CN220380351U - Waste heat recovery device - Google Patents
Waste heat recovery device Download PDFInfo
- Publication number
- CN220380351U CN220380351U CN202321957813.0U CN202321957813U CN220380351U CN 220380351 U CN220380351 U CN 220380351U CN 202321957813 U CN202321957813 U CN 202321957813U CN 220380351 U CN220380351 U CN 220380351U
- Authority
- CN
- China
- Prior art keywords
- waste heat
- medium
- recovery device
- inlet
- heat recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002918 waste heat Substances 0.000 title claims abstract description 187
- 238000011084 recovery Methods 0.000 title claims abstract description 44
- 238000001816 cooling Methods 0.000 claims abstract description 45
- 238000001704 evaporation Methods 0.000 claims description 32
- 230000008020 evaporation Effects 0.000 claims description 32
- 238000004891 communication Methods 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 15
- 238000010248 power generation Methods 0.000 claims description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- MSSNHSVIGIHOJA-UHFFFAOYSA-N pentafluoropropane Chemical compound FC(F)CC(F)(F)F MSSNHSVIGIHOJA-UHFFFAOYSA-N 0.000 claims description 3
- 125000004122 cyclic group Chemical group 0.000 claims 1
- 230000006866 deterioration Effects 0.000 abstract description 5
- 238000000034 method Methods 0.000 description 15
- 238000010586 diagram Methods 0.000 description 12
- 238000002156 mixing Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Abstract
The application discloses a waste heat recovery device relates to waste heat recovery technical field. The waste heat recovery device includes: the waste heat supply unit is used for supplying waste heat media and comprises a cooling device, and the cooling device is used for reducing the superheat degree of the waste heat media; and the heat exchange unit comprises a working medium with circulating circulation, and the heat exchange unit is communicated with the waste heat supply unit, so that a waste heat medium flows through the heat exchange unit to exchange heat with the working medium. Therefore, the superheat degree of the waste heat medium is reduced by arranging the cooling device, and the problem that the temperature of the waste heat medium is usually higher than the highest limit temperature of the working medium in the prior art, and the deterioration and failure of the working medium are easily caused by direct heat exchange is solved.
Description
Technical Field
The application relates to the technical field of waste heat recovery, in particular to a waste heat recovery device.
Background
As surplus heat energy released in the production process, waste heat is widely used in petrochemical industry, coal, steel, building materials, textile, metallurgy and other industries. The fluid that generates the waste heat is typically in a superheated state, i.e., the current temperature of the fluid is higher than the saturation temperature corresponding to the current pressure. The waste heat contains a large amount of energy, and a large amount of energy can be saved by recycling the waste heat. Therefore, recycling waste heat is one of the important methods for saving energy.
At present, heat exchange is performed between a working medium and a waste heat medium most commonly used for waste heat recovery, however, the temperature of the waste heat medium is usually higher than the highest limit temperature of the working medium, and direct heat exchange is easy to cause deterioration and failure of the working medium.
Disclosure of Invention
The embodiment of the application provides a waste heat recovery device, reduces the temperature of waste heat medium through setting up heat sink, solves among the prior art temperature of waste heat medium and is higher than the highest extreme temperature of working medium generally, and direct heat transfer causes the working medium to deteriorate inefficacy easily.
The embodiment of the application provides a waste heat recovery device, include:
the waste heat supply unit is used for supplying waste heat medium and comprises a cooling device which is used for reducing the temperature of the waste heat medium;
the heat exchange unit comprises a working medium with circulating circulation, and the heat exchange unit is communicated with the waste heat supply unit, so that the waste heat medium flows through the heat exchange unit to exchange heat with the working medium.
In some embodiments, further comprising:
and the power generation unit is communicated with the heat exchange unit.
In some embodiments, the temperature reduction device is an ejector.
In some embodiments, the cooling device comprises:
the first inlet is used for inputting the waste heat medium;
the second inlet is used for inputting a cooling medium; the cooling medium is used for cooling the waste heat medium;
and the cooling outlet is used for outputting the cooled waste heat medium.
In some embodiments, a supercharging device is also included, the supercharging device in communication with the second inlet.
In some embodiments, the pressurizing device is also in communication with the heat exchange unit.
In some embodiments, further comprising:
and the separation device is arranged between the heat exchange unit and the supercharging device.
In some embodiments, the heat exchange unit comprises an evaporator, an expander, a condenser, and a working fluid pump in cyclical communication, wherein,
the evaporator comprises a first evaporation inlet, a second evaporation inlet and a second evaporation outlet; the first evaporation inlet is communicated with the cooling outlet, the second evaporation inlet is communicated with the working medium pump, and the second evaporation outlet is communicated with the expansion machine.
In some embodiments, the evaporator further comprises a first evaporation outlet in communication with the second inlet.
In some embodiments, the expander is an axial flow turbine expander, a centripetal turbine expander, a centrifugal turbine expander, a screw expander, a scroll expander, or a piston expander.
In some embodiments, the waste heat medium is one or more of steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, raw gas, and natural gas.
In some embodiments, the working fluid is one or more of R410a, R152a, R132, R290, R134a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and aqueous ammonia.
Compared with the prior art, the waste heat recovery device of this application embodiment includes: the waste heat supply unit is used for supplying waste heat medium, and comprises a cooling device which is used for reducing the temperature of the waste heat medium; and the heat exchange unit comprises a working medium with circulating circulation, and the heat exchange unit is communicated with the waste heat supply unit, so that a waste heat medium flows through the heat exchange unit to exchange heat with the working medium. Therefore, the temperature of the waste heat medium is reduced by arranging the cooling device, and the problem that the temperature of the waste heat medium is usually higher than the highest limit temperature of a working medium in the prior art, and the direct heat exchange is easy to cause deterioration and failure of the working medium is solved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the description of the embodiments will be briefly introduced below, it being obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a waste heat recovery device according to an embodiment of the present application;
fig. 2 is a schematic structural diagram of a waste heat recovery device according to an embodiment of the present disclosure;
fig. 3 is a schematic structural diagram III of a waste heat recovery device according to an embodiment of the present application;
fig. 4 is a schematic structural diagram of a waste heat recovery device according to an embodiment of the present disclosure;
fig. 5 is a temperature entropy diagram of a waste heat recovery device according to an embodiment of the present disclosure;
fig. 6 is a second temperature entropy diagram of a waste heat recovery device according to an embodiment of the present application.
Reference numerals: 100-waste heat supply unit; 110-a cooling device; 120-ejector; 130-a first inlet; 140-a second inlet; 150-cooling outlet; 200-a heat exchange unit; 210-an evaporator; 211-a first evaporation inlet; 212-a first evaporation outlet; 213-a second evaporation inlet; 214-a second evaporation outlet; 220-an expander; 230-a condenser; 240-working medium pump; 300-a power generation unit; 400-supercharging device; 500-separation device.
Detailed Description
The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application. It will be apparent that the described embodiments are only some, but not all, of the embodiments of the present application. All other embodiments, which can be made by those skilled in the art based on the embodiments herein without making any inventive effort, are intended to be within the scope of the present application.
The first embodiment of the present application provides a waste heat recovery device, referring to fig. 1, which is a schematic structural diagram of the waste heat recovery device provided in the embodiment of the present application, as can be seen from fig. 1, the waste heat recovery device includes a waste heat supply unit 100 and a heat exchange unit 200.
Specifically, the waste heat supply unit 100 is configured to supply a waste heat medium, the waste heat supply unit 100 includes a cooling device 110, and the cooling device 110 is configured to reduce a temperature of the waste heat medium; the heat exchange unit 200 comprises a working medium with circulating circulation inside, and the heat exchange unit 200 is communicated with the waste heat supply unit 100, so that a waste heat medium flows through the heat exchange unit 200 to exchange heat with the working medium; and a power generation unit 300, the power generation unit 300 being in communication with the heat exchange unit 200.
Specifically, the waste heat medium is in an overheat state, and the inventor of the application finds that when the waste heat medium is directly used for heat exchange in the actual operation process, the highest temperature of the working medium is easily exceeded, so that the working medium is deteriorated and loses efficacy. Therefore, the temperature of the waste heat medium is reduced through pretreatment of the method, so that the service life of the working medium is prolonged.
Specifically, the saturation temperature t of the waste heat medium 0 The range of (2) is 50-500 ℃, 50 ℃, 52 ℃, 54 ℃, 60 ℃, 70 ℃, 80 ℃, 100 ℃, 140 ℃, 200 ℃, 250 ℃, 300 ℃, 400 ℃, 490 ℃, 500 ℃ and the like. The superheat degree of the waste heat medium ranges from 1 ℃ to 200 ℃, and the superheat degree can be 1 ℃,3 ℃, 5 ℃, 7 ℃, 10 ℃, 15 ℃, 20 ℃, 30 ℃, 50 ℃, 100 ℃, 200 ℃ and the like.
Referring to fig. 2 for a schematic structural diagram of a waste heat recovery device provided in this embodiment, as can be seen from fig. 2, in one embodiment, the cooling device 110 is an ejector 120, and the pressure of the waste heat medium is higher than that of the heat reducing medium.
Specifically, due to the characteristics of the ejector, the low-pressure fluid can be driven to flow through the high-pressure fluid, and the waste heat medium can drive the heat reducing medium to flow.
In one embodiment, the cooling device 110 includes:
a first inlet 130, the first inlet 130 for inputting a waste heat medium;
a second inlet 140, the second inlet 140 being for inputting a cooling medium; the cooling medium is used for cooling the waste heat medium;
the cooling outlet 150, the cooling outlet 150 is used for outputting the cooled waste heat medium.
Specifically, the first inlet 130 is used for inputting the waste heat medium; the second inlet 140 is used for inputting a heat reducing medium; the cooling outlet 150 is used for outputting cooled waste heat medium; wherein the temperature of the heat reducing medium is lower than that of the waste heat medium, and the heat reducing medium and the waste heat medium are mixed in the waste heat supply unit 100 to obtain the cooled waste heat medium.
So, this application is through reducing the heat medium and mixing the waste heat medium and cooling down to avoid the damage to the working medium, promote the life of working medium.
Specifically, the heat reducing medium can be the same as or different from the waste heat medium, and when the heat reducing medium is different from the waste heat medium, the low-temperature fluid and the original waste heat medium do not react chemically, so that the operation of the original device is not affected.
Referring to fig. 3, a schematic structural diagram of a waste heat recovery device according to an embodiment of the present application is shown; as can be seen from fig. 3, in one embodiment, the apparatus further comprises a pressurizing device 400, wherein the pressurizing device 400 is in communication with the second inlet 140 for outputting the heat reducing medium to the heat reducing device 110; wherein, the temperature of the heat reducing medium is lower than that of the waste heat medium, and the heat reducing medium and the waste heat medium are cooled in the cooling device 110 to obtain the cooled waste heat medium.
Specifically, the pressurizing device 400 may pressurize the heat reducing medium, and then enter the waste heat supply unit 100, thereby improving the mixing efficiency with the waste heat medium.
In one embodiment, the pressurizing device 400 is further in communication with the heat exchange unit 200, so that the cooled waste heat medium flows through the heat exchange unit 200 to form a working medium; the pressurizing device 400 is communicated with the heat exchange unit 200, and the working medium passes through the pressurizing device 400 to form a heat reducing medium.
Specifically, at least part of the waste heat medium is separated from the working medium and recycled after being pressurized, so that the energy utilization rate can be further improved while the mixing efficiency with the waste heat medium is improved.
Referring to fig. 4, a schematic structural diagram of a waste heat recovery device according to an embodiment of the present application is shown; as can be seen from fig. 4, in one possible embodiment, the waste heat recovery device further comprises: the separation device 500, the separation device 500 is disposed between the heat exchange unit 200 and the pressurizing device 400, for inputting at least part of the working medium into the pressurizing device 400.
In particular, the use of the separation device 500 may further control the flow rate of the returned working medium. The superheat degree of the waste heat medium, the heat load of the superheat section and the working medium are determined according to the pressure, the temperature and the flow of the waste heat medium. The reflux quantity of the working medium is determined according to the superheat degree of the waste heat medium, the heat load of the superheat section and the state of the working medium, wherein the superheat section is a stage that the temperature of the waste heat medium is higher than the saturation temperature.
Specifically, the heat load of the superheat section is determined by the following formula:
Q 1 ＝c p1 ×m 1 ×(t 1 -t 0 )，t 1 ＝t 0 +(1～200℃）， (1)
wherein Q is 1 C, for the heat load of the waste heat medium in the superheating section p1 Specific heat m of waste heat medium in overheat state 1 Is the flow rate when the waste heat medium is the superheated fluid, t 1 T is the temperature of the waste heat medium before cooling 0 The corresponding saturation temperature of the waste heat medium under the current pressure is adopted.
Specifically, the heat load of the mixed cooling is determined by the following formula:
Q 2 ＝c p1 ×m 1 ×(t 1 -t 3 )，t 3 ≥t 0 ，Q 2 ≤Q 1 ， (2)
wherein Q is 2 C, for the heat load of the waste heat medium in the mixed cooling section p1 Specific heat m of waste heat medium in overheat state 1 Is the flow rate when the waste heat medium is the superheated fluid, t 1 T is the temperature of the waste heat medium before cooling 3 T is the temperature of the residual heat medium after cooling 0 Is the corresponding saturation temperature of the waste heat medium under pressure.
Specifically, the amount of reflux of the working medium is determined according to the following formula:
m 2 ＝Q 2 /q 2 ， (3)
wherein m is 2 For the reflux amount of the working medium, Q 2 For the heat load of the waste heat medium in the mixed cooling section, q 2 Is the latent heat of vaporization of the working medium.
It will be appreciated that t in equation (1) 1 Far above t 0 T in formula (2) 3 And t 0 Equal to, or t 3 Ratio t 0 High, so that the final Q 2 Lower than or equal to Q 1 I.e. the waste heat medium is in a saturated temperature state when entering the evaporator 210, orA state of slight overheating. T is the number of 3 For a set temperature value, t is preferred 3 Ratio t 0 High range of [0,3 ]]。
In one embodiment, heat exchange unit 200 includes an evaporator 210, an expander 220, a condenser 230, and a working fluid pump 240 in cyclical communication.
Specifically, the evaporator 210 includes a first evaporation inlet 211, a second evaporation inlet 213, and a second evaporation outlet 214; the first evaporation inlet 211 is communicated with the cooling outlet 150, the second evaporation inlet 213 is communicated with the working medium pump 240, and the second evaporation outlet 214 is communicated with the expander 220.
Specifically, the cooled residual heat medium enters the evaporator 210 through the first evaporation inlet 211, the working medium enters the evaporator 210 through the second evaporation inlet 213, and the working medium is output from the second evaporation outlet 214 after heat exchange is completed.
Specifically, the heat exchange unit 200 exchanges heat through the evaporator 210, specifically, exchanges heat between the working medium and the cooled waste heat medium. At this time, the temperature of the cooled waste heat medium is greatly reduced, so that the effective degree of the working medium is not influenced any more, and the service life of the working medium is greatly prolonged. The working medium vapor is expanded and depressurized in the expander 220, then is generated by the power generation unit 300, is condensed into a liquid-phase working medium by the condenser 230, and finally is pressurized by the pressurizing pump 250 and then enters the evaporator 210 for recycling.
In one embodiment, the evaporator 210 further includes a first evaporation outlet 212, the first evaporation outlet 212 being in communication with the second inlet 140.
Specifically, the temperature of the cooled waste heat medium is further reduced after heat exchange, and the cooled waste heat medium can enter the second inlet 140 through the first evaporation outlet 212, so that heat exchange is performed with the waste heat medium again.
Specifically, the expander 220 is an axial flow type turbo expander, a centripetal type turbo expander, a centrifugal type turbo expander, a screw type expander, a scroll type expander, or a piston type expander.
In one embodiment, the waste heat medium is one or more of steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, raw gas and natural gas.
In one embodiment, the working fluid is one or more of R410a, R152a, R132, R290, R134a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and aqueous ammonia.
Compared with the prior art, the waste heat recovery device of this application embodiment includes: the waste heat supply unit 100, the waste heat supply unit 100 is used for supplying waste heat medium, the waste heat supply unit 100 comprises a cooling device 110, and the cooling device 110 is used for reducing the temperature of the waste heat medium; the heat exchange unit 200, the heat exchange unit 200 includes a working medium having circulation flow therein, and the heat exchange unit 200 is communicated with the waste heat supply unit 100, so that the waste heat medium flows through the heat exchange unit 200 to exchange heat with the working medium; and a power generation unit 300, the power generation unit 300 being in communication with the heat exchange unit 200. Therefore, the temperature of the waste heat medium is reduced by arranging the cooling device, and the problem that the temperature of the waste heat medium is usually higher than the highest limit temperature of a working medium in the prior art, and the direct heat exchange is easy to cause deterioration and failure of the working medium is solved.
Accordingly, a second embodiment of the present application provides a waste heat power generation method, employing a waste heat recovery device as described in any one of the foregoing embodiments;
the power generation method comprises the following steps:
step 101, preprocessing the waste heat medium to obtain the cooled waste heat medium; wherein the temperature of the cooled waste heat medium is lower than that of the waste heat medium;
step 102, heating the working medium by utilizing the cooled waste heat medium to obtain steam, and generating power by utilizing the steam.
In one embodiment, step 101 includes:
acquiring a heat reducing medium, wherein the temperature of the heat reducing medium is lower than that of the waste heat medium;
and mixing the heat reducing medium with the waste heat medium to obtain the cooled waste heat medium.
In one embodiment, step 102 includes:
heating the working medium by utilizing the cooled waste heat medium, and gasifying to obtain high-pressure working medium steam;
the expander is driven to generate power by high-pressure working medium steam;
condensing the working medium vapor to obtain working medium liquid, and repeatedly utilizing the cooled waste heat medium to heat the working medium to obtain vapor.
Specifically, referring to fig. 5, a temperature entropy diagram of a waste heat recovery device provided in an embodiment of the present application is shown; the waste heat medium enters the system from the H0 state, is mixed with the fluid in the state H4 after the part from the state H3 is pressurized to a saturation point, and then releases heat according to the process of the state points H1-H2-H3; the working medium is changed into steam after being subjected to an endothermic evaporation process of 1-2-3, the pressure is reduced after being subjected to an expansion working process of 3-4, the working medium is changed into working medium liquid after being subjected to a cooling condensation process of 4-5-6, and then the heat of the saturated waste heat medium is absorbed again after being subjected to a pressurization process of 6-1. In addition, referring to fig. 6, a temperature entropy diagram of a waste heat recovery device according to an embodiment of the present application is different from fig. 5 in that the waste heat medium is a single fluid.
Specifically, the waste heat medium is in a gas phase in the H0 state; when the waste heat medium passes through the cooling device 110 and is converted into an H1 state, the waste heat medium is in a liquid phase or a gas-liquid mixed phase, and the volume of the waste heat medium in the H1 state is reduced compared with that in the H0 state; then, the waste heat medium in the H1 state enters the heat exchange unit 200, particularly the evaporator 210 in the heat exchange unit 200 and then exchanges heat with the working medium, and the state of the waste heat medium is changed into H1-H2-H3 in the process; and then, the waste heat medium in the H3 state is pressurized to obtain the waste heat medium in the H4 state, and the waste heat medium is re-fed into the cooling device to be mixed with the waste heat medium in the H1 state, so that the circulation of the steps is continued.
Further, the comparison of the residual heat medium in the H0-H1 state with the residual heat medium in the H1-H2 state is shown in Table 1:
TABLE 1 comparison of residual heat Medium State changes
As can be seen from table 1, the recovery of waste heat prior to the use of this scheme occurs in both stages H0-H1 and H1-H2, but the overall heat exchange volume is very large due to the too large gas phase volume of H0. By adopting the technology, the actual waste heat recovery occurs in the H1-H2 stage. That is, the waste heat medium after cooling directly enters the efficient condensation process after entering the heat exchange unit 200, compared with the waste heat medium before adopting the scheme, the heat exchange area is reduced by 20%, so that the problems of huge equipment volume and high input cost of the heat exchange unit 200 caused by poor heat exchange effect and large required heat exchange area in the gas phase cooling process of the overheating medium in the H0-H1 process are solved.
Compared with the prior art, the power generation method of the embodiment of the application adopts the waste heat recovery device and comprises the following steps: pretreating the waste heat medium to obtain the cooled waste heat medium; wherein the temperature of the cooled waste heat medium is lower than that of the waste heat medium; and heating the working medium by utilizing the cooled waste heat medium to obtain steam, and generating power by utilizing the steam. Therefore, the problem that the temperature of the waste heat medium is usually higher than the highest limit temperature of the working medium in the prior art, and the direct heat exchange is easy to cause deterioration and failure of the working medium is solved by reducing the temperature of the waste heat medium. In addition, the volume flow of the waste heat medium can be reduced by cooling the waste heat medium, so that the caliber of a pipeline required by the circulation of the waste heat medium is reduced, and the investment cost of pipeline construction is further saved.
The above describes in detail a waste heat recovery device provided in the embodiment of the present application, and specific examples are applied herein to illustrate the principles and embodiments of the present application, where the description of the above embodiment is only for helping to understand the technical solution and core ideas of the present application; those of ordinary skill in the art will appreciate that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the corresponding technical solutions from the scope of the technical solutions of the embodiments of the present application.
Claims (12)
1. A waste heat recovery device, comprising:
a waste heat supply unit (100), the waste heat supply unit (100) being configured to supply a waste heat medium, the waste heat supply unit (100) comprising a cooling device (110);
the heat exchange unit (200), the heat exchange unit (200) comprises a working medium with circulating circulation inside, and the heat exchange unit (200) is communicated with the cooling device (110) in the waste heat supply unit (100).
2. The waste heat recovery device of claim 1, further comprising:
-a power generation unit (300), the power generation unit (300) being in communication with the heat exchange unit (200).
3. The waste heat recovery device of claim 1, wherein the cooling device (110) is an ejector (120).
4. The heat recovery device according to claim 1, wherein the cooling device (110) comprises:
-a first inlet (130), said first inlet (130) for inputting said waste heat medium;
a second inlet (140), the second inlet (140) being for inputting a cooling medium; the cooling medium is used for cooling the waste heat medium;
and the cooling outlet (150) is used for outputting the cooled waste heat medium.
5. The waste heat recovery device of claim 4, further comprising a pressurizing device (400), the pressurizing device (400) being in communication with the second inlet (140).
6. Waste heat recovery device according to claim 5, wherein the pressurizing means (400) is also in communication with the heat exchange unit (200).
7. The waste heat recovery device of claim 5, further comprising:
and a separation device (500), wherein the separation device (500) is arranged between the heat exchange unit (200) and the supercharging device (400).
8. The waste heat recovery device of claim 4, wherein the heat exchange unit (200) comprises an evaporator (210), an expander (220), a condenser (230) and a working fluid pump (240) in cyclic communication, wherein,
the evaporator (210) comprises a first evaporation inlet (211), a second evaporation inlet (213) and a second evaporation outlet (214); the first evaporation inlet (211) is communicated with the cooling outlet (150), the second evaporation inlet (213) is communicated with the working medium pump (240), and the second evaporation outlet (214) is communicated with the expander (220).
9. The waste heat recovery device of claim 8, wherein the evaporator (210) further comprises a first evaporation outlet (212), the first evaporation outlet (212) being in communication with the second inlet (140).
10. A waste heat recovery device according to claim 8, wherein the expander (220) is an axial flow turbo expander, a centripetal turbo expander, a centrifugal turbo expander, a screw expander, a scroll expander or a piston expander.
11. The waste heat recovery device of claim 10, wherein the waste heat medium is one of steam, nitrogen, carbon dioxide, hydrogen, carbon monoxide, oxygen, methanol, raw gas, and natural gas.
12. The waste heat recovery device of claim 11, wherein the working fluid is one of R410a, R152a, R132, R290, R134a, R600, R601a, R123, R245fa, R1234yf, R1234ze, and aqueous ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321957813.0U CN220380351U (en) | 2023-07-24 | 2023-07-24 | Waste heat recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321957813.0U CN220380351U (en) | 2023-07-24 | 2023-07-24 | Waste heat recovery device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220380351U true CN220380351U (en) | 2024-01-23 |
Family
ID=89571853
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321957813.0U Active CN220380351U (en) | 2023-07-24 | 2023-07-24 | Waste heat recovery device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220380351U (en) |
-
2023
- 2023-07-24 CN CN202321957813.0U patent/CN220380351U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6808166B2 (en) | Generation of process steam by high temperature heat pump | |
| JP2009537774A (en) | Method and system for generating power from a heat source | |
| CN103089356A (en) | Flash evaporation-double work medium combined power generation device | |
| CN108798808B (en) | CO for recovering waste heat of high-temperature flue gas２Cyclic cogeneration system | |
| CN102575531A (en) | Method and system for generating high pressure steam | |
| KR20150000422A (en) | Heat recovery apparatus | |
| RU2665794C1 (en) | Method and plant for mechanical and thermal energy generation | |
| CN220380351U (en) | Waste heat recovery device | |
| CN103527268A (en) | Double-stage full-flow screw expander organic Rankine cycle system | |
| CN111396291B (en) | Compressed gas waste heat recovery power generation system | |
| CN115750004A (en) | Residual pressure waste heat recovery power receiving and transmitting system and residual pressure waste heat recovery method | |
| CN116641769A (en) | Energy storage utilization system based on carbon dioxide working medium | |
| JPH09264158A (en) | Gas turbine cycle | |
| CN114483232B (en) | Compressed air energy storage system based on organic flash evaporation circulation and control method | |
| CN211777627U (en) | Power generation system for recovering waste heat at different temperature levels | |
| CN203531985U (en) | Organic Rankine cycle system for double-stage full-flow screw expander | |
| KR101294948B1 (en) | Power system for improved thermal and condensing efficiency | |
| KR20110096239A (en) | Transcritical rankine power cycle by using a pure working fluids | |
| CN111042885A (en) | Power generation system and power generation method for recovering waste heat at different temperature levels | |
| CN220103095U (en) | Waste heat recovery power generation system of propane dehydrogenation device | |
| CN110630344A (en) | Power generation and energy storage method and system | |
| CN216342357U (en) | Power generation system using waste incineration waste heat utilization CO2 as circulating medium | |
| KR102230950B1 (en) | Steam suplly system and method for steam supplying | |
| CN213684260U (en) | ORC electricity, cold antithetical couplet confession system | |
| CN115900136A (en) | Low-grade heat source heat recovery system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |