CN210595964U - NG cold air generating device - Google Patents
NG cold air generating device Download PDFInfo
- Publication number
- CN210595964U CN210595964U CN201921141706.4U CN201921141706U CN210595964U CN 210595964 U CN210595964 U CN 210595964U CN 201921141706 U CN201921141706 U CN 201921141706U CN 210595964 U CN210595964 U CN 210595964U
- Authority
- CN
- China
- Prior art keywords
- lng
- inlet
- gas
- liquid separator
- entry
- 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.)
- Withdrawn - After Issue
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 160
- 239000003345 natural gas Substances 0.000 claims abstract description 80
- 239000007788 liquid Substances 0.000 claims abstract description 66
- 239000007789 gas Substances 0.000 claims abstract description 58
- 238000002156 mixing Methods 0.000 claims abstract description 33
- 238000004378 air conditioning Methods 0.000 claims abstract description 11
- 238000007599 discharging Methods 0.000 claims abstract description 11
- 230000003068 static effect Effects 0.000 claims description 12
- 238000009413 insulation Methods 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 6
- 238000000889 atomisation Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 17
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000002309 gasification Methods 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 description 133
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- 238000001816 cooling Methods 0.000 description 10
- 241000234295 Musa Species 0.000 description 4
- 235000018290 Musa x paradisiaca Nutrition 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- NLOAOXIUYAGBGO-UHFFFAOYSA-N C.[O] Chemical compound C.[O] NLOAOXIUYAGBGO-UHFFFAOYSA-N 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005429 filling process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Images
Landscapes
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The utility model relates to a NG cold air generating device, which comprises an LNG discharging tank, an LNG mixing device and an LNG gas-liquid separator; LNG discharges the LNG export of jar and links to each other with LNG mixing arrangement's LNG entry, and LNG mixing arrangement's NG entry linkage normal atmospheric temperature natural gas line in the LNG station, LNG mixing arrangement's NG atomized gas exit linkage LNG vapour and liquid separator's NG atomized gas entry, LNG vapour and liquid separator's condensate outlet connection LNG discharges the backward flow liquid entry of jar, and LNG vapour and liquid separator's NG air conditioning exit linkage NG air conditioning eduction tube. The utility model discloses utilize NG's sensible heat gasification LNG, the NG air conditioning of production is used for LNG pipe-line system's precooling process, and NG air conditioning generating device has simple structure, with low costs and safe and reliable's characteristics.
Description
Technical Field
The utility model relates to a LNG pipeline precooling technical field especially relates to a NG air conditioning generating device.
Background
The process of cooling the LNG pipeline system from ambient temperature to operating temperature is referred to as pre-chilling. In the precooling process, a certain amount of low-temperature working medium needs to be evaporated in order to cool the pipeline, the heat insulation layer and the surrounding soil, and the thermal stability state can be achieved after a long time. The design calculation of the precooling process is to determine the consumption of the low-temperature medium and the precooling time, and the precooling process of the LNG pipeline system is a complex heat transfer process. The LNG pipeline system can utilize latent heat of vaporization of the low-temperature working medium and sensible heat absorbed when the temperature of the vaporized gas rises in the pre-cooling process, and the consumption of the low-temperature working medium required in the pre-cooling process is changed along with the utilization degree of the sensible heat.
The LNG transfer pipeline, the cryogenic pipeline and the cryogenic tank in the LNG vaporization station are first fully cooled, i.e., pre-cooled, before cryogenic liquid is formally introduced. If LNG is suddenly injected into a normal-temperature pipeline, the pipeline can be rapidly contracted, and the control of the precooling process is very important in order to avoid the damage of the pipeline structure due to quenching. The bottom of the pipeline is in direct contact with boiling LNG, the temperature is relatively low, nucleate boiling or film boiling occurs in the pipeline due to the fact that the LNG absorbs heat of pipeline materials, the generated NG fills the top of the pipeline, the temperature of the top of the pipeline is relatively high, and the temperature gradient on the cross section of the pipeline can cause a banana effect. Namely: due to the fact that the top and the bottom of the pipeline are not shrunk uniformly, the pipeline system is deformed unpredictably, and further damage to the pipeline, the support, the expansion joint and the connecting flange is caused, therefore, in the case of start-up after production and overhaul of the LNG pipeline system, pre-cooling of the pipeline system is required to be carried out, the pre-cooling process is required to be carried out gradually and slowly, and according to relevant operation experience, the cooling rate of the pipeline system is controlled to be safe when the cooling rate is controlled to be about 50 ℃/h. When the temperature of the LNG pipeline system reaches-95 ℃ to-118 ℃, the LNG pipeline system can be put into operation formally.
At present, a low-temperature working medium used for precooling an LNG pipeline system is usually liquid nitrogen, the liquid nitrogen is transported to the vicinity of an LNG device by a plurality of large tank trucks and is gasified by absorbing latent heat of air in a vaporizer, the system pressure in the process is higher than the normal pressure, and related equipment is a pressure container. Because the temperature of the liquid nitrogen is lower than that of the LNG, the probability of banana effect of the pipeline system is higher and the time consumed for the whole pipeline system to finish precooling is longer when precooling operation is carried out. And because a large amount of liquid nitrogen needs to be purchased additionally, the precooling process is high in cost and long in preparation time.
By carrying out model analysis on the precooling operation of the LNG pipeline system, the ideal low-temperature working medium can be determined to be low-temperature gas, and the condition that the low-temperature working medium presents a gas-liquid two-phase state in the pipeline system is avoided as much as possible, because the gas-liquid two-phase state is the root cause of the banana effect of the pipeline. In engineering practice, the lower temperature limit for precooling an LNG pipeline system is the dew point of clean NG (around-120 ℃). When the low-temperature gas enters the pipeline system for pre-cooling, the temperature difference does not exist in the pipeline, the temperature on the circumference of the pipeline is uniform, and the pipeline system is gradually cooled along the extension direction along with the diffusion of the low-temperature gas in the pipeline. Such a pre-cooling process is performed slowly with the diffusion of the cryogenic gas, reducing the probability of deformation of the piping system. When the temperature of the pipeline system gradually drops and reaches the dew point of the low-temperature gas, the low-temperature working medium is in a gas-liquid two-phase state again. Therefore, the ideal low temperature working medium should have such physical properties: the dew point of the LNG system is close to the dew point of the LNG and at least cannot be too high, otherwise the target temperature is not reached during pre-cooling operation and a gas-liquid two-phase state is generated prematurely. And the dew point of the nitrogen after air separation is about-69 ℃, so that the liquid nitrogen is not suitable to be used as a working medium in the second half of the LNG precooling operation. Liquid nitrogen is widely used for precooling operation of LNG pipeline systems only because of its relatively easy availability and relatively low boiling point.
Disclosure of Invention
The utility model provides a NG cold air generating device, which selects NG and LNG as working medium, uses the sensible heat of NG to gasify LNG, and the generated NG cold air is used in the precooling process of an LNG pipeline system, without an additional vaporizer, an additional power and an external liquid nitrogen; the NG cold air generating device has the characteristics of simple structure, low cost, safety and reliability.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
an NG cold gas generating device comprises an LNG discharging tank, an LNG mixing device and an LNG gas-liquid separator; the LNG discharge tank is provided with an LNG outlet and a reflux inlet, the LNG mixing device is provided with an NG inlet, an LNG inlet and an NG atomization gas outlet, and the LNG gas-liquid separator is provided with an NG atomization gas inlet, an NG cold gas outlet and a condensate outlet; LNG discharges the LNG export of jar and links to each other with LNG mixing arrangement's LNG entry, and LNG mixing arrangement's NG entry linkage normal atmospheric temperature natural gas line in the LNG station, LNG mixing arrangement's NG atomized gas exit linkage LNG vapour and liquid separator's NG atomized gas entry, LNG vapour and liquid separator's condensate outlet connection LNG discharges the backward flow liquid entry of jar, and LNG vapour and liquid separator's NG air conditioning exit linkage NG air conditioning eduction tube.
The LNG discharging tank is a closed pressure container with a horizontal tank, a vertical tank or a ship-shaped groove structure, a pressure safety valve is arranged at the top of the LNG discharging tank, and a heat insulation layer is arranged on the outer layer of the LNG discharging tank.
The LNG mixing device comprises a premixing section and a static mixer, wherein the premixing section is provided with an NG inlet, an LNG inlet and a mixed gas outlet, the static mixer is provided with a mixed gas inlet and an NG atomized gas outlet, and the mixed gas outlet of the premixing section is connected with the mixed gas inlet of the static mixer; a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge are respectively arranged on the NG inlet pipe connected with the NG inlet and the LNG inlet pipe connected with the LNG inlet; the outer layer of the LNG mixing device is provided with a heat insulation layer.
The premixing section is of a three-way pipe structure, an NG inlet and a mixed gas outlet are arranged oppositely in the three-way pipe structure, and a Venturi nozzle is arranged at an LNG inlet.
The premixing section is of an inner sleeve and an outer sleeve structure, one end of the inner sleeve is an NG inlet, the same end of the annular channel between the inner sleeve and the outer sleeve is an LNG inlet, the other end of the inner sleeve extends to the middle of the outer sleeve, and the other end of the outer sleeve is a mixed gas outlet.
Premixing section is for abreast double-barrelled structure, and double-barrelled LNG inlet tube and NG inlet tube of being respectively, and the one end of LNG inlet tube is the LNG entry, and the one end of NG inlet tube is the NG entry, and the LNG inlet tube communicates with the middle part of NG inlet tube, and the gas mixture export is established to the other end.
The LNG gas-liquid separator is a cyclone type, vortex type or column plate type gas-liquid separator, and a heat insulation layer is arranged on the outer layer of the LNG gas-liquid separator; and a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flow meter are arranged on the NG cold air delivery pipe, and a valve, a thermometer and a flow meter are arranged on a pipeline connecting a condensate outlet of the LNG gas-liquid separator and a reflux liquid inlet of the LNG discharge tank.
Compared with the prior art, the beneficial effects of the utility model are that:
1) the working medium can be directly obtained from the LNG plant station, and no external liquid nitrogen is needed, so that a series of equipment for loading, unloading and introducing the liquid nitrogen can be saved;
2) LNG is gasified by utilizing the sensible heat of the natural gas at normal temperature without a vaporizer and an additional heat source;
3) the NG cold air generating device is simple in structure, small in equipment occupied area and particularly suitable for large and medium LNG plants;
4) the utility model can realize the stable control of the precooling process by collecting the temperature, flow and pressure data of various materials, is safe and reliable in the process, greatly reduces the risk of the pipeline system generating banana effect, and is helpful to improve the production efficiency, reduce the operation cost and improve the safety of the LNG system;
5) but precooling theory of operation wide application in other cryogenic liquids pipeline's precooling, like liquid nitrogen, liquid oxygen and liquid hydrogen etc..
Drawings
Fig. 1 is a schematic structural diagram of a NG cold air generator according to the present invention.
Fig. 2 is the structural schematic diagram of the LNG mixing device of the present invention.
Fig. 3 is the structural schematic diagram of the LNG gas-liquid separator of the present invention.
Fig. 4 is a process flow diagram of the NG cold air generating device of the present invention.
In the figure: LNG discharge tank 2, LNG mixing device 21, NG inlet 22, LNG inlet 23, Venturi nozzle 24, static mixer 3, LNG gas-liquid separator 31, NG atomized gas inlet 32, NG cold gas outlet 33, condensate outlet
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in fig. 1, the NG cold air generating device of the present invention includes an LNG discharge tank 1, an LNG mixing device 2, and an LNG gas-liquid separator 3; the LNG discharge tank 1 is provided with an LNG outlet and a reflux inlet, the LNG mixing device 2 is provided with an NG inlet 21, an LNG inlet 22 and an NG atomized gas outlet (shown in figure 2), and the LNG gas-liquid separator 3 is provided with an NG atomized gas inlet 31, an NG cold gas outlet 32 and a condensate outlet 33 (shown in figure 3); LNG discharges jar 1's LNG export and LNG mixing arrangement 2's LNG entry 22 and links to each other, and LNG mixing arrangement 2's NG entry 21 connects the normal atmospheric temperature natural gas line in the LNG station, and LNG mixing arrangement 2's NG atomizing gas exit linkage LNG vapour and liquid separator 3's NG atomizing gas entry 31, and LNG vapour and liquid separator 3's condensate outlet connection 33 connects LNG and discharges jar 1's backward flow liquid entry, and LNG vapour and liquid separator 3's NG cold air export 32 connects NG cold air eduction tube.
The LNG discharging tank 1 is a closed pressure container with a horizontal tank, a vertical tank or a ship-shaped groove structure, a pressure safety valve is arranged at the top of the LNG discharging tank, and a heat insulation layer is arranged on the outer layer of the LNG discharging tank.
The LNG mixing device 2 consists of a premixing section and a static mixer 24, wherein the premixing section is provided with an NG inlet 21, an LNG inlet 22 and a mixed gas outlet, the static mixer 24 is provided with a mixed gas inlet and an NG atomized gas outlet, and the mixed gas outlet of the premixing section is connected with the mixed gas inlet of the static mixer 24; a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge are respectively arranged on the NG inlet pipe connected with the NG inlet 21 and the LNG inlet pipe connected with the LNG inlet 22; the outer layer of the LNG mixing device 2 is provided with a heat insulation layer.
As shown in fig. 2, the premixing section is a three-way pipe structure, the NG inlet 21 and the mixed gas outlet are arranged opposite to each other in the three-way pipe structure, and the LNG inlet 22 is provided with a venturi nozzle 23.
The premixing section is of an inner sleeve and an outer sleeve structure, one end of the inner sleeve is an NG inlet, the same end of the annular channel between the inner sleeve and the outer sleeve is an LNG inlet, the other end of the inner sleeve extends to the middle of the outer sleeve, and the other end of the outer sleeve is a mixed gas outlet.
Premixing section is for abreast double-barrelled structure, and double-barrelled LNG inlet tube and NG inlet tube of being respectively, and the one end of LNG inlet tube is the LNG entry, and the one end of NG inlet tube is the NG entry, and the LNG inlet tube communicates with the middle part of NG inlet tube, and the gas mixture export is established to the other end.
The LNG gas-liquid separator 3 is a cyclone type, vortex type or column plate type gas-liquid separator, and a heat insulation layer is arranged on the outer layer of the LNG gas-liquid separator 3; the NG cold air eduction tube is provided with a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flow meter, and the pipeline connecting the condensate outlet 33 of the LNG gas-liquid separator 3 and the reflux inlet of the LNG discharging tank 1 is provided with a valve, a thermometer and a flow meter.
An LNG pipeline precooling apparatus utilizes normal atmospheric temperature NG's sensible heat gasification LNG to form NG air conditioning, carries out the precooling with NG air conditioning to the LNG pipeline.
As shown in fig. 4, the utility model relates to an operating method of LNG pipeline precooling apparatus specifically is: the LNG from the LNG discharging tank 1 and normal-temperature NG are fully mixed in an LNG mixing device 2 to generate low-temperature NG atomized gas, the low-temperature NG atomized gas is separated by an LNG gas-liquid separator 3 to obtain dry NG cold gas, and the dry NG cold gas is used as precooling circulating gas before LNG pipelines and equipment are started; the liquid separated by the LNG gas-liquid separator 3 is returned to the LNG discharge tank 1.
With the LNG mixing arrangement (as shown in fig. 2) that adopts three-way pipe structure to mix the section in advance as an example, LNG pipeline precooling apparatus's theory of operation as follows: in the premixing section of the LNG mixing device 2, LNG (liquefied natural gas at a temperature of about-165 ℃) sprayed by the venturi nozzle 23 is primarily mixed with normal-temperature Natural Gas (NG), the vaporized low-temperature natural gas and the normal-temperature natural gas enter the static mixer 24 to be uniformly mixed, and low-temperature natural gas (NG atomized gas at a temperature of about-158 ℃) containing fog drops coming out of the static mixer 24 enters the LNG gas-liquid separator 3 to be separated from gas and liquid through adsorption and impact. The temperature and the flow of the output NG cold air are regulated and controlled by regulating the flow ratio of the two materials in the LNG mixing device 2. And the separated dry NG cold gas (low-temperature natural gas) enters an LNG pipeline system to be used for precooling circulation before starting of pipelines and equipment. The separated liquid (re-condensed LNG) is accumulated at the bottom of the LNG gas-liquid separator 3, and after a certain amount of the accumulated liquid is accumulated, the liquid is periodically returned to the LNG discharge tank 1 by opening a valve.
With the rapid increase of the demand of China on LNG, more large and medium LNG plants are built in coastal areas, and the NG cold air generating device has wider application prospect. Due to the fact that the liquid oxygen-methane type space launching technology is mature day by day, the liquid oxygen-methane type space launching device has a sufficient application prospect in the fuel filling process of LNG.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (7)
1. The NG cold gas generation device is characterized by comprising an LNG discharge tank, an LNG mixing device and an LNG gas-liquid separator; the LNG discharge tank is provided with an LNG outlet and a reflux inlet, the LNG mixing device is provided with an NG inlet, an LNG inlet and an NG atomization gas outlet, and the LNG gas-liquid separator is provided with an NG atomization gas inlet, an NG cold gas outlet and a condensate outlet; LNG discharges the LNG export of jar and links to each other with LNG mixing arrangement's LNG entry, and LNG mixing arrangement's NG entry linkage normal atmospheric temperature natural gas line in the LNG station, LNG mixing arrangement's NG atomized gas exit linkage LNG vapour and liquid separator's NG atomized gas entry, LNG vapour and liquid separator's condensate outlet connection LNG discharges the backward flow liquid entry of jar, and LNG vapour and liquid separator's NG air conditioning exit linkage NG air conditioning eduction tube.
2. An NG cold air generation device according to claim 1, wherein said LNG discharging tank is a closed pressure vessel of a horizontal tank, a vertical tank or a ship-shaped trough structure, a pressure safety valve is arranged at the top, and a heat insulating layer is arranged at the outer layer.
3. The NG cold air generation device of claim 1, wherein the LNG mixing device comprises a premixing section and a static mixer, the premixing section is provided with an NG inlet, an LNG inlet and a mixed gas outlet, the static mixer is provided with a mixed gas inlet and an NG atomized gas outlet, and the mixed gas outlet of the premixing section is connected with the mixed gas inlet of the static mixer; a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge are respectively arranged on the NG inlet pipe connected with the NG inlet and the LNG inlet pipe connected with the LNG inlet; the outer layer of the LNG mixing device is provided with a heat insulation layer.
4. The NG cold air generation device of claim 3, wherein the pre-mixing section is a three-way pipe structure, an NG inlet and a mixed gas outlet are arranged in the three-way pipe structure, and a Venturi nozzle is arranged at an LNG inlet.
5. The NG cold air generation device of claim 3, wherein the premixing section is of an inner-outer sleeve structure, one end of the inner sleeve is an NG inlet, the same end of the annular channel between the inner sleeve and the outer sleeve is an LNG inlet, the other end of the inner sleeve extends to the middle of the outer sleeve, and the other end of the outer sleeve is a mixed air outlet.
6. The NG cold air generation device of claim 3, wherein the pre-mixing section is of a parallel double-pipe structure, the double pipes are an LNG inlet pipe and an NG inlet pipe respectively, one end of the LNG inlet pipe is an LNG inlet, one end of the NG inlet pipe is an NG inlet, the LNG inlet pipe is communicated with the middle of the NG inlet pipe, and the other end of the LNG inlet pipe is provided with a mixed air outlet.
7. The NG cold gas generation device of claim 1, wherein the LNG gas-liquid separator is a cyclone type, a vortex type or a plate-type LNG gas-liquid separator, and a heat insulation layer is arranged on the outer layer of the LNG gas-liquid separator; the LNG cold air eduction tube is provided with a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flow meter, and the pipeline connecting the condensate outlet of the LNG gas-liquid separator and the reflux inlet of the LNG discharge tank is provided with a valve, a thermometer and a flow meter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921141706.4U CN210595964U (en) | 2019-07-19 | 2019-07-19 | NG cold air generating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921141706.4U CN210595964U (en) | 2019-07-19 | 2019-07-19 | NG cold air generating device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210595964U true CN210595964U (en) | 2020-05-22 |
Family
ID=70721729
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921141706.4U Withdrawn - After Issue CN210595964U (en) | 2019-07-19 | 2019-07-19 | NG cold air generating device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210595964U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110257118A (en) * | 2019-07-19 | 2019-09-20 | 中冶焦耐(大连)工程技术有限公司 | A kind of LNG pipeline forecooling method and NG cold air generating device |
-
2019
- 2019-07-19 CN CN201921141706.4U patent/CN210595964U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110257118A (en) * | 2019-07-19 | 2019-09-20 | 中冶焦耐(大连)工程技术有限公司 | A kind of LNG pipeline forecooling method and NG cold air generating device |
| CN110257118B (en) * | 2019-07-19 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | LNG pipeline precooling method and NG cold air generating device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2753861B1 (en) | Method and apparatus for power storage | |
| CN100424450C (en) | Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof | |
| CN103267394B (en) | Method and device for efficiently utilizing cold energy of liquefied natural gas | |
| CN210595964U (en) | NG cold air generating device | |
| CN105164462A (en) | Low-temperature liquefied gas tank | |
| Wang et al. | Feasibility study on a novel heat exchanger network for cryogenic liquid regasification with cooling capacity recovery: Theoretical and experimental assessments | |
| CN207635720U (en) | Gas liquefaction system | |
| US20220082210A1 (en) | Method and filling device for filling a transport tank | |
| CN110257118B (en) | LNG pipeline precooling method and NG cold air generating device | |
| KR101354188B1 (en) | Cooling tower for recovering energy and method for recovering energy using the same | |
| CN102618300B (en) | Coke quenching method for coke quenching furnace with gas-liquid two-phase distributor | |
| CN210601047U (en) | LNG pipeline precooling system adopting diffusion ignition | |
| CN116972340A (en) | Integrated management system and method for liquid hydrogen aircraft | |
| CN210345021U (en) | Self-circulation type LNG pipeline precooling system | |
| CN204387683U (en) | A kind of LNG stores supplier | |
| CN114688445B (en) | Hydrogen liquid hydrogen hydrogenation station | |
| CN115419822A (en) | Liquid hydrogen storage and transportation type hydrogen filling system for hydrogen refueling station by using cold energy generated by para-ortho hydrogen conversion | |
| Ma et al. | Thermodynamic analysis and the recuperator’s effects on two cycle systems aiming for hypersonic vehicles | |
| CN202485329U (en) | Methane liquefaction device for scattered air source points | |
| CN110285322A (en) | A kind of LNG pipeline pre-cooling technique using release igniting | |
| CN115596990A (en) | System and method for liquefied gas storage with vaporization management | |
| CN113309591A (en) | LNG cold energy utilization device | |
| CN101876399A (en) | Energy-saving liquid gas vaporizer | |
| RU2352876C1 (en) | System of liquefying carbon dioxide from mixture of exhaust gases, used in air-independent hydrocarbon fuel power station | |
| JP3003809B2 (en) | Liquefied natural gas heating system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20200522 Effective date of abandoning: 20240426 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20200522 Effective date of abandoning: 20240426 |
|
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |