CN205316815U - High -efficient liquefaction recovery unit of natural gas - Google Patents
High -efficient liquefaction recovery unit of natural gas Download PDFInfo
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- CN205316815U CN205316815U CN201521066993.9U CN201521066993U CN205316815U CN 205316815 U CN205316815 U CN 205316815U CN 201521066993 U CN201521066993 U CN 201521066993U CN 205316815 U CN205316815 U CN 205316815U
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Abstract
The utility model relates to a high -efficient liquefaction recovery unit of natural gas. Including low temperature container, natural gas precooling heat exchanger, the tube side both ends of natural gas precooling heat exchanger are connected on natural gas input pipeline, and the natural gas inlet end of natural gas precooling heat exchanger tube side is equipped with admission valve and intake pressure instrumentation, in low temperature container was introduced to natural gas input pipeline, the exit end of its natural gas extended to the liquid nitrogen bottom in the low temperature container, be connected the nitrogen gas blast pipe between the shell side of natural gas precooling heat exchanger and low temperature container's the gaseous phase space, discharge valve and discharge pressure instrumentation are equipped with in natural gas precooling heat exchanger shell pass's nitrogen gas import, the liquid nitrogen is added or LNG takes the pipeline out and is connected with the natural gas inlet end of natural gas precooling heat exchanger, and liquid nitrogen joining or LNG take out and be equipped with the control valve on the pipeline. The utility model discloses can extensively be used for the liquefaction of microminiature air supply, the BOG who especially is fit for the LNG air entrainment retrieves.
Description
Technical field
The low temperature that the utility model relates to Sweet natural gas stores and transport, specifically a kind of efficient recovery device of liquefied of Sweet natural gas.
Background technology
At present, the production of Sweet natural gas, storage and transport mainly contain two kinds of modes: one is gas procedure, uses high pressure to store by pressurization, adopts vehicle or pipeline transportation; Two is by natural gas liquefaction, significantly to reduce storage volume. It is too big that gas vehicle mode accounts for volume, and transport inconvenience, gas pipeline mode must have enough quantity and stable gas source, just likely. And liquid mode, also there is certain sufficient gas source, technology is complicated, and cost of investment is huge. To the continuous or discrete natural air-air source little, loose produced, store and exist or produce in using, then invest too expensive because of prior art and often all cannot reclaim and utilize, drained after major part directly emptying or burning all in vain. Not only waste resource, also pollute the environment, produce potential safety hazard etc.
In existing natural gas liquefaction recovery technology; because Sweet natural gas (mainly methane gas) liquefaction temperature is up to-160 degree; this kind of dark cold generation needs multistage high pressure compressed and condensing heat-exchange; owing to condition is harsh; equipment is all very high; do not reach certain scale and substantially there is no economic worth, be not substantially applicable to the economical and practical technology of discontinuous or small-sized natural gas liquefaction at present. Also have in the prior art and adopt the liquefaction of liquid nitrogen interchanger to reclaim Sweet natural gas, but need heat exchanger area huge, need special low-temperature (low temperature) vessel equipment, complicated operation is not also accepted by market in addition.
Practical novel content
The problems referred to above that the utility model exists for prior art, it is provided that a kind of low cost, the efficient recovery device of liquefied of Sweet natural gas being convenient to application.
The utility model solves the technical scheme of its technical problem employing:
A kind of efficient recovery device of liquefied of Sweet natural gas, comprising: low-temperature (low temperature) vessel, fills liquid nitrogen in low-temperature (low temperature) vessel, and gas-phase space is arranged at the liquid nitrogen top in low-temperature (low temperature) vessel;
Sweet natural gas precool heat exchanger device, the pipe journey two ends of Sweet natural gas precool heat exchanger device are connected on Sweet natural gas input channel, and the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device Guan Cheng is equipped with intake valve and intake pressure measuring instrument;Sweet natural gas input channel is introduced in low-temperature (low temperature) vessel, and the exit end of its Sweet natural gas extends to the liquid nitrogen bottom in low-temperature (low temperature) vessel;
Being connected nitrogen exhaust pipe between the shell side of Sweet natural gas precool heat exchanger device and the gas-phase space of low-temperature (low temperature) vessel, the nitrogen inlet of Sweet natural gas precool heat exchanger device shell side is equipped with vent valve and exhaust pressure measuring instrument;
Liquid nitrogen adds or LNG extraction pipeline is connected with the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device, and liquid nitrogen adds or on LNG extraction pipeline, control valve is housed;
Intake valve and intake pressure measuring instrument, vent valve and exhaust pressure measuring instrument, control valve are connected with controller.
Further, nitrogen exhaust pipe internal diameter sectional area is greater than the internal diameter cross-sectional area of Sweet natural gas input channel.
Further, Sweet natural gas input channel is one or more, introduces from low-temperature (low temperature) vessel top and the liquid nitrogen bottom immediate vicinity that extends perpendicularly in low-temperature (low temperature) vessel, and the exit end of Sweet natural gas arranges guiding device.
Further, Sweet natural gas precool heat exchanger device is vertical or is inclined and mounted on the top of low-temperature (low temperature) vessel.
Further, low-temperature (low temperature) vessel is 450L low temperature cylinder.
Principle of the present utility model is:
Utilize liquid nitrogen boiling point for-196 DEG C and Sweet natural gas (main nail alkane, below all for methane gas characteristic) liquefaction temperature be-161.5 degree, methane freezing temperature is the difference of-182.5 boiling points different separately spent, freezing point and temperature of saturation and pressure, as long as controlling liquid nitrogen temperature higher than-182.5 DEG C (such as-181 DEG C), then leading to the methane in liquid nitrogen and would not freeze and can liquefy rapidly. Again because in control low-temperature (low temperature) vessel, liquid nitrogen temperature of saturation point is far below the boiling point of liquid methane, methane can not gasify at this temperature and pressure; Liquid nitrogen will heat up after absorbing the Sweet natural gas heat energy led to, when liquid nitrogen temperature is higher than the saturation pressure value controlled, it is vaporized and temperature under maintaining the saturation pressure of control with regard to having part liquid nitrogen, liquefaction is entered along with continuous outside Sweet natural gas, liquid nitrogen in low-temperature (low temperature) vessel also will progressively be vaporized amount discharge container, after the liquid nitrogen in low-temperature (low temperature) vessel is all vaporized discharge, liquid in container has all been replaced as liquid natural gas and LNG.
LNG liquid now is still supercooled liquid near freezing point temperature, at this temperature, Sweet natural gas can not be vaporized, because of the evenly vaporization of the liquid nitrogen overwhelming majority under original control pressure, nitrogen is not had to discharge again, under original valve opening, pressure of the inside of a bottle meeting rapid reduction, liquid nitrogen remaining under new pressure continues to be vaporized discharges outside low-temperature (low temperature) vessel, so just achieve being separated of liquid nitrogen and LNG, that is: under liquid methane and liquid nitrogen mix, the liquefaction of Sweet natural gas can be completed by high efficient heat exchanging, can finally make again liquid nitrogen vaporization separate completely from LNG liquid.
In sum, adopting the utility model of technique scheme, compared with prior art, its useful effect is:
By control low-temperature (low temperature) vessel internal liquid saturation pressure, thus indirectly control the temperature of low temperature saturated liquid temperature higher than Sweet natural gas freezing point, Sweet natural gas is only liquefied, and liquid nitrogen vaporization is separated; Judge whether liquid nitrogen all vaporizes discharge by measuring the pressure change of turnover low-temperature (low temperature) vessel gas again; Reclaim the available full liquid nitrogen vessel directly more renewed after terminating, or control container pressure, the Sweet natural gas of liquefaction is exported in other container, add liquid nitrogen again and reuptake Sweet natural gas, it is achieved reclaim continuously