CN103822409A - Falling film type heat exchanger with tubes in spiral arrangement - Google Patents
Falling film type heat exchanger with tubes in spiral arrangement Download PDFInfo
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- CN103822409A CN103822409A CN201410028802.3A CN201410028802A CN103822409A CN 103822409 A CN103822409 A CN 103822409A CN 201410028802 A CN201410028802 A CN 201410028802A CN 103822409 A CN103822409 A CN 103822409A
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Abstract
The invention discloses a falling film type heat exchanger with tubes in spiral arrangement. The falling film type heat exchanger is characterized in that heat exchange tubes are in horizontal and spiral arrangement, and shell-side working media flow down along the outer wall surfaces of the tubes in a film-shaped manner. The falling type heat exchanger specifically comprises a shell, a fluid A inlet, a gaseous fluid A outlet, a liquid fluid A outlet, a fluid B inlet and a fluid B outlet are formed in the shell, a fluid A distributor is arranged in the shell, and at least one layer of spiral tubes and a collection tube communicated with outlets of the spiral tubes are further arranged in the shell; fluid inlets of the spiral tubes are all communicated with the fluid B inlet; a spiral form of the tubes is one of an Archimedes spiral form, a line segment evolvent form, a regular polygon evolvent form, a circle evolvent form and an ellipse evolvent form. Tube-side fluid inlet modes can be a direct fluid inlet method, a tube-in-tube fluid inlet method and a hose type fluid inlet method. The novel falling film type heat exchanger greatly widens working situations and application fields of conventional falling film type heat exchangers, and has good market application prospect.
Description
Technical field
The invention belongs to falling film type design of heat exchanger technical field, specifically relate to the falling film type heat exchanger that a kind of spiral pipeline is arranged.
Background technology
Along with social fast development, social industry-by-industry is progressively deepened for utilization and the degree of dependence of the energy, and in order more effectively to utilize the energy, society increases day by day to the demand of efficient heat-exchanger rig.Heat exchange efficiently not only can improve the utilization ratio of the energy, and can effectively utilize the used heat in life by suitable design, therefore its research is significant.Falling film type 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 starts to be applied in field of Refrigeration and Air-conditioning the nineties in 20th century.Sum up the achievement in research about cooling horizontal downward film evaporator both at home and abroad, known it compare flooded evaporator and there is larger advantage; 1) have the very high coefficient of heat transfer: the main 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 that the size of device can be done, cost-saving; The mobile main driving force of working medium is gravity simultaneously, and what therefore in evaporimeter, power pressure reduced is very little, and 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 that flows into base of evaporator is actually the mixing material that oil concentration is higher, after again improving, just can directly 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 exists some problems at present.The performance parameter that affects evaporimeter is a lot: the flow of cold-producing medium, design of the layout of fluidised form, pipeline, surface texture, distributor etc.Wherein one of problem of most critical is how to design distributor the working medium of spray is uniformly distributed to greatest extent, if because spray working medium skewness, just may there is dry-out in pipe surface so, the deteriorated significantly heat exchange property of evaporimeter of the appearance of dry-out.Therefore further research and the discussion to distributor problem, is significant for the business application that advances 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 Reducing membrane type evaporimeter occurred for a long time, and current application mainly concentrates on the industries such as empty point, oil, chemical industry, pharmacy, and people have accumulated a lot of experiences in its design.Vertical Reducing membrane type 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 Reducing membrane type evaporimeter adopts mostly is the straight tube of vertical layout, some employing be 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 to adopt to be welded to connect, therefore the cleaning of pipeline and maintenance difficulty very.The simultaneously selection of tube side fluid is also very restricted, and in the time adopting flue gas etc. as thermal source, the solid particle in flue gas may be in the inner deposition that occurs of pipe, and then occurs the phenomenon of stopping up.In the time adopting the larger fluid of viscosity as thermal source, the resistance in flow process is very large in addition, and spent pump merit will be very large in running for this evaporimeter.
