat exchange chamber 12 is located between the cold medium temporary storage chamber 11 and the exhaust chamber 13, that is, the cold medium temporary storage chamber 11 and the exhaust chamber 13 are located at the head and tail ends of the tubular shell 1, and the volume of each chamber is set according to actual requirements. Through the above arrangement, the liquid cold medium (such as freon) stored in the cold medium temporary storage chamber 11 enters the heat exchange chamber 12 through the pipeline to exchange heat with the gaseous heat medium inside the heat exchange chamber, so that the liquid cold medium can be converted into the gaseous state and discharged through the exhaust chamber 13, and the gaseous heat medium is liquefied into the liquid and discharged through the liquid discharge port.
Specifically, in the embodiment of the invention, an inlet is formed in the cold medium temporary storage chamber 11, the cold medium temporary storage chamber 11 is communicated with the refrigerant liquid inlet pipe 4 through the inlet, and the cold medium temporary storage chamber 11 is used for temporarily storing the liquid cold medium, so that the problem that the flow entering the heat exchange pipe subsequently is not uniform due to uneven or overhigh pressure of the liquid cold medium entering the cold medium temporary storage chamber 11 and the heat exchange efficiency is influenced is avoided. Preferably, the refrigerant inlet pipe 4 of the present invention is connected with a throttling device (not shown in the figures, but prior art), and the liquid refrigerant flowing into the refrigerant temporary storage chamber 11 is depressurized by the throttling device.
In the embodiment of the invention, a plurality of spiral heat exchange tubes 5 are uniformly distributed in a heat exchange cavity 12 along the axial direction of a tubular shell 1, one end of each spiral heat exchange tube 5 penetrates through a partition plate 3 and then is communicated with an exhaust cavity 13, the other end of each spiral heat exchange tube 5 is provided with a cyclone spray head 6, the cyclone spray head 6 is positioned between two pressure equalizing plates 2, each pressure equalizing plate 2 is provided with a threaded hole 21, the cyclone spray head 6 is arranged on the pressure equalizing plate 2 and is communicated with a cold medium temporary storage cavity 11 through the threaded hole 21, the tube wall of the heat exchange cavity 12 is respectively provided with a gaseous heat medium inlet 121 and a liquid discharge port 122, the gaseous heat medium inlet 121 is arranged close to one side of the cold medium temporary storage cavity 11 and is connected with a carrier gas pipeline, and the liquid discharge port 122 is arranged close to one side of the exhaust cavity 13 and is used for discharging liquid which is liquefied by the gaseous heat medium through the heat exchange cavity 12; the exhaust chamber 13 is provided with an exhaust port 131 for exhausting the gas vaporized from the liquid refrigerant in the heat exchange chamber 12.
Preferably, in the embodiment of the invention, the gas-state heat medium inlet 121 and the cold medium temporary storage chamber 11 are both provided with filter screens, and the filter screens are used for filtering, removing impurities and purifying the medium entering the evaporator, so that the occurrence of scaling phenomena on the inner wall of the heat exchange chamber 12 and the inner and outer walls of the spiral heat exchange tube 5 is reduced, and the long-term stable operation of the evaporator is ensured.
The heat exchange chamber 12 of the embodiment of the invention is composed of a first chamber 12-1 and a second chamber 12-2 which are coaxial, the diameter of the first chamber 12-1 is larger than that of the second chamber 12-2, a gaseous heat medium inlet 121 is arranged on the tube wall of the first chamber 12-1, and a liquid outlet 122 is arranged at the bottom of the tail end of the second chamber 12-2, namely the space of the gaseous heat medium which just enters the heat exchange chamber 12 is relatively large, so that the gaseous heat medium is in full and uniform contact with the spiral heat exchange tube 5 (a cold medium is arranged in the tube) while the resistance is reduced, and the heat exchange efficiency is improved.
