CN103822409B - The falling-film heat exchanger that a kind of spiral pipeline is arranged - Google Patents
The falling-film heat exchanger that a kind of spiral pipeline is arranged Download PDFInfo
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- CN103822409B CN103822409B CN201410028802.3A CN201410028802A CN103822409B CN 103822409 B CN103822409 B CN 103822409B CN 201410028802 A CN201410028802 A CN 201410028802A CN 103822409 B CN103822409 B CN 103822409B
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Abstract
The invention discloses the falling-film heat exchanger that a kind of spiral pipeline is arranged, be characterized in that heat exchange pipeline flat spin is arranged, shell side working medium flows down along pipeline outer wall facial mask shape.Specifically comprise shell, this shell is provided with fluid A import, gaseous fluid A outlet, fluid liquid A outlet, fluid B import and fluid B and exports, be provided with fluid A distributor in this shell, and be provided with the collection conduits of at least one helical layer pipeline and the outlet with described helical pipe; The inlet of helical pipe all with described fluid B inlet communication; The spiral form of pipeline is the one in spiral of Archimedes form, Made up of Line Segment Involute form, regular polygon involute in form, circle involute form, ellipse evolute form.The feed liquor mode of tube side fluid can be direct feed liquor method, bushing type feed liquor method and hose type feed liquor method.This Novel falling film formula heat exchanger has widened workplace and the application of conventional falling-film heat exchanger greatly, has good market application foreground.
Description
Technical field
The invention belongs to falling-film heat exchanger design field, specifically relate to the falling-film heat exchanger that a kind of spiral pipeline is arranged.
Background technology
Along with the fast development of society, social industry-by-industry is progressively deepened for the utilization of the energy and degree of dependence, and in order to more effectively utilize the energy, society increases day by day to the demand of efficient heat-exchanger rig.Efficient heat exchange can not only improve the utilization ratio of the energy, and effectively can utilize the used heat in life by suitable design, is therefore significant to its research.Falling-film heat exchanger is paid close attention to and developmental research in recent years widely as a kind of heat exchanger with huge prospect, and it started to be applied in field of Refrigeration and Air-conditioning the nineties in 20th century.Sum up both at home and abroad about the achievement in research of cooling horizontal downward film evaporator, known it compare flooded evaporator there is larger advantage; 1) have the very high coefficient of heat transfer: the dominant thermal resistance of downward film evaporator is liquid film, because working medium flows down along pipeline is membranaceous, therefore the thermal resistance of this part is very little, and experimental data shows, the heat transfer coefficient of falling film type evaporation is even high than pool boiling.Because downward film evaporator has such characteristic, it is very little, cost-saving that the size of device can be done; The driving force that simultaneously flowing of working medium is main is gravity, therefore in evaporimeter power pressure reduce very little, the temperature difference before and after cold-producing medium is also less; 2) less refrigerant charge: from a large amount of experimental results, under identical cold condition, the charging amount of cold-producing medium can reduce and is about 25%, be specially adapted to function admirable but charging amount can not be too large working medium; 3) oil return performance is good: the refrigerant liquid flowing into base of evaporator is actually the higher mixing material of oil concentration, after again improving, just directly can send compressor to by the oil-in of compressor.
Although horizontal downward film evaporator has above-mentioned plurality of advantages, it is to be solved that it also also exists some problems at present.The performance parameter affecting evaporimeter is a lot: the flow of cold-producing medium, the design etc. of the layout of fluidised form, pipeline, surface texture, distributor.Wherein one of the problem of most critical is that how designing distributor makes the working medium sprayed be uniformly distributed to greatest extent, if because spray working medium skewness, so just may there is dry-out in pipe surface, and the appearance of dry-out has deteriorated significantly the heat exchange property of evaporimeter.Therefore to the further research and exploitation of distributor problem, be significant for advancing the application of the business of downward film evaporator.Meanwhile, the downward film evaporator of horizontal pipe is due to the particularity of the structure of pipeline and the relative position of pipeline and distributor, and the volume utilization of heat exchanger inside is not high, leaves very large space in the side of pipeline.
Vertical falling film evaporimeter has occurred for a long time, and current application mainly concentrates on the industries such as sky divides, oil, chemical industry, pharmacy, and people have accumulated a lot of experience in its design.Vertical falling film evaporimeter has some advantages that horizontal downward film evaporator does not have, and its occupation of land scope is little, and the heat exchange amount of unit volume is large, is specially adapted to large-scale heat-exchanger rig.The heat exchanger tube that common vertical falling film evaporimeter adopts mostly is the straight tube vertically arranged, what some adopted is helix tube.Although the latter's compact conformation, good effect of heat exchange, because the distance between pipeline is very little, adding between distributor and helical pipe is adopt to be welded to connect, therefore pipeline cleaning and safeguard unusual difficulty.The simultaneously selection of tube side fluid is also very restricted, and when adopting flue gas etc. as thermal source, deposition may appear in the solid particle in flue gas in pipe inside, and then occurs the phenomenon of blocking.In addition when adopting the larger fluid of viscosity as thermal source, the resistance in flow process is very large, and the pump merit spent in running of this evaporimeter will be very large.
In general, when application level downward film evaporator, more be concerned about the variations in temperature of shell-side fluid or the change of concentration, therefore in order to better realize the control to shell side heat transfer process, all can be optimized design to the distributor of shell-side fluid, the allocation strategy for the heat source fluid of tube side is then relatively simple; Typical vertical falling film evaporimeter is then be optimized the assignment of traffic of tube side fluid, the heat source fluid of shell side adopts the mode of " singly entering singly to go out ", do not have the strategy of corresponding assignment of traffic, this just limits the application scenario of two kinds of downward film evaporators to a certain extent.In conjunction with the feature of falling film type heat exchange, simultaneously enhanced heat exchange pipeline both sides fluid heat transfer effect and strengthen the advantage that better can play falling film type heat exchange to the control of both flows.
Improvement at present for downward film evaporator is mainly optimized the layout of its pipeline and structure, such as patent document (publication No. CN102759225A) discloses a kind of downward film evaporator of vertical spiral-flow type, this patent enhances the heat exchange of pipeline wall by arranging helical baffles, decrease and occur dry possibility.But because the Working fluid flow region in enclosure cavity is comparatively large, the strengthening effect that working medium is brought due to flow disturbance in helical flow process is also not obvious, and the heat exchange of pipe interior fluid side does not also take enhancements; Simultaneously because tube bank is for vertically arranging, the lifting that the vertical falling film evaporimeter that therefore working medium is traditional compared with the time of tube wall Falling film heat transfer in whole runner is too not large, the effect of membranaceous heat exchange need further excavation.Patent document (CN102759227A) discloses a kind of cooling horizontal downward film evaporator, and feature is by arranging one section of liquid refrigerant supercooling tube road and the further heat exchange of gaseous refrigerant completing heat exchange, to add big supercooling degree.This patent document limitation is that the arrangement form of pipeline still adopts traditional arrangement, and this layout makes the space availability ratio of evaporimeter lower.Patent document (CN103153419A) discloses a kind of novel downward film evaporator, the evaporimeter principal character of the type is the tube bank that evaporimeter comprises two or more, each tube bank is configured with respective tube sheet and collection conduit, change design and can avoid the dry of pipe surface preferably by tube bank being arranged as " sub-falling film type system ", but because the material of pipeline both sides heat exchange is not still extended time of contact preferably, the raising of exchange capability of heat is limited.
Can find out from the above mentioned, horizontal downward film evaporator and vertical falling film evaporimeter all have respective advantage and application scenario, also have respective inferior position simultaneously.The coefficient of heat transfer of horizontal downward film evaporator is high, but the space availability ratio of heat exchanger inside is lower; And although vertical downward film evaporator space availability ratio is low, the heat-exchange time of shell-side fluid and tube side fluid is too short.Two kinds of heat exchangers just to being concerned about that the flow of fluid adopts allocation strategy, and do not adopt corresponding strategy for another fluid streams.Develop and can greatly can widen the application scenario of falling-film heat exchanger by simultaneously the forgo Novel falling film formula heat exchanger of inferior position of both heat exchange advantage integrated, will huge market application foreground be had.
Summary of the invention
The invention provides the high-efficiency falling film type heat exchanger that a kind of spiral pipeline is arranged, have the advantage of vertical falling film evaporimeter and horizontal downward film evaporator concurrently, heat transfer coefficient is high, good effect of heat exchange, flow-control allocation strategy all be have employed to two strands of heat exchanging fluids simultaneously, further improve the flexibility of this falling-film heat exchanger.
The falling-film heat exchanger that a kind of spiral pipeline is arranged, comprise shell, this shell is provided with fluid A import, gaseous fluid A outlet, fluid liquid A outlet, fluid B import and fluid B and exports, be provided with fluid A distributor in this shell, in described shell, be provided with the collection conduits of at least one helical layer pipeline and the outlet with described helical pipe; The inlet of described helical pipe all with described fluid B inlet communication; Described collection conduits one end is closed, the other end and described fluid B outlet.
Fluid B enters heat exchanger in the side of housing, after helical pipe, collection conduits, finally at the bottom outflow heat exchanger of housing.And fluid A enters heat exchanger from the fluid A import at the top of housing, fluid liquid A comes together in the bottom of housing, export and discharge, and the fluid of gaseous state is drawn from the gaseous fluid A outlet of the side of housing from fluid liquid A.
For ease of the designing and making of helical pipe, as preferably, the spiral form that described helical pipe adopts is the one in spiral of Archimedes form, Made up of Line Segment Involute form, regular polygon involute in form, circle involute form, ellipse evolute form.Suitable correction to be carried out to curve in helical pipe and the junction of collection conduits and the junction of pipeline and housing.Which kind of spiral form of concrete employing needs to determine according to actual conditions.The diameter of described helical pipe contains microchannel and the conventional pipeline of refrigeration, and when device is less, the diameter of pipeline can get the small value, and change thermal requirement larger time, caliber can take large values.
Described helical pipe surfaces externally and internally all can adopt enhanced heat exchange means, outer surface comprises modes such as adopting fin, fin, groove, spiral, inner surface comprises ripple and helicitic texture etc., and pipeline can adopt pipe, elliptical tube, conic section pipe, high order curve pipeline etc. simultaneously.Complex surface effectively can produce disturbance to the formation of liquid film, reduces the thickness in boundary layer, thus enhanced heat exchange effect.
Owing to needing in helical pipe junction to bear larger stress, in order to the intensity of stiffening device, during actual installation, in helical pipe and shell junction, can arrange supporting construction as required, supporting construction comprises the wall etc. of support column, brace summer or thickening, to meet requirement of strength.
According to the difference of fluid B character, fluid B can adopt multiple feed liquor form, when fluid B is gas, can directly be input in helical pipe by gas, this kind of form we referred to as direct-type feed liquor method.Do not need additionally to increase distributor.When fluid B is liquid, according to the difference of fluid B uninterrupted and use occasion, other two kinds of forms can be divided into again, i.e. bushing type feed liquor method and hose type feed liquor method.Now, as preferably: the falling-film heat exchanger that described spiral pipeline is arranged also comprises fluid B and distributes cavity, this fluid B distributes cavity and is provided with liquid inlet, is provided with fluid B distributor and is arranged on the fluid B distribution duct between fluid B distributor and fluid B import in this fluid B distribution cavity.
When be used in space comparatively narrow space time, as preferably, described fluid B distribution duct is at least two, and the entrance end portion of multiple fluid B distribution duct is mutually sheathed, and the port of export of inner fluid B distribution duct is connected with described fluid B import through outside fluid B distribution duct.This kind of form is above-mentioned bushing type feed liquor method.
Preferred as another kind, described fluid B distribution duct is separate two or more flexible pipes.The quantity of flexible pipe is identical with the quantity of helical pipe.This kind of form is above-mentioned hose type feed liquor method.
For ease of the fixing of flexible pipe with change, as preferably, described flexible pipe one end is through the dispensing orifice of described fluid B distributor, and this end end is provided with the flange face interfixed with described fluid B distributor.
For the demand of satisfied different occasion, be convenient to replacing and installation that fluid B distributes cavity, as preferably, for removably connecting between described fluid B distribution cavity and shell.Such as, clamp connection can be adopted, be threaded.
Described collection conduits is positioned at the centre of circular shell, connects the helical pipe of each differing heights layer.The diameter of collection conduits is larger than the diameter of heat exchange pipeline, specifically can by the flow determination range of fluid B.As preferably, the diameter of described collection conduits is 2 ~ 4 times of helical pipe diameter.The diameter of collection conduits is greater than helical pipe, and what be convenient to fluid B collects discharge smoothly, the diameter of collection conduits, needs to determine according to the flow of fluid B.
Helical pipe level can be installed or tilt angle certain and install when mounted, and the distance between adjacent two also can regulate.As preferably, the angle between described helical pipe and horizontal plane is 0 ~ 30 °.Helical pipe in the vertical direction can deflect certain angle and arrange, can reduce the dry of helical pipe like this.Distance pipeline between adjoining spiral pipeline is also adjustable.The angle departed from and distance are determined according to actual conditions.
The structure of the distributor adopted in the present invention can adopt orifice-plate type distributor, nozzle-type distributor, plough groove type distributor or other combined type distributors.Selection and the concrete design parameter of distributor depend on the circumstances.
The high-efficiency falling film type heat exchanger that spiral pipeline of the present invention is arranged, the operation principle of the rotating falling-film heat exchanger of the horizontal helical described in it is: during this device busy, fluid A enters heat exchanger from the fluid A import on heat exchanger top, then after fluid A distributor, be evenly distributed on the heat exchange pipeline of spiral, form falling film type heat exchange.Liquid film flows along the outside wall surface of helical pipe, when dropping onto lower floor helical pipe surface, liquid film is subject to power upwards, the speed of vertical direction changes, transfer the circumferential movement along helical pipe, experience stagnation fluidised form, development fluidised form respectively, develop fluidised form completely, finally flow down in the bottom of helical pipe.Due to the fluid B heat exchange in liquid film and helical pipe, the fluid A of gaseous state can be formed in heat exchanger, the fluid A of gaseous state draws heat exchanger by the steam (vapor) outlet (gaseous fluid A exports) being arranged in housing side, the fluid A not having enough time to vaporize then hoards the bottom at heat exchanger, when the liquid level of bottom is higher than preset value, liquid A exports outflow heat exchanger through fluid liquid A.Fluid B then successively flows through fluid B distributor, and input duct, helical pipe, collection conduits, fluid B export.When flat spin pipeline, belong to horizontal falling film type heat exchange with the heat exchange of fluid A, relative motion is the circumference of pipeline; And belonging to vertical falling film heat exchange in the heat exchange of collection conduits and liquid, relative motion is along the axis of pipeline.
In the present invention, fluid B, before entering collection conduits, belongs to horizontal falling film type heat exchange with the heat exchange of fluid A, and after fluid enters collection conduits, still carry out heat exchange with fluid A, heat exchange form class is now similar to common vertical falling film evaporimeter.In whole flow process, all participate in heat exchange, therefore there is longer heat-exchange time and the heat exchange property of Geng Gao.
Compared with prior art, the high-efficiency falling film type heat exchanger that novel spiral pipeline of the present invention is arranged has larger advantage:
(1) pipeline is screw arrangement, the spiral form of pipeline is the one in spiral of Archimedes form, Made up of Line Segment Involute form, regular polygon involute in form, circle involute form, ellipse evolute form, therefore in heat exchanger, the length of heat exchanger tube is longer, and the pipeline arranged in unit volume is also longer.This just makes heat exchanger can reach very large heat exchange amount when less volume on the one hand, and have very high heat transfer density, be therefore comparatively applicable to large-scale heat-exchanger rig, when being applied in the less occasion of heat exchange, device now more easily realizes miniaturization; On the other hand, due to the layout that both can be parallel to each other between helical pipe, also can the angle certain according to actual conditions relative tilt arrange, so just can strengthen the disturbance of shell-side fluid in the process fallen, the thickness reducing liquid film strengthens heat-transfer effect, also greatly reduces the possibility that pipe surface dry-out occurs simultaneously.(2) passage of fluid B is divided into two stages, and the first stage flows in helical pipe, and second stage vertically flows down in collection conduits.In the first phase, because the track of fluid motion is curve, therefore the fluid state in helical pipe is similar to the flowing of elbow, a large amount of Secondary Flows can be produced, the existence of Secondary Flow strengthens the disturbance of helical pipe internal flow greatly, facilitate the exchange of momentum between each fluid layer and energy, therefore helical pipe inside heat transfer effect compared with horizontal straight tube road or the less pipeline of elbow number better.When second stage, fluid B flows down along collection conduits is membranaceous, carries out heat exchange with the fluid A outside collection conduits, and process and the vertical falling film evaporator heat exchange process of heat exchange are similar.During due to vertical membranaceous heat exchange, the very thin thickness of liquid film, add on thin film drainage direction, collection conduits is furnished with inlet again at a certain distance, the fluid B flowed into by different inlet destroys the Development of Boundary Layer of upper strata liquid film, reduces the thickness of liquid film.Now the coefficient of heat transfer in inner-walls of duct face is higher.Again because the circular profile of distributor designs, close with the layout profile of pipeline, therefore the wettability effect in pipeline outer wall face is fine, and this is also conducive to the stability of this Novel falling film formula heat exchanger work.
(3) this invention proposes three kinds of feed liquor mode schemes for the uniform distribution of fluid B in the vertical direction, and the first is direct method, and this method is applicable to fluid B when being gas.Latter two is bushing type feed liquor method and hose type feed liquor method, and both is applicable to the situation that fluid B is liquid.As long as meeting fluid B can drop onto in the pipeline of below respective layer, namely beyond pipeline is corresponding with the layout in duct with the size of distributor junction caliber, the diameter of all the other pipeline sections can be inconsistent, such as makes caliber reduction etc. progressively, and this just makes this kind of method have very large flexibility.Hose type feed liquor method connects distributor and helical pipe by flexible pipe, in theory, a lot of runners can be divided into, and the flow of each runner can be regulated accurately by the size and distribution controlling duct, the program has very large flexibility, can according to the difference of each layer pipeline heat transfer effect when practical application, the factors such as flow is different, the position of import are optimized improvement to this feed liquor scheme.Simultaneously, the connection of the connection of soft pipeline and distributor, soft pipeline and helical pipe, side cavities (namely fluid B distributes cavity) are designed to detachable form with the connection of heat exchanger main body, can not only realize commercial Application flexibly very convenient-disassembly, cleaning and change suitable convenience, be also conducive to the standardization realizing fluid B inlet distributor form, soft pipeline caliber etc. simultaneously.
Accompanying drawing explanation
The spiral form structural representation that Fig. 1 adopts for spiral pipeline of the present invention.
Fig. 2 is the arrangement figure of fluid B distribution duct in a kind of embodiment of falling-film heat exchanger of spiral pipeline of the present invention layout.
Fig. 3 is the top view of the figure of arrangement shown in Fig. 2.
Fig. 4 is the partial enlarged drawing of C part in Fig. 2.
Fig. 5 is the arrangement figure of fluid B distribution duct in the another kind of embodiment of falling-film heat exchanger that spiral pipeline of the present invention is arranged.
Fig. 6 is the partial enlarged drawing of D part in Fig. 5.
Fig. 7 is the structural representation of the third embodiment of falling-film heat exchanger that spiral pipeline of the present invention is arranged.
The E-E face profile that Fig. 8 is falling-film heat exchanger shown in Fig. 7.
The F-F face profile that Fig. 9 is falling-film heat exchanger shown in Fig. 7.
In above-mentioned accompanying drawing:
1 is shell; 2 is fluid A import; 3 export for gaseous fluid A; 4 export for fluid liquid A; 5 is fluid B import; 6 export for fluid B; 7 is fluid A distributor; 8 is helical pipe; 8(a) be the inlet of helical pipe; 8b is the outlet of helical pipe 8; 9 is collection conduits; 10 is fluid channel B; 11 is fluid B distribution cavity; 11a is inlet; 12 is fluid B distributor; 13 is fluid B distribution duct; 12a is duct; 13 is soft pipeline.
Detailed description of the invention
As shown in Fig. 1,7 ~ 9: the falling-film heat exchanger that a kind of spiral pipeline is arranged, comprise shell 1, this shell 1 is provided with fluid A import 2, gaseous fluid A outlet 3, fluid liquid A outlet 4, fluid B import 5 and fluid B and exports 6, fluid A distributor 7 is provided with, the collection conduits 9 being provided with at least one helical layer pipeline 8 in shell 1 and being communicated with the outlet 8b of helical pipe 8 in this shell 1; The inlet 8a of helical pipe 8 is all communicated with fluid B import 5; Collection conduits 9 one end is closed, and the other end and fluid B export 6 and be communicated with.
As shown in Figure 1, helical pipe 8 can adopt multiple spiral form, conventional form is for spiral of Archimedes form (as Suo Shi Fig. 1 (c)), Made up of Line Segment Involute form are (as shown in Fig. 1 (b),), regular polygon involute in form (as shown in Figure 1 (d) shows, Fig. 1 (d) is square involute in form), one in circle involute form (as Suo Shi Fig. 1 (a)), ellipse evolute form.In Fig. 1,8a is helical pipe 8 import.
The diameter of collection conduits 9 is 2 ~ 4 times of helical pipe 8 diameter.Angle between helical pipe 8 and horizontal plane is 0 ~ 30 °.Helical pipe 8 is pipe, elliptical tube, conic section pipe, high order curve pipe.The inner surface of helical pipe 8 and outer surface can take enhanced heat exchange means.Helical pipe 8 also can adopt enhanced heat exchange pipeline, comprises bellows, helix tube, elliptical tube, finned tube etc.In helical pipe 8 and shell 1 junction, be provided with supporting construction, supporting construction comprises support column, brace summer etc., to meet requirement of strength.
The heat exchanger channels of fluid comprises fluid A channel and fluid channel B, and fluid A and fluid B carries out the exchange of heat by the collection conduits that horizontally disposed helical pipe and vertical direction are arranged.Fluid A successively flows through fluid A import, distributor, helical pipe outside wall surface, fluid A export (comprise gaseous fluid A export and fluid liquid A exports), and fluid B exports through fluid B distributor, input duct, helical pipe, collection conduits and fluid B.At helical pipe and collection conduits place, the exchange of two fluid generation heats.Because the screw arrangement of heat exchange pipeline and the feed liquor of fluid B have carried out particular design, the present invention can provide larger heat exchange heat flow density, and the flexibility with timer also improves greatly.Illustrate that the present invention is applied in the advantage place in commercial Application below in conjunction with instantiation.
Embodiment 1
Be applicable to the evaporimeter in field of Refrigeration and Air-conditioning as Fig. 7,8,9 examples, fluid A elects cold-producing medium as, fluid B(air) elect refrigerating medium as.Fluid A was gas-liquid mixture phase before entering this heat exchanger, after entering heat exchanger by the fluid A import 2 at top, fluid A uniform spray after fluid A distributor 7 arrives the outside wall surface of helical pipe 8, dirty in the outside wall surface film-like of helical pipe 8, because in cold-producing medium A(the present embodiment 1, fluid A and cold-producing medium A refers to same substance) temperature refer to same substance lower than fluid B and refrigerating medium B in refrigerating medium B(the present embodiment 1), therefore heat is transmitted to cold-producing medium from refrigerating medium, and refrigerant temperature reduces.The refrigerant vapour produced exports 3 from the gaseous fluid A in housing 1 side arrangement and is drawn, and delivers to compressor.And be cryogenic fluid and oily mixing material in for dense fluids of exchanger base, oil concentration is higher, is directly drawn out to next workpiece by fluid liquid A outlet.Refrigerating medium is assigned to working region after fluid channel B 10.Owing to adopting falling film type heat exchange, therefore the pressure of evaporimeter reduces little, and variations in temperature is little, therefore when identical evaporating temperature, heat transfer temperature difference can arrange lower.
In the present embodiment, different from the heat exchange characteristic of refrigerating medium B according to cold-producing medium A, two different phases can be divided into, the heat exchange of both first stages has been flowed relatively in helical pipe 8 both sides, this stage, cold-producing medium A formed liquid film outside helical pipe 8, helical pipe 8 due to every one deck is all screw arrangement, therefore on system of unit cryogen height of drop, the length of heat exchange pipeline will significantly be greater than conventional levels downward film evaporator, not only reduce the heat exchange " dead volume " of heat exchanger cavity inside, and make heat exchange area larger, when other conditions are the same, heat exchange area imply that greatly heat exchange amount is larger.Moreover the refrigerating medium B in helical pipe 8 moves along helical pipe, its direction of motion is changing always, the a large amount of Secondary Flows produced in motion process enhance inner disturbance greatly, boundary layer is not easily developed and thinning, also provide enhanced heat transfer coefficient from inside, thus greatly strengthen heat exchange.The heat exchange of second stage is in the both sides of collection conduits 9, now two fluids all vertically film-like flow down, due to the layout feature of helical pipe 8, make the development in boundary layer can only could sustainable development in the middle of two-layer pipeline, and interrupted in the junction of pipeline, again form new boundary layer.Comprehensive above two features are known, not only substantially prolongs the heat-exchange time of cold-producing medium and refrigerating medium, also mechanism, greatly enhance heat transfer effect simultaneously when the present invention is applied to this example.
