CN109357159B - Cryogenic supercritical fluid regasification experimental system and working method - Google Patents
Cryogenic supercritical fluid regasification experimental system and working method Download PDFInfo
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- CN109357159B CN109357159B CN201811354132.9A CN201811354132A CN109357159B CN 109357159 B CN109357159 B CN 109357159B CN 201811354132 A CN201811354132 A CN 201811354132A CN 109357159 B CN109357159 B CN 109357159B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
- F17C7/02—Discharging liquefied gases
- F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
- F17C13/02—Special adaptations of indicating, measuring, or monitoring equipment
- F17C13/026—Special adaptations of indicating, measuring, or monitoring equipment having the temperature as the parameter
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
- F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/03—Heat exchange with the fluid
- F17C2227/0302—Heat exchange with the fluid by heating
- F17C2227/0309—Heat exchange with the fluid by heating using another fluid
- F17C2227/0316—Water heating
Abstract
The invention discloses a cryogenic supercritical fluid regasification experimental system and a working method thereof. The hot water loop and the medium temperature medium loop exchange heat through the floating coil heat exchanger, and the medium temperature medium loop and the deep cooling supercritical fluid loop exchange heat through the supercritical fluid gasifier. The hot water loop comprises a floating coil heat exchanger, an electric heater, an expansion water tank, a hot water pump and the like which are sequentially communicated; the medium temperature medium loop comprises a floating coil heat exchanger, a supercritical fluid gasifier, a liquid storage device, a circulating pump and the like which are sequentially communicated; the cryogenic supercritical fluid loop comprises a liquid storage tank, an immersed pump, a pressure stabilizing tank, a supercritical fluid gasifier, a back pressure valve and the like which are sequentially communicated. The invention is suitable for the regasification of various supercritical fluids, and the medium temperature medium has high controllability and better engineering value.
Description
Technical Field
The invention relates to the technical field of cryogenic supercritical fluid heat transfer, in particular to a cryogenic supercritical fluid regasification experimental system which can meet the regasification requirements of various cryogenic supercritical fluids.
Background
Supercritical fluid is fluid with temperature and pressure higher than its critical state, and has the characteristics of viscosity and diffusion coefficient similar to that of gas, density and solvating power similar to that of liquid, and various properties of supercritical fluid are sensitive to temperature and pressure change. Cryogenic supercritical fluids generally refer to supercritical fluids having a temperature in the range of-40.15 ℃ to-196.15 ℃. Generally, industrial gases such as LNG, liquid oxygen, liquid hydrogen, liquid nitrogen, liquid carbon dioxide, etc. need to be stored and transported in a liquid form and then re-gasified at a terminal for use. In the case of LNG, since the LNG volume is only 1/600 of the Natural Gas (NG) volume, NG typically needs to be liquefied and then gasified for use in order to meet storage and remote transportation requirements. However, the critical temperature of LNG is-163 ℃, and the phenomenon of icing of a heat exchange medium or incomplete gasification is easily caused in the gasification process.
Therefore, the development of a system capable of satisfying the cryogenic supercritical fluid regasification is urgently needed. The deep-cooling supercritical fluid regasification system adopting the medium-temperature medium loop avoids direct heat exchange between a heat source and the supercritical fluid, indirectly transfers heat of the heat source to the supercritical fluid through the medium-temperature medium, can completely meet the requirement of the deep-cooling supercritical fluid regasification, and can effectively control the gasification amount.
The invention patent with application number 201280010015.5 entitled "apparatus for regasification of liquefied gas and method for producing regasified gas" discloses a system and method for regasifying low temperature liquefied gas. In the system, liquefied gas firstly flows through a heat exchanger for preheating, exchanges heat with a first heat exchanger, then flows into the heat exchanger for preheating as a heat source to exchange heat with incoming low-temperature liquefied gas, and then enters a second heat exchanger for regasification. However, the temperature of the liquefied gas cannot be obviously raised by using the liquefied gas after the first temperature rise to preheat the low-temperature liquefied gas, and the heat exchange between the liquefied gas after the temperature rise and the low-temperature liquefied gas is only carried out through temperature difference heat transfer due to the same flow of the liquefied gas in the pipeline, so that energy is wasted to a certain extent. In addition, the low-temperature liquefied gas in the first heat exchanger directly exchanges heat with water or seawater, so that the problem of icing is avoided, the heat exchange effect is influenced, and the operation efficiency of the system is integrally reduced. This patent adopts medium temperature medium step transfer heat, and the effectual icing problem of avoiding has frozen.
The invention patent with the application number of 201710014179.X and the name of LNG regasification system discloses an LNG regasification system, which takes seawater as a heat source, exchanges heat with the seawater for three times through an intermediate medium, transfers the heat to LNG and drives an expander to generate power at the same time, and achieves the purposes of generating power and regasifying LNG. However, the system realizes LNG regasification through multiple heat exchanges, so that the system structure is complex, the required seawater flow is huge, the energy consumption of a water pump is high, and in addition, the seawater temperature changes all the year round, and the stable operation of the system is influenced. In addition, the NG outlet temperature of the system cannot meet the use requirement, and the temperature needs to be increased again to meet the use requirement. The invention can meet the requirement of NG outlet temperature through one-time heat exchange, so that the system is not limited to region position limitation, can meet the experimental performance analysis of various cryogenic supercritical fluids, and has stable operation, simplicity and high efficiency.
Therefore, a system capable of operating at high efficiency and suitable for various cryogenic supercritical fluid regasification systems has become a difficult problem for cryogenic supercritical fluid regasification.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a cryogenic supercritical fluid regasification experimental system.
The invention can meet the requirements of regasification of various cryogenic supercritical fluids, can operate stably with high efficiency and is not limited by fields.
In order to achieve the aim, the technical scheme adopted by the invention for achieving the aim is as follows:
a cryogenic supercritical fluid regasification experimental system comprises a hot water loop, a medium temperature medium loop and a cryogenic supercritical fluid loop;
the hot water loop and the medium temperature medium loop exchange heat through a floating coil heat exchanger; the medium temperature medium loop and the deep cooling supercritical fluid loop exchange heat through the supercritical fluid gasifier; the hot water loop comprises a floating coil heat exchanger, an electric heater, an expansion water tank, a blow-down valve, a hot water pump and a three-way valve which are connected in sequence; the medium temperature medium loop comprises a floating coil heat exchanger, a supercritical fluid gasifier, a liquid storage device, a circulating pump and a three-way valve which are connected in sequence; the cryogenic supercritical fluid loop comprises a liquid storage tank, an immersed pump, a liquid outlet valve, a pressure stabilizing tank, a supercritical fluid gasifier and a back pressure valve which are connected in sequence;
further, a supercritical fluid gasifier in the supercritical fluid loop adopts PCHE;
further, the medium temperature medium of the medium temperature medium loop adopts freon refrigerant with lower boiling point, such as R290, R23 or propane;
further, the cryogenic supercritical fluid in the supercritical fluid loop is LNG, liquid nitrogen, liquid oxygen, liquid hydrogen or liquid carbon dioxide;
further, a blow-down valve of the hot water circuit is arranged at the lowest point of the expansion tank;
furthermore, a reversing port of a three-way valve in the hot water loop is connected with an outlet of the floating coil heat exchanger;
furthermore, a reversing port of a three-way valve in the medium temperature medium loop is connected with an inlet of the liquid storage device;
further, an immersed pump of the deep-cooling supercritical fluid circuit is placed at the lowest position in the liquid storage tank; (ii) a
In order to solve the problems in the prior art, the invention adopts another technical scheme that:
a working method of a cryogenic supercritical fluid regasification experimental system comprises the following steps: in the hot water loop, cold water is heated in the electric heater to raise the temperature, is pressurized by the hot water pump, flows through the three-way valve, enters the floating coil heat exchanger to exchange heat with the medium temperature medium to obtain cold energy reduced temperature, and then enters the electric heater again to heat, thereby completing circulation. The expansion tank has the functions of water supplement, constant pressure and expansion so as to stabilize the working pressure of the hot water loop. The three-way valve connects the hot water pump, the floating coil heat exchanger and the electric heater to realize variable flow regulation and match the change of heat exchange quantity;
in the medium temperature medium loop, liquid medium in the liquid reservoir is pressurized by a circulating pump, enters a floating coil heat exchanger through a three-way valve, is subjected to heat exchange vaporization with hot water, is pressurized, enters a supercritical fluid gasifier to exchange heat with a deep cooling supercritical fluid, is regasified, and is liquefied after the medium temperature medium obtains cold energy and returns to the liquid reservoir. The three-way valve connects the circulating pump, the floating coil heat exchanger and the inlet of the reservoir, when the vaporization quantity of the cryogenic supercritical fluid is small, the three-way valve is adjusted to reduce the flow of the medium temperature medium flowing into the floating coil heat exchanger and increase the flow of the medium temperature medium flowing into the reservoir; when the vaporization quantity of the cryogenic supercritical fluid is large, the adjustment method is opposite, so that the requirement of the vaporization quantity of the cryogenic supercritical fluid is matched;
in the cryogenic supercritical fluid loop, after a liquid outlet valve is opened, the low-temperature low-pressure cryogenic supercritical fluid is pressurized to a supercritical fluid state by an immersed pump in a liquid storage tank and flows out, the pressure is stabilized by a pressure stabilizing tank, then the low-temperature low-pressure cryogenic supercritical fluid enters a supercritical fluid gasifier to exchange heat with a medium-temperature medium, the temperature is raised for vaporization, and the low-temperature low-pressure cryogenic supercritical fluid is discharged through a back pressure valve. The purpose of the surge tank is to maintain the pressure in the circuit, and since the fluid is in a supercritical state after being pressurized, and its properties are close to those of gas, a gas surge tank is used here. A back pressure valve is arranged at the tail end of the system and realizes pressure adjustment through an internal spring, and when the system pressure is lower than the set pressure, the diaphragm blocks the pipeline under the action of the elasticity of the spring to form a pressure-holding mode, so that the inlet pressure reaches the rated pressure; when the system pressure is higher than the set pressure, the diaphragm compresses the spring and the pipeline is connected, so that the outlet pressure is stabilized.
The cryogenic supercritical fluid regasification experimental system and method provided by the invention have the outstanding advantages in the following aspects:
1. by adding the medium-temperature medium loop, the direct heat exchange between a heat source and the deep-cooling supercritical fluid is avoided, and simultaneously, a large amount of latent heat is released by utilizing the phase change heat exchange of the medium-temperature medium, so that the possibility of icing of the supercritical fluid gasifier is effectively reduced, and the high-efficiency operation of the gasifier is ensured;
2. because the medium temperature medium has high controllability, the medium temperature medium can be matched with the critical temperature, pressure and flow of different cryogenic supercritical fluids to achieve the optimal heat exchange effect;
3. by adopting the PCHE gasifier, the regasification efficiency is high, and the size of the gasifier is effectively reduced, so that the overall floor area of a regasification system is reduced, and the regasification requirement of a limited space is met;
4. the flow opening of the reversing port of the three-way valve of the hot water loop and the medium temperature loop is controlled, so that the demand of the gas chemical quantity can be adjusted and matched quickly in time;
5. all the devices of the system are connected by stainless steel pipes in a welding or flange connection mode, so that the requirement of high pressure in the system can be met, and the system can be flexibly installed according to the field condition;
6. the invention solves the technical problem of the cryogenic supercritical fluid regasification system, so the invention has practical engineering significance, can be referred by engineering personnel and has considerable application prospect.
Drawings
FIG. 1 is a schematic diagram of the construction of a cryogenic supercritical fluid regasification experimental system according to the present invention;
the reference numbers in the figures illustrate: 1-floating coil heat exchanger, 2-electric heater, 3-expansion water tank, 4-blowoff valve, 5-hot water pump, 6-three-way valve, 7-supercritical fluid gasifier, 8-reservoir, 9-circulating pump, 10-three-way valve, 11-reservoir, 12-immersed pump, 13-liquid outlet valve, 14-surge tank, 15-backpressure valve.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
As shown in fig. 1, a cryogenic supercritical fluid regasification experimental system of the present invention includes a hot water circuit, a medium temperature medium circuit, and a cryogenic supercritical fluid circuit; the method is characterized in that: the hot water loop and the medium temperature medium loop exchange heat through the floating coil heat exchanger 1; the medium temperature medium loop and the deep cooling supercritical fluid loop exchange heat through a supercritical fluid gasifier 7; the hot water loop comprises a floating coil heat exchanger 1, an electric heater 2, an expansion water tank 3, a blow-down valve 4, a hot water pump 5 and a three-way valve 6 which are connected in sequence; the medium temperature medium loop comprises a floating coil heat exchanger 1, a supercritical fluid gasifier 7, a liquid storage device 8, a circulating pump 9 and a three-way valve 10 which are connected in sequence; the cryogenic supercritical fluid loop comprises a liquid storage tank 11, an immersed pump 12, a liquid outlet valve 13, a pressure stabilizing tank 14, a supercritical fluid gasifier 7 and a back pressure valve 15 which are connected in sequence;
as shown in fig. 1, the supercritical fluid gasifier 7 adopts a printed plate gasifier, and the printed plate gasifier not only has high regasification efficiency, but also has a compact structure, so that the overall floor area of the regasification system is greatly reduced to meet the regasification requirement of a limited space;
as shown in FIG. 1, the intermediate temperature medium of the intermediate temperature medium circuit adopts freon refrigerant with lower boiling point, such as R290, R23 or propane. Because the medium temperature medium has high controllability, the medium temperature medium can be matched according to the critical temperature, pressure and flow of different cryogenic supercritical fluids to achieve the optimal heat exchange effect, and simultaneously, the phase change heat exchange of the medium temperature medium is utilized to release a large amount of latent heat, so that the possibility of icing of the supercritical fluid gasifier 7 is effectively reduced, and the high-efficiency operation of the gasifier is ensured;
as shown in fig. 1, the cryogenic supercritical fluid of the cryogenic supercritical fluid circuit is LNG, liquid nitrogen, liquid oxygen, liquid hydrogen, and liquid carbon dioxide.
As shown in fig. 1, a blowoff valve 4 of the hot water loop is arranged at the lowest point of the expansion tank 3 to prevent impurities in water from blocking pipelines and affecting the stable operation of the system;
as shown in fig. 1, a three-way valve 6 is arranged at an inlet of the floating coil heat exchanger 1 of the hot water loop, and a reversing port of the three-way valve 6 is connected with an outlet of the floating coil heat exchanger 1, and is used for adjusting hot water flow and outlet temperature during system operation so as to match the requirement of medium temperature medium heat exchange quantity;
as shown in fig. 1, the intermediate temperature medium loop is provided with a three-way valve 10 at the inlet of the floating coil heat exchanger 1, and a reversing port of the three-way valve 10 is connected with the inlet of the reservoir 8, and is used for adjusting the flow rate and the outlet temperature of the intermediate temperature medium when the system operates, so as to match the requirement of the gasification amount of the cryogenic supercritical fluid;
as shown in fig. 1, the deep-cooling supercritical fluid circuit immersed pump 12 is placed at the lowest position in the liquid storage tank 11, and the immersed pump 12 is ensured to be always under the liquid level and used for pressurizing the deep-cooling supercritical fluid to the supercritical state and providing power for the deep-cooling supercritical fluid circuit;
as the further supplement, in the hot water loop, cold water is heated in the electric heater 2 to raise the temperature, is pressurized by the hot water pump 5, then flows through the three-way valve 6, enters the floating coil heat exchanger 1 to exchange heat with the medium temperature medium to obtain cold energy, lowers the temperature, and then enters the electric heater 2 again to heat, thereby completing the circulation. The expansion tank 3 has the functions of water supplement, constant pressure and expansion so as to stabilize the working pressure of the hot water loop. The three-way valve 6 connects the hot water pump, the floating coil heat exchanger and the electric heater to realize variable flow regulation and match the change of the heat exchange quantity of the medium temperature medium;
in the medium temperature medium loop, the liquid medium temperature medium in the liquid reservoir 8 is subjected to pressure increase through a circulating pump 9, enters the floating coil heat exchanger 1 through a three-way valve 10, is subjected to heat exchange vaporization with hot water, is subjected to temperature increase, enters the supercritical fluid gasifier 7 to exchange heat with the deep-cooling supercritical fluid, is re-gasified, and is liquefied after the medium temperature medium obtains cold energy and returns to the liquid reservoir 8. The three-way valve 10 connects the circulating pump 9, the floating coil heat exchanger 1 and the inlet of the liquid storage device 8, when the vaporization quantity of the cryogenic supercritical fluid is small, the three-way valve 10 is adjusted to reduce the flow of the medium temperature medium flowing into the floating coil heat exchanger 1 and increase the flow of the medium temperature medium flowing into the liquid storage device 8; when the vaporization quantity of the cryogenic supercritical fluid is large, the adjustment method is opposite, so that the requirement of the vaporization quantity of the cryogenic supercritical fluid is matched;
in the cryogenic supercritical fluid loop, after a liquid outlet valve 13 is opened, the low-temperature low-pressure cryogenic supercritical fluid is pressurized to a supercritical fluid state by an immersed pump 12 in a liquid storage tank 11 and then flows out, enters a supercritical fluid gasifier 7 to exchange heat with a medium-temperature medium after the pressure is stabilized by a pressure stabilizing tank 14, is heated and vaporized, and is discharged through a back pressure valve 15. The purpose of surge tank 14 is to maintain the pressure in the circuit, and since the fluid is in a supercritical state after being pressurized, and its properties are close to those of gas, a gas surge tank is used here. A back pressure valve 15 is arranged at the tail end of the system, the back pressure valve 15 realizes pressure adjustment through an internal spring, and when the system pressure is lower than the set pressure, the diaphragm blocks a pipeline under the action of the elasticity of the spring to form pressure build-up, so that the inlet pressure reaches the rated pressure; when the system pressure is higher than the set pressure, the diaphragm compresses the spring and the pipeline is connected, so that the outlet pressure is stabilized.
The foregoing is only a preferred embodiment of the present invention. Of course, the present invention can have other various embodiments, and a plurality of embodiments can be used together as needed, and any person skilled in the art can make various corresponding changes and modifications according to the present invention without departing from the spirit and essence of the present invention. All technical solutions which are formed by adopting equivalent substitutions or equivalent transformations shall fall within the protection scope of the appended claims.
Claims (6)
1. A cryogenic supercritical fluid regasification experimental system comprises a hot water loop, a medium temperature medium loop and a cryogenic supercritical fluid loop; the method is characterized in that: the hot water loop and the medium temperature medium loop exchange heat through a floating coil heat exchanger (1); the medium temperature medium loop and the deep cooling supercritical fluid loop exchange heat through a supercritical fluid gasifier (7); the hot water loop comprises a floating coil heat exchanger (1), an electric heater (2), an expansion water tank (3), a blow-down valve (4), a hot water pump (5) and a three-way valve I (6) which are connected in sequence; the medium temperature medium loop comprises a floating coil heat exchanger (1), a supercritical fluid gasifier (7), a liquid storage device (8), a circulating pump (9) and a three-way valve II (10) which are connected in sequence; the cryogenic supercritical fluid loop comprises a liquid storage tank (11), an immersed pump (12), a liquid outlet valve (13), a pressure stabilizing tank (14), a supercritical fluid gasifier (7) and a back pressure valve (15) which are connected in sequence; wherein, a blowoff valve (4) of the hot water loop is arranged at the lowest point of the expansion tank (3); a reversing port of a first three-way valve (6) in the hot water loop is connected with an outlet of the floating coil heat exchanger (1); a reversing port of a second three-way valve (10) in the medium temperature medium loop is connected with an inlet of the liquid storage device (8); the deep cooling supercritical fluid loop immersed pump (12) is placed at the lowest position in the liquid storage tank (11).
2. The cryogenic supercritical fluid regasification experimental system according to claim 1, wherein: the supercritical fluid gasifier (7) is a printed plate gasifier.
3. The cryogenic supercritical fluid regasification experimental system according to claim 1, wherein: the medium temperature medium of the medium temperature medium loop adopts Freon refrigerant.
4. The cryogenic supercritical fluid regasification experimental system according to claim 3, wherein: the Freon refrigerant is R290, R23 or propane.
5. The cryogenic supercritical fluid regasification experimental system according to claim 1, wherein: the cryogenic supercritical fluid of the cryogenic supercritical fluid loop is liquefied natural gas, liquid nitrogen, liquid oxygen, liquid hydrogen or liquid carbon dioxide.
6. A method for operating a cryogenic supercritical fluid regasification laboratory system according to any one of claims 1 to 5, wherein: in the hot water loop, cold water is heated in the electric heater (2) to raise the temperature, is pressurized by the hot water pump (5), flows through the three-way valve I (6), enters the floating coil heat exchanger (1) to exchange heat with a medium temperature medium to obtain cold energy, lowers the temperature, and then enters the electric heater (2) again to heat to complete circulation; in the medium temperature medium loop, the liquid medium temperature medium in the liquid reservoir (8) is subjected to pressure rise through a circulating pump (9), enters the floating coil heat exchanger (1) through a three-way valve II (10), is subjected to heat exchange vaporization with hot water, is subjected to temperature rise, enters the supercritical fluid gasifier (7) to exchange heat with the deep-cooling supercritical fluid, and is liquefied and returned to the liquid reservoir (8) after the medium temperature medium obtains cold energy; after the liquid outlet valve (13) is opened, the cryogenic supercritical fluid loop is pressurized to a supercritical fluid state by the immersed pump (12) in the liquid storage tank (11) and then flows out, and after the pressure is stabilized by the pressure stabilizing tank (14), the cryogenic supercritical fluid enters the supercritical fluid gasifier (7) to exchange heat with a medium temperature medium, is heated and vaporized, and is discharged for use through the back pressure valve (15).
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| CN111692524A (en) * | 2020-06-19 | 2020-09-22 | 江苏科技大学 | LNG regasification experimental system and experimental method |
| JP2023045007A (en) * | 2021-09-21 | 2023-04-03 | 株式会社神戸製鋼所 | Liquid hydrogen vaporization device and generation method for generating hydrogen |
| CN114576555B (en) * | 2022-03-17 | 2023-08-22 | 广西西江重工有限责任公司 | Ship LNG vaporization system applied to low-temperature environment and application method |
| CN115382585B (en) * | 2022-08-30 | 2023-10-24 | 合肥通用机械研究院有限公司 | Low-temperature vacuum composite experimental device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202832698U (en) * | 2012-07-04 | 2013-03-27 | 武汉东测科技有限责任公司 | Improved engine oil temperature control device |
| CN202914168U (en) * | 2012-07-04 | 2013-05-01 | 武汉东测科技有限责任公司 | Improved engine coolant temperature control device |
| CN203629017U (en) * | 2012-12-25 | 2014-06-04 | 三菱电机株式会社 | Air conditioning device |
| CN203797763U (en) * | 2014-04-05 | 2014-08-27 | 刘立臣 | Solar, electric and combustion medium hybrid heat and domestic hot water supply unit |
| CN204440208U (en) * | 2015-02-05 | 2015-07-01 | 中国第一汽车股份有限公司 | A kind of coolant temperature for engine rig test and volume control device |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004031644A1 (en) * | 2002-10-04 | 2004-04-15 | Hamworthy Kse A.S. | Regasification system and method |
| CA2615850C (en) * | 2005-07-18 | 2011-01-25 | Fluor Technologies Corporation | Configurations and methods for power generation in lng regasification terminals |
| KR101641394B1 (en) * | 2008-07-15 | 2016-07-20 | 크라이오스타 에스아에스 | Conversion of liquefied natural gas |
| KR20150080087A (en) * | 2013-12-30 | 2015-07-09 | 현대중공업 주식회사 | A Treatment System Liquefied Gas |
| CN205448814U (en) * | 2016-03-10 | 2016-08-10 | 西安交通大学 | A middle medium heat transfer device for supercritical water oxidation system |
| CN105776492B (en) * | 2016-03-10 | 2018-08-10 | 西安交通大学 | A kind of indirect heat exchange type supercritical water oxidation system and control method |
| CN106870938B (en) * | 2017-03-09 | 2019-12-10 | 中国石油大学(华东) | Tube-fin type intermediate medium gasifier |
| CN106895255B (en) * | 2017-04-07 | 2023-09-29 | 山东德裕石油装备有限公司 | LNG cold energy utilization system for cooling workshop |
-
2018
- 2018-11-14 CN CN201811354132.9A patent/CN109357159B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202832698U (en) * | 2012-07-04 | 2013-03-27 | 武汉东测科技有限责任公司 | Improved engine oil temperature control device |
| CN202914168U (en) * | 2012-07-04 | 2013-05-01 | 武汉东测科技有限责任公司 | Improved engine coolant temperature control device |
| CN203629017U (en) * | 2012-12-25 | 2014-06-04 | 三菱电机株式会社 | Air conditioning device |
| CN203797763U (en) * | 2014-04-05 | 2014-08-27 | 刘立臣 | Solar, electric and combustion medium hybrid heat and domestic hot water supply unit |
| CN204440208U (en) * | 2015-02-05 | 2015-07-01 | 中国第一汽车股份有限公司 | A kind of coolant temperature for engine rig test and volume control device |
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