In addition, in the embodiment of the invention, a plurality of spiral heat exchange tubes 5 are arranged in a plurality of layers in the heat exchange cavity 12 in a staggered winding manner according to the spiral line shape, and the intervals between any two adjacent layers of spiral heat exchange tubes 5 are the same, and the spiral winding directions are opposite; each layer of spiral heat exchange tubes 5 are distributed in an annular array by taking the axial lead of the tubular shell 5 as the center, the number of each layer of spiral heat exchange tubes 5 is increased from the inner layer to the outer layer in sequence, the screw pitches, the spiral radiuses and the spiral directions of the spiral heat exchange tubes 5 positioned on the same layer are the same, and the distribution diagram of the end parts of the spiral heat exchange tubes is shown in fig. 2. When the arrangement is used, the cold medium in the heat exchange tube flows along the spiral direction of the heat exchange tube, the gaseous heat medium in the heat exchange chamber 12 flows along the spiral channel formed by the spiral tubes in the same layer, and the heat exchange advantages are shown in the following aspects: firstly, as the cold medium generates secondary circulation in the process of spiral flow, and the spiral angles of the two adjacent layers of spiral pipes are opposite numbers, the turbulence degree of the heat exchange chamber 12, the spiral heat exchange pipe 5 and the adjacent layers of the spiral heat exchange pipe 5 is increased, and the heat exchange capacity is enhanced; secondly, the heat exchange tube adopts a spiral tube winding mode, the length of the heat exchange tube is far greater than that of the heat exchange cavity 12, the heat exchange area is increased, the heat exchange time is greatly prolonged, and the heat exchange efficiency is further improved.
As shown in fig. 4 and 5, the spiral flow nozzle 6 adopted in the present invention includes a nozzle 61 and a spray shell 62 sleeved outside the nozzle 61, the inlet end of the spray shell 62 is detachably connected with a filter mesh cover 63, the filter mesh cover 63 is smaller than the filter mesh aperture at the inlet of the cold medium temporary storage chamber 11 to filter the fine impurities in the cold medium to prevent the spiral flow nozzle 6 from being blocked, the outlet port is provided with a spray hole 621, one side of the nozzle 61 located at the spray hole 621 is annularly provided with three spiral flow guide grooves 611, so that when the liquid cooling medium passes through the internal channel of the spiral flow nozzle 6, the liquid cooling medium passing through the spiral flow nozzle 6 is tangentially acted by the three spiral flow guide grooves 611, that is, the liquid cooling medium can be uniformly sprayed in the form of fan-shaped mist in the tube wall of the spiral heat exchange tube 5, each spiral flow nozzle 6 corresponds to one spiral heat exchange tube 5, and it is ensured that the heat exchange effect of each spiral heat exchange tube 5 is the same or close.
In the embodiment of the invention, the connection part of the rotational flow nozzle 6 and the pressure equalizing plate 2, the connection part of the rotational flow nozzle 6 and the spiral heat exchange tube 5 and the connection part of the spiral heat exchange tube 5 and the partition plate 3 are in sealed connection, such as welding, so as to prevent gas or liquid from leaking.
The evaporator of the invention can realize small end difference even if adopting a concurrent flow mode because the liquid is uniformly evaporated on the tube side and is almost in an isothermal process, so a vertical or horizontal arrangement mode can be selected according to the field environment or the equipment requirement, and when the evaporator is vertically arranged, the cold medium temporary storage chamber 11 is positioned at the top end of the tubular shell 1.
The above description is merely illustrative of particular embodiments of the invention that enable those skilled in the art to understand or practice the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention.
It will be understood that the invention is not limited to what has been described above and that various modifications and changes can be made without departing from the scope thereof. The scope of the invention is limited only by the appended claims.
Claims (8)
1. The pressure-equalizing spiral shell type falling film evaporator is characterized by comprising a tubular shell (1) with two closed ends, wherein a chamber of the tubular shell (1) is axially divided into a cold medium temporary storage chamber (11), a heat exchange chamber (12) and an exhaust chamber (13) through a pressure equalizing plate (2) and a partition plate (3), and the heat exchange chamber (12) is positioned between the cold medium temporary storage chamber (11) and the exhaust chamber (13);
the cold medium temporary storage chamber (11) is communicated with the refrigerant liquid inlet pipe (4) and is used for temporarily storing liquid cold medium;
a plurality of spiral heat exchange tubes (5) are uniformly distributed in the heat exchange cavity (12) along the axial direction of the tubular shell (1), one end of each spiral heat exchange tube (5) penetrates through the partition plate (3) and then is communicated with the exhaust cavity (13), a swirl nozzle (6) is installed at the other end of each spiral heat exchange tube (5) and is located between the two pressure equalizing plates (2), each pressure equalizing plate (2) is provided with a threaded hole (21), the swirl nozzle (6) is installed on each pressure equalizing plate (2) and is communicated with the cold medium temporary storage cavity (11) through the threaded hole (21), a gaseous heat medium inlet (121) and a liquid discharge port (122) are respectively formed in the tube wall of the heat exchange cavity (12), the gaseous heat medium inlet (121) is formed at one side close to the cold medium temporary storage cavity (11) and is connected with a carrier gas pipeline, and the liquid discharge port (122) is formed at one side close to the exhaust cavity (13) and is used for discharging liquid liquefied by the gaseous heat exchange medium through the heat exchange cavity (12);
and the exhaust chamber (13) is provided with an exhaust port (131) for exhausting gas obtained by vaporizing the liquid cooling medium through the heat exchange chamber (12).
