CN108332578B - A kind of gas-liquid two-phase flow tube shell type heat exchanger - Google Patents
A kind of gas-liquid two-phase flow tube shell type heat exchanger Download PDFInfo
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- CN108332578B CN108332578B CN201710651947.2A CN201710651947A CN108332578B CN 108332578 B CN108332578 B CN 108332578B CN 201710651947 A CN201710651947 A CN 201710651947A CN 108332578 B CN108332578 B CN 108332578B
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- fin
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- 239000007788 liquid Substances 0.000 title claims abstract description 34
- 230000005514 two-phase flow Effects 0.000 title claims abstract description 13
- 239000003381 stabilizer Substances 0.000 claims abstract description 65
- 239000012530 fluid Substances 0.000 claims abstract description 28
- 238000012546 transfer Methods 0.000 claims abstract description 27
- 238000000034 method Methods 0.000 claims abstract description 9
- 230000008569 process Effects 0.000 claims abstract description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 230000003416 augmentation Effects 0.000 abstract description 6
- 230000003313 weakening effect Effects 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 24
- 230000000694 effects Effects 0.000 description 17
- 230000001965 increasing effect Effects 0.000 description 17
- 239000007791 liquid phase Substances 0.000 description 10
- 238000013016 damping Methods 0.000 description 9
- 238000009826 distribution Methods 0.000 description 8
- 230000009467 reduction Effects 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000005520 cutting process Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000006641 stabilisation Effects 0.000 description 4
- 238000011105 stabilization Methods 0.000 description 4
- 238000010276 construction Methods 0.000 description 3
- 210000004262 dental pulp cavity Anatomy 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 241000208340 Araliaceae Species 0.000 description 2
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 2
- 235000003140 Panax quinquefolius Nutrition 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 235000008434 ginseng Nutrition 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 208000031481 Pathologic Constriction Diseases 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
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- 230000002035 prolonged effect Effects 0.000 description 1
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- 238000004088 simulation Methods 0.000 description 1
- 230000036262 stenosis Effects 0.000 description 1
- 208000037804 stenosis Diseases 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
- F28F1/40—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only inside the tubular element
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
- F28F13/12—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media by creating turbulence, e.g. by stirring, by increasing the force of circulation
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Geometry (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The present invention provides a kind of gas-liquid two-phase flow tube shell type heat exchangers, including shell, end socket is respectively set in the shell both ends, tube sheet is arranged in the link position of the end socket and shell, the tube sheet at heat exchanger tube connection both ends, gas phase in biphase gas and liquid flow is insoluble or slightly solubility gas, i.e. in heat transfer process, gas will not be dissolved in liquid, biphase gas and liquid flow flows in tube side, constant-current stabilizer is set in the heat exchanger tube, the constant-current stabilizer includes core and shell, the core setting is in the shell, the shell is connected and fixed with heat transfer tube wall, the core includes from core-center to the more radial bars radially extended, the fin that the more directions from radial bars to fluid flow pair extend is set in the radial bars, the fin has tip, the tip extends towards the direction of fluid flow pair.The present invention provides a kind of heat exchanger of the constant-current stabilizer of Novel structure, there are when gas liquid two-phase flow in pipeline, augmentation of heat transfer, while weakening the vibration of pipeline, reduce noise level.
Description
Technical field
The present invention relates to a kind of shell-and-tube heat exchangers, exchange heat more particularly, to a kind of two-phase flow containing condensable steam
Device.
Background technique
Biphase gas and liquid flow heat exchange is universally present in various heat-exchanger rigs, and biphase gas and liquid flow is in heat transfer process because of gas
The presence of phase, it is low to will lead to heat exchange efficiency, deteriorates heat exchange, process fluid flow is unstable, and will lead to the hair of water hammer
It is raw.When the liquid phase of two-phase working substance is without uniformly mixing and discontinuous flowing, large-sized liquid group can occupy air mass at high speed
Space causes two-phase flow unstable, so that tempestuously impact device and pipeline, generates sharp pounding and noise, seriously prestige
Coerce equipment operational safety.
The present inventor also devises some constant-current stabilizers, such as multitube constant-current stabilizer in applying in front, referring to Fig. 8 institute
Show.But such device is found in operation, because being to be closely linked between pipe, is formed between three root canals
Space A it is relatively small because the convex arc that space A is three root canals is formed, most of area stenosis of space A can be made
It is difficult to enter and passes through at fluid, cause fluid short, to affect the heat exchange of fluid, good current stabilization can not be played the role of.
Simultaneously as more root canal subgroups of above structure are combined, manufacture is difficult.
Therefore in view of the above-mentioned problems, the present invention provides a kind of heat exchangers of the constant-current stabilizer of Novel structure, to solve
Above-mentioned problem.
Summary of the invention
The object of the present invention is to provide a kind of heat exchangers of the constant-current stabilizer of Novel structure, and there are gas-liquid two-phases in pipeline
When flowing, weaken the vibration in biphase gas and liquid flow heat exchanger tube, reduces noise level, while augmentation of heat transfer.
To achieve the goals above, technical scheme is as follows:
End socket, the end socket is respectively set in a kind of gas-liquid two-phase flow tube shell type heat exchanger, including shell, the shell both ends
Tube sheet is set with the link position of shell, heat exchanger tube connects the tube sheet at both ends, and the gas phase in biphase gas and liquid flow is insoluble or difficult
Insoluble gas, i.e., in heat transfer process, gas will not be dissolved in liquid, and biphase gas and liquid flow flows in tube side, set in the heat exchanger tube
Constant-current stabilizer is set, the constant-current stabilizer includes core and shell, and the core is arranged in the shell, in the shell and heat exchanger tube
Wall is connected and fixed, and the core includes being arranged more in the radial bars from core-center to the more radial bars radially extended
The fin extended from radial bars to the direction of fluid flow pair, the fin have tip, and the tip is flowed towards fluid
Opposite direction extends.
Preferably, the core includes the stem that the heart in the core is arranged, described radial bars one end is fixed in stem.
Preferably, groove is arranged in the heat transfer tube wall, the shell of the constant-current stabilizer is arranged in groove, described outer
The inner wall of shell and the aligning inner of heat exchanger tube.
Preferably, heat exchanger tube is welded for multi-segment structure, constant-current stabilizer is arranged in the junction of multi-segment structure.
Preferably, the fin is triangular fin.
Preferably, a bottom edge of triangle is located in radial bars, with the vertex at corresponding angle and this while in
75-135 ° of angle of line and the radial bars formation of point.
Preferably, angle is 90 °.
Preferably, the triangular fin is isosceles triangle fin, the bottom edge of the isosceles triangle is located at diameter
To on bar.
Preferably, the size of the apex angle of isosceles triangle is A, the length on the bottom edge of isosceles triangle is Y, adjacent isosceles
The distance between triangle is J, then meets following require:
Y/J= d-a*sin(A)3-b*sin(A)2-c* sin (A)；Wherein sin is trigonometric function, and a, b, c, d are ginsengs
Number；
0.353<a<0.358,
0.485<b<0.486,
0.082 < c < 0.083,
0.403 < d < 0.404,4 < A < 33 °,
0.1765<Y/J <0.4118。
Preferably, a=0.3559, b=0.4859, c=0.08294, d=0.4033.
Preferably, radial bars are 5-10 root, the angle between the radial bars is all equal.
Preferably, radial bars are 8.
Preferably, the length on the bottom edge of isosceles triangle is 0.02-0.03 times of heat exchange bore.
Compared with prior art, of the invention to have the advantage that
1) the present invention provides a kind of constant-current stabilizers of Novel structure, and two-phase fluid is separated into liquid phase by constant-current stabilizer
And gas phase, liquid phase is divided into small liquid group, gas phase is divided into minute bubbles, inhibits the reflux of liquid phase, promotes gas phase smooth outflow,
Play the role of regime flow, has the effect of vibration and noise reducing.Relative to bar wing formula constant-current stabilizer, current stabilization effect is further increased
Fruit, augmentation of heat transfer, and be simple to manufacture.
2) present invention is equivalent to by setting bar wing formula constant-current stabilizer and increases interior heat exchange area in heat exchanger tube, strengthens
Heat exchange, improves heat transfer effect.
3) present invention avoids existing because gas-liquid two-phase is divided in the entire cross-section location of heat exchanger tube
Only heat transfer tube wall face is split in technology, expands gas-liquid interface and gas phase to realize on entirely heat exchange tube section
The contact area of boundary layer and cooling wall simultaneously enhances disturbance, reduces noise and vibration, enhances heat transfer.
4) present invention is by setting up the distance between adjacent constant-current stabilizer, the length of constant-current stabilizer in tube height side
The rule variation of the parameters sizes such as degree, fin size reduces noise to further reach steady flow result, improves heat transfer effect.
5) present invention is changed by the way that the rule of the parameters sizes such as phase fin size, spacing is arranged in radial directions, thus
Further reach steady flow result, reduce noise, improves heat transfer effect.
6) present invention has been carried out widely by heat exchange rule caused by the variation to bar wing formula constant-current stabilizer parameters
Research, when meeting flow resistance, realizes the best relation formula of the effect of vibration and noise reducing.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of two-phase flow tube shell type heat exchanger of the invention；
Fig. 2 is the heat transfer tube structure diagram of two-phase flow tube shell type heat exchanger of the invention；
Fig. 3 constant-current stabilizer structural schematic diagram of the present invention；
Fig. 4 is constant-current stabilizer of the present invention arrangement schematic diagram in heat exchanger tube；
Fig. 5 is another schematic diagram that constant-current stabilizer of the present invention is arranged in heat exchanger tube.
Fig. 6 is that constant-current stabilizer of the present invention arranges cross-sectional view in heat exchanger tube.
Fig. 7 is the scale diagrams of constant-current stabilizer of the present invention.
Fig. 8 is the structural schematic diagram of the two-phase flow tube shell type heat exchanger in background technique.
Appended drawing reference is as follows: front head 1, cover flange 2, front tube sheet 3, shell 4, constant-current stabilizer 5, heat exchanger tube 6, back tube sheet
7, cover flange 8, rear head 9, support 10, support 11, tube-side inlet pipe 12, tube side outlet 13, shell side inlet pipe 14, shell side
Outlet 15, stem 51, radial bars 52, fin 53, shell 54.
Specific embodiment
Specific embodiments of the present invention will be described in detail with reference to the accompanying drawing.
Herein, if without specified otherwise, it is related to formula, "/" indicates that division, "×", " * " indicate multiplication.
It should be noted that if the two phase flow that the present invention mentions is biphase gas and liquid flow, gas herein without specified otherwise
Gas phase in liquid two-phase is insoluble or slightly solubility gas, i.e., in heat transfer process, gas will not be dissolved in liquid.
A kind of shell-and-tube heat exchanger as shown in Figure 1, the shell-and-tube heat exchanger include shell 4, heat exchanger tube 6, tube side
Inlet tube 12, tube side outlet 13, shell side inlet adapter tube 14 and shell-side outlet adapter tube 15；6 groups of multiple heat exchanger tubes disposed in parallel
At heat-exchanging tube bundle be connected to front tube sheet 3, on back tube sheet 7；The front end of the front tube sheet 3 is connect with front head 1, back tube sheet 7
Rear end connects rear head 9；The tube-side inlet pipe 12 is arranged on rear head 9；The tube side outlet 13 is arranged preceding
On end socket 1；The shell side inlet adapter tube 14 and shell-side outlet adapter tube 15 is arranged on shell 4；The fluid of two phase flow is from pipe
Journey inlet tube 12 enters, and exchanges heat by heat exchanger tube, goes out from tube side outlet 13.
As in Figure 3-5, bar wing formula constant-current stabilizer 5 is set in heat exchanger tube 6.The structure of the bar wing formula constant-current stabilizer 5
See Fig. 3-4.As shown in figure 3, the constant-current stabilizer 5 includes core and shell 54, the core is arranged in shell 54, described outer
Shell 54 is connected and fixed with 6 inner wall of heat exchanger tube, the core include from core-center to the more radial bars 52 radially extended, it is described
The fin 53 that the more directions from radial bars 52 to fluid flow pair extend is set in radial bars 52, and the fin 53 has point
Portion, the tip extend towards the direction of fluid flow pair.
Bar wing formula constant-current stabilizer is arranged in the present invention in heat exchanger tube, mainly passes through the tip of bar wing formula constant-current stabilizer, will
Liquid and gas in two-phase fluid are separated, and liquid phase is divided into small liquid group, and gas phase is divided into minute bubbles, inhibits liquid phase
Reflux, promote gas phase smooth outflow, play the role of regime flow, have the effect of vibration and noise reducing.Apply relative to front
Constant-current stabilizer, further increase steady flow result, augmentation of heat transfer, and be simple to manufacture.
The present invention is equivalent to by setting bar wing formula constant-current stabilizer and increases interior heat exchange area in heat exchanger tube, enhanced
Heat exchange, improves heat transfer effect.
The present invention is because all cross-section locations by gas-liquid two-phase in all heat exchanger tubes are divided, thus entire
The segmentation of gas-liquid interface and gas phase boundary and the contact area of cooling wall are realized on heat exchange tube section and enhances disturbance, greatly
Big reduces noise and vibration, enhances heat transfer.
Preferably, the core includes the stem 51 that the heart in the core is arranged, described 52 one end of radial bars is fixed on core
In column 51.
By the way that stem is arranged, radial bars 52 can be further fixed.
Further preferably, as shown in fig. 7, heat exchanger tube 6 is welded for multi-segment structure, the junction setting of multi-segment structure is steady
Flow device 5.This mode makes being simple to manufacture for the tedge that constant-current stabilizer is arranged, and cost reduces.
Further preferably, as shown in fig. 7, groove is arranged inside the heat exchanger tube 6, the shell 54 of the constant-current stabilizer 5 is set
It sets in groove.
Preferably, the aligning inner of the inner wall of shell 54 and heat exchanger tube 6.By alignment, so that heat transfer tube wall face table
Reach on face in the same plane, guarantees the smooth of surface.
Preferably, the thickness of shell 54 is less than the depth of groove, heat transfer tube wall face can be made to form groove in this way,
To carry out augmentation of heat transfer.
Preferably, as Figure 4-Figure 6, the fin 53 is triangular fin.Because triangular fin itself has three
A tip can make full use of tip to carry out current stabilization effect downwards in this way.
The present invention can be further increased by setting radial bars and along the outwardly extending triangular fin of radial bars
Heat exchange area improves heat transfer effect, and because setting triangular fin, passes through the three of the similar acicular texture of triangular fin
Angular tip can further increase flow-disturbing, so that fluid is sufficiently mixed, can further destroy the increase of bubble and gather
Collection, improves heat transfer effect.
Further preferably, radial bars cross section is rectangle, is preferably square.
Further preferably, radial bars cross section is circle.
Preferably, the engineering diameter of radial bars is 42 times of 0.21-0., preferably 0.32 times of the engineering diameter of stem.
Preferably, the radial bars are shaft, from the center of circle along the radial inner wall for extending to condenser pipe.
Preferably, multiple triangular fins are arranged in each radial bars, multiple triangular fins are similar figures.
Three interior angles in correspondence with each other of i.e. different triangular fins are identical.
Preferably, the radial bars are round bar, a diameter of 0.7-1.1mm, preferably 0.8mm.
Preferably, fin is extended downwardly from the center line of round bar.The fin is slab construction.The slab construction is prolonged
Stretch the center line that stem is passed through in face, and center line of the slab construction extended surface Jing Guo radial bars.
Preferably, shown in 5, multiple fins 53 are arranged in same radial bars, the fin 53 is similar figures (i.e. wing such as 4
Piece is of similar shape), from the stem 51 of heat exchanger tube 6 to radially extending on direction, the size of the fin in same radial bars
It is increasing.Be apart from heat exchanger tube central axis apart from stem 51() distance be S1, the size of fin is C1, and C1 is distance
The function of S1, i.e. C1=F4(S1), meet following require:
C1 ' > 0, wherein C1 ' is the first order derivative of C1.
Because heat exchange occurs mainly in pipe wall of heat exchange pipe, by increasing by 53 size of fin of pipe wall of heat exchange pipe, so that
The ability enhancing of the cutting gas phase and liquid phase of near-wall, is reinforced the cutting power of near-wall by emphasis, can be directed to
The noise reduction damping of carry out in light of the circumstances of property, to further realize noise reduction damping effect, while also can further strengthen biography
Heat.
Further preferably, from the stem of heat exchanger tube to radially extending on direction, the size of the fin in same radial bars is got over
Constantly increase come bigger amplitude.That is C1 " > 0, wherein C1 " is the secondary inverse of C1 respectively.
Show the variation of above-mentioned increasing degree by numerical simulation and experimental study, noise reduction can be further realized
Damping, effect can be turned up close to 8%.
Preferably, multiple fins 53 are arranged in same radial bars 52, from the stem 51 of heat exchanger tube 6 to radially extending direction
On, the spacing between the fin 53 constantly reduces.The amplitude that spacing between the fin constantly reduces is continuous
Increase.
It is S1 apart from the distance of stem, the spacing of fin is J1, J1=F5(S1), meet following require:
J1 '<0, J1 ">0, wherein J1 ', J1 " are the first order derivative and secondary inverse of J1 respectively.
Concrete principle is same as above.Because heat exchange occurs mainly in pipe wall of heat exchange pipe, by the wing for increasing pipe wall of heat exchange pipe
The distribution of piece 53, so that the ability of the cutting gas phase of near-wall and liquid phase enhances, by reinforcing the noise reduction damping of near-wall,
To further realize noise reduction damping effect, while also can further augmentation of heat transfer.
Preferably, a bottom edge of triangle is located in radial bars 52, when with the vertex at corresponding angle with this
The angle that the line and radial bars at midpoint are formed is 75-135 °.Mainly by the setting of above-mentioned angle, fin is enabled to
Tip carries out the cutting of gas-liquid two-phase to the full extent, to further increase effect of the invention.
Preferably, the angle that the line and radial bars at the midpoint when vertex at corresponding angle is with this are formed is 90 °
Preferably, as shown in figure 5, the triangular fin is isosceles triangle fin, the isosceles triangle
Bottom edge is located in radial bars.
It is learnt by analyzing and testing, the spacing between fin 43 cannot be excessive, leads to damping noise reduction if excessive
Effect is bad, while can not be too small, causes resistance excessive if too small, and similarly, the height of fin can not excessive or mistake
Small, the effect for also resulting in damping noise reduction is bad or resistance is excessive, therefore the present invention is through a large number of experiments, is preferentially meeting
Normal flow resistance (total pressure-bearing be 2.5Mpa hereinafter, the on-way resistance of single riser be less than or equal to 5Pa/M) feelings
Under condition, so that being optimal of damping noise reduction, has arranged the optimal relationship of parameters.
The size of the apex angle of isosceles triangle is A, and the length on the bottom edge of isosceles triangle is Y, adjacent isosceles triangle it
Between distance be J, then meet following require:
Y/J= d-a*sin(A)3-b*sin(A)2-c* sin (A)；Wherein sin is trigonometric function, and a, b, c, d are ginsengs
Number；
0.353<a<0.358,
0.485<b<0.486,
0.082 < c < 0.083,
0.403 < d < 0.404,4 < A < 33 °,
0.1765<Y/J <0.4118。
Wherein the distance between adjacent isosceles triangle J is adjacent the distance between the midpoint of triangle base.
Preferably, a=0.3559, b=0.4859, c=0.08294, d=0.4033.
Preferably, 5 < A < 30 °.
Preferably, radial bars are 5-10 root, the angle between the radial bars is all equal.
Preferably, radial bars are 8.
Preferably, the length on the bottom edge of isosceles triangle is 0.02-0.03 times for rising bore.
Preferably, along the flow direction of heat exchange tube fluid, the multiple separating devices of setting in heat exchanger tube, from heat exchanger tube
Entrance to the middle part of heat exchanger tube, the distance between adjacent separating device is increasingly longer, from the middle part of heat exchanger tube to heat exchanger tube
Outlet, the distance between adjacent separating device are shorter and shorter.I.e. the length of heat exchanger tube is L, the distance apart from heat exchange tube inlet
For X, the distance between adjacent separating device is S, S=F1(X), S ' is the first order derivative of S, meets following require:
S’>0, 0<=X<L/2;
S’<0, L/2<=X<=L;
Main cause is because containing on-condensible gas in fluid, and along the flow direction of fluid, on-condensible gas is still
In the presence of, will not because heat exchange tube fluid heat release and condense.From 6 entrance of heat exchanger tube to 6 middle part of heat exchanger tube, because fluid seals in the past
First 1 enters in heat exchanger tube, and in the flowing of the front of heat exchanger tube 6, the vibration of fluid and noise are relatively smaller, therefore can will divide at this time
Every the larger of the distance between device setting, damping both may be implemented and reduced noise, while resistance can also be reduced.But
Backward from the middle part of heat exchanger tube, because in the presence of the variation from heat exchanger tube 6 to the space of 9 this section of rear head from small to large, this
The variation of section will lead to quickly flowing upwards out and assemble for gas, and liquid also quickly can flow out and assemble in item lower part, therefore empty
Between variation will lead to the gas phase (air mass) of aggregation and enter end socket from tubesheet location, due to gas (vapour) liquid density contrast, air mass, which leaves, to be connect
Pipe position will move rapidly upward, and air mass original spatial position is pushed away the liquid of wall surface while also will be sprung back and hit rapidly by air mass
Wall surface is hit, water hammer is formed.Gas (vapour) liquid phase is more discontinuous, and air mass aggregation is bigger, and water hammer energy is bigger.Water hammer can be made
At the vibration of biggish noise and mechanical shock, equipment is damaged.Therefore in order to avoid the generation of this phenomenon, it is arranged at this time
The distance between adjacent separating device it is shorter and shorter, to constantly separate gas phase and liquid phase in fluid delivery process, from
And vibration and noise are reduced to the full extent.
It is found through experiments that, by above-mentioned setting, can both reduce vibration and noise to the full extent, while can protect
Card reduces the flow resistance of fluid.
Further preferably, from the entrance of heat exchanger tube to the middle part of heat exchanger tube, the distance between adjacent separating device is increasingly
Long amplitude is continuously increased, and from the middle part of heat exchanger tube to the outlet of heat exchanger tube, the distance between adjacent separating device is increasingly
Short amplitude is continuously increased.That is S " is the second derivative of S, meets following require:
S”>0,0<=X<L/2;
S”>0, L/2<=X<=L;
It is found through experiments that, by being reduced simultaneously so set, 8% or so vibration and noise can be further decreased
The resistance of flowing 6% or so.
Preferably, the length of each constant-current stabilizer remains unchanged.
Preferably, other than the distance between adjacent constant-current stabilizer, constant-current stabilizer others parameter (such as length,
Caliber etc.) it remains unchanged.
Preferably, along the flow direction of fluid in heat exchanger tube 6, the multiple constant-current stabilizers 5 of setting in heat exchanger tube 6, from changing
The entrance of heat pipe 6 is increasing after the size of the fin of constant-current stabilizer 5 is first smaller and smaller to the outlet of heat exchanger tube 6.As excellent
Choosing, the middle part from the entrance of heat exchanger tube 6 to heat exchanger tube, the size of the fin of constant-current stabilizer 5 is smaller and smaller, from the central island of heat exchanger tube
The size of the outlet of heat exchanger tube 6, the fin of constant-current stabilizer 5 is increasing.I.e. the fin of constant-current stabilizer is having a size of C, C=F2(X),
C ' is the first order derivative of C, meets following require:
C’<0, 0<=X<L/2;
C’>0, L/2<=X<=L;
Preferably, middle part, the size of the fin of constant-current stabilizer 5 are smaller and smaller from the entrance of heat exchanger tube 6 to heat exchanger tube
Amplitude is continuously increased, from the outlet of the central island heat exchanger tube 6 of heat exchanger tube, the increasing width of the size of the fin of constant-current stabilizer 5
Degree is continuously increased.That is C " is the second derivative of C, meets following require:
C”>0,0<=X<L/2;
C”>0, L/2<=X<=L。
The variation of the distance between for example adjacent constant-current stabilizer of specific reason is identical.
Preferably, the distance between adjacent constant-current stabilizer remains unchanged.
Preferably, the length in addition to constant-current stabilizer is outside one's consideration, constant-current stabilizer others parameter (such as adjacent spacing, caliber
Deng) remain unchanged.
Preferably, along the flow direction of fluid in heat exchanger tube 6, the multiple constant-current stabilizers of setting in heat exchanger tube 6, from heat exchange
The entrance of pipe 6 is increasing after fin distribution density in different constant-current stabilizers 5 is smaller and smaller before this to the outlet of heat exchanger tube 6.
Preferably, the fin distribution density in different constant-current stabilizers 5 is smaller and smaller from the entrance of heat exchanger tube 6 to the middle part of heat exchanger tube；
From the outlet of the central island heat exchanger tube 6 of heat exchanger tube, the fin distribution density in different constant-current stabilizers 5 is increasing.I.e. current stabilization fills
The fin distribution density set is D, D=F3(X), D ' is the first order derivative of D, meets following require:
D’<0, 0<=X<L/2;
D’>0, L/2<=X<=L;
Preferably, the fin distribution density from the entrance of heat exchanger tube 6 to the middle part of heat exchanger tube, in different constant-current stabilizers 5
Smaller and smaller amplitude constantly increases；Fin from the outlet of the central island heat exchanger tube 6 of heat exchanger tube, in different constant-current stabilizers 5
Distribution density amplitude increasing before this is continuously increased.I.e.
D " is the second derivative of D, meets following require:
D”>0,0<=X<L/2;
D”>0, L/2<=X<=L。
The variation of the distance between for example adjacent constant-current stabilizer of specific reason is identical.
Preferably, the length of constant-current stabilizer and the distance of adjacent constant-current stabilizer remain unchanged.
Preferably, other than the fin distribution density of constant-current stabilizer, constant-current stabilizer others parameter (such as length, phase
The distance between adjacent constant-current stabilizer etc.) it remains unchanged.
The distance between adjacent constant-current stabilizer is S, and the internal diameter of heat exchange tube is W, and wherein the interval S of constant-current stabilizer is adjacent
Adjacent the distance between the radial bars central axis of constant-current stabilizer.
34mm<W<58mm；
50mm<S<80mm。
Preferably, heat exchanger tube length L is between 3000-5500mm.Further preferably, between 3500-4500mm.
Further preferably, 40mm < W < 50mm；
55mm<S<60mm。
Preferably, S is greater than 1.4 times of the height of fin.
For parameters such as other parameters, such as tube wall, shell wall thickness according to normal standard setting.
Preferably, fluid is water in shell side.
Preferably, tube side inner fluid speed 3-5m/S.
Preferably, the length L of heat exchanger tube and the diameter of the housing ratio of heat exchanger are 6-10.
Although the present invention has been disclosed in the preferred embodiments as above, present invention is not limited to this.Any art technology
Personnel can make various changes or modifications, therefore protection scope of the present invention is answered without departing from the spirit and scope of the present invention
When being defined by the scope defined by the claims..
Claims (3)
1. a kind of gas-liquid two-phase flow tube shell type heat exchanger, including shell, the shell both ends are respectively set end socket, the end socket and
Tube sheet is arranged in the link position of shell, and heat exchanger tube connects the tube sheet at both ends, and the gas phase in biphase gas and liquid flow is insoluble or indissoluble
Property gas, i.e., in heat transfer process, gas will not be dissolved in liquid, which is characterized in that biphase gas and liquid flow flows in tube side, described to change
Constant-current stabilizer is set in heat pipe, the constant-current stabilizer includes core and shell, the core setting in the shell, the shell with
Heat transfer tube wall is connected and fixed, and the core includes from core-center to the more radial bars radially extended, in the radial bars
The fin that more directions from from radial bars to fluid flow pair extend is set, the fin has a tip, the tip towards
The direction of fluid flow pair extends；The core includes the stem that the heart in the core is arranged, and described radial bars one end is fixed on
In stem；The fin is triangular fin, and a bottom edge of triangle is located in radial bars, the top at angle corresponding with the bottom edge
75-135 ° of angle of line and the radial bars formation at point and the midpoint on the bottom edge；
Multiple fins are set in same radial bars, from the stem of heat exchanger tube to radially extending on direction, between the fin
Spacing constantly reduces；The amplitude that spacing between the fin constantly reduces constantly increases.
2. shell-and-tube heat exchanger as described in claim 1, which is characterized in that groove is arranged in the heat transfer tube wall, described steady
The shell for flowing device is arranged in groove, the inner wall of the shell and the aligning inner of heat exchanger tube.
3. shell-and-tube heat exchanger as described in claim 1, which is characterized in that heat exchanger tube is welded for multi-segment structure, multistage
Constant-current stabilizer is arranged in the junction of structure.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910082546.9A CN109654918B (en) | 2017-08-02 | 2017-08-02 | Gas-liquid two-phase flow heat exchange tube |
| CN201710651947.2A CN108332578B (en) | 2017-08-02 | 2017-08-02 | A kind of gas-liquid two-phase flow tube shell type heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710651947.2A CN108332578B (en) | 2017-08-02 | 2017-08-02 | A kind of gas-liquid two-phase flow tube shell type heat exchanger |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910082546.9A Division CN109654918B (en) | 2017-08-02 | 2017-08-02 | Gas-liquid two-phase flow heat exchange tube |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108332578A CN108332578A (en) | 2018-07-27 |
| CN108332578B true CN108332578B (en) | 2019-04-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910082546.9A Active CN109654918B (en) | 2017-08-02 | 2017-08-02 | Gas-liquid two-phase flow heat exchange tube |
| CN201710651947.2A Active CN108332578B (en) | 2017-08-02 | 2017-08-02 | A kind of gas-liquid two-phase flow tube shell type heat exchanger |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910082546.9A Active CN109654918B (en) | 2017-08-02 | 2017-08-02 | Gas-liquid two-phase flow heat exchange tube |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1003013A (en) * | 1962-05-28 | 1965-09-02 | Patterson Kelley Co | Heat exchange device |
| CN2854484Y (en) * | 2005-12-15 | 2007-01-03 | 苏州新太铜高效管有限公司 | Heat-exchange pipe for evaporimeter |
| CN106767007A (en) * | 2016-11-25 | 2017-05-31 | 中国核动力研究设计院 | The heat exchanger of pointed structures is set outside a kind of pipe |
| CN106969652A (en) * | 2017-05-09 | 2017-07-21 | 山东大学 | A kind of condensable annular and separation device heat exchanger of length change |
-
2017
- 2017-08-02 CN CN201910082546.9A patent/CN109654918B/en active Active
- 2017-08-02 CN CN201710651947.2A patent/CN108332578B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1003013A (en) * | 1962-05-28 | 1965-09-02 | Patterson Kelley Co | Heat exchange device |
| CN2854484Y (en) * | 2005-12-15 | 2007-01-03 | 苏州新太铜高效管有限公司 | Heat-exchange pipe for evaporimeter |
| CN106767007A (en) * | 2016-11-25 | 2017-05-31 | 中国核动力研究设计院 | The heat exchanger of pointed structures is set outside a kind of pipe |
| CN106969652A (en) * | 2017-05-09 | 2017-07-21 | 山东大学 | A kind of condensable annular and separation device heat exchanger of length change |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108332578A (en) | 2018-07-27 |
| CN109654918A (en) | 2019-04-19 |
| CN109654918B (en) | 2021-02-19 |
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