In general, in the time of application level downward film evaporator, more to be concerned about the variations in temperature of shell-side fluid or the variation of concentration, therefore in order better to realize the control to shell side heat transfer process, all can be optimized design to the distributor of shell-side fluid, relatively simple for the allocation strategy of the heat source fluid of tube side; Typical Vertical Reducing membrane type evaporimeter is that the assignment of traffic of tube side fluid is optimized, the heat source fluid of shell side adopts the mode of " singly entering singly ", there is no the strategy of corresponding assignment of traffic, this has just limited 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, the advantage of falling film type heat exchange can be better brought into play in the heat transfer effect of enhanced heat exchange pipeline both sides fluid and reinforcement simultaneously to the control of both flows.
At present mainly that layout and structure to its pipeline is optimized for the improvement of downward film evaporator, for example patent documentation (publication No. CN102759225A) has been announced a kind of downward film evaporator of vertical spiral-flow type, this patent has been strengthened the heat exchange of pipeline wall by helical baffles is set, reduced and occurred dry possibility.But because the Working fluid flow region in enclosure cavity is larger, the strengthening effect that working medium is brought due to flow disturbance in helical flow process is also not obvious, and enhancements is not taked in the heat exchange of pipe interior fluid one side yet; Simultaneously because tube bank is for vertically arranging, the therefore traditional too not large lifting of Vertical Reducing membrane type evaporimeter compared with the time of working medium and tube wall Falling film heat transfer in whole runner, the effect of membranaceous heat exchange need further excavation.Patent documentation (CN102759227A) discloses a kind of cooling horizontal downward film evaporator, and feature is by one section of liquid refrigerant supercooling tube road and the further heat exchange of gaseous refrigerant that completes heat exchange are set, to add big supercooling degree.This patent documentation limitation is that the arrangement form of pipeline still adopts traditional arrangement, and this layout makes the space availability ratio of evaporimeter lower.Patent documentation (CN103153419A) has been announced a kind of novel downward film evaporator, the evaporimeter principal character of the type is the tube bank that evaporimeter comprises two or more, tube sheet and collection conduit separately disposed in each tube bank, change design and can avoid preferably the dry of pipe surface by tube bank being arranged as to " 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 Reducing membrane type evaporimeter all have advantage and application scenario separately, also have inferior position separately simultaneously.The coefficient of heat transfer of horizontal downward film evaporator is high, but the space availability ratio of heat exchanger inside is lower; Although and 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 adopt allocation strategy to the flow of being concerned about fluid, and do not adopt corresponding strategy for another fluid streams.Develop can be integrated both the heat exchange advantage application scenario that the Novel falling film formula heat exchanger of inferior position can widen falling film type heat exchanger greatly of simultaneously forgoing, will there is huge market application foreground.
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 Reducing membrane type evaporimeter and horizontal downward film evaporator concurrently, heat transfer coefficient is high, good effect of heat exchange, two strands of heat exchanging fluids are all adopted to flow-control allocation strategy simultaneously, further promoted the flexibility of this falling film type heat exchanger.
The falling film type 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 outlet, in this shell, be provided with fluid A distributor, the collection conduits that is provided with at least one helical layer pipeline in described shell and is communicated with the outlet of described helical pipe; The inlet of described helical pipe is all communicated with described fluid B import; Described collection conduits one end sealing, the other end is communicated with described fluid B outlet.
Fluid B enters heat exchanger in the side of housing, after helical pipe, collection conduits, last at the bottom of housing outflow heat exchanger.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, discharge, and the fluid of gaseous state is drawn from the gaseous fluid A outlet of the side of housing from fluid liquid A outlet.
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 form, circle involute form, oval involute form.To carry out suitable correction to curve in the junction of helical pipe and collection conduits and the junction of pipeline and housing.Concrete which kind of spiral form that adopts need to be determined according to actual conditions.The diameter of described helical pipe is contained microchannel and the conventional pipeline of refrigeration, when device hour, the diameter of pipeline can get the small value, and heat exchange amount requires when larger, the desirable large value of caliber.
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 can effectively produce disturbance to the formation of liquid film, reduces the thickness in boundary layer, thus enhanced heat exchange effect.
Owing to need to bearing larger stress in helical pipe junction, for the intensity of stiffening device, when actual installation, in helical pipe and shell junction, supporting construction can be set as required, and supporting construction comprises the wall of support column, brace summer or thickening etc., to meet requirement of strength.