Advantage of the present invention also can carry out quantitative explanation by following comparing calculation, because in the evaporimeter of this exemplary application in air-conditioning, therefore contrast object and elect conventional levels downward film evaporator as: set the length of contrast flooded evaporator as 1000mm, the diameter 300mm of main part, pipe row is 6 rows, is furnished with altogether pipeline number 55, and the diameter of each pipeline is 10mm, length is 900mm, and in hypothesis, the logarithm heat transfer temperature difference of outer fluid is 10 DEG C; When adopting the present embodiment, the height of heat exchanger is 1000mm, and main diameter is 300mm, and the diameter of each helical pipe is also 10mm, and the length of each root pipeline is 1.20m, and the number of plies of helical pipe is 45, and the diameter of collection conduits is 30mm, is highly 900mm.Meanwhile, the time of membranaceous heat exchange is 0.5s, is the movement of falling object when all the other do not move on pipeline.When not adopting enhanced heat exchange pipeline, the coefficient of heat transfer selecting heat exchanger is 1000W/ (m
2k), the rotating heat exchanger of the horizontal helical of present embodiment is 1100W/ (m
2k).Be the result of calculation summary sheet of contrast two kinds of heat exchangers below: as can be seen from the result of calculation of table 1, this flat spin evaporimeter can not only extend the heat-exchange time between two fluids greatly, also the heat exchange area of increase can be utilized to improve heat exchange amount, comparative benefits is quite obvious simultaneously.
Table 1 spiral pipeline heat exchanger and flooded evaporator performance comparison
Embodiment 2
This example is applicable to chemical industry and pharmaceutical field, the concentrated and purification of material.Setting fluid A is liquid to be concentrated, and the something a concentration now in fluid A is lower, and fluid channel B is connected with the higher hot fluid of temperature (steam of high temperature).Similar in heat transfer process between the two and embodiment 1, successively after each layer heat exchange pipeline, owing to obtaining heat, the moisture in fluid A can components vaporize.Along with the carrying out of heat exchange, the material a concentration in fluid A is increasing, and moisture or liquid impurity tail off.Therefore, produce the fluid A containing higher concentration a in the bottom of heat exchanger, when reaching necessary requirement, heat exchanger can be isolated from bottom.
This embodiment also has a variants, namely the separation of the liquid refrigerant of two kinds of different boiling is realized, during work, fluid A is mixing material, if two kinds of fluids are respectively a1 and a2, the boiling point of two fluids is respectively 50 DEG C and 200 DEG C, fluid B now remains and adds hot fluid, selects the temperature adding hot fluid to be 100 DEG C.Along with the carrying out of heat transfer process, lower boiling a1 component is constantly vaporized into gas at pipeline external surface, and is drawn at the steam (vapor) outlet preset, and high boiling fluid a2 finally flows to the bottom of heat exchanger, exceedes after certain altitude also drawn until liquid level.
When the present invention is applied to this embodiment, because heat exchange pipeline is longer than conventional falling-film heat exchanger a lot, the area of heat exchange is much bigger, what therefore heat transfer process can carry out is more abundant, specifically when being applied to the purification of material, the more liquid that strongly makes of heat exchange is vaporizated into gas, and in the solution obtained bottom resulting device, the concentration of material a is higher.And when being applied to the separation of different boiling liquid, more low boiling working fluid can be isolated from mixing material, the separative efficiency of device significantly improves.
The advantage of the concentration process of solution is used for below by calculation specifications the present invention, the object of contrast is the vertical falling film heat exchanger commonly used in chemical industry: suppose that the barrel diameter contrasting vertical falling film evaporimeter and the rotating heat exchanger of horizontal helical is 300mm, be highly 1000mm, the height of distributor is 20mm; The riser number of vertical falling film pipeline is 100, and the effective heat exchange length of every root is 600mm, and the caliber of every root is 10mm.The coefficient of heat transfer is taken as 3500W/ (m2K).Horizontal helical rotating pipeline arrangement identical with embodiment 1 with relevant parameter, comparison between calculation results is summarized as in following table: as can be seen from final result of calculation, when the present invention is applied to solution concentrated, although the advantage of heat exchange area disappears, but due to can heat-exchange time be ensured, therefore the fluid of unit mass is still very large to the heat exchange amount that outflow heat exchanger is total from entering heat exchanger, and therefore total advantage exists.
2 flat spin heat exchangers and vertical falling film performance of evaporator contrast
Illustrate: the equivalent vaporization biodiversity in table 2 is the ratio of the latent heat of total heat exchange amount and water.
Embodiment 3
If Fig. 2 and Fig. 3 is another kind of way of realization of the present invention, comprise fluid B and distribute cavity 11, this fluid B distributes cavity 11 and is provided with fluid intake 11a, is provided with fluid B distributor 12 and is arranged on the fluid B distribution duct 13 between fluid B distributor 12 and fluid B import 5 in this fluid B distribution cavity 11.Fluid B distribution duct 13 is two, and the entrance end portion of multiple fluid B distribution duct 13 is mutually sheathed, and the port of export of inner fluid B distribution duct is connected with fluid B import through outside fluid B distribution duct.
The present embodiment is applicable to heat exchange between two kinds of liquid working substances and the very little situation of the heat exchange amount required, because heat exchange amount is very little, suppose the helical pipe layering number less (the present embodiment is for 3 layers) in vaporizer body now, working condition and other embodiments of vaporizer body part are similar, do not state at this tired.Fluid B(hot fluid) enter from the side cavity of evaporimeter, after the distributor (fluid B distributor 12) of a porous, the flow flowing through each hole is identical, duct 12a on fluid B distributor 12 is divided into three groups (schematic diagram as shown in Figure 3) according to the distance difference of distance side chamber central, in the below of distributor by being welded to connect two sleeve pipes (fluid B distribution duct 13), inner layer pipe immediately below the hot water that the value of designing requirement pipe diameter must make innermost layer duct flow down all enters, the duct in intermediate layer stays the rear intermediate layer pipeline all entered below, pipeline is before entering vaporizer body part, be bent into an angle of 90 degrees, be connected with the fluid B import on helical pipe by joint or clip.The distributor that whole embodiment is used and fundamental diagram are as shown in figs. 2 to 4.
What this embodiment adopted is bushing type feed liquor method, the method is separately for fluid B devises a distributor and input duct, be not only to allow fluid B evenly be assigned in helical pipe, can the more important thing is and can carry out the ducted flow distribution of each helical layer of fine adjustment by regulating the selection of the pore distribution in fluid B distributor and pipe diameter.When this kind of method for designing is used in the design of heat exchanger instead, device has very large flexibility and the space of improvement, is equivalent to provide " interface " that is improved upgrading to device.Illustrate as follows: find in certain embody rule occasion under specific operation, be not fluid flow in helical pipe consistent time performance best, but the flow of upper strata pipeline is few, when the flow of lower floor's pipeline is large, heat transfer effect is better, now only need the distributor of redesign fluid B and change, and not needing to carry out larger improvement.This greatly facilitates the maintenance of this heat exchanger and the upgrade cost of performance.Simultaneously, the size of the weld caliber at distributor and pipeline is needed to meet certain relational expression according to known of the explanation of the method, do not need other pipeline section places also to meet, therefore the concrete layout of pipeline section bottom, the distribution etc. of caliber can improve according to actual requirement.
Illustrate that the rotating heat exchanger of horizontal helical that this embodiment requires is for situation during following situation below, be provided with a heat exchanger when being operated in certain operating mode, flow in requirement horizontal pipe from top to bottom ratio is respectively 4:2:1, the diameter of known helical pipeline is 10mm, the diameter that fluid B distributes cavity 11 is 80mm, now according to Fig. 2 and Fig. 3, design process is described, from requiring, flow needs a certain ratio instead of equal, therefore the difference designing duct number on distributor is needed, the height selecting distributor is 20mm, the quantity in innermost layer duct is 6, the diameter in duct is 4mm, the excentric distance in its center of circle is 20mm, the pipe diameter of below is 25mm, access ground floor pipeline.The quantity in duct, intermediate layer is 6, and the diameter in duct becomes 2.8mm, and the number in outermost layer duct is 6, and diameter becomes 2mm; Can certainly be consistent by the diameter controlling duct, regulate the number in duct.The related data of two kinds of methods for designing is summarized as follows shown in table:
The design parameter of horizontal helical rotating heat exchanger when table 3 flowrate proportioning is 4:2:1
Illustrate: the ratio of the actual flow in this form is as requested not accurate, and its chief reason considers that actual processing problems has carried out rounding to data.
Embodiment 4
If Fig. 5 and Fig. 6 is another kind of way of realization of the present invention, comprise fluid B and distribute cavity 11, this fluid B distributes cavity 11 and is provided with fluid intake 11a, is provided with fluid B distributor 12 and is arranged on the fluid B distribution duct 13 between fluid B distributor 12 and fluid B import 5 in this fluid B distribution cavity 11.Fluid B distribution duct is separate two or more flexible pipes, and flexible pipe can adopt soft pipeline.Flexible pipe one end is through the dispensing orifice of described fluid B distributor, and this end end is provided with the flange face 15 interfixed with described fluid B distributor.Fluid B distributes between cavity and shell for removably connecting.Flexible pipe adopts soft pipeline.
The present embodiment is applicable to heat exchange between two kinds of liquid working substances and the very large situation of the heat exchange amount required, helical pipe layering number in vaporizer body is now more (this example is for 10 layers), working condition and other embodiments of vaporizer body part are similar, do not state at this tired.The distributor now selected is dismountable software distributor (schematic diagram as shown in Figure 5), except the through hole that distributor (fluid B distributor 12) makes hot water flow down to enter except being designed with pipeline, also be provided with the vexed hole 14 for fixed soft body pipeline, soft pipeline and distributor adopt the thin flange joint of pipe end (flange face 15) and screw 16 to fix at the upper side of distributor, have 10 through holes on the dispenser, each through hole will be connected with a soft pipeline, soft pipeline and through hole be arranged as matched in clearance.The length of each flexible pipe differs, and its length designs according to the entrance of the helical pipe of correspondence, the entrance of pipe flexible pipe difference each root helical pipe corresponding.The distributor that whole embodiment is used and fundamental diagram are as shown in Figure 5.
What this embodiment adopted is hose type feed liquor method, similar with bushing type feed liquor method, this feed liquor method also effectively and accurately can regulate the feed liquor flow of fluid B, and the mode of adjustment is the distribution in the duct of improving in distributor, and can not convection current amount have an impact to the improvement of soft pipeline.In this feed liquor scheme, the cavity of side, fluid B distributor, connection between soft pipeline and helical pipe are all dismountable, be exactly that side cavity can be connected with the main part of evaporimeter by screw specifically, the connection of distributor and soft pipeline then relies on thin flange joint and the screw of hose end, be fixed in the vexed hole of distributor upper side, soft pipeline can use proprietary joint or clip to be connected with the connection of helical pipe.The device that is designed to like this provides very large flexibility, the making of heat exchanger and process more convenient.Meanwhile, the assembly of distributor, soft pipeline multidutyly can also be used in other occasions, can dismantle if desired and use instead, and the cleaning of device and updating maintenance are also very convenient in addition, only needs to change associated components wherein.Flow regulating function and the embodiment 3 of this embodiment are similar, can reference example 3.
As can be seen from above four embodiments, when the falling-film heat exchanger of a kind of pipe level screw arrangement that the present invention proposes is applied in industrial production, effectively can not only promote the performance of existing apparatus, such as it is a lot of to make the heat exchange density of evaporimeter improve in embodiment 1, what make the density of the concentrated liquid obtained from exchanger base fluid that is higher and two kinds of different boiling separate in embodiment 2 is more abundant etc., but also reserved " interface " for performance boost from now on, if desired, only need Partial key parts wherein, such as distributor, carry out design and change i.e. realizability can lifting.
Claims (5)
1. the falling-film heat exchanger of a spiral pipeline layout, comprise shell (1), this shell is provided with fluid A import (2), gaseous fluid A exports (3), fluid liquid A exports (4), fluid B import (5) and fluid B and exports (6), fluid A distributor (7) is provided with in this shell, it is characterized in that, in described shell (1), be provided with at least one helical layer pipeline (8) and the collection conduits (9) with the outlet of described helical pipe (8); The inlet of described helical pipe (8) is all communicated with described fluid B import (5); Described collection conduits (9) one end is closed, and the other end exports (6) with described fluid B and is communicated with;
Also comprise fluid B and distribute cavity (11), this fluid B distributes cavity and is provided with fluid intake (11a), is provided with fluid B distributor (12) and is arranged on the fluid B distribution duct (13) between fluid B distributor and fluid B import in this fluid B distribution cavity;
Described fluid B distribution duct (13) is at least two, the entrance end portion of multiple fluid B distribution duct (13) is mutually sheathed, and the port of export of inner fluid B distribution duct is connected with described fluid B import (5) through outside fluid B distribution duct.
2. the falling-film heat exchanger of spiral pipeline layout according to claim 1, it is characterized in that, the spiral form that described helical pipe (8) adopts is the one in spiral of Archimedes form, Made up of Line Segment Involute form, regular polygon involute in form, circle involute form, ellipse evolute form.
3. the falling-film heat exchanger of spiral pipeline layout according to claim 1 and 2, it is characterized in that, the diameter of described collection conduits (9) is 2 ~ 4 times of helical pipe (8) diameter.
4. the falling-film heat exchanger of spiral pipeline layout according to claim 1 and 2, it is characterized in that, the angle between described helical pipe (8) and horizontal plane is 0 ~ 30 °.
5. the falling-film heat exchanger of spiral pipeline layout according to claim 1 and 2, it is characterized in that, described helical pipe (8) is the one in pipe or elliptical tube.
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| EP2433689B1 (en) * | 2010-09-28 | 2013-07-24 | Rinheat Oy | Falling film evaporator |
| JP2013057484A (en) * | 2011-09-09 | 2013-03-28 | Modec Inc | Falling film type heat exchanger, absorption refrigeration system, ship, offshore structure and underwater structure |
| CN102384608A (en) * | 2011-11-11 | 2012-03-21 | 佛山市顺德区高美空调设备有限公司 | Falling-film evaporator for refrigeration system |
| CN102759225B (en) * | 2012-06-29 | 2014-08-20 | 西安交通大学 | Riser spiral-flow type falling-film evaporator for refrigerating air conditioner |
| CN203011011U (en) * | 2012-12-21 | 2013-06-19 | 攀枝花钢城集团瑞通制冷设备有限公司 | Hot water heat exchanger for heat pump |
| CN203083209U (en) * | 2013-01-08 | 2013-07-24 | 浙江思科国祥制冷设备有限公司 | Dry-type evaporator |
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