CN105716331A - Variable flow channel type heat exchanger capable of improving organic Rankine cycle efficiency - Google Patents
Variable flow channel type heat exchanger capable of improving organic Rankine cycle efficiency Download PDFInfo
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Abstract
The invention discloses a variable flow channel type heat exchanger capable of improving organic Rankine cycle efficiency. An organic Rankine cycle system comprises an evaporator, an expanding machine, a power generator, a condenser and a working medium pump which are connected through pipelines. In order to improve the efficiency of the system, the evaporator and the condenser in the system adopt the following variable flow channel modes: as for a tube-shell heat exchanger, the number of heat exchanger flow channels is changed by adding heat exchange tube branch tubes gradually; and as for a plate type heat exchanger, the number of heat exchanger flow channels is changed by elongating the flow path of working media in cavities between plates. By adopting the variable flow channel type heat exchanger, the problem that increasing flow resistance is caused by working medium phase changes of traditional heat exchangers is solved, and the flow pattern of the working media tends to be in a ring shape all the time, so that the heat exchange capability of the heat exchanger is enhanced, and then the thermal collection efficiency and condensing efficiency of the organic Rankine cycle system are improved. The variable flow channel type heat exchanger is suitable for phase change heat transfer on cold and heat source sides of the organic Rankine cycle system.
Description
Technical field
The present invention relates to a kind of heat exchanger, the cycle fluid change in flow in organic Rankine bottoming cycle including vaporizer and condenser, particularly relate to a kind of variable flow channel type heat exchanger optimizing Rankine cycle efficiency.
Background technology
In organic Rankine bottoming cycle dynamical system, vaporizer (1), decompressor (2), condenser (4), working medium pump (5), vaporizer (1) are sequentially carried out connection.Electromotor (3) is connected with decompressor (2) by bearing.
Wherein, vaporizer (1) and condenser (4) belong to heat exchanger, and organic Rankine bottoming cycle efficiency is played material impact by its heat exchange efficiency.
In organic Rankine bottoming cycle dynamical system, cycle fluid absorbs heat in vaporizer makes liquid refrigerant be evaporated to gas completely, then promotes decompressor to do work.Gas after acting releases heat in condenser makes gaseous working medium liquefy completely as liquid.
When cycle fluid be a kind of mixed working fluid be applied in organic Rankine bottoming cycle dynamical system time, mixed working fluid can produce strong phase transformation in heat exchanger.Mixed working fluid is become from liquid in the process of gaseous state, gaseous state becoming in the process of liquid, and its volume flow can differ 2 to 3 orders of magnitude.
So extreme adds the cycle fluid of gaseous state flow velocity in vaporizer, reduces cycle fluid heat absorption capacity in heat exchanger, and the degree of superheat of heat exchanger exit gaseous working medium reduces.On the contrary, extremely reduce the cycle fluid of liquid flow velocity within the condenser, reduce cycle fluid emission capacity within the condenser.
A kind of higher cycle efficieny can be applied to the heat exchanger in organic Rankine bottoming cycle dynamical system it is thus desirable to develop, make heat exchanger avoid because the change in flow of cycle fluid causes that heat exchange efficiency reduces.
Summary of the invention
The technical problem to be solved in the present invention is: how to improve the degree of superheat of evaporator outlet working medium in organic rankine cycle system by the method for change heat exchanger runner, improves the heat exchange efficiency of condenser and vaporizer.And then improve the power output efficiency of organic rankine cycle system.
The present invention solves that above-mentioned technical problem adopts below scheme:
A kind of variable flow channel type heat exchanger, including: the heat exchange runner that the circulatory flow that at least one first working medium flows through and at least one second working medium flow through, heat exchange along with the first working medium Yu the second working medium, first working medium gradually changes between liquid and gaseous state, and first working medium flow velocity in circulatory flow gradually changes simultaneously；Wherein, described circulatory flow includes at least one-level branch flow passage and sprue, and every one-level branch flow passage is made up of the identical branch flow passage of more than two, is connected with in upper level branch flow passage or upper level sprue；Wherein, in the flow passage entry of each branch flow passage or sprue, the flow velocity of the first working medium is within default flow velocity limits；At the runner exit place of each branch flow passage or sprue, the flow velocity of the first working medium is outside default flow velocity limits.
According to another aspect of the present invention, a kind of variable flow channel type heat exchanger is provided, including: the heat exchange runner that the circulatory flow that at least one first working medium flows through and at least one second working medium flow through, heat exchange along with the first working medium Yu the second working medium, first working medium gradually changes between liquid and gaseous state, and first working medium flow velocity in circulatory flow gradually changes simultaneously；Wherein, described circulatory flow includes at least one-level branch flow passage and sprue, and every one-level branch flow passage is made up of the identical branch flow passage of more than two, is connected with in upper level branch flow passage or upper level sprue；Wherein, in the flow passage entry of each branch flow passage or sprue, the flow velocity of the first working medium is within default flow velocity limits；At the runner exit place of each branch flow passage or sprue, the flow velocity of the first working medium is outside default flow velocity limits.Wherein, the first working medium is the cycle fluid in organic rankine cycle system, and it can be mixed working fluid, but is not limited to mixed working fluid.First working medium is one or more mixing in R245fa, R136fa, R600, R601, R601a.
According to a further aspect of the invention, a kind of variable flow channel type vaporizer is provided, wherein: the first working medium is flowed into by sprue in circulatory flow, thereafter branch flow passage at different levels is flowed through according to by little level time to big level time, flowed out by afterbody branch flow passage, along with the heat exchange of the first working medium Yu the second working medium, the first working medium is gradually varied to gaseous state by liquid, and first working medium flow velocity in circulatory flow accelerates gradually simultaneously；In the flow passage entry of sprue or each branch flow passage, the flow velocity of the first working medium is less than default maximum flow rate value；At the runner exit place of sprue or each branch flow passage, the flow velocity of the first working medium is be more than or equal to default maximum flow rate value.Wherein, the second working medium can be conduction oil, but is not limited to conduction oil.
According to a further aspect of the invention, a kind of variable flow channel type condenser is provided, wherein: the first working medium is flowed into by afterbody branch flow passage in circulatory flow, thereafter branch flow passage at different levels is flowed through according to by big level time to little level time, flowed out by sprue, along with the heat exchange of the first working medium Yu the second working medium, the first working medium is gradually varied to liquid by gaseous state, and first working medium flow velocity in circulatory flow is slack-off gradually simultaneously；In the flow passage entry of each branch flow passage or sprue, the flow velocity of the first working medium is more than default lower flow rate limit value；At the runner exit place of each branch flow passage or sprue, the flow velocity of the first working medium is less than or equal to default lower flow rate limit value.Wherein, the second described working medium can be cooling water, but is not limited to cooling water.
According to a further aspect of the invention, it is provided that a kind of variable flow channel type shell-and-tube heat exchanger；Wherein, the circulatory flow that the first working medium flows through is the pipeline section runner of shell-and-tube heat exchanger, and the heat exchange runner that the second working medium flows through is the housing runner of shell-and-tube heat exchanger；The length of pipe section of described branch flow passage at different levels or sprue and caliber are determined according to the flow velocity of the first working medium in pipeline section.
According to a further aspect of the invention, it is provided that a kind of variable flow channel type shell-and-tube heat exchanger；Its shell is the housing of a taper, little side, conical shell cross section few with heat exchanger tube hop count amount in the same side, big side, conical shell cross section many with heat exchanger tube hop count amount in the same side, be provided with deflection plate in the space between conical shell and heat exchange pipeline section.
According to a further aspect of the invention, it is provided that a kind of variable flow channel type plate type heat exchanger；Wherein, between the heat exchange runner plate that between the circulatory flow plate that the first working medium flows through, cavity and the second working medium flow through, cavity is spaced；Between the plate of described branch flow passage at different levels, the quantity of cavity is determined according to the flow velocity of the first working medium in cavity.
The present invention is suitable in working medium phase-change heat transfer heat exchanger, for instance the diabatic process of vaporizer and condenser in organic Rankine bottoming cycle, but is not limited to organic Rankine bottoming cycle.
The present invention adopts above technical scheme, has the advantages that the heat exchange efficiency improving organic Rankine bottoming cycle vaporizer and condenser；The degree of superheat making evaporator outlet place working medium is higher.
Accompanying drawing explanation
Fig. 1 is the system schematic of the organic Rankine bottoming cycle of prior art；
Fig. 2 is the schematic diagram of the pipe heat exchanger structure of the present invention；
Fig. 3 is the schematic diagram in the pipe heat exchanger cross section of the present invention；
Fig. 4 be the present invention pipe heat exchanger in the schematic diagram of heat exchange tube structure；
Fig. 5 is the schematic diagram of the plate type heat exchanger structure of the present invention；
The plate that Fig. 6 is the present invention changes the structural representation of cavity runner between formula heat exchanger single plate.
Accompanying drawing labelling implication is:, 1 be vaporizer, 2 be decompressor, 3 be electromotor, 4 be condenser, 5 for working medium pump.
Detailed description of the invention
Below in conjunction with accompanying drawing, by detailed description of the invention, the invention will be further described.
Such as Fig. 1, vaporizer (1), decompressor (2), condenser (4), working medium pump (5), vaporizer (1) are sequentially carried out connection.Electromotor (3) is connected with decompressor (2) by bearing.Present invention is generally directed to improve vaporizer (1) and condenser (4) heat exchange efficiency in organic rankine cycle system, improve the degree of superheat of vaporizer (1) exit working medium.And then improve organic Rankine bottoming cycle efficiency.
Such as Fig. 2, a kind of shell-and-tube heat exchanger for organic Rankine bottoming cycle: first liquid the first working medium A enters a house steward, along with the heat exchange of the first working medium A with the outer second working medium B of pipe, the first working medium A evaporation, the first working medium A is become gaseous state from liquid gradually.In pipe, the first working medium A mean flow rate changes greatly place, separately two arms.Same the first working medium A change in flow larger part in two arms, respectively separates two arms ..., the like separate two arms again at each arm end separately.So on the flow direction of working medium, the quantity of pipeline is become 2 from 1, and 2 become 4 ... namely become 2 in the quantity of sender property outlet place pipelinenIndividual, n is the number of times that pipeline carries out branch.The length of arm and the selection of caliber are fluctuated within the specific limits according to the flow velocity of the first working medium A in pipeline section and are determined.Under this flow velocity, efficiency of heat exchanger is the highest.The housing of a taper on additionally overlapping outside heat exchanger tube.Little side, conical shell cross section few with heat exchange tube hop count amount in the same side, big side, conical shell cross section many with heat exchange tube hop count amount in the same side.Space between conical shell and heat exchanger tube arranges deflection plate.
Such as Fig. 2, the AB end at tapered cylinders ABCD opens a hole, and inserts heat exchange pipeline section ab.AB end and heat transfer manifold ab are tightly connected.The number of openings of the CD end of tapered cylinders ABCD is equal with the quantity of de end arm, and perforate size is identical with branch diameter, and arm and CD end are tightly connected.Connect the cylinder CDGH of one section of opening at CD end again, be used for the gas collected from arm out.Such as Fig. 2, in the perforate of E, F place, respectively as the export and import of the second working medium B, position of opening is also not necessarily limited to shown in Fig. 1, but in ensureing tapered cylinders ABCD, the second working medium B of circulation is adverse current with the first working medium A in heat exchanger tube.In Fig. 2, in ab, bc, cd, de section, the quantity of heat exchanger tube and size are determined according to the velocity variations of fluid in heat exchanger tube.To ensure in Fig. 2 in ab, bc, cd, de section that in heat exchanger tube, the change in flow of working medium is within claimed range in a word.As Fig. 2, tapered cylinders ABCD are segmented into ab, bc, cd, de section, but it is not limited to these 4 sections, it should carry out segmentation according to concrete operating mode, should not necessarily be limited by the one in Fig. 2.First working medium A is the cycle fluid in organic rankine cycle system, and it can be mixed working fluid, but is not limited to mixed working fluid.When vaporizer made by the shell-and-tube heat exchanger in organic rankine cycle system, the second working medium B can be conduction oil, but is not limited to conduction oil.When it is as condenser, the second working medium B can be cooling water, but is not limited to cooling water.
Such as Fig. 3, heat exchanger tube layout in tapered cylinders ABCD should symmetrical all with layout.And deflection plate is set in tapered cylinders ABCD.
The threeway that is connected by such as Fig. 4, a heat transfer manifold and two heat exchange arms connects, and the caliber of same heat exchanger tube is identical, and the caliber of various heat exchange pipe can be different according to different operating modes.The determination of heat exchange tube diameter and length, with the flow velocity of heat exchange intraductal working medium for foundation.Figure only depicts the heat exchanger of a kind of arm quantity, but it is a kind of to be not limited to this.
Such as Fig. 5, a kind of plate type heat exchanger for organic Rankine bottoming cycle: when liquid the first working medium A and the second working medium B carries out heat exchange, the first working medium A is become gaseous state from liquid gradually.In the meantime, first working medium A and the second working medium B passes crosswise the runner of plate type heat exchanger successively and carries out heat exchange, namely the working medium passed sequentially through in plate type heat exchanger runner is: the first working medium A, second working medium B, first working medium A, second working medium B......, when the flow velocity of the first working medium A exceed certain value make heat exchanger efficiency reduce time, start plate type heat exchanger is carried out bend flow channel process, namely the working medium passed sequentially through in plate type heat exchanger runner is: the second working medium B, first working medium A, first working medium A, second working medium B, first working medium A, first working medium A, first working medium A, second working medium B......, in above rule, the second working medium B is all the time by a plate change of current road.In the second working medium B two side runner, the plate change of current number of channels that the first working medium A passes through is incremented by successively.These are only a kind of mode of plate type heat exchanger bend flow channel.Its general principle is that several the fluctuation within the specific limits according to first working medium A flow velocity in runner of runner that the first working medium A continues through is determined under the second working medium B premise by a plate change of current road.Under this flow velocity, efficiency of heat exchanger is the highest.
Such as Fig. 5,12,23,34,45,56,67,78,89 is the runner of plate type heat exchanger.When liquid the first working medium A and the second working medium B carries out heat exchange, the first working medium A is become gaseous state from liquid gradually.In the meantime, first working medium A and the second working medium B passes crosswise the runner of plate type heat exchanger successively and carries out heat exchange, namely the first working medium A passes through 12 plate type heat exchanger runners, second working medium B passes through 23 plate type heat exchanger runners, when the flow velocity of the first working medium A exceed certain value make heat exchanger efficiency reduce time, start plate type heat exchanger is carried out bend flow channel process, namely the first working medium A continues through 34,45 plate type heat exchanger runners, second working medium B passes through 56 plate type heat exchanger runners, and the first working medium A continues through 67,78,89 plate type heat exchanger runners.These are only a kind of mode of plate type heat exchanger bend flow channel, but be not limited to this kind of form.The general principle of this bend flow channel is that several the fluctuation within the specific limits according to first working medium A flow velocity in runner of runner that the first working medium A continues through is determined under the second working medium B premise by a plate change of current road.Under this flow velocity, efficiency of heat exchanger is the highest.First working medium A is the cycle fluid in organic rankine cycle system, and it can be mixed working fluid, but is not limited to mixed working fluid.When vaporizer made by the plate type heat exchanger of organic Rankine bottoming cycle, the second working medium B can be conduction oil, but is not limited to conduction oil.When it is as condenser, the second working medium B can be cooling water, but is not limited to cooling water.
If Fig. 6, heat exchanger plates 11a1b1c and heat exchanger plates 22a2b2c middle cavity are the runner of heat exchanger plates.
According to the present invention for the shell-and-tube heat exchanger of organic Rankine bottoming cycle and plate type heat exchanger all can with the vaporizer in organic rankine cycle system and condenser.
According to the present invention, the first working medium A is the cycle fluid in organic rankine cycle system, and it can be mixed working fluid, but is not limited to mixed working fluid.When vaporizer made by the shell-and-tube heat exchanger of organic Rankine bottoming cycle or plate type heat exchanger, the second working medium B can be conduction oil, but is not limited to conduction oil.When it is as condenser, the second working medium B can be cooling water, but is not limited to cooling water.
Unaccounted equipment and back-up system thereof in the present invention, pipeline, instrument, valve, the bypass facility etc. that is incubated, has regulatory function adopt known mature technology to carry out supporting.
In addition, it should be noted that, unless stated otherwise or point out, otherwise the description such as the term in description " first ", " second ", " the 3rd " is used only for each assembly in differentiation description, element, step etc., rather than is used for logical relation or the ordering relation etc. that represent between each assembly, element, step.
Although it is understood that the present invention discloses as above with preferred embodiment, but above-described embodiment is not limited to the present invention.For any those of ordinary skill in the art, without departing under technical solution of the present invention ambit, all may utilize the technology contents of the disclosure above and technical solution of the present invention is made many possible variations and modification, or be revised as the Equivalent embodiments of equivalent variations.Therefore, every content without departing from technical solution of the present invention, the technical spirit of the foundation present invention, to any simple modification made for any of the above embodiments, equivalent variations and modification, all still falls within the scope of technical solution of the present invention protection.
Claims (9)
1. a variable flow channel type heat exchanger, including:
The heat exchange runner that the circulatory flow that at least one first working medium flows through and at least one second working medium flow through, heat exchange along with the first working medium Yu the second working medium, first working medium gradually changes between liquid and gaseous state, and first working medium flow velocity in circulatory flow gradually changes simultaneously；
It is characterized in that, described circulatory flow includes at least one-level branch flow passage and sprue, and every one-level branch flow passage is made up of the identical branch flow passage of more than two, is connected with in upper level branch flow passage or upper level sprue；
Wherein, in the flow passage entry of each branch flow passage or sprue, the flow velocity of the first working medium is within default flow velocity limits；At the runner exit place of each branch flow passage or sprue, the flow velocity of the first working medium is outside default flow velocity limits.
2. a kind of variable flow channel type heat exchanger described in claim 1, it is characterised in that described heat exchanger is vaporizer, wherein:
First working medium is flowed into by sprue in circulatory flow, thereafter branch flow passage at different levels is flowed through according to by little level time to big level time, flowed out by afterbody branch flow passage, heat exchange along with the first working medium Yu the second working medium, first working medium is gradually varied to gaseous state by liquid, and first working medium flow velocity in circulatory flow accelerates gradually simultaneously；
In the flow passage entry of sprue or each branch flow passage, the flow velocity of the first working medium is less than default maximum flow rate value；At the runner exit place of sprue or each branch flow passage, the flow velocity of the first working medium is be more than or equal to default maximum flow rate value.
3. a kind of variable flow channel type heat exchanger described in claim 2, it is characterised in that the second described working medium is conduction oil.
4. a kind of variable flow channel type heat exchanger described in claim 1, it is characterised in that described heat exchanger is condenser, wherein:
First working medium is flowed into by afterbody branch flow passage in circulatory flow, thereafter branch flow passage at different levels is flowed through according to by big level time to little level time, flowed out by sprue, heat exchange along with the first working medium Yu the second working medium, first working medium is gradually varied to liquid by gaseous state, and first working medium flow velocity in circulatory flow is slack-off gradually simultaneously；
In the flow passage entry of each branch flow passage or sprue, the flow velocity of the first working medium is more than default lower flow rate limit value；At the runner exit place of each branch flow passage or sprue, the flow velocity of the first working medium is less than or equal to default lower flow rate limit value.
5. a kind of variable flow channel type heat exchanger described in claim 3, it is characterised in that the second described working medium is cooling water.
6. according to the arbitrary described a kind of variable flow channel type heat exchanger of claim 1 to 5, it is characterised in that described heat exchanger is shell-and-tube heat exchanger；
Wherein, the circulatory flow that the first working medium flows through is the pipeline section runner of shell-and-tube heat exchanger, and the heat exchange runner that the second working medium flows through is the housing runner of shell-and-tube heat exchanger；
The length of pipe section of described branch flow passage at different levels or sprue and caliber are determined according to the flow velocity of the first working medium in pipeline section.
7. a kind of variable flow channel type heat exchanger described in claim 6, it is characterized in that, the shell of described shell-and-tube heat exchanger is the housing of a taper, little side, conical shell cross section few with heat exchanger tube hop count amount in the same side, big side, conical shell cross section many with heat exchanger tube hop count amount in the same side, be provided with deflection plate in the space between conical shell and heat exchange pipeline section.
8. according to the arbitrary described a kind of variable flow channel type heat exchanger of claim 1 to 5, it is characterised in that described heat exchanger is plate type heat exchanger；
Wherein, between the heat exchange runner plate that between the circulatory flow plate that the first working medium flows through, cavity and the second working medium flow through, cavity is spaced；
Between the plate of described branch flow passage at different levels, the quantity of cavity is determined according to the flow velocity of the first working medium in cavity.
9. according to the arbitrary described a kind of variable flow channel type heat exchanger of claim 1 to 5, it is characterised in that the first described working medium is one or more mixing in R245fa, R136fa, R600, R601, R601a.
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| CN201410724448.8A CN105716331B (en) | 2014-12-02 | 2014-12-02 | A kind of variable flow channel type heat exchanger improving Organic Rankine Cycle efficiency |
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| CN201410724448.8A CN105716331B (en) | 2014-12-02 | 2014-12-02 | A kind of variable flow channel type heat exchanger improving Organic Rankine Cycle efficiency |
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| CN105716331B CN105716331B (en) | 2019-01-22 |
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| CN106642831A (en) * | 2016-12-31 | 2017-05-10 | 潍坊小禾节能科技有限公司 | Composite heat exchanger for organic Rankine cycle power generating system |
| CN106839527A (en) * | 2016-12-31 | 2017-06-13 | 潍坊小禾节能科技有限公司 | A kind of organic Rankine cycle power generation system composite heat exchanger with separation layer |
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| CN105716331B (en) | 2019-01-22 |
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