According to the difference of fluid B character, fluid B can adopt multiple feed liquor form, in the time that fluid B is gas, can directly gas be input in helical pipe, this kind of form we referred to as direct-type feed liquor method.Do not need additionally to increase distributor.In the time that fluid B is liquid state, according to the difference of fluid B uninterrupted and use occasion, can be divided into again other two kinds of forms, i.e. bushing type feed liquor method and hose type feed liquor method.Now, as preferably: the falling film type heat exchanger that described spiral pipeline is arranged also comprises that fluid B distributes cavity, this fluid B distributes cavity to be provided with liquid inlet, this fluid B distribute be provided with fluid B distributor in cavity and be arranged on fluid B distributor and fluid B import between fluid B distribution duct.
When using in space comparatively when narrow space, as preferably, described fluid B distribution duct is at least two, and the arrival end part 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 interfixing with described fluid B distributor.
For meeting the demand of different occasions, be convenient to fluid B and distribute replacing and the installation of cavity, as preferably, described fluid B distributes between cavity and shell for removably connecting.For example, can adopt clamp connection, be threaded etc.
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 pass through 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, and the diameter of collection conduits need to be determined according to the flow of fluid B.
Helical pipe when mounted can level be installed or is tilted angle certain and installs, 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 be arranged by deflection certain angle, can reduce like this dry of helical pipe.Distance pipeline between adjacent helical pipe is also adjustable.The angle departing from is determined according to actual conditions with distance.
The structure of the distributor adopting in the present invention can adopt orifice-plate type distributor, nozzle-type distributor, plough groove type distributor or other combined type distributors.The selection of distributor and concrete design parameter 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 type heat exchanger of horizontal helical described in it is: when 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, in the time dropping onto lower floor's helical pipe surface, liquid film is subject to power upwards, the speed of vertical direction changes, transfer the circumferential movement along helical pipe, experience respectively stagnation fluidised form, development fluidised form, 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, in heat exchanger, can form the fluid A of gaseous state, the fluid A of gaseous state draws heat exchanger by the steam (vapor) outlet (gaseous fluid A outlet) that is arranged in housing side, the fluid A that does not have enough time to vaporize hoards the bottom at heat exchanger, when the liquid level of bottom is during higher than preset value, liquid A is through fluid liquid A outlet outflow heat exchanger.The fluid B fluid B distributor of successively flowing through, input duct, helical pipe, collection conduits, fluid B outlet.In the time of flat spin pipeline, belong to horizontal falling film type heat exchange with the heat exchange of fluid A, what relative motion was pipeline is circumferential; And belonging to the heat exchange of Vertical Reducing membrane type in the heat exchange of collection conduits and liquid, relative motion is axial along pipeline.
In the present invention, fluid B, entering before collection conduits, belongs to horizontal falling film type heat exchange with the heat exchange of fluid A, when fluid enters after collection conduits, still carries out heat exchange with fluid A, and heat exchange form class is now similar to common Vertical Reducing membrane type 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 form, circle involute form, oval involute form, therefore in heat exchanger, the length of heat exchanger tube is longer, and the pipeline of arranging in unit volume is also longer.This just makes heat exchanger in the time of less volume, to reach very large heat exchange amount on the one hand, has very high heat transfer density, is therefore applicable to large-scale heat-exchanger rig, and when being applied in the less occasion of heat exchange, device now is more easily realized miniaturization; On the other hand, due to the layout that both can be parallel to each other between helical pipe, also can arrange according to the certain angle of actual conditions relative tilt, so just can strengthen the disturbance of shell-side fluid in the process falling, the thickness that reduces 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 is to flow in helical pipe, and second stage is vertically to flow down in collection conduits.In the first stage, because the track of fluid motion is curve, therefore the fluid state in helical pipe is similar to flowing of elbow, can produce a large amount of Secondary Flows, the disturbance of helical pipe internal flow has been strengthened in the existence of Secondary Flow greatly, promoted momentum between each fluid layer and the exchange of energy, therefore the heat transfer effect of helical pipe inside is better compared with horizontal straight tube road or the less pipeline of elbow number.In the time of second stage, fluid B flows down along collection conduits is membranaceous, carries out heat exchange with the fluid A in collection conduits outside, and the process of heat exchange and Vertical Reducing membrane type evaporimeter heat transfer process are similar.During due to vertical membranaceous heat exchange, the very thin thickness of liquid film, adds on liquid film flow direction, and collection conduits is furnished with again inlet at a certain distance, the fluid B being flowed into by different inlets has destroyed the Development of Boundary Layer of upper strata liquid film, has reduced the thickness of liquid film.Now the coefficient of heat transfer of inner-walls of duct face is higher.Due to the circular profile design of distributor, close with the layout profile of pipeline, therefore the wettability effect of pipeline outer wall face is fine again, and this is also conducive to the stability of this Novel falling film formula heat exchanger work.
(3) for fluid B in the vertical direction, uniform distribution has proposed three kinds of feed liquor mode schemes in this invention, and the first is direct method, when this method is applicable to fluid B and is gas.Latter two is bushing type feed liquor method and hose type feed liquor method, and the two is applicable to the situation that fluid B is liquid.As long as meet fluid B can drop onto below respective layer pipeline in, beyond pipeline is corresponding with the size of distributor junction caliber and the layout in duct, the diameter of all the other pipeline sections can be inconsistent, and such as making caliber reducing progressively etc., 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, can be divided into a lot of runners, and can regulate accurately the flow of each runner by controlling the size in duct and distributing, this scheme has very large flexibility, can be according to the difference of each layer of pipeline heat transfer effect in the time of practical application, the factors such as the position of flow difference, import are optimized improvement to this feed liquor scheme.Simultaneously, being connected of being connected of soft pipeline and distributor, soft pipeline and helical pipe, side cavity (being that fluid B distributes cavity) are designed to detachable form with being connected of heat exchanger main body, not only can realize commercial Application very convenient flexibly-disassembly, cleaning and change suitable convenience, be also conducive to realize the standardization of 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 type heat exchanger of arranging of spiral pipeline of the present invention.
Fig. 3 is the top view of arrangement figure 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 the falling film type heat exchanger of spiral pipeline layout of the present invention.
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 type heat exchanger of spiral pipeline layout of the present invention.
Fig. 8 is the E-E face profile of falling film type heat exchanger shown in Fig. 7.
Fig. 9 is the F-F face profile of falling film type heat exchanger shown in Fig. 7.
In above-mentioned accompanying drawing:
1 is shell; 2 is fluid A import; 3 is gaseous fluid A outlet; 4 is fluid liquid A outlet; 5 is fluid B import; 6 is fluid B outlet; 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 B passage; 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.
The specific embodiment
As shown in Fig. 1,7～9: the falling film type 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 outlet 6, in this shell 1, be provided with fluid A distributor 7, the collection conduits 9 that is provided with at least one helical layer pipeline 8 in shell 1 and is communicated with the outlet 8b of helical pipe 8; The inlet 8a of helical pipe 8 is all communicated with fluid B import 5; Collection conduits 9 one end sealings, the other end is communicated with fluid B outlet 6.
As shown in Figure 1, helical pipe 8 can adopt multiple spiral form, conventional form is that spiral of Archimedes form (as shown in Fig. 1 (c)), Made up of Line Segment Involute form are (as shown in Fig. 1 (b),), one in regular polygon involute form (as shown in Figure 1 (d) shows, Fig. 1 (d) is square involute form), circle involute form (as shown in Fig. 1 (a)), oval involute form.In Fig. 1,8a is helical pipe 8 imports.
The diameter of collection conduits 9 is 2～4 times of helical pipe 8 diameters.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 be taked 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 B passage, and the collection conduits that fluid A and fluid B arrange by horizontally disposed helical pipe and vertical direction is carried out the exchange of heat.Fluid A successively flow through fluid A import, distributor, helical pipe outside wall surface, fluid A outlet (comprising gaseous fluid A outlet and fluid liquid A outlet), 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, also greatly improves with the flexibility of timer.Below in conjunction with instantiation explanation, the present invention is applied in the advantage place in commercial Application.
As Fig. 7,8,9 examples are applicable to the evaporimeter in field of Refrigeration and Air-conditioning, fluid A elects cold-producing medium as, fluid B(air) elect refrigerating medium as.Fluid A was gas-liquid mixed state before entering this heat exchanger, fluid A import 2 by top enters after heat exchanger, fluid A sprays uniformly the outside wall surface of helical pipe 8 after fluid A distributor 7, become membranaceous dirty in the outside wall surface of helical pipe 8, because fluid A and cold-producing medium A in cold-producing medium A(the present embodiment 1 refer 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 producing is drawn from the gaseous fluid A outlet 3 in housing 1 side arrangement, delivers to compressor.And be cryogenic fluid and oily mixing material in the dense thick liquid of heat exchanger bottom, 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 B path 10.Owing to adopting falling film type heat exchange, therefore the pressure decreased of evaporimeter is little, and variations in temperature is little, therefore in the time of 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, can be divided into two different phases, both heat exchange of first stage have been flowed relatively in helical pipe 8 both sides, this stage cold-producing medium A forms liquid film in helical pipe 8 outsides, because the helical pipe 8 of 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, in the time that other conditions are the same, it is larger that heat exchange area is meaning greatly heat exchange amount.Moreover 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 that produce in motion process have been strengthened inner disturbance greatly, make boundary layer be difficult for development and attenuation, also strengthen heat transfer coefficient from inside, thereby greatly strengthened heat exchange.The heat exchange of second stage is the both sides in collection conduits 9, now two fluid streams all vertically become membranaceous flowing down, due to the layout feature of helical pipe 8, make the development in boundary layer can only be in the middle of two-layer pipeline could sustainable development, and interrupted in the junction of pipeline, again form new boundary layer.Comprehensive above two features are known, not only greatly extended the heat-exchange time of cold-producing medium and refrigerating medium when the present invention is applied to this example, also mechanism, greatly strengthened heat transfer effect simultaneously.
Advantage of the present invention also can be carried 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: the length of establishing contrast flooded evaporator is 1000mm, the diameter 300mm of main part, pipe row is 6 rows, is furnished with altogether 55 of pipeline numbers, 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 ℃; In the time 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, and all the other are the movement of falling object while not moving on pipeline.In the time not adopting enhanced heat exchange pipeline, selecting the coefficient of heat transfer of heat exchanger is 1000W/ (m
2k), the rotating heat exchanger of the horizontal helical of present embodiment is 1100W/ (m
2k).Below for contrasting the result of calculation summary sheet of two kinds of heat exchangers: the result of calculation by table 1 can be found out, this flat spin evaporimeter not only can extend the heat-exchange time between two fluid streams greatly, also can utilize the heat exchange area of increase to improve heat exchange amount, comparative benefits is quite obvious simultaneously.
Table 1 spiral pipeline heat exchanger and flooded evaporator performance comparison
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 now the something a concentration in fluid A is lower, and fluid B passage is connected with the hot fluid that temperature is higher (steam of high temperature).Similar in heat transfer process between the two and embodiment 1, after each layer of heat exchange pipeline, owing to obtaining heat, the moisture in fluid A can part vaporization successively.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, while reaching necessary requirement, can isolate heat exchanger from bottom.
This embodiment also has one to become example, realize the separation of the liquid refrigerant of two kinds of different boiling, when 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 ℃ and 200 ℃, fluid B now remains and adds hot fluid, and the temperature that selection adds hot fluid is 100 ℃.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 default steam (vapor) outlet, and high boiling fluid a2 finally flows to the bottom of heat exchanger, after liquid level exceedes certain altitude, is also drawn.
When the present invention is applied to this embodiment, because heat exchange pipeline is long more a lot of than conventional falling film type heat exchanger, the area of heat exchange is much bigger, what therefore heat transfer process can carry out is more abundant, specifically in the time being applied to the purification of material, the more liquid that strongly makes of heat exchange is vaporizated into gas, and in the solution that resulting device bottom obtains, the concentration of material a is higher.And in the time being applied to the separation of different boiling liquid, can from mixing material, isolate more low boiling working fluid, the separative efficiency of device obviously improves.
Advantage below by calculation specifications the present invention for the concentration process of solution, the object of contrast is the Vertical Reducing membrane type heat exchanger of commonly using in chemical industry: the barrel diameter of supposing contrast Vertical Reducing membrane type 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 Reducing membrane type pipeline is 100, and every effective heat exchange length is 600mm, and the caliber of every is 10mm.The coefficient of heat transfer is taken as 3500W/ (m2K).It is identical with embodiment 1 with relevant parameter that the rotating pipeline of horizontal helical is arranged, comparison between calculation results is summarized as in following table: can find out from final result of calculation, when the present invention is applied to solution concentrated, although the advantage of heat exchange area disappears, but owing to can guaranteeing heat-exchange time, therefore the fluid of unit mass is still very large to the total heat exchange amount of outflow heat exchanger from entering heat exchanger, and therefore total advantage exists.
2 flat spin heat exchangers and the contrast of Vertical Reducing membrane type performance of evaporator
Illustrate: the equivalent vaporization biodiversity in table 2 is the ratio of the latent heat of total heat exchange amount and water.
If Fig. 2 and Fig. 3 are another kind of way of realization of the present invention, comprise that fluid B distributes cavity 11, this fluid B distributes cavity 11 to be provided with fluid intake 11a, this fluid B distribute be provided with fluid B distributor 12 in cavity 11 and be arranged on fluid B distributor 12 and fluid B import 5 between fluid B distribution duct 13.Fluid B distribution duct 13 is two, and the arrival end part 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 two kinds of heat exchange between liquid working substance and the very little situation of heat exchange amount of requirement, because heat exchange amount is very little, suppose the helical pipe layering number less (the present embodiment is take 3 layers as example) in vaporizer body now, the working condition of vaporizer body part and other embodiment are similar, do not state tired at this.Fluid B(hot fluid) enter from the side cavity of evaporimeter, after the distributor (fluid B distributor 12) of a porous, the flow in each hole of flowing through is identical, duct 12a on fluid B distributor 12 is according to be divided into three groups (schematic diagram as shown in Figure 3) apart from the distance difference at cavity center, side, below distributor by being welded to connect two sleeve pipes (fluid B distribution duct 13), the value of designing requirement pipe diameter must make hot water that innermost layer duct the flows down inner layer pipe under all entering, the duct in intermediate layer stays the rear intermediate layer pipeline all entering 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 Fig. 2～4.
What this embodiment adopted is bushing type feed liquor method, the method is separately for fluid B has designed a distributor and input duct, be not only for fluid B can be more evenly distributed in helical pipe, the more important thing is and can carry out the ducted flow distribution of the each helical layer of fine adjustment by the pore distribution in adjusting fluid B distributor and the selection of pipe diameter.In the time that this kind of method for designing used in the design of heat exchanger instead, device has very large flexibility and improved space, and being equivalent to provides " interface " that improves upgrading to device.Illustrate as follows: in certain concrete application scenario, find under specific operation, be not fluid flow in helical pipe when consistent 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 to redesign the distributor of 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, need to meet certain relational expression in the size of the weld caliber of distributor and pipeline according to known of the explanation of the method, do not need other pipeline section places also to meet, therefore concrete layout, the distribution of caliber etc. of pipeline section bottom can improve according to actual requirement.
The situation of the rotating heat exchanger of horizontal helical that illustrates this embodiment requirement below during for following situation, when being provided with a heat exchanger and 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, it is 80mm that fluid B distributes the diameter of cavity 11, now according to Fig. 2 and Fig. 3, design process is described, from requiring, flow needs a certain ratio rather than equates, therefore need to design the difference of duct number on distributor, selecting the height of 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 in control 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 the rotating heat exchanger of horizontal helical when table 3 flowrate proportioning is 4:2:1
Illustrate: the ratio of the actual flow in this form does not have as requested accurate, its chief reason is to consider that actual processing problems carried out rounding to data.
Embodiment 4
If Fig. 5 and Fig. 6 are another kind of way of realization of the present invention, comprise that fluid B distributes cavity 11, this fluid B distributes cavity 11 to be provided with fluid intake 11a, this fluid B distribute be provided with fluid B distributor 12 in cavity 11 and be arranged on fluid B distributor 12 and fluid B import 5 between fluid B distribution duct 13.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 interfixing 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 two kinds of heat exchange between liquid working substance and the very large situation of heat exchange amount of requirement, helical pipe layering number more (this example is take 10 layers as example) in vaporizer body now, the working condition of vaporizer body part and other embodiment are similar, do not state tired at this.The distributor of now selecting is dismountable software distributor (schematic diagram as shown in Figure 5), upper except being designed with the through hole that makes to enter under flow of hot water pipeline at distributor (fluid B distributor 12), also be provided with the vexed hole 14 for fixed soft body pipeline, soft pipeline and distributor adopt thin flange joint (flange face 15) and the screw 16 of pipe end to fix at the upper side of distributor, on distributor, have 10 through holes, 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 corresponding helical pipe, the entrance of respectively corresponding each the root helical pipe of a pipe flexible pipe.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 can effectively and accurately regulate the feed liquor flow of fluid B, and the mode of adjusting is to improve the distribution in the duct in distributor, and the improvement of soft pipeline can convection current amount not exerted an influence.Connection in this feed liquor scheme between the cavity of side, fluid B distributor, soft pipeline and helical pipe is all dismountable, be exactly that side cavity can be connected with the main part of evaporimeter by screw specifically, distributor and the thin flange joint and the screw that rely on hose end being connected of soft pipeline, be fixed in the vexed hole of distributor upper side, soft pipeline was connected with using proprietary joint or clip being connected of helical pipe.The device that is designed to like this provides very large flexibility, more convenient in making and the process of heat exchanger.Meanwhile, the assembly of distributor, soft pipeline can also multidutyly be used in other occasions, can dismantle and use instead if desired, and cleaning and the updating maintenance of device are also very convenient in addition, only needs to change associated components wherein.The flow regulating function of this embodiment and embodiment 3 are similar, can reference example 3.
Can find out from four above embodiment, a kind of falling film type heat exchanger applications of pipe level screw arrangement proposing as the present invention is in industrial production time, not only can effectively promote the performance of existing apparatus, such as the heat exchange density that makes evaporimeter in embodiment 1 improves a lot, what in embodiment 2, make that the density fluid higher and two kinds of different boiling of the concentrated liquid obtaining from heat exchanger bottom separates is more abundant etc., but also reserve " interface " for performance boost from now on, if desired, only need to be to part critical component wherein, such as distributor, carry out the lifting that can realize performance designing and changing.
Claims (10)
1. the falling film type heat exchanger that spiral pipeline is arranged, comprise shell (1), this shell is provided with fluid A import (2), gaseous fluid A outlet (3), fluid liquid A outlet (4), fluid B import (5) and fluid B outlet (6), in this shell, be provided with fluid A distributor (7), it is characterized in that the collection conduits (9) that is provided with at least one helical layer pipeline (8) in described shell (1) and is communicated 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 sealing, the other end exports (6) with described fluid B and is communicated with.
2. the falling film type heat exchanger that spiral pipeline according to claim 1 is arranged, 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 form, circle involute form, oval involute form.
3. the falling film type heat exchanger that spiral pipeline according to claim 1 is arranged, it is characterized in that, also comprise that fluid B distributes cavity (11), this fluid B distributes cavity to be provided with fluid intake (11a), this fluid B distribute be provided with fluid B distributor (12) in cavity and be arranged on fluid B distributor and fluid B import between fluid B distribution duct (13).
4. the falling film type heat exchanger that spiral pipeline according to claim 3 is arranged, it is characterized in that, described fluid B distribution duct (13) is at least two, the arrival end part 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.
5. the falling film type heat exchanger that spiral pipeline according to claim 3 is arranged, is characterized in that, described fluid B distribution duct (13) is separate two or more flexible pipes.
6. the falling film type heat exchanger that spiral pipeline according to claim 5 is arranged, is characterized in that, 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 (15) interfixing with described fluid B distributor.
7. the falling film type heat exchanger that spiral pipeline according to claim 6 is arranged, is characterized in that, described fluid B distributes between cavity (11) and shell (1) for removably connecting.
8. the falling film type heat exchanger of arranging according to the spiral pipeline described in the arbitrary claim of claim 1～7, is characterized in that, the diameter of described collection conduits (9) is 2～4 times of helical pipe (8) diameter.
9. the falling film type heat exchanger of arranging according to the spiral pipeline described in the arbitrary claim of claim 1～7, is characterized in that, the angle between described helical pipe (8) and horizontal plane is 0～30 °.
10. the falling film type heat exchanger of arranging according to the spiral pipeline described in the arbitrary claim of claim 1～7, is characterized in that, described helical pipe (8) is pipe, elliptical tube, conic section pipe, high order curve pipe.
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| CN113505502A (en) * | 2021-09-10 | 2021-10-15 | 中国人民解放军国防科技大学 | Method for designing special-shaped microchannel heat exchange tube, computer equipment and storage medium |
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