2. A pressure equalizing spiral shell type falling film evaporator according to claim 1, characterized in that the heat exchange chamber (12) consists of a first chamber (12-1) and a second chamber (12-2) which are coaxial, and the first chamber (12-1) has a larger diameter than the second chamber (12-2), and the gaseous heat medium inlet (121) is provided on the tube wall of the first chamber (12-1) for bringing the gaseous heat medium just entering the heat exchange chamber (12) into substantially uniform contact with the spiral heat exchange tubes (5).
3. The pressure equalizing spiral tube shell type falling film evaporator as claimed in claim 1 or 2, characterized in that a plurality of spiral heat exchange tubes (5) are arranged in a heat exchange chamber (12) in a multilayer manner and are wound in a staggered manner according to a spiral line shape, and the distance between any two adjacent layers of spiral heat exchange tubes (5) is the same, and the spiral winding directions are opposite.
4. A pressure equalizing spiral shell type falling film evaporator as claimed in claim 3, characterized in that each layer of the spiral heat exchange tubes (5) is arranged in an annular array with the axis of the tubular shell (1) as the center, the number of the spiral heat exchange tubes (5) in each layer increases from the inner layer to the outer layer in sequence, and the screw pitch, the spiral radius and the spiral direction of the spiral heat exchange tubes (5) in the same layer are the same.
5. The pressure equalizing spiral shell type falling film evaporator of claim 1, wherein the swirl nozzle (6) comprises a nozzle (61) and a spray shell (62) sleeved outside the nozzle (61), a filter screen cover (63) is detachably connected at an inlet end of the spray shell (62), a spray hole (621) is formed at an outlet end, and three spiral guide grooves (611) are annularly and uniformly distributed on one side of the nozzle (61) positioned at the spray hole (621).
6. The pressure equalizing spiral shell type falling film evaporator as claimed in claim 1, wherein the connection of the swirl nozzle (6) and the pressure equalizing plate (2), the connection of the swirl nozzle (6) and the spiral heat exchange tube (5) and the connection of the spiral heat exchange tube (5) and the partition plate (3) are in sealing connection to prevent gas or liquid leakage.
7. A pressure equalizing spiral shell type falling film evaporator as claimed in any one of claims 1 to 6, characterized in that the falling film evaporator is installed in a vertical or horizontal arrangement, and when vertically arranged, the cold medium temporary storage chamber (11) is located at the top end of the tubular shell (1).
8. A pressure equalizing spiral shell and tube falling film evaporator as claimed in claim 7, characterized in that the refrigerant feed pipe (4) is connected to a throttle device for depressurizing the liquid refrigerant flowing into the refrigerant buffer chamber (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210801615.9A CN115218557A (en) | 2022-07-07 | 2022-07-07 | Pressure-equalizing spiral shell type falling film evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210801615.9A CN115218557A (en) | 2022-07-07 | 2022-07-07 | Pressure-equalizing spiral shell type falling film evaporator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115218557A true CN115218557A (en) | 2022-10-21 |
Family
ID=83610628
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210801615.9A Pending CN115218557A (en) | 2022-07-07 | 2022-07-07 | Pressure-equalizing spiral shell type falling film evaporator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115218557A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117164043A (en) * | 2023-10-10 | 2023-12-05 | 开普工程技术有限公司 | Falling film evaporation treatment system for high-salt wastewater in coal chemical industry, scale prevention method and scale removal method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0884549A2 (en) * | 1997-06-10 | 1998-12-16 | Komax Systems, Inc. | Static mixer-heat exchanger |
| CN104296562A (en) * | 2014-10-21 | 2015-01-21 | 张家港市江南锅炉压力容器有限公司 | Novel falling film type evaporator |
| CN104976905A (en) * | 2015-06-26 | 2015-10-14 | 北京广厦环能科技股份有限公司 | Vacuum condensation cooler |
