CN104390125A - Method and device applied to constant-pressure recovery of liquefied natural gas flash steam - Google Patents
Method and device applied to constant-pressure recovery of liquefied natural gas flash steam Download PDFInfo
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- CN104390125A CN104390125A CN201410584596.4A CN201410584596A CN104390125A CN 104390125 A CN104390125 A CN 104390125A CN 201410584596 A CN201410584596 A CN 201410584596A CN 104390125 A CN104390125 A CN 104390125A
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Abstract
The invention provides a method and a device applied to constant-pressure recovery of liquefied natural gas flash steam. The method comprises the following steps: feeding supercooled and liquefied natural gas by a low-temperature storage tank and introducing the supercooled and liquefied natural gas into a low-temperature pressure container to arrive at a filler bed; boosting the liquefied natural gas flash steam generated in the low-temperature storage tank by a low-temperature compressor and feeding the liquefied natural gas flash steam into the filler bed of the low-temperature pressure container; exchanging heat of the liquefied natural gas flash steam introduced into the low-temperature pressure container and the supercooled and liquefied natural gas by virtue of materials of the filler bed, and instantly dissolving the liquefied natural gas flash steam in supercooled and liquefied natural gas in the unsaturated state; feeding high-pressure nitrogen into the low-temperature pressure container to enable the pressure to be constant; converting all the liquefied natural gas flash steam from gaseous state into liquid state, and enabling all the liquefied natural gas in the process of dissolving the liquefied natural gas flash steam to flow out of the low-temperature pressure container and enter subsequent technical processes. The device comprises a low-temperature pressure container, wherein the low-temperature pressure container is internally provided with the filler bed. The device is stable in running, high in safety and low in emission; the vibration noise is reduced; the operation cost is lowered.
Description
Technical field
The present invention relates to a kind of LNG Liquefied natural gas flashed vapour constant voltage recovery method and equipment.
Background technique
Current coal, oil are still mankind's major consumers energy, and in primary energy consumption structure, coal accounts for 68.5%, and oil accounts for 17.7%, and rock gas only accounts for 4.7%, the world average level far below 24%.This energy consumption structure based on coal can hide some dangers for atmosphere environment.LNG Liquefied natural gas (LNG) is the Optimum storage form of rock gas, under the situation that current environmental requirement is increasingly serious, for the LNG industry of technology-intensive type, research and development LNG correlation technique, especially LNG stores correlation technique, has important Social benefit and economic benefit to the development of LNG industry.
Due to the heat input produced in external heat and operating process, the LNG Liquefied natural gas in storage tank constantly will produce flashed vapour.Big-and-middle-sized LNG facility for the processing form of flashed vapour to be recovered as master, Normal practice adopts condensing pressure container again, flashed vapour after compression and supercooled liquid rock gas are introduced by upper vessel portion respectively with following current form, both carry out thing heat exchange by the structured packing bed in the middle part of container, make flashed vapour be dissolved in LNG Liquefied natural gas, realize it and reclaim and liquefy again.The deficiency of this way is adopted to be, in actual motion, the generation of flashed vapour is discontinuous, it is meeting mineralization pressure cumulative process in pressurized container, after usual pressure rises to about 0.8MPa, flashed vapour is instantaneous to be dissolved in LNG Liquefied natural gas, causes container inner pressure to be down to 0.3 to 0.5MPa fast, go round and begin again, make pressurized container vibrate and noise serious.Normal practice is in order to reduce noise vibration, led back in pressurized container by the high-pressure natural gas that subsequent technique gasification produces and carry out pressure regulation, the flashed vapour dissolved in LNG Liquefied natural gas is undersaturated condition, progressively separates out after entering subsequent process flow, enter flashed vapour house steward, form the accumulation of more flashed vapours.So just make cryogenic compressor load increase, system overpressure and emptying probability increase, and flashed vapour processing cost increases, and receiving station's operation grade declines, and bring operation and potential safety hazard.
Therefore, ubiquitous problem in the process of LNG Liquefied natural gas flashed vapour, must carry out technological adjustment to process detail setting, adopt the way improved, make the smooth operation of natural gas vaporization gas disposal equipment, meet the Security in operation and cost-effectiveness requirement.
Summary of the invention
Main purpose of the present invention is to solve existing natural gas vaporization gas recovery method above shortcomings part, and LNG Liquefied natural gas flashed vapour constant voltage recovery method and equipment are provided, filler in its low-temperature pressure container is as bedding, by LNG Liquefied natural gas flashed vapour and the supercooled liquid rock gas counter-flowing heat exchange of compression, LNG Liquefied natural gas flashed vapour is reclaimed, stable, vibrating noise reduction, high safety, discharge amount are low, and operation cost significantly reduces.
The object of the invention is to be realized by following technological scheme:
LNG Liquefied natural gas flashed vapour constant voltage recovery method of the present invention, is characterized in that, comprise the following steps:
(1) enter in low-temperature pressure container 2 by pumping out the supercooled liquid gas inlet 1 of supercooled liquid rock gas by low-temperature pressure container 2 in the tank in low temperature storing tank and then arrive packed bed 4;
(2) packed bed 4 in low-temperature pressure container 2 is entered after the LNG Liquefied natural gas flashed vapour produced due to regular job and external world's heat input in low temperature storing tank delivers to the LNG Liquefied natural gas flashed vapour entrance 6 of low-temperature pressure container 2 by cryogenic compressor boosting;
(3) enter LNG Liquefied natural gas flashed vapour in low-temperature pressure container 2 and supercooled liquid rock gas is contacted with each other by the packed bed 4 be arranged in low-temperature pressure container 2 and then thing heat exchange occurs, make LNG Liquefied natural gas flashed vapour at once be dissolved in undersaturated condition supercooled liquid rock gas;
(4) liquid nitrogen plant being arranged on low-temperature pressure container 2 outside or nitrogen gas generating system is utilized in low-temperature pressure container 2, to send into high pressure nitrogen by the nitrogen inlet 3 of low-temperature pressure container 2, ftercompction is carried out to low-temperature pressure container 2 inside, makes low-temperature pressure container 2 internal pressure constant;
(5) under nitrogen ftercompction, LNG Liquefied natural gas flashed vapour dissolves in supercooled liquid rock gas, LNG Liquefied natural gas flashed vapour is made all to change liquid state into by gaseous state, realize the recovery of LNG Liquefied natural gas flash gasoline, the superpressure avoiding gas build to cause and torch burning, realize the whole LNG Liquefied natural gas after LNG Liquefied natural gas flashed vapour course of dissolution and export 5 outflow low-temperature pressure containers 2 by the LNG Liquefied natural gas of low-temperature pressure container 2, enter subsequent process flow.
Aforesaid LNG Liquefied natural gas flashed vapour constant voltage recovery method, wherein, the supercooled liquid gas pressure that described () is sent in low-temperature pressure container 2 by pump in the tank in low temperature storing tank is about 1MPa; The LNG Liquefied natural gas flashed vapour pressure boosted in feeding low-temperature pressure container 2 by cryogenic compressor in described (two) is about 1MPa; Carry out ftercompction to low-temperature pressure container 2 inside in described (four), make low-temperature pressure container 2 internal pressure constant, this constant pressure maintains 0.8MPa.
The equipment that LNG Liquefied natural gas flashed vapour constant voltage recovery method of the present invention uses, it is characterized in that, comprise low-temperature pressure container 2, packed bed 4 is provided with in this low-temperature pressure container 2, this low-temperature pressure container top end socket is provided with supercooled liquid gas inlet 1, low-temperature pressure container 2 bottom bulkhead side-walls is provided with LNG Liquefied natural gas flashed vapour entrance 6, the low-temperature pressure container sidewall locations arranged above packed bed 4 is provided with ftercompction nitrogen inlet 3, and low-temperature pressure container bottom bulkhead establishes LNG Liquefied natural gas to export 5 bottom.
The equipment that aforesaid LNG Liquefied natural gas flashed vapour constant voltage recovery method uses, wherein, described low-temperature pressure container 2 is the tank bodies be made up of 304 stainless steels, and this tank body height is 8 ± 0.1 meters, diameter 2.5 meters, operation pressure 1 to 0.8MPa, tank body wall thickness 20 ± 5mm.
The equipment that aforesaid LNG Liquefied natural gas flashed vapour constant voltage recovery method uses, wherein, described packed bed 4 is Raschig ring dumped packing bed, this packed bed 4 is positioned in the middle part of low-temperature pressure container 2, packed bed 4 support is the plate body corresponding to low-temperature pressure container 2 transverse shape, the cross sectional area of this plate body is less than low-temperature pressure container 2 cross sectional area, and this plate body evenly lays several sieve aperture, plate body overlapping edges is being bolted on several links of low-temperature pressure container inwall, plate body sieve aperture is 3/4 cun, the Raschig ring filler in 1 cun of ring footpath is piled up on packed bed support with the form of the heap that falls apart in a jumble, it is highly 1000 ± 50mm that filler is piled up.
The equipment that aforesaid LNG Liquefied natural gas flashed vapour constant voltage recovery method uses, wherein, described supercooled liquid gas inlet 1 adopts caliber to be the pipeline section of 10 cun, and it is 400 ± 10mm that entrance pipeline section stretches into container length; Described LNG Liquefied natural gas flashed vapour entrance 6 adopts caliber to be the pipeline section of 4 cun, and it is 400 ± 10mm that pipeline section stretches into container length; The specification of described Raschig ring filler is 304 stainless steels, and ring footpath is 1 cun, and height 1000 ± 50mm piled up by filler; Described ftercompction nitrogen inlet 3 adopts caliber to be the pipeline section of 4 cun, and it is 200 ± 10mm that entrance pipeline section stretches into container length; Described LNG Liquefied natural gas outlet 5 employing caliber is the pipeline section of 20 cun, and it is 200 ± 10mm that this pipeline section stretches into container length.
Beneficial effect of the present invention: the present invention is owing to adopting technique scheme, make the smooth operation of boil-off gas processing equipment, reuse efficiency raising, meet the Security in operation and cost-effectiveness requirement, effectively can be applied in all kinds of middle-size and small-size LNG Liquefied natural gas receiving station, Storage, peak regulation station etc., make that it is stable, high safety, discharge amount are low, operation cost significantly reduces.
The flashed vapour reclaiming system of all kinds of middle-size and small-size LNG Vaporizing Station, Fen Shu satellite station and storage vault can be widely used in, effective reduction system pressure fluctuates the noise and vibration that cause, make system cloud gray model steady, reduce the generation of boil-off gas, avoid the generation of overpressure alarm and cold and hot air defense, decrease torch burning waste, reduce CO2 emission and operation cost.
Accompanying drawing explanation
Fig. 1 is that LNG Liquefied natural gas flashed vapour constant voltage recovery method of the present invention uses equipment schematic diagram.
Major label description in figure:
1 supercooled liquid gas inlet, 2 low-temperature pressure containers, 3 ftercompction nitrogen inlets, 4 Raschig ring dumped packing beds, 5 LNG Liquefied natural gas outlets, 6 LNG Liquefied natural gas flashed vapour entrances.
Embodiment
Below in conjunction with accompanying drawing, the invention will be further described.
As shown in Figure 1, the equipment that LNG Liquefied natural gas flashed vapour constant voltage recovery method of the present invention uses, it comprises low-temperature pressure container 2, packed bed 4 is provided with in this low-temperature pressure container 2, this low-temperature pressure container top end socket is provided with supercooled liquid gas inlet 1, low-temperature pressure container 2 bottom bulkhead side-walls is provided with LNG Liquefied natural gas flashed vapour entrance 6, the low-temperature pressure container sidewall locations arranged above packed bed 4 is provided with ftercompction nitrogen inlet 3, and low-temperature pressure container bottom bulkhead establishes LNG Liquefied natural gas to export 5 bottom.
As shown in Figure 1, the enforcement of LNG Liquefied natural gas flashed vapour constant voltage recovery method of the present invention, enter in low-temperature pressure container 2 by the supercooled liquid rock gas pumping out pressure in the tank in low temperature storing tank and be about 1MPa by the supercooled liquid gas inlet 1 of low-temperature pressure container 2, low-temperature pressure container is by 304 stainless steel manufactures, highly about 8 meters, diameter 2.5 meters, operation pressure 0.8MPa, container wall thickness is about 20mm, supercooled liquid gas inlet 1 is installed on this low-temperature pressure container top end socket, employing caliber is the pipeline section of 10 cun, and it is 400mm that entrance pipeline section stretches into container length, this low-temperature pressure container 2 Raschig ring dumped packing bed 4 is entered by the LNG Liquefied natural gas flashed vapour entrance 6 of low-temperature pressure container 2 by the cryogenic compressor LNG Liquefied natural gas flashed vapour sent that boosts, LNG Liquefied natural gas flashed vapour pressure is about 1MPa, its entrance is arranged on low-temperature pressure container 2 bottom bulkhead side-walls, employing caliber is the pipeline section of 4 cun, it is 400mm that entrance pipeline section stretches into container length, suction pressure 1MPa, Raschig ring filler bed adopts 304 stainless steels 1 cun in bulk, the specification of Raschig ring filler is 304 stainless steels, ring footpath is 1 cun, height 1000mm piled up by filler, packed bed support is the plate body corresponding to low-temperature pressure container 2 transverse shape, the cross sectional area of this plate body is less than low-temperature pressure container 2 cross sectional area, and this plate body evenly lays several sieve aperture, plate body overlapping edges is being bolted on several links of low-temperature pressure container inwall, plate body sieve aperture is 3/4 cun, the Raschig ring filler in 1 cun of ring footpath is piled up on packed bed support with the form of the heap that falls apart in a jumble, flashed vapour and supercooled liquid rock gas are contacted by a large amount of surface of contact that Raschig ring dumped packing bed 4 provides and then thing heat exchange occur, and because excessively cold LNG Liquefied natural gas is undersaturated condition, flashed vapour is dissolved in LNG Liquefied natural gas at once, ftercompction nitrogen enters in low-temperature pressure container 2 through the ftercompction nitrogen inlet 3 of low-temperature pressure container, the pressure drop caused for flashed vapour rapid solution compensates, unnecessary nitrogen gas dissolved in LNG Liquefied natural gas, because low its content that can not cause of the solubility of nitrogen in LNG Liquefied natural gas is excessive, complete course of dissolution realize flashed vapour reclaim after, namely all flashed vapours change liquid state into by gaseous state, realize the whole LNG Liquefied natural gas after flashed vapour course of dissolution and export 5 outflow low-temperature pressure containers 2 by this low-temperature pressure container 2 LNG Liquefied natural gas and enter subsequent process flow, LNG Liquefied natural gas outlet 5 is installed on low-temperature pressure container bottom bulkhead bottom, and employing caliber is the pipeline section of 20 cun, and it is 200mm that this pipeline section stretches into container length.Owing to adopting the comprehensive function of Raschig ring filler, countercurrent flow and nitrogen ftercompction in LNG Liquefied natural gas flashed vapour constant voltage callback course, low-temperature pressure container 2 internal pressure can be controlled and remain on about 0.8MPa, reclaim the most favourable for the dissolving of flashed vapour under this pressure condition, the periodic vibration noise due to course of dissolution generation that constant pressure is avoided.
Utilize and introduce outside nitrogen ftercompction and make container inner pressure constant in 0.8MPa, ftercompction nitrogen and flashed vapour are dissolved in LNG Liquefied natural gas simultaneously, because nitrogen solubility is low, can fluctuate and the impact of external gas transmission component by pilot pressure.
Embodiment 1:
Certain LNG Liquefied natural gas peak regulation station annual capacity 2000000 tons, adopt after-condenser pressurized container, treating capacity about 10 tons/hour, utilize compression flashed vapour and supercooled liquid rock gas in structured packing bed, not by nitrogen ftercompction, be depressurized to about 1MPa by the outer gas transmission of high pressure and return ftercompction in incoming pressure container, because high pressure air ftercompction causes LNG Liquefied natural gas to be in hypersaturated state, enter after in subsequent process flow and again discharged rapidly, by antiaircraft pipeline gather to boil-off gas house steward formed boil-off gas accumulate, build-up of pressure raises reports to the police and is disposed to torch burning, in addition due to vibration that the inner flashed vapour course of dissolution of pressurized container brings, make internals, the mouth of pipe and accessory structure need three months to carry out repair and maintenance, cause production suspension induced losses.The above-mentioned annual loss that amounts to fails to keep an appointment 2,500 ten thousand yuans.
Conventional production facility is transformed according to technological method of the present invention and equipment, above-mentioned after-condenser pressurized container is transformed according to low-temperature pressure container in the inventive method, after transformation, the supercooled liquid rock gas being about 1MPa by the pressure pumped out in the tank in low temperature storing tank enters low-temperature pressure container by the supercooled liquid gas inlet 1 of low-temperature pressure container, operation pressure 0.8MPa, Raschig ring dumped packing bed 4 is entered by the LNG Liquefied natural gas flashed vapour entrance 6 of low-temperature pressure container by the cryogenic compressor LNG Liquefied natural gas flashed vapour sent that boosts, LNG Liquefied natural gas flashed vapour pressure is about 1MPa, flashed vapour and supercooled liquid rock gas are contacted by a large amount of surface of contact that Raschig ring dumped packing bed 4 provides and then thing heat exchange occur, because excessively cold LNG Liquefied natural gas is undersaturated condition, flashed vapour is dissolved in LNG Liquefied natural gas at once, ftercompction nitrogen enters in low-temperature pressure container 2 through the ftercompction nitrogen inlet 3 of low-temperature pressure container, the pressure drop that flashed vapour rapid solution causes is compensated, unnecessary nitrogen gas dissolved in LNG Liquefied natural gas, because low its content that can not cause of the solubility of nitrogen in LNG Liquefied natural gas is excessive, complete course of dissolution realize flashed vapour reclaim after, namely all flashed vapours change liquid state into by gaseous state, realize the whole LNG Liquefied natural gas after flashed vapour course of dissolution and export 5 outflow low-temperature pressure containers by the LNG Liquefied natural gas of low-temperature pressure container, then subsequent process flow is entered.Owing to adopting the comprehensive function of Raschig ring filler, countercurrent flow and nitrogen ftercompction in this process, low-temperature pressure container 2 internal pressure can be controlled and remain on about 0.8MPa, reclaim the most favourable for the dissolving of flashed vapour under this pressure condition, the periodic vibration noise due to course of dissolution generation that constant pressure is avoided.
After evaporation gas recycling system is transformed according to this method and described equipment, the noise and vibration produced by the intermittent course of dissolution of former scheme rock gas is eliminated comprehensively, internals, the mouth of pipe, auxiliary support structure is made to realize non-maintaining state, without the need to inspection once in three months, compressor realizes smooth running, reduce start and stop every day about 3 times, reduce maintenance cost.Reduce the number of times of overpressure alarm and emptying simultaneously, monthly reduce about 3 to 5 times, decrease torch burning waste, also reduce CO2 emission and operation cost.Therefore, the direct economic loss 2,500 ten thousand yuan because LNG Liquefied natural gas flash distillation causes can be reduced.
The content be not described in the present embodiment is prior art, therefore no longer repeats.
The above, it is only preferred embodiment of the present invention, not any pro forma restriction is done to the present invention, every above embodiment is done according to technical spirit of the present invention any simple modification, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (6)
1. a LNG Liquefied natural gas flashed vapour constant voltage recovery method, is characterized in that, comprise the following steps:
(1) enter in low-temperature pressure container by pumping out the supercooled liquid gas inlet of supercooled liquid rock gas by low-temperature pressure container in the tank in low temperature storing tank and then arrive packed bed;
(2) packed bed in low-temperature pressure container is entered after the LNG Liquefied natural gas flashed vapour produced due to regular job and external world's heat input in low temperature storing tank delivers to the LNG Liquefied natural gas flashed vapour entrance of low-temperature pressure container by cryogenic compressor boosting;
(3) enter LNG Liquefied natural gas flashed vapour in low-temperature pressure container and supercooled liquid rock gas is contacted with each other by the packed bed be arranged in low-temperature pressure container and then thing heat exchange occurs, make LNG Liquefied natural gas flashed vapour at once be dissolved in undersaturated condition supercooled liquid rock gas;
(4) liquid nitrogen plant being arranged on low-temperature pressure container outside or nitrogen gas generating system is utilized in low-temperature pressure container, to send into high pressure nitrogen by the nitrogen inlet of low-temperature pressure container, ftercompction is carried out to low-temperature pressure container inside, makes low-temperature pressure container internal pressure constant;
(5) under nitrogen ftercompction, LNG Liquefied natural gas flashed vapour dissolves in supercooled liquid rock gas, LNG Liquefied natural gas flashed vapour is made all to change liquid state into by gaseous state, realize the recovery of LNG Liquefied natural gas flash gasoline, the superpressure avoiding gas build to cause and torch burning, realize the whole LNG Liquefied natural gas after LNG Liquefied natural gas flashed vapour course of dissolution and export outflow low-temperature pressure container by the LNG Liquefied natural gas of low-temperature pressure container, enter subsequent process flow.
2. LNG Liquefied natural gas flashed vapour constant voltage recovery method according to claim 1, is characterized in that,
The supercooled liquid gas pressure that described (one) is sent in low-temperature pressure container by pump in the tank in low temperature storing tank is about 1MPa;
The LNG Liquefied natural gas flashed vapour pressure boosted in feeding low-temperature pressure container by cryogenic compressor in described (two) is about 1MPa;
Carry out ftercompction to low-temperature pressure container inside in described (four), make low-temperature pressure container internal pressure constant, this constant pressure maintains 0.8MPa.
3. the equipment of a LNG Liquefied natural gas flashed vapour constant voltage recovery method use as claimed in claim 1, it is characterized in that, comprise low-temperature pressure container, packed bed is provided with in this low-temperature pressure container, this low-temperature pressure container top end socket is provided with supercooled liquid gas inlet, low-temperature pressure container bottom bulkhead side-walls is provided with LNG Liquefied natural gas flashed vapour entrance, the low-temperature pressure container sidewall locations arranged above packed bed is provided with ftercompction nitrogen inlet, and low-temperature pressure container bottom bulkhead establishes LNG Liquefied natural gas to export bottom.
4. the equipment of LNG Liquefied natural gas flashed vapour constant voltage recovery method use according to claim 3, it is characterized in that, described low-temperature pressure container is the tank body be made up of 304 stainless steels, this tank body height is 8 ± 0.1 meters, diameter 2.5 meters, operation pressure 1 to 0.8MPa, tank body wall thickness 20 ± 5mm.
5. the equipment that the LNG Liquefied natural gas flashed vapour constant voltage recovery method according to claim 3 or 4 uses, it is characterized in that, described packed bed is Raschig ring dumped packing bed, this packed bed is positioned in the middle part of low-temperature pressure container, packed bed support is the plate body corresponding to low-temperature pressure container transverse shape, the cross sectional area of this plate body is less than low-temperature pressure container cross sectional area, and this plate body evenly lays several sieve aperture, plate body overlapping edges is being bolted on several links of low-temperature pressure container inwall, plate body sieve aperture is 3/4 cun, the Raschig ring filler in 1 cun of ring footpath is piled up on packed bed support with the form of the heap that falls apart in a jumble, it is highly 1000 ± 50mm that filler is piled up.
6. the equipment of LNG Liquefied natural gas flashed vapour constant voltage recovery method use according to claim 3, is characterized in that, described supercooled liquid gas inlet employing caliber is the pipeline section of 10 cun, and it is 400 ± 10mm that entrance pipeline section stretches into container length; Described LNG Liquefied natural gas flashed vapour entrance employing caliber is the pipeline section of 4 cun, and it is 400 ± 10mm that pipeline section stretches into container length; The specification of described Raschig ring filler is 304 stainless steels, and ring footpath is 1 cun, and height 1000 ± 50mm piled up by filler; Described ftercompction nitrogen inlet employing caliber is the pipeline section of 4 cun, and it is 200 ± 10mm that entrance pipeline section stretches into container length; Described LNG Liquefied natural gas outlet employing caliber is the pipeline section of 20 cun, and it is 200 ± 10mm that this pipeline section stretches into container length.
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| CN201410584596.4A CN104390125B (en) | 2014-10-27 | 2014-10-27 | Liquefied natural gas flashed vapour constant voltage recovery method and equipment |
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| CN201410584596.4A CN104390125B (en) | 2014-10-27 | 2014-10-27 | Liquefied natural gas flashed vapour constant voltage recovery method and equipment |
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| CN104913196A (en) * | 2015-07-07 | 2015-09-16 | 中国海洋石油总公司 | BOG (boil-off gas) treatment process and device under normal operation condition of LNG (liquefied natural gas) receiving station |
| CN107883672A (en) * | 2017-10-25 | 2018-04-06 | 中石化广州工程有限公司 | A kind of vertical liquefied natural gas after-condenser device |
| CN108020024A (en) * | 2017-11-01 | 2018-05-11 | 中石化广州工程有限公司 | Liquefied natural gas after-condenser device |
| CN109373197A (en) * | 2018-12-11 | 2019-02-22 | 马鞍山钢铁股份有限公司 | A kind of pressure release noise reduction recyclable device for cryogenic liquid tank lorry |
| CN111795293A (en) * | 2019-04-09 | 2020-10-20 | 马格纳斯泰尔汽车技术两合公司 | Storage tank for cryogenic liquefied gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109373197A (en) * | 2018-12-11 | 2019-02-22 | 马鞍山钢铁股份有限公司 | A kind of pressure release noise reduction recyclable device for cryogenic liquid tank lorry |
| CN111795293A (en) * | 2019-04-09 | 2020-10-20 | 马格纳斯泰尔汽车技术两合公司 | Storage tank for cryogenic liquefied gas |
| US11415084B2 (en) | 2019-04-09 | 2022-08-16 | Magna Steyr Fahrzeugtechnik Ag & Co Kg | Storage tank for cryogenic liquid gas |
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| CN104390125B (en) | 2016-06-15 |
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Address after: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Co-patentee after: Offshore Oil Engineering Co., Ltd. Patentee after: China Offshore Oil Group Co., Ltd. Address before: 100010 Chaoyangmen North Street, Dongcheng District, Dongcheng District, Beijing Co-patentee before: Offshore Oil Engineering Co., Ltd. Patentee before: China National Offshore Oil Corporation |