CN108759508A - A kind of heat exchanger and its design method based on centrifugation - Google Patents
A kind of heat exchanger and its design method based on centrifugation Download PDFInfo
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- CN108759508A CN108759508A CN201810632196.4A CN201810632196A CN108759508A CN 108759508 A CN108759508 A CN 108759508A CN 201810632196 A CN201810632196 A CN 201810632196A CN 108759508 A CN108759508 A CN 108759508A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention discloses a kind of heat exchanger and its design method based on centrifugation, is related to Machine Design manufacturing technology field.The method includes the steps：Step 1：Two or more fluids to be exchanged heat are entered by respective flow channel respectively carries out mixed heat transfer in mixing chamber, obtain fluid-mixing；Step 2：The fluid-mixing enters centrifugal chamber by mixing chamber, is separated fluid-mixing using centrifugal separation method, the target fluid after being exchanged heat；Step 3：The target fluid is flowed out by respective flow pass respectively.Design of heat exchanger method provided by the present invention, it is proposed the direct mixed heat transfer in mixing chamber, heat transfer effect is efficient, the design of heat exchanger proposed is simple in structure small, due to being based on centrifugal separation technology, eliminates the metal partion (metp) of inner passage setting, therefore weight decreases, it is not easy to plug inside heat exchanger, while convenient for the cleaning of heat exchanging device, greatly facilitating the heat exchange between fluid.
Description
Technical field
The present invention relates to Machine Design manufacture and technical field of heat exchangers, more particularly to a kind of changing based on centrifugation
Hot device and its design method.
Background technology
The application of heat exchanger in the industry is extremely wide, to realize that the fields such as power, chemical industry, ship, refrigeration and machinery are set
Standby low energy consumption and Effec-tive Function be unable to do without the design of advanced heat exchanger.And widely applied gas turbine, diesel oil in the industry
Machine, transmission system etc. transmit the occasion that energy height is concentrated, since high temperature caused by high rotating speed, high power makes mechanical part
Working environment is severe, thus generally requires reliable lubricating oil and cooling system and support, at this time lubricating oil can undertake simultaneously lubrication and
Cooling task.And lubricating oil maximum operation (service) temperature is usually no more than 200 DEG C at present, it is therefore necessary to be carried out to lubricating oil effective cold
But.The oil cooler in current each field mainly uses water as cold medium.In modern large ship, due to the specific heat capacity of water
High, heat absorption capacity generally cools down cunning in marine gas turbine by force and convenient for being obtained from desalination plant using water
Oil.
The type of common oil heat exchanger mainly has plate-fin and shell-and-tube.But both heat exchangers are to have reached
Heat transfer effect, inner passage narrow structures are complicated, this so that it is designed and processing difficulties, cost are higher；On the other hand, both
Either solid material ratio high (plate heat exchanger close to 0.5) or volume are larger for structure so that the weight of these heat exchangers,
Space hold is larger.From the point of view of the design present situation of entire heat exchanger industry, the method for improving heat transfer effect for a long time all surrounds
Increase heat exchange area, improve heat transfer temperature difference and these three modes of enhancing heat transfer to carry out, and increases heat exchange area and usually lead
Excessive equipment or runner smaller are caused, is more difficult to process, is more easy to block, increases heat transfer temperature difference and is not easily accomplished and whole system can be reduced
It is available can, the means of enhancing heat transfer generally can along with resistance raising thus consume more pump work.
Therefore it provides it is a kind of it is simple in structure, compact, processing cost is low, light-weight and heat transfer efficient new type heat exchanger
Design method has great importance and practical prospect.
Invention content
Solved by the invention is that existing heat exchanger complexity is high, and heat exchange design is complicated, and heat exchange power has been approached reason
Think maximum heat exchange power, it is difficult to continue to lift up, easily be blocked inside heat exchanger, it is difficult to process, the larger problem of weight and volume.
In order to solve the above technical problems, the present invention provides a kind of heat exchanger and its design method based on centrifugation, institute
The design of heat exchanger method based on centrifugation stated includes step：
Step 1：Two or more fluids to be exchanged heat respectively by respective flow channel enter in mixing chamber into
Row mixed heat transfer, obtains fluid-mixing；Described two mutual temperature of above fluid are different, density is different and immiscible；
Step 2：The fluid-mixing enters centrifugal chamber by mixing chamber, will be mixed using centrifugal separation method in centrifugal chamber
Collaborate body separation, obtains two or more target fluids；
Step 3：The two or more target fluids obtained after the separation pass through respective flow pass stream respectively
Go out.
The present invention also provides a kind of heat exchanger based on centrifugation, the heat exchanger includes：More than two flow into is led to
Road, flow pass identical with flow channel quantity, mixing chamber, centrifugal chamber and centrifugal device.
Described two above flow channels are connected to mixing chamber, and the flow pass is connected to centrifugal chamber, the inflow
It is non-interference between channel and flow pass, two or more fluids to be exchanged heat respectively by respective flow channel into
Enter and carry out mixed heat transfer in mixing chamber, obtain fluid-mixing, described two mutual temperature of above fluid are different, density not
It is same and immiscible；Centrifugal device is located at centrifugal chamber inside center, for will flow into the fluid-mixing of centrifugal chamber by mixing chamber
It centrifuges, after separating the fluid-mixing after mixed heat transfer by centrifugal method, obtains two or more target fluids, it is described
Two or more target fluids is flowed out by respective flow pass respectively again.
The advantage of the invention is that：
Design of heat exchanger method provided by the present invention proposes the direct mixed heat transfer in mixing chamber, and heat exchange efficiency is efficient,
The design of heat exchanger proposed is simple in structure small, due to being based on centrifugal separation technology, eliminates the gold of inner passage setting
Belong to partition board, therefore weight decreases, and is not easy to plug inside heat exchanger, while convenient for the cleaning of heat exchanging device, greatly facilitating reality
Heat exchange between existing fluid.
Description of the drawings
Fig. 1 is a kind of design of heat exchanger method flow diagram based on centrifugation of the present invention；
Fig. 2 is the first heat exchanger structure schematic diagram based on centrifugation of the embodiment of the present invention；
Fig. 3 is to centrifuge force analysis schematic diagram；
Fig. 4 is second of heat exchanger structure schematic diagram based on centrifugation of the embodiment of the present invention；
In figure：
1：First flow channel；2：Second flow channel；3：First flow pass；4：Second flow pass；
5：First mixing chamber；6：First centrifugal chamber；7：Centrifugal device A；8：Third flow channel；
9：4th flow channel；10：5th flow channel；11：Second mixing chamber；12：Second centrifugal chamber；
13：Centrifugal device B；14：Third flow pass；15：4th flow pass；16：5th flow pass.
Specific implementation mode
The present invention is described in detail with reference to the accompanying drawings and examples.
The present invention provides a kind of heat exchanger and its design method based on centrifugation, as shown in Figure 1, for the present invention one
Design of heat exchanger method flow diagram of the kind based on centrifugation, the design of heat exchanger method based on centrifugation specifically include
Step：
Step 1：Two or more fluids to be exchanged heat respectively by respective flow channel enter in mixing chamber into
Row mixed heat transfer, obtains fluid-mixing；Described two mutual temperature of above fluid are different, density is different and immiscible；
Described waits for that heat exchanging fluid sprays into the form of spraying in mixing chamber, and realization is sufficiently mixed heat exchange.
Step 2：The fluid-mixing enters centrifugal chamber by mixing chamber, is detached fluid-mixing using centrifugal separation method,
Obtain two or more target fluids；
Fluid-mixing is layered reverse flow under the comprehensive function of centrifugal force, frictional force and buoyancy in centrifugal chamber, mixes
Collaborate the big fluid position that radius is big into the centrifugal chamber flowing of density in body, the small fluid of density radius into centrifugal chamber is small
Position is flowed, and finally separates fluid-mixing.
The centrifugal separation method refers to by centrifugal force so that the centrifugation suffered by the fluid of different specific weight (density)
Power is different, therefore can be collected at different centrifugation radiuses, achievees the purpose that separation.
Rotation center position (the driving axle position of centrifuge blade in centrifugal separation method described in the outlet face of the mixing chamber
Set), ensure that different fluids is detached under the action of the centrifugal force.
Step 3：The two or more target fluids obtained after the separation pass through respective flow pass stream respectively
Go out.
The present invention also provides a kind of heat exchangers based on centrifugation, including：More than two flow channels and inflow
The identical flow pass of number of channels, mixing chamber, centrifugal chamber and centrifugal device.
Described two above flow channels are connected to mixing chamber, and the flow pass is connected to centrifugal chamber, the inflow
Non-interference between channel and flow pass, two or more fluids enter mixing chamber by respective flow channel respectively
Middle carry out mixed heat transfer, obtains fluid-mixing.Described two mutual temperature of above fluid are not different, density is different and mutually not
It mixes；Centrifugal device is located at centrifugal chamber inside center, for centrifuging fluid-mixing, is changed mixing by centrifugal method
After fluid-mixing after heat separates, two or more target fluids is obtained, described two above target fluids pass through respectively again
Respective flow pass outflow.
As shown in Fig. 2, for the first the heat exchanger structure schematic diagram of the embodiment of the present invention based on centrifugation design method；
Fluid A is entered by the first flow channel 1 in the first mixing chamber 5, and fluid B enters the by the second flow channel 2
In one mixing chamber 5, fluid A and fluid B are subjected to mixed heat transfer, obtain fluid-mixing.The temperature of the fluid A and fluid B is not
Together, density is different and immiscible；If the temperature of fluid A is T1(unit K), density ρ1(unit kg/m3), flow m1
(unit kg/s), specific heat capacity c1(unit is J/ (kgK), correspondingly, temperature, density, flow and the specific heat capacity of fluid B
Respectively T2、ρ2、m2And c2.After fluid A and fluid B carries out being sufficiently mixed heat exchange in the first mixing chamber 5, ideally, recognize
It is adiabatic for entire first mixing chamber 5, known by the conservation of energy：
m1c1T1+m2c2T2=(m1c1+m2c2)T0
Therefore after being sufficiently mixed heat exchange, the temperature of fluid-mixing is：
T0=(m1c1T1+m2c2T2)/(m1c1+m2c2)
By mass-conservation equation after mixing it is found that the flow of fluid-mixing is：
m0=m1+m2
Derived by the above basic principle it is found that this heat exchanger heat exchange it is extremely strong, can reach most in short time, small space
Good heat transfer effect.And in the target temperature T of given fluid-mixing0When, there are best inlet flow rate ratios：Its key parameter is fluid flow, fluid A flows m1Ranging from 0.1~2kg/s, fluid B fluid flows m2
Range is determined according to best inlet flow rate relationship：Fluid A temperature T1Ranging from 350~450K；Mixing
The temperature T of fluid0Ranging from 310~400K；Heat exchanger volume range is from 0.1~0.4m3。
Fluid-mixing enters the first centrifugal chamber 6 will be mixed after mixed heat transfer using centrifugal separation method by centrifugal device A7
Collaborate body to separate, obtains target fluid A and target fluid B；Centrifugal device A7 is as shown in Figure 2, the drive shaft of centrifugal device A7
External power plant is connected, centrifugation force effect Fluid field motion analysis calculates as follows：
It is illustrated in figure 3 and centrifuges force analysis schematic diagram, a certain liquid pearl is analyzed, two solid black point tables in figure
Show same liquid pearl, for the force analysis under different stressing conditions, the centrifugal force suffered by liquid pearl is：
Fc=m ω2r
Wherein, FcFor the centrifugal force (unit N) suffered by liquid pearl, m is the quality (unit Kg) of liquid pearl, and ω is that centrifugation fills
The angular velocity of rotation (unit rad/s) of A7 is set, r is the distance between liquid pearl and the drive shaft of centrifugal device A7 radius (unit
For m).
The downward component of the centrifugal force is：
F′c=Fc·sinα
Suffered normal pressure N (unit N) is the liquid pearl under the action of the centrifugal force：
N=Fc·cosα
Wherein α refers to the angle between the centrifuge blade and drive shaft of centrifugal device A7, generally takes 30 °~50 °, it is described from
Lobus cardiacus piece level is on the lower side.
Buoyancy F suffered by the liquid pearlf(unit N) is：
Ff=ρ gV
Wherein, ρ is density (the unit Kg/m of liquid pearl3), V is volume (the unit m of liquid pearl3), g is acceleration of gravity.
The upward component of the buoyancy is
F′f=Ff·cosα
Liquid pearl normal pressure N ' (unit N) suffered under buoyancy is
N '=Ff·sinα
The then frictional force suffered by liquid pearl：
Fm=f (N+N ')
Wherein, f refers to the frictional force between liquid pearl and the centrifuge blade.
By the relationship between power and movement it is found that the movement of final liquid pearl is by the downward component F ' of centrifugal forcecAnd friction
Power FmThe separation F ' upward with buoyancyfThe sum of determine.For heavy-fluid pearl, centrifugal force component is more than the sum of frictional force and buoyancy component,
That is F 'c> Fm+F′f, liquid pearl moves to the first big centrifugal chamber position of radius；For light liquid pearl, centrifugal force component is less than frictional force
The sum of with buoyancy component, i.e. F 'c< Fm+F′f, liquid pearl floats to be moved to the first small centrifugal chamber position of radius.It can be seen that density
Different weight liquid will be layered reverse flow in the first centrifugal chamber, be based on this, two kinds of fluids will positioned at the first centrifugal chamber not
It is flowed out at the flow pass of radius, it is assumed that target fluid A density is more than target fluid B, and the big target fluid A of density is from radius
Big the second flow pass 4 outflow, the small target fluid B of density is from small the first flow pass 3 outflow of radius, finally by its point
It leaves.
Fluid A, B are passed through in the first mixing chamber 5, wherein assuming that fluid A is main heat exchanging fluid.Be passed through fluid A with
The mode that atomization sprays into may be used when fluid B, increase contact surface and it is forced to be uniformly mixed, or add in 5 body of the first mixing chamber
Enter a blender or temperature-uniforming plate to realize quickly blending and heat exchange, to keep the temperature of fluid-mixing almost the same.
Target fluid A and target fluid B is flowed out by the second flow pass 4 and the first flow pass 3 respectively, to avoid mesh
Mark fluid A and target fluid B is wasted, and design of heat exchanger method of the invention, which can be arranged, makes target fluid A or target fluid B follow
The device that ring utilizes.Such as after previous step centrifuges, more pure and that density the is big fluid of the small fluid of usual density can contain
The fluid for having a small amount of density small, therefore can the small fluid discharge of density be subjected to subsequent work flow or collection, and when needs avoid
When the small fluid wastage of density, the big fluid of density should then be recycled, therefore density can be kept small with design cycle device
Fluid circulation utilize.It should be noted that the big fluid flow of density cannot directly be counted according to the big fluid of import density at this time
It calculates, and needs to consider the accounting of the small fluid of density wherein.Therefore the big fluid flow needs of density are rationally controlled.
Using the heat exchanger of the design of heat exchanger method provided by the present invention based on centrifugation, not using tradition enhancing
The mode of heat exchange proposes that the direct mixed heat transfer of heat exchanger, heat transfer efficient, power improve 19.1%~138.1%, structure letter
Single, compact, processing is simple, small, due to being based on centrifugal separation technology, eliminates the metal partion (metp) of inner passage setting, interior
Portion is simple in structure, easy processing, facilitates the heat exchange realized between fluid.
The heat exchanger of design method design of the present invention applies also for a variety of density not in addition to the heat exchange between two fluids of realization
Heat exchange with, temperature between different and immiscible fluid, as shown in figure 4, being the embodiment of the present invention based on centrifugation
Second of heat exchanger structure schematic diagram of design of heat exchanger method design, three kinds of fluids pass through third flow channel the 8, the 4th respectively
Flow channel 9 and the 5th flow channel 10 enter the second mixing chamber 11, after being adequately mixed heat exchange, enter back into the second centrifugal chamber 12
It is centrifuged afterwards by centrifugal device B13, under the action of centrifugation, the fluid of different densities is detached under the effect of centrifugation
To the place of 12 different radii of the second centrifugal chamber, then flowed respectively from third flow pass 14, the 4th flow pass 15 and the 5th
Go out the outflow of channel 16, thus completes the heat exchange between three kinds of fluids.
Through this embodiment it can be seen that based on the heat exchanger that design method of the present invention is provided, can easily realize
On the basis of exchanging heat between two kinds of different fluids, the heat exchange between multiple fluid is realized.
Lubricating oil and water are changed using the first heat exchanger of the design of heat exchanger method the present invention is based on centrifugation
Heat operation；
(1), known fluid A, that is, oil flow is m1=0.1kg/s, temperature T1=350K, density, specific heat capacity are false
It is set as constant value：ρ1=800kg/m3, c1=1.87 × 103J/(kg·k).Fluid-mixing temperature is T0=310K, takes heat exchanger
Volume is 0.1m3.If its assist medium fluid B is water, temperature T2=293K, and assume that its density, specific heat capacity are：ρ2=
1000kg/m3, c2=4.20 × 103J/ (kgk), rotating speed are 7000~14000rpm.
The flow m that best water flows into can be obtained as previously described2=0.1kg/s.
The heat exchanger can be quickly obtained under specific operation by simultaneous energy conservation equation and mass-conservation equation
Heat transfer effect, equivalent heat exchange power are
P=7.48kW
(2), known fluid A, that is, oil flow is m1=2kg/s, temperature T1=450K, density, specific heat capacity are assumed
For constant value：ρ1=800kg/m3, c1=1.87 × 103J/(kg·k).Fluid-mixing temperature is T0=400K takes the body of heat exchanger
Product is 0.2m3.If its assist medium fluid B is water, temperature T2=293K, and assume that its density, specific heat capacity are：ρ2=
1000kg/m3, c2=4.20 × 103J/ (kgk), rotating speed are 7000~14000rpm.
The flow m that best water flows into can be obtained as previously described2=0.416kg/s.
The heat exchanger can be quickly obtained under specific operation by simultaneous energy conservation equation and mass-conservation equation
Heat transfer effect, equivalent heat exchange power are
P=187kW
The volume coefficient of heat transfer of existing typical shell-and-tube heat exchanger is 5kW/ (m3K), it is assumed that the heat exchanger with it is aforementioned
The volume of heat exchanger is identical with the temperature of the fluid-mixing after mixed heat transfer, and the heat exchange power for being not difficult to obtain the heat exchanger is：P
'=157kW, it can be seen that the heat exchanger heat exchange efficiency designed by the method in the power of existing shell-and-tube heat exchanger first than carrying
It is high by 19.1% or so.This assumes that heat transfer process is always maintained at the entrance temperature difference, but practical shell-and-tube heat exchanger was exchanging heat
The temperature difference of two fluids constantly reduces in journey, and no entrance that exchanges heat is strong, and therefore, the heat exchange power actually improved will higher.
(3), known A fluids, that is, oil flow is m1=2kg/s, temperature T1=450K, density, specific heat capacity are assumed
For constant value：ρ1=800kg/m3, c1=1.87 × 103J/(kg·K).Outlet temperature is T0=350K, takes the volume of heat exchanger to be
0.4m3.If its assist medium fluid B is water, temperature T2=293K, and assume that its density, specific heat capacity are：ρ2=1000kg/
m3, c2=4.20 × 103J/ (kgk), rotating speed are 7000~14000rpm.
The heat exchanger can be quickly obtained under specific operation by simultaneous energy conservation equation and mass-conservation equation
Heat transfer effect, equivalent heat exchange power are
P=374kW
The volume coefficient of heat transfer of typical shell-and-tube heat exchanger is 5kW/ (m3K), it is assumed that the heat exchanger and aforementioned heat exchange
The volume of device is identical with the temperature of the fluid-mixing after mixed heat transfer, and the heat exchange power for being not difficult to obtain the heat exchanger is：P '=
314kW, it can be seen that the heat exchanger heat exchange efficiency designed by the method is first improved than the power in shell-and-tube heat exchanger
19.1% or so.
(4), known fluid A, that is, oil flow is m1=1kg/s, temperature T1=450K, density, specific heat capacity are assumed
For constant value：ρ1=800kg/m3, c1=1.87 × 103J/(kg·K).Outlet temperature is T0=310K, takes the volume of heat exchanger to be
0.2m3.If its assist medium fluid B is water, temperature T2=293K, and assume that its density, specific heat capacity are：ρ2=1000kg/
m3, c2=4.20 × 103J/ (kgk), rotating speed are 7000~14000rpm.
The heat exchanger can be quickly obtained under specific operation by simultaneous energy conservation equation and mass-conservation equation
Heat transfer effect, equivalent heat exchange power are
P=261.8kW
The volume coefficient of heat transfer of typical shell-and-tube heat exchanger is 5kW/ (m3K), it is assumed that the heat exchanger and aforementioned heat exchange
The volume of device is identical with the temperature of the fluid-mixing after mixed heat transfer, and the heat exchange power for being not difficult to obtain the heat exchanger is：P '=
157kW, it can be seen that the heat exchanger heat exchange efficiency designed by the method is first improved than the power in shell-and-tube heat exchanger
38.1% or so.
(5), known hot fluid, that is, oil flow is m1=1kg/s, temperature T1=450K, density, specific heat capacity are assumed
For constant value：ρ1=800kg/m3, c1=1.87 × 103J/(kg·K).Outlet temperature is T0=350K, takes the volume of heat exchanger to be
0.1m3.If its assist medium is water, temperature T2=293k, and assume that its density, specific heat capacity are：ρ2=1000kg/m3, c2=
4.20×103J/ (kgK), rotating speed are 7000~14000rpm.
The heat exchanger can be quickly obtained under specific operation by simultaneous energy conservation equation and mass-conservation equation
Heat transfer effect, equivalent heat exchange power are
P=187kW
The volume coefficient of heat transfer of typical shell-and-tube heat exchanger is 5kW/ (m3K), it is assumed that the heat exchanger and aforementioned heat exchange
The volume of device is identical with the temperature of the fluid-mixing after mixed heat transfer, and the heat exchange power for being not difficult to obtain the heat exchanger is：P '=
78.5kW, it can be seen that the heat exchanger heat exchange efficiency designed by the method is first improved than the power in shell-and-tube heat exchanger
138.1% or so.It can be seen that under the conditions of low outlet temperature, big flow, small size, heat exchanger of the invention is compared to shell
Formula heat transfer effect will be obviously improved.
In conclusion using design of heat exchanger method provided by the present invention, not by the way of tradition enhancing heat exchange, carry
Go out direct mixed heat transfer, heat transfer efficient in heat exchanger；Simultaneously because being based on centrifugal separation technology, the logical of internal setting is eliminated
The metal partion (metp) in road, internal structure is simple, small, easy processing, therefore weight slightly reduces；And there is no slype, because
It is not easy to plug inside this heat exchanger, is convenient for the cleaning of heat exchanging device；The heat exchange realized between multiple fluid can also be facilitated simultaneously.
Claims (5)
1. a kind of design of heat exchanger method based on centrifugation, including step：
Step 1：Two or more fluids to be exchanged heat are entered by respective flow channel in mixing chamber respectively to be mixed
Heat exchange is closed, fluid-mixing is obtained；Described two mutual temperature of above fluid are different, density is different and immiscible；
Step 2：The fluid-mixing enters centrifugal chamber by mixing chamber, uses centrifugal separation method by mixed flow in centrifugal chamber
Body detaches, and obtains two or more target fluids；
Step 3：The two or more target fluids obtained after the separation are flowed out by respective flow pass respectively.
2. a kind of design of heat exchanger method based on centrifugation according to claim 1, it is characterised in that：It is described two
Above fluid enters mixing chamber in a manner of being atomized penetrating and realizes mixed heat transfer.
3. a kind of design of heat exchanger method based on centrifugation according to claim 1, it is characterised in that：The stream
Body is fluid A and fluid B, if the temperature T of fluid A1, flow m1, specific heat capacity c1, the temperature T of fluid B2, flow m2And specific heat
Hold c2；In the temperature T of given fluid-mixing0When, there are inlet flow rate ratios：
4. a kind of design of heat exchanger method based on centrifugation according to claim 1, which is characterized in that fluid-mixing
Can in the comprehensive function lower leaf reverse flow of centrifugal force, frictional force and buoyancy, in fluid-mixing the big fluid of density to from
The position flowing that radius is big in the chambers of the heart, the small position flowing of the small fluid of density radius into centrifugal chamber, finally by fluid-mixing
It separates.
5. a kind of heat exchanger based on centrifugation, it is characterised in that：The heat exchanger include more than two flow channels, with
The identical flow pass of flow channel quantity, mixing chamber, centrifugal chamber and centrifugal device, described two above flow channels with it is mixed
Chamber connection is closed, the flow pass is connected to centrifugal chamber, and centrifugal device is located at centrifugal chamber inside center, and being used for will be by mixing chamber
The fluid-mixing for flowing into centrifugal chamber centrifuges, and after separating the fluid-mixing after mixed heat transfer by centrifugal method, obtains two
Kind or more target fluid, described two above target fluids are flowed out by respective flow pass respectively again.
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| CN201810632196.4A CN108759508A (en) | 2018-06-19 | 2018-06-19 | A kind of heat exchanger and its design method based on centrifugation |
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| CN201810632196.4A CN108759508A (en) | 2018-06-19 | 2018-06-19 | A kind of heat exchanger and its design method based on centrifugation |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4371382A (en) * | 1980-08-06 | 1983-02-01 | Caribbean Properties Limited | Process and apparatus for the contact and separation of immiscible fluids |
| US5363909A (en) * | 1991-11-27 | 1994-11-15 | Praxair Technology, Inc. | Compact contacting device |
| CN1265602A (en) * | 1997-06-27 | 2000-09-06 | 莫普罗产品有限公司 | Apparatus and method for separating mixture of less dense liquid and more dense liquid |
| CN102341180A (en) * | 2009-03-06 | 2012-02-01 | 阿尔法拉瓦尔股份有限公司 | Centrifugal separator |
| CN206138787U (en) * | 2016-08-10 | 2017-05-03 | 姚登程 | Chemical industry pharmacy experiment extraction device |
-
2018
- 2018-06-19 CN CN201810632196.4A patent/CN108759508A/en not_active Withdrawn
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4371382A (en) * | 1980-08-06 | 1983-02-01 | Caribbean Properties Limited | Process and apparatus for the contact and separation of immiscible fluids |
| US5363909A (en) * | 1991-11-27 | 1994-11-15 | Praxair Technology, Inc. | Compact contacting device |
| CN1265602A (en) * | 1997-06-27 | 2000-09-06 | 莫普罗产品有限公司 | Apparatus and method for separating mixture of less dense liquid and more dense liquid |
| CN102341180A (en) * | 2009-03-06 | 2012-02-01 | 阿尔法拉瓦尔股份有限公司 | Centrifugal separator |
| CN206138787U (en) * | 2016-08-10 | 2017-05-03 | 姚登程 | Chemical industry pharmacy experiment extraction device |
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Application publication date: 20181106 |
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