| CN206392284U (en) * | 2016-12-30 | 2017-08-11 | 东莞市鑫悦净化科技有限公司 | A kind of atomizer of convenient cleaning |
| CN108426470A (en) * | 2017-02-15 | 2018-08-21 | 东管重工(沈阳)有限公司 | Circulating air heat exchanger |
| CN208671425U (en) * | 2018-08-17 | 2019-03-29 | 江西浩金欧博空调制造有限公司 | A kind of highly effective dry-type shell and tube evaporator with spiral nozzle distributor |
| CN209188147U (en) * | 2018-09-13 | 2019-08-02 | 启东神农机械有限公司 | The vertical pipe evaporator of multiple-effect |
| CN114136023A (en) * | 2021-12-06 | 2022-03-04 | 台州龙江化工机械科技有限公司 | Evaporator, manufacturing method of evaporator and refrigeration system with evaporator |
-
2022
- 2022-07-07 CN CN202210801615.9A patent/CN115218557A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0884549A2 (en) * | 1997-06-10 | 1998-12-16 | Komax Systems, Inc. | Static mixer-heat exchanger |
| CN104296562A (en) * | 2014-10-21 | 2015-01-21 | 张家港市江南锅炉压力容器有限公司 | Novel falling film type evaporator |
| CN104976905A (en) * | 2015-06-26 | 2015-10-14 | 北京广厦环能科技股份有限公司 | Vacuum condensation cooler |
| CN206392284U (en) * | 2016-12-30 | 2017-08-11 | 东莞市鑫悦净化科技有限公司 | A kind of atomizer of convenient cleaning |
| CN108426470A (en) * | 2017-02-15 | 2018-08-21 | 东管重工(沈阳)有限公司 | Circulating air heat exchanger |
| CN208671425U (en) * | 2018-08-17 | 2019-03-29 | 江西浩金欧博空调制造有限公司 | A kind of highly effective dry-type shell and tube evaporator with spiral nozzle distributor |
| CN209188147U (en) * | 2018-09-13 | 2019-08-02 | 启东神农机械有限公司 | The vertical pipe evaporator of multiple-effect |
| CN114136023A (en) * | 2021-12-06 | 2022-03-04 | 台州龙江化工机械科技有限公司 | Evaporator, manufacturing method of evaporator and refrigeration system with evaporator |
Non-Patent Citations (1)
| Title |
|---|
| 吴龙标，张洪江，李力编: "《细水雾灭火技术与应用》", 江西科学技术出版社, pages: 108 - 109 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117164043A (en) * | 2023-10-10 | 2023-12-05 | 开普工程技术有限公司 | Falling film evaporation treatment system for high-salt wastewater in coal chemical industry, scale prevention method and scale removal method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103727707A (en) | Full-falling-film evaporator with double refrigerant distribution devices | |
| JP7138795B2 (en) | Refrigerant distributor and evaporator provided with same | |
| WO2014032488A1 (en) | Heat exchanger for micro channel | |
| CN115218557A (en) | Pressure-equalizing spiral shell type falling film evaporator | |
| CN106839531A (en) | A kind of gas bypass micro-channel evaporator | |
| CN113713508B (en) | Centrifugal separation pipe, gas-liquid separation device and refrigeration system with device | |
| WO2021228101A1 (en) | Cascade evaporation-condensation heat exchanger | |
| CN106679250A (en) | Gas-liquid separation device and condensation evaporator with gas-liquid separation function | |
| WO2008151500A1 (en) | A gas-liquid separating method and a gas-liquid separating type evaporator | |
| CN107356017A (en) | Downward film evaporator liquid distributor | |
| CN113983723A (en) | Heat exchanger and air conditioning equipment | |
| CN102032825A (en) | Heat exchange tube for evaporator and evaporator formed by same | |
| CN208671425U (en) | A kind of highly effective dry-type shell and tube evaporator with spiral nozzle distributor | |
| CN106895611A (en) | A kind of distribution method of dry evaporator and refrigerant | |
| CN206449940U (en) | Falling-film heat exchanger | |
| CN210663986U (en) | Heat exchange structure of gas dryer | |
| CN106766392B (en) | Spray tank type heat exchanger and use method thereof | |
| CN217604434U (en) | Pressure-equalizing spiral shell type evaporator | |
| CN204006813U (en) | A kind of highly effective dry-type shell-and-tube evaporator | |
| WO2023065600A1 (en) | Siphon evaporation device having heat exchange structure, and operation method and application thereof | |
| CN114001497A (en) | Liquid distribution device, heat exchanger and air conditioner | |
| CN106985637B (en) | A kind of automobile air-conditioning refrigeration equipment | |
| CN103673404B (en) | A kind of micro channel heat exchanger | |
| WO2021228017A1 (en) | Dry-type evaporator | |
| CN206739683U (en) | A kind of gas bypass micro-channel evaporator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |