CN110257118B - LNG pipeline precooling method and NG cold air generating device - Google Patents
LNG pipeline precooling method and NG cold air generating device Download PDFInfo
- Publication number
- CN110257118B CN110257118B CN201910655668.2A CN201910655668A CN110257118B CN 110257118 B CN110257118 B CN 110257118B CN 201910655668 A CN201910655668 A CN 201910655668A CN 110257118 B CN110257118 B CN 110257118B
- Authority
- CN
- China
- Prior art keywords
- lng
- gas
- inlet
- liquid separator
- cold air
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 172
- 239000003345 natural gas Substances 0.000 claims abstract description 86
- 239000007788 liquid Substances 0.000 claims abstract description 73
- 239000007789 gas Substances 0.000 claims abstract description 66
- 238000002156 mixing Methods 0.000 claims abstract description 33
- 238000010992 reflux Methods 0.000 claims abstract description 10
- 238000004378 air conditioning Methods 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims description 15
- 238000007599 discharging Methods 0.000 claims description 12
- 230000003068 static effect Effects 0.000 claims description 12
- 238000009413 insulation Methods 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 239000003949 liquefied natural gas Substances 0.000 description 149
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- 241000234295 Musa Species 0.000 description 4
- 235000018290 Musa x paradisiaca Nutrition 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- NLOAOXIUYAGBGO-UHFFFAOYSA-N C.[O] Chemical compound C.[O] NLOAOXIUYAGBGO-UHFFFAOYSA-N 0.000 description 1
- 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
- 238000004364 calculation method Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011049 filling 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
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 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
- 239000002689 soil Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/12—Liquefied petroleum gas
Abstract
The invention relates to an LNG pipeline precooling method and an NG cold air generating device, wherein the NG cold air generating device comprises an LNG discharge tank, an LNG mixing device and an LNG gas-liquid separator; LNG export and LNG mixing arrangement's LNG entry link to each other of LNG emission jar, and LNG mixing arrangement's NG entry linkage LNG factory intra-station normal atmospheric temperature natural gas pipeline, LNG mixing arrangement's NG atomizing gas exit linkage LNG gas-liquid separator's NG atomizing gas entry, LNG gas-liquid separator's condensate exit linkage LNG emission jar reflux liquid entry, LNG gas-liquid separator's NG air conditioning exit linkage NG air conditioning delivery tube. The invention gasifies LNG by utilizing the sensible heat of NG, and the generated NG cold air is used for the precooling process of the LNG pipeline system, and the NG cold air generating device has the characteristics of simple structure, low cost, safety and reliability.
Description
Technical Field
The invention relates to the technical field of LNG pipeline precooling, in particular to an LNG pipeline precooling method and an NG cold air generating device.
Background
The process of cooling the LNG piping system from ambient temperature to operating temperature is referred to as pre-cooling. In the pre-cooling 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 a thermal stability state can be achieved after a relatively long time. The design calculation of the pre-cooling process is to determine the low-temperature medium consumption and the pre-cooling time, and the pre-cooling process of the LNG pipeline system is a complex heat transfer process. The LNG pipeline system can utilize the vaporization latent heat of the low-temperature working medium in the precooling process and can also utilize the sensible heat absorbed when the temperature of the evaporated gas rises, and the consumption of the low-temperature working medium required in the precooling process is changed along with the utilization degree of the sensible heat.
The LNG delivery pipeline and the cryogenic pipeline and cryogenic storage tank in the LNG vaporization station are first sufficiently cooled, i.e., precooled, prior to formally inputting cryogenic liquid. If LNG is suddenly injected into a pipeline at normal temperature, the pipeline is rapidly contracted, and in order to avoid damage of the pipeline structure due to quenching, control of the pre-cooling process is very important. The bottom of the pipeline is in direct contact with boiled LNG and is relatively low in temperature, nucleate boiling or film boiling occurs in the pipeline due to the heat absorbed by the LNG by the pipeline material, and the generated NG fills the top of the pipeline, so that the temperature at the top of the pipeline is relatively high, and a temperature gradient in the section of the pipeline can cause a banana effect. The method comprises the following steps: because the top and bottom of the pipeline shrink unevenly, the pipeline system is unpredictably deformed, and the pipeline, the support, the expansion joint and the connecting flange are damaged, the precooling of the pipeline system is necessary in the condition of starting up after the LNG pipeline system is put into production and overhauled, the precooling process is necessary to be gradually and slowly carried out, and the cooling rate of the pipeline system is controlled to be about 50 ℃ per hour according to the related operation experience. When the temperature of the LNG pipeline system reaches-95 ℃ to-118 ℃, the LNG pipeline system can be put into production for running formally.
At present, the low-temperature working medium adopted for precooling the LNG pipeline system is usually liquid nitrogen, a plurality of large tank trucks transport the liquid nitrogen to the vicinity of the LNG device, and the vaporization is realized by absorbing the latent heat of air in a vaporizer, wherein the system pressure in the process is higher than the normal pressure, and related equipment is a pressure container. Because the temperature of liquid nitrogen is lower than LNG, when precooling operation is carried out, the probability of banana effect of the pipeline system is larger, and the time spent by the whole pipeline system for precooling is longer. And because a large amount of liquid nitrogen is required to be purchased additionally, the pre-cooling process has high cost and long preparation time.
By carrying out model analysis on the precooling operation of the LNG pipeline system, the ideal low-temperature working medium is low-temperature gas, and the low-temperature working medium is prevented from presenting a gas-liquid two-phase state in the pipeline system as much as possible, because the gas-liquid two-phase state is the root cause of banana effect of the pipeline. In engineering practice, the lower temperature limit of the precooling operation of the LNG pipeline system is the dew point (-120 ℃) of pure NG. When the low-temperature gas enters the pipeline system to be precooled, no temperature difference exists in the pipeline, the temperature is uniform on the circumference of the pipeline, and the pipeline system is gradually cooled along the extending direction along with the diffusion of the low-temperature gas in the pipeline. Such pre-cooling is performed slowly with the diffusion of the cryogenic gas, reducing the probability of deformation of the tubing. When the temperature of the pipeline system gradually decreases 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, an ideal low temperature working medium should have such physical properties: the dew point is close to the dew point of the LNG and at least cannot be raised too much, otherwise, in the pre-cooling operation, the target temperature is not reached and a gas-liquid two-phase state occurs too early. The dew point of nitrogen after air separation is about-69 ℃, so that liquid nitrogen is not suitable for being used as a working medium in the second half of LNG precooling operation. Liquid nitrogen is widely used for precooling LNG piping systems only because it is relatively easy to obtain and has a relatively low boiling point.
Disclosure of Invention
The invention provides an LNG pipeline precooling method and an NG cold air generating device, which select NG and LNG as working media, utilize the sensible heat of the NG to gasify the LNG, and the generated NG cold air is used for the precooling process of an LNG pipeline system, and does not need an additional vaporizer, does not need additional power and does not need exogenous 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 invention is realized by adopting the following technical scheme:
An LNG pipeline precooling method utilizes sensible heat of normal-temperature NG to gasify LNG to form NG cold air, and the LNG pipeline is precooled by the NG cold air.
An LNG pipeline precooling method specifically comprises the following steps: LNG from the LNG discharge tank and normal-temperature NG are fully mixed in an LNG mixing device to generate low-temperature NG atomized gas, the low-temperature NG atomized gas is separated by an LNG gas-liquid separator to obtain dry NG cold gas, and the dry NG cold gas is used as pre-cooling circulating gas before an LNG pipeline and equipment start-up; the liquid separated by the LNG gas-liquid separator is returned to the LNG discharging tank.
An NG cold air generating device for realizing the method comprises an LNG discharging tank, an LNG mixing device and an LNG gas-liquid separator; the LNG discharging tank is provided with an LNG outlet and a reflux liquid inlet, the LNG mixing device is provided with an NG inlet, an LNG inlet and an NG atomized gas outlet, and the LNG gas-liquid separator is provided with an NG atomized gas inlet, an NG cold gas outlet and a condensate outlet; LNG export and LNG mixing arrangement's LNG entry link to each other of LNG emission jar, and LNG mixing arrangement's NG entry linkage LNG factory station internal normal atmospheric temperature natural gas pipeline, LNG mixing arrangement's NG atomizing gas exit linkage LNG vapour and liquid separator's NG atomizing gas entry, LNG vapour and liquid separator's condensate outlet connection LNG emission jar's reflux liquid entry, LNG vapour and liquid separator's NG air conditioning exit linkage NG air conditioning delivery tube.
The LNG discharging tank is a closed pressure container with a horizontal tank, a vertical tank or a ship-shaped groove structure, the top of the LNG discharging tank is provided with a pressure safety valve, and the outer layer of the LNG discharging tank is provided with a heat insulation layer.
The LNG mixing device consists of 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; the LNG inlet pipe connected with the LNG inlet is respectively provided with a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge; and an 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 in the three-way pipe structure oppositely, and a venturi nozzle is arranged at the LNG inlet.
The premixing section is of an inner sleeve and outer sleeve structure, one end of the inner sleeve is an NG inlet, the same end of an 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.
The premixing 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 gas outlet.
The LNG gas-liquid separator is a cyclone type, vortex type or tray type gas-liquid separator, and the outer layer of the LNG gas-liquid separator is provided with a heat insulation layer; the NG cold air delivery pipe is provided with a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flowmeter, and a pipeline connected with a condensate outlet of the LNG gas-liquid separator and a reflux inlet of the LNG discharge tank is provided with a valve, a thermometer and a flowmeter.
Compared with the prior art, the invention has the beneficial effects that:
1) The working medium can be directly obtained from an LNG factory station, exogenous liquid nitrogen is not needed, and a series of equipment for loading, unloading and introducing the liquid nitrogen can be saved;
2) LNG is gasified by utilizing sensible heat of normal-temperature natural gas, and a vaporizer and an additional heat source are not needed;
3) The NG cold air generating device has simple structure and small equipment occupation area, and is particularly suitable for large and medium LNG plant stations;
4) The invention can realize 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 banana effect of a pipeline system, and is beneficial to improving the production efficiency, reducing the operation cost and improving the safety of an LNG system;
5) The precooling working principle of the invention can be widely applied to precooling of other low-temperature liquid conveying pipelines, such as liquid nitrogen, liquid oxygen, liquid hydrogen and the like.
Drawings
Fig. 1 is a schematic view of a NG cool air generating apparatus according to the present invention.
Fig. 2 is a schematic structural view of the LNG mixing device according to the present invention.
Fig. 3 is a schematic diagram of the structure of the LNG gas-liquid separator according to the present invention.
Fig. 4 is a process flow diagram of the NG cool air generating apparatus according to 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 atomizing gas inlet 32 NG cold gas outlet 33 condensate outlet
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
According to the LNG pipeline precooling method, the LNG is gasified by utilizing sensible heat of the normal-temperature NG to form NG cold air, and the LNG pipeline is precooled by the NG cold air.
As shown in fig. 4, the method for precooling an LNG pipeline according to the present invention specifically includes: the LNG from the LNG discharge tank 1 and the normal-temperature NG are fully mixed in the LNG mixing device 2 to generate low-temperature NG atomized gas, the low-temperature NG atomized gas is separated by the LNG gas-liquid separator 3 to obtain dry NG cold gas, and the dry NG cold gas is used as pre-cooling circulating gas before an LNG pipeline and equipment start-up; the liquid separated by the LNG gas-liquid separator 3 is returned to the LNG discharge tank 1.
As shown in fig. 1, an NG cold air generating apparatus for implementing the method 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 liquid inlet, the LNG mixing device 2 is provided with an NG inlet 21, an LNG inlet 22 and an NG atomizing gas outlet (as shown in fig. 2), and the LNG gas-liquid separator 3 is provided with an NG atomizing gas inlet 31, an NG cold gas outlet 32 and a condensate outlet 33 (as shown in fig. 3); the LNG export of LNG drain jar 1 links to each other with the LNG entry 22 of LNG mixing arrangement 2, and the normal atmospheric temperature natural gas pipeline in the LNG factory station is connected to the NG entry 21 of LNG mixing arrangement 2, and the NG atomizing gas entry 31 of LNG vapour and liquid separator 3 is connected to the NG atomizing gas exit linkage LNG of LNG mixing arrangement 2, and the reflux liquid entry of LNG drain jar 1 is connected to the condensate outlet of LNG vapour and liquid separator 3, and NG cold air export 32 of LNG vapour and liquid separator 3 connects the NG cold air delivery line.
The LNG discharging tank 1 is a closed pressure container with a horizontal tank, a vertical tank or a ship-shaped groove structure, the top of the LNG discharging tank is provided with a pressure safety valve, and the outer layer of the LNG discharging tank is provided with a heat insulation layer.
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 NG inlet pipe connected with the NG inlet 21 and an LNG inlet pipe connected with the LNG inlet 22 are respectively provided with a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge; 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 in a three-way pipe structure, in which an NG inlet 21 is opposite to a mixed gas outlet, and an LNG inlet 22 is provided with a venturi nozzle 23.
The premixing section is of an inner sleeve and outer sleeve structure, one end of the inner sleeve is an NG inlet, the same end of an 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.
The premixing 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 gas outlet.
The LNG gas-liquid separator 3 is a cyclone type, vortex type or tray type gas-liquid separator, and the outer layer of the LNG gas-liquid separator 3 is provided with a heat insulation layer; the NG cold air delivery pipe is provided with a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flow gauge, and a pipeline connecting the condensate outlet 33 of the LNG gas-liquid separator 3 with the reflux inlet of the LNG discharge tank 1 is provided with a valve, a thermometer and a flow gauge.
Taking an LNG mixing device (shown in fig. 2) adopting a premixing section with a tee pipe structure as an example, the working principle of the LNG pipeline precooling method of the present invention is as follows: in the premixing section of the LNG mixing device 2, LNG (liquefied natural gas at a temperature of about-165 ℃) and Natural Gas (NG) at normal temperature are primarily mixed, the vaporized low-temperature natural gas and the normal-temperature natural gas enter a static mixer 24 to be uniformly mixed, and the low-temperature natural gas (NG atomized gas at a temperature of about-158 ℃) containing mist drops exiting from the static mixer 24 enters an LNG gas-liquid separator 3 again to realize gas-liquid separation 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. The separated dry NG cold gas (cryogenic natural gas) enters the LNG pipeline system for pre-cooling circulation before pipeline and equipment start-up. The separated liquid (re-condensed LNG) is collected at the bottom of the LNG gas-liquid separator 3, and after a certain amount of liquid is accumulated, the valve is periodically opened to return the liquid to the LNG discharge tank 1 for storage.
Along with the rapid increase of the demand of China for LNG, more large and medium-sized LNG plants are built in coastal areas, and the NG cold air generating device has wider application prospect. As the liquid oxygen-methane type spaceflight launching technology is mature, the invention has a full application prospect in the process of filling fuel by using LNG.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (8)
1. The LNG pipeline precooling method is characterized in that the LNG is gasified by utilizing sensible heat of normal-temperature NG to form NG cold air, and the LNG pipeline is precooled by the NG cold air; the method comprises the following steps: LNG from the LNG discharge tank and normal-temperature NG are fully mixed in an LNG mixing device to generate low-temperature NG atomized gas, the low-temperature NG atomized gas is separated by an LNG gas-liquid separator to obtain dry NG cold gas, and the dry NG cold gas is used as pre-cooling circulating gas before an LNG pipeline and equipment start-up; the liquid separated by the LNG gas-liquid separator is returned to the LNG discharging tank.
2. An NG cool air generating apparatus for implementing the method of claim 1, comprising an LNG discharge tank, an LNG mixing device, and an LNG gas-liquid separator; the LNG discharging tank is provided with an LNG outlet and a reflux liquid inlet, the LNG mixing device is provided with an NG inlet, an LNG inlet and an NG atomized gas outlet, and the LNG gas-liquid separator is provided with an NG atomized gas inlet, an NG cold gas outlet and a condensate outlet; LNG export and LNG mixing arrangement's LNG entry link to each other of LNG emission jar, and LNG mixing arrangement's NG entry linkage LNG factory station internal normal atmospheric temperature natural gas pipeline, LNG mixing arrangement's NG atomizing gas exit linkage LNG vapour and liquid separator's NG atomizing gas entry, LNG vapour and liquid separator's condensate outlet connection LNG emission jar's reflux liquid entry, LNG vapour and liquid separator's NG air conditioning exit linkage NG air conditioning delivery tube.
3. The NG cold air generating device according to claim 2, wherein the LNG discharging tank is a closed pressure vessel of a horizontal tank, a vertical tank or a ship-shaped tank structure, the top is provided with a pressure safety valve, and the outer layer is provided with a heat insulation layer.
4. The LNG cold air generating device according to claim 2, wherein the LNG mixing device is composed of 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; the LNG inlet pipe connected with the LNG inlet is respectively provided with a safety valve, a pressure regulating valve, a thermometer, a flowmeter and a pressure gauge; and an outer layer of the LNG mixing device is provided with a heat insulation layer.
5. The NG cold air generating device according to claim 4, wherein the premixing section is a three-way pipe structure, an NG inlet and a mixed gas outlet are arranged opposite to each other in the three-way pipe structure, and a venturi nozzle is arranged at the LNG inlet.
6. The NG cold air generating device according to claim 4, wherein the premixing section has an inner and 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.
7. The NG cold air generating device according to claim 4, wherein the premixing section has a parallel double-pipe structure, the double-pipe structure is an LNG inlet pipe and an NG inlet pipe, 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 is provided with a mixed gas outlet.
8. The NG cold air generating device according to claim 2, wherein the LNG gas-liquid separator is a cyclone type, vortex type or tray type gas-liquid separator, and an outer layer of the LNG gas-liquid separator is provided with a heat insulation layer; the LNG cold air delivery pipe is provided with a safety valve, a pressure regulating valve, a thermometer, a pressure gauge and a flow gauge, and a pipeline connected with a condensate outlet of the LNG gas-liquid separator and a reflux inlet of the LNG discharge tank is provided with a valve, a thermometer and a flow gauge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910655668.2A CN110257118B (en) | 2019-07-19 | 2019-07-19 | LNG pipeline precooling method and NG cold air generating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910655668.2A CN110257118B (en) | 2019-07-19 | 2019-07-19 | LNG pipeline precooling method and NG cold air generating device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110257118A CN110257118A (en) | 2019-09-20 |
| CN110257118B true CN110257118B (en) | 2024-04-26 |
Family
ID=67927226
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910655668.2A Active CN110257118B (en) | 2019-07-19 | 2019-07-19 | LNG pipeline precooling method and NG cold air generating device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110257118B (en) |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0770575A (en) * | 1993-09-03 | 1995-03-14 | Tokyo Gas Co Ltd | Method and apparatus for treating boil-off gas produced in storage tank of liquefied natural gas |
| CN1894537A (en) * | 2003-12-15 | 2007-01-10 | Bp北美公司 | Systems and methods for vaporization of liquefied natural gas |
| CN102636000A (en) * | 2012-03-13 | 2012-08-15 | 新地能源工程技术有限公司 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
| CN102686930A (en) * | 2009-11-13 | 2012-09-19 | 海威气体系统公司 | A plant for regasification of LNG |
| CN205316815U (en) * | 2015-12-21 | 2016-06-15 | 刘印同 | High -efficient liquefaction recovery unit of natural gas |
| CN206071658U (en) * | 2016-08-31 | 2017-04-05 | 航天晨光股份有限公司 | A kind of LNG cold energy utilization system |
| CN106839486A (en) * | 2017-03-07 | 2017-06-13 | 宁波市弘祥能源有限公司 | LNG cold energy cooling cycle systems |
| CN206695421U (en) * | 2017-03-07 | 2017-12-01 | 宁波市弘祥能源有限公司 | LNG cold energy refrigerating circulatory devices |
| CN210595964U (en) * | 2019-07-19 | 2020-05-22 | 中冶焦耐(大连)工程技术有限公司 | NG cold air generating device |
-
2019
- 2019-07-19 CN CN201910655668.2A patent/CN110257118B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0770575A (en) * | 1993-09-03 | 1995-03-14 | Tokyo Gas Co Ltd | Method and apparatus for treating boil-off gas produced in storage tank of liquefied natural gas |
| CN1894537A (en) * | 2003-12-15 | 2007-01-10 | Bp北美公司 | Systems and methods for vaporization of liquefied natural gas |
| CN102686930A (en) * | 2009-11-13 | 2012-09-19 | 海威气体系统公司 | A plant for regasification of LNG |
| CN102636000A (en) * | 2012-03-13 | 2012-08-15 | 新地能源工程技术有限公司 | Method for refrigerating liquefied natural gas by aid of single mixed working medium and device |
| CN205316815U (en) * | 2015-12-21 | 2016-06-15 | 刘印同 | High -efficient liquefaction recovery unit of natural gas |
| CN206071658U (en) * | 2016-08-31 | 2017-04-05 | 航天晨光股份有限公司 | A kind of LNG cold energy utilization system |
| CN106839486A (en) * | 2017-03-07 | 2017-06-13 | 宁波市弘祥能源有限公司 | LNG cold energy cooling cycle systems |
| CN206695421U (en) * | 2017-03-07 | 2017-12-01 | 宁波市弘祥能源有限公司 | LNG cold energy refrigerating circulatory devices |
| CN210595964U (en) * | 2019-07-19 | 2020-05-22 | 中冶焦耐(大连)工程技术有限公司 | NG cold air generating device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110257118A (en) | 2019-09-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20180128171A1 (en) | Method and apparatus for power storage | |
| CN1052053C (en) | An improved liquefied natural gas fueled combined cycle power plant | |
| JP5354543B2 (en) | Outside air type vaporizer | |
| CN115419829B (en) | High-pressure liquid hydrogen conveying system and method for liquid hydrogen engine test | |
| CN210595964U (en) | NG cold air generating device | |
| CN110257118B (en) | LNG pipeline precooling method and NG cold air generating device | |
| US3726101A (en) | Method of continuously vaporizing and superheating liquefied cryogenic fluid | |
| CN207635720U (en) | Gas liquefaction system | |
| CN210345021U (en) | Self-circulation type LNG pipeline precooling system | |
| CN116972340A (en) | Integrated management system and method for liquid hydrogen aircraft | |
| CN110345378B (en) | Experimental device for testing flow of liquefied natural gas non-equilibrium gas-liquid two-phase pipeline | |
| CN115076592B (en) | BOG control system and method for liquid hydrogen storage tank and liquid hydrogen storage tank | |
| CN114440552B (en) | Method for extracting and liquefying high-purity methane by using liquefied natural gas | |
| CN206723838U (en) | A kind of LNG tank BOG recovery systems | |
| CN202485329U (en) | Methane liquefaction device for scattered air source points | |
| Ma et al. | Thermodynamic analysis and the recuperator’s effects on two cycle systems aiming for hypersonic vehicles | |
| CN113309591A (en) | LNG cold energy utilization device | |
| CN113368920A (en) | Large-scale high low temperature environment simulation test system of two cold sources | |
| CN106731600A (en) | A kind of collecting carbonic anhydride liquefying plant | |
| CN110345386A (en) | A kind of LNG pipeline pre-cooling technique of self-circulation type | |
| RU2352876C1 (en) | System of liquefying carbon dioxide from mixture of exhaust gases, used in air-independent hydrocarbon fuel power station | |
| RU2193740C1 (en) | Gas liquefying apparatus | |
| CN116292243B (en) | Closed continuous self-feedback cryogenic pump test system depending on liquefied natural gas factory | |
| CN114348302B (en) | Liquid hydrogen storage tank space exhaust cooling capacity utilization system based on vortex tube | |
| JP3003809B2 (en) | Liquefied natural gas heating system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |