CN113446881A - Heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device - Google Patents
Heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device Download PDFInfo
- Publication number
- CN113446881A CN113446881A CN202110698336.XA CN202110698336A CN113446881A CN 113446881 A CN113446881 A CN 113446881A CN 202110698336 A CN202110698336 A CN 202110698336A CN 113446881 A CN113446881 A CN 113446881A
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- secondary refrigerant
- cold energy
- temperature liquid
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- 239000007788 liquid Substances 0.000 title claims abstract description 71
- 238000002309 gasification Methods 0.000 title claims abstract description 37
- 238000011084 recovery Methods 0.000 title claims abstract description 18
- 238000010438 heat treatment Methods 0.000 title abstract description 6
- 239000003507 refrigerant Substances 0.000 claims abstract description 45
- 238000010521 absorption reaction Methods 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims abstract description 26
- 230000007547 defect Effects 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims 7
- 239000007789 gas Substances 0.000 abstract description 9
- 239000002918 waste heat Substances 0.000 abstract description 2
- 239000002826 coolant Substances 0.000 description 9
- 239000003949 liquefied natural gas Substances 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 238000004146 energy storage Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000004378 air conditioning Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
Abstract
The invention discloses a heat pipe type cold energy recovery device in a high-pressure low-temperature liquid gasification heating process, which comprises a high-pressure side cold absorption system and a low-pressure side cold release system; the high-pressure side cold absorption system comprises a high-pressure pipeline and a cold absorption device arranged in the high-pressure pipeline, and the low-pressure side cold release system comprises a secondary refrigerant box and a cold release device arranged in the secondary refrigerant box; the high-pressure low-temperature liquid flows out after entering the high-pressure pipeline for gasification, the gaseous working medium in the cold absorption device absorbs cold energy generated by the gasification of the high-pressure low-temperature liquid, the cold energy is condensed into liquid and flows into the cold release device, the liquid returns to the cold absorption device after absorbing heat from the secondary refrigerant and being gasified, and the cooled secondary refrigerant is conveyed to an external cold energy utilization device through a secondary refrigerant pump to release cold energy and then returns to the secondary refrigerant box. The invention can be used for recovering and utilizing cold energy in the process of gasifying high-pressure low-temperature liquid, and can also be used for recovering and utilizing gas waste heat under the working conditions of medium pressure, low pressure or negative pressure.
Description
Technical Field
The invention relates to the technical field of heat pipe type heat exchangers, in particular to a cold energy recovery device used in a high-pressure low-temperature liquid gasification process.
Background
For the high-pressure liquid air at the energy release section of the liquid compressed air energy storage system and the LNG gasification in the LNG gasification process, the pressure is very high, the temperature is low and the requirement on a heat exchanger is high during the two low-temperature liquid working media. If a shell and tube heat exchanger is used, a bulky heat exchanger is required due to the low heat transfer coefficient of the air side. If the plate heat exchanger is adopted, the plate heat exchanger cannot bear larger pressure difference between two sides, and therefore the plate heat exchanger cannot be applied. The heat pipe has the advantages of good heat transfer performance, capability of increasing the heat exchange area on the side with low heat exchange coefficient and the like, and is particularly suitable for the heat exchange environment of gas working media. Therefore, a high-efficiency compact heat exchanger with high comprehensive heat exchange coefficient can be developed based on the heat pipe principle.
Disclosure of Invention
The invention aims to provide a heat pipe type cold energy recovery device for a high-pressure low-temperature liquid gasification and temperature rise process, which is used for recovering and utilizing cold energy in a liquid air gasification process and cold energy in a low-temperature working medium gasification process of LNG (liquefied natural gas) or liquid oxygen, liquid nitrogen or liquid argon and the like.
In order to achieve the purpose, the invention adopts the technical scheme that:
a heat pipe type cold energy recovery device in a high-pressure low-temperature liquid gasification heating process comprises a high-pressure side cold absorption system and a low-pressure side cold release system; the high-pressure side cold absorption system comprises a high-pressure pipeline and a cold absorption device arranged in the high-pressure pipeline, and the low-pressure side cold release system comprises a secondary refrigerant box and a cold release device arranged in the secondary refrigerant box; the liquid working medium outlet of the cold absorbing device is connected with the liquid working medium inlet of the cold releasing device, and the gaseous working medium outlet of the cold carrying and releasing device is connected with the gaseous working medium inlet of the cold absorbing device to form a working medium circulation loop; the secondary refrigerant box is filled with secondary refrigerant and is connected with an external cold energy utilization device through a secondary refrigerant pipeline and a secondary refrigerant pump to form a secondary refrigerant circulation loop; the high-pressure low-temperature liquid flows out after entering the high-pressure pipeline for gasification, the gaseous working medium in the cold absorption device absorbs cold energy generated by the gasification of the high-pressure low-temperature liquid, the cold energy is condensed into liquid and flows into the cold release device, the liquid returns to the cold absorption device after absorbing heat from the secondary refrigerant and being gasified, and the cooled secondary refrigerant is conveyed to an external cold energy utilization device through a secondary refrigerant pump to release cold energy and then returns to the secondary refrigerant box.
Preferably, the pipe diameter of the high-pressure pipeline is larger than that of the high-pressure low-temperature liquid pipeline, and two ends of the high-pressure pipeline are in a conical shape with the pipe diameter gradually reduced and are connected with the high-pressure low-temperature liquid pipeline through flanges.
As preferred, cold absorption device is cylindrical, including last collection pipe, heat pipe and collection pipe down, goes up the collection pipe and includes the branch pipe that gathers on and the person in charge that gathers on, and the branch pipe semicircular in shape that gathers on, and symmetrical connection is in the person in charge both sides of gathering last, and the interval is provided with the hole that is used for connecting the heat pipe on the branch pipe that gathers on, and the collection pipe is including the branch pipe that gathers down and the person in charge of gathering down, and the branch pipe semicircular in shape that gathers down, and symmetrical connection gathers the person in charge both sides under, and the interval is provided with the hole that is used for connecting the heat pipe on the branch pipe that gathers down, and the heat pipe is many, and vertical connection gathers between the branch pipe under and the branch pipe at last.
Preferably, the upper collecting branch pipe and the lower collecting branch pipe are both multiple and are concentrically connected to two sides of the upper collecting main pipe and the lower collecting main pipe respectively.
Preferably, the heat pipe is a finned pipe, the defect of low heat exchange coefficient at the gas side is overcome by increasing the heat exchange area, and the compactness, high efficiency, stability and reliability of the heat exchange process are ensured.
Preferably, the working medium circulation loop is connected with a vacuum maintaining device, so that the working medium circulation loop maintains a certain vacuum degree.
Preferably, the working medium in the working medium circulation loop is evaporated at-30 ℃ and condensed at about-35 ℃.
Preferably, the normal working temperature of the refrigerating medium is between-15 ℃ and-20 ℃.
Compared with the prior art, the invention has the beneficial effects that:
1. the cold energy recovery device has the advantages of flexible installation, simple maintenance, small volume, low investment, convenient transportation and the like, and can meet the requirements of different working conditions on low-grade heat exchange.
2. The cold energy recovery device can be used for recovering cold energy in the gasification and temperature rise process of high-pressure low-temperature liquid, can also be used for recovering medium-low temperature cold energy under various working conditions of medium pressure, low pressure and negative pressure, can meet the heat exchange requirements under various pressure working conditions in industrial production, has long service life and low cost, and can also effectively recycle the cold energy.
Drawings
FIG. 1 is a schematic diagram of the overall structure of a heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device;
FIG. 2 is a front view of the cold sink;
FIG. 3 is a top view of the cold sink;
description of reference numerals: 1-high pressure pipeline; 2-a cold absorption device; 3-a secondary refrigerant tank; 4-a cooling device; 5-a steam inlet pipeline; 6-a liquid drainage pipeline; 7-a coolant pipeline; 8-coolant pump; 9-vacuum holding means; 10-an upper flange; 11-a lower flange; 12-an upper header pipe; 13-a heat pipe; 14-lower manifold; 12 a-upper collecting branch; 12 b-Upper Collection Master.
Detailed Description
The technical solutions of the present application will be described clearly and completely with reference to the accompanying drawings in the embodiments, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
Examples
As shown in fig. 1, a heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device mainly comprises a high-pressure side cold absorption system positioned at the upper part and a low-pressure side cold release system positioned at the lower part, and the device can be used for recovering and utilizing cold energy in a high-pressure low-temperature liquid gasification process and also can be used for recovering and utilizing gas waste heat under medium-pressure, low-pressure or negative-pressure working conditions. The cold energy of the high-pressure low-temperature liquid gasification process comprises cold energy of a liquid air energy storage system in the liquid air gasification process in the energy release process and cold energy of LNG or liquid oxygen, liquid nitrogen or liquid argon and other low-temperature working media in the gasification process.
The high-pressure side cold absorption system comprises a high-pressure pipeline 1 and a cold absorption device 2 arranged inside the high-pressure pipeline 1. The high-pressure pipeline 1 is vertically arranged, the upper end and the lower end of the high-pressure pipeline are respectively connected with a high-pressure low-temperature liquid pipeline (not shown in the figure) through an upper flange 10 and a lower flange 11, high-pressure low-temperature liquid flows out after entering the high-pressure pipeline 1 and is gasified along the shell pass, and cold energy generated by the gasification of the high-pressure low-temperature liquid is absorbed by the cold absorption device 2. Preferably, the pipe diameter of the high-pressure pipeline 1 is larger than that of the high-pressure low-temperature liquid pipeline, namely, two ends of the high-pressure pipeline 1 are in a conical shape with the pipe diameter gradually reduced, so that the gasification efficiency of the high-pressure low-temperature liquid can be improved.
The low-pressure side cooling system includes a coolant tank 3 and a cooling device 4 disposed inside the coolant tank 3. The coolant tank 4 is filled with coolant and is connected to an external cold energy utilization device (not shown) through a coolant pipeline 7 and a coolant pump 8 to form a coolant circulation loop. The secondary refrigerant is non-freezing liquid, the freezing temperature is-55 ℃, and the normal working temperature is between-15 ℃ and-20 ℃. Through the refrigerating medium circulation loop, the cold energy absorbed by the high-pressure side cold absorption system can be timely transported out, on one hand, the normal operation of the heat exchange process can be ensured, on the other hand, the cold energy can be recycled, and economic benefits are generated.
The liquid working medium outlet at the lower part of the cold absorbing device 2 is connected with the liquid working medium inlet at the lower part of the cold releasing device 4 through a liquid discharging pipeline 6, and the gaseous working medium outlet at the upper part of the cold releasing device 4 is connected with the gaseous working medium inlet at the upper part of the cold absorbing device 2 through a steam inlet pipeline 5, so that a working medium circulation loop is formed. A certain amount of working medium is filled in the working medium circulation loop, a certain vacuum degree is kept through the vacuum keeping device 9, and the working medium in the working medium circulation loop is evaporated at minus 30 ℃ and condensed at about minus 35 ℃.
High-pressure low-temperature liquid flows out after entering the high-pressure pipeline 1 to be gasified, gaseous working media in the cold absorption device 2 absorb cold energy generated by the gasification of the high-pressure low-temperature liquid, the cold energy is condensed into liquid and flows into the cold release device 4 of the secondary refrigerant box 3, the secondary refrigerant absorbs heat from the secondary refrigerant and returns to the cold absorption device 2 in the high-pressure pipeline 1 after being gasified, and the cooled secondary refrigerant is conveyed to an external cold energy utilization device through a secondary refrigerant pump 8 to release cold energy (for example, the cold energy can be used for producing ice bricks or used for air conditioning refrigeration) and returns to the secondary refrigerant box 3.
In this embodiment, the heat pipe type heat exchangers are used for both the cold absorption device 2 and the cold release device 4, and the heat exchange mode of the working medium is boiling and condensing heat exchange (the working medium is condensed into liquid from gas in the cold absorption device 2, and the right liquid is evaporated into gas in the cold release device 4), which is more than 1000 times of the conventional convective heat transfer coefficient. The cold absorbing device 2 and the cold releasing device 4 are respectively vertically arranged in the high-pressure pipeline 1 and the refrigerating medium box 3. Therefore, after being condensed, the gaseous working medium in the cold absorption device 2 flows back to the cold release device 4 at the lower part by the self-weight, and automatically rises to the cold absorption device 2 at the upper part after the cold release device 4 is gasified, so that power equipment such as a circulating pump and the like can be omitted, the structure of the device is simplified, and the cost is reduced. Moreover, the gaseous working medium of the cold absorption device 2 is liquefied and then automatically flows back to the cold release device 4, so that the solidification phenomenon of the high-pressure cold absorption side is avoided.
As shown in fig. 2 and 3, the heat sink 2 has an overall cylindrical shape and includes an upper header pipe 12, a heat pipe 13, and a lower header pipe 14. The upper collecting pipe 12 is connected to the steam inlet pipe 5, and the lower collecting pipe 14 is connected to the liquid discharge pipe 6. The upper collecting branch pipe 12 comprises an upper collecting branch pipe 12a and an upper collecting main pipe 12b, the upper collecting branch pipe 12a is semicircular and is concentrically and symmetrically connected to two sides of the upper collecting main pipe 12b, and holes for connecting the heat pipes 13 are formed in the upper collecting branch pipe 12a at intervals. The structure of the lower collecting pipe 14 is the same as that of the upper collecting pipe 12, and comprises lower collecting branch pipes and lower collecting main pipes, wherein the lower collecting branch pipes are semicircular, are concentrically and symmetrically connected with the two sides of the lower collecting main pipes, and are provided with holes for connecting heat pipes at intervals. The heat pipes 13 are connected vertically between the upper and lower collecting branches 12, 14.
In the high-pressure pipeline 1, the high-pressure low-temperature liquid is gasified and then converted into gas to perform forced convection heat exchange, and because the convection heat exchange coefficient of the gas is low, fins are arranged outside the heat pipe 13, namely the heat pipe 13 adopts finned tubes, so that the heat exchange area can be increased, the defect of low gas side heat exchange coefficient is overcome, and the compactness, high efficiency, stability and reliability of the heat exchange process are ensured.
The structure of the cold releasing device 4 is basically the same as that of the cold absorbing device 2, and the cold releasing device 4 is soaked in the secondary refrigerant, which belongs to liquid phase heat exchange, so that the heat exchange coefficient is larger, fins do not need to be added outside heat pipes, and finned pipes do not need to be adopted.
The working process of the invention is as follows:
a. high-pressure low-temperature liquid gasification loop: after entering the high-pressure pipeline 1, the high-pressure low-temperature liquid is gasified along the shell pass and then flows out, and the cold energy generated by the gasification is absorbed by the cold absorption device 2.
b. A working medium circulation loop: the outside of the cold absorption device 2 is high-pressure low-temperature liquid to be gasified below 100 ℃, a gaseous working medium in the cold absorption device 2 is cooled by the high-pressure low-temperature liquid, is condensed at about minus 35 ℃, is further cooled to below minus 50 ℃, the condensed working medium flows back to the cold release device 4 by self weight, a secondary refrigerant is arranged outside the cold release device 4, has the temperature of minus 15 ℃, is the condensed working medium in the cold release device 4, has the temperature lower than minus 50 ℃, the working medium in the cold release device 4 is heated and evaporated, absorbs heat from the secondary refrigerant in the gasification process, and returns to the cold absorption device 2 from the steam exhaust pipeline 5 to complete a cycle.
c. A secondary refrigerant circulation circuit: the temperature of the secondary refrigerant entering the secondary refrigerant box 3 is-15 ℃, heat energy is released to the working medium in the cold release device 4, the temperature is reduced to about-20 ℃, the working medium is pressurized by the secondary refrigerant pump 8 and then flows out to exchange heat with the outside, and when the temperature reaches about-15 ℃, the working medium returns to the secondary refrigerant box 3 again. The temperature difference between the inlet and the outlet is about 5 ℃, and cold energy is continuously taken out of the system.
The above embodiments are only for illustrating the technical concept and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention accordingly, and not to limit the protection scope of the present invention accordingly. All equivalent changes or modifications made in accordance with the spirit of the present disclosure are intended to be covered by the scope of the present disclosure.
Claims (8)
1. The utility model provides a heat pipe type high pressure low temperature liquid gasification intensification process cold energy recovery unit which characterized in that: comprises a high-pressure side cold absorption system and a low-pressure side cold release system; the high-pressure side cold absorption system comprises a high-pressure pipeline and a cold absorption device arranged in the high-pressure pipeline, and the low-pressure side cold release system comprises a secondary refrigerant box and a cold release device arranged in the secondary refrigerant box; the liquid working medium outlet of the cold absorbing device is connected with the liquid working medium inlet of the cold releasing device, and the gaseous working medium outlet of the cold carrying and releasing device is connected with the gaseous working medium inlet of the cold absorbing device to form a working medium circulation loop; the secondary refrigerant box is filled with secondary refrigerant and is connected with an external cold energy utilization device through a secondary refrigerant pipeline and a secondary refrigerant pump to form a secondary refrigerant circulation loop; the high-pressure low-temperature liquid flows out after entering the high-pressure pipeline for gasification, the gaseous working medium in the cold absorption device absorbs cold energy generated by the gasification of the high-pressure low-temperature liquid, the cold energy is condensed into liquid and flows into the cold release device, the liquid returns to the cold absorption device after absorbing heat from the secondary refrigerant and being gasified, and the cooled secondary refrigerant is conveyed to an external cold energy utilization device through a secondary refrigerant pump to release cold energy and then returns to the secondary refrigerant box.
2. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 1, characterized in that: the pipe diameter of the high-pressure pipeline is larger than that of the high-pressure low-temperature liquid pipeline, and two ends of the high-pressure pipeline are in a conical shape with the pipe diameter gradually reduced and are connected with the high-pressure low-temperature liquid pipeline through flanges.
3. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 1, characterized in that: the cold absorbing device is cylindrical, including last collection house steward, heat pipe and collection house steward down, go up the collection house steward including the branch pipe that gathers and last the person in charge that gathers, go up the branch pipe semicircular in shape that gathers, the symmetric connection is in last the person in charge both sides that gather, the interval is provided with the hole that is used for connecting the heat pipe on the branch pipe that gathers on, the collection house steward includes the branch pipe that gathers down and gathers the person in charge down, the branch pipe semicircular in shape that gathers down, the symmetric connection gathers the person in charge both sides under, the interval is provided with the hole that is used for connecting the heat pipe on the branch pipe that gathers down, the heat pipe is many, vertical connection gathers at last the branch pipe and gathers down between the branch pipe.
4. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 3, characterized in that: the upper gathering branch pipe and the lower gathering branch pipe are multiple and are concentrically connected to two sides of the upper gathering main pipe and the lower gathering main pipe respectively.
5. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 3 or 4, characterized in that: the heat pipe is a finned pipe, the defect of low gas side heat exchange coefficient is overcome by increasing the heat exchange area, and the compactness, high efficiency, stability and reliability of the heat exchange process are guaranteed.
6. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 1, characterized in that: the working medium circulation loop is connected with a vacuum maintaining device, so that the working medium circulation loop maintains a certain vacuum degree.
7. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 1, characterized in that: the working medium in the working medium circulation loop is evaporated at minus 30 ℃ and condensed at about minus 35 ℃.
8. The heat pipe type high-pressure low-temperature liquid gasification warming process cold energy recovery device according to claim 7, characterized in that: the normal working temperature of the secondary refrigerant is between 15 ℃ below zero and 20 ℃ below zero.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110698336.XA CN113446881A (en) | 2021-06-23 | 2021-06-23 | Heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110698336.XA CN113446881A (en) | 2021-06-23 | 2021-06-23 | Heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device |
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|---|---|
| CN113446881A true CN113446881A (en) | 2021-09-28 |
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| CN202110698336.XA Pending CN113446881A (en) | 2021-06-23 | 2021-06-23 | Heat pipe type high-pressure low-temperature liquid gasification heating process cold energy recovery device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113891626A (en) * | 2021-10-09 | 2022-01-04 | 欧伏电气股份有限公司 | Secondary refrigerant circulating method and automatic circulating system for data center |
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| CN113891626A (en) * | 2021-10-09 | 2022-01-04 | 欧伏电气股份有限公司 | Secondary refrigerant circulating method and automatic circulating system for data center |
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Application publication date: 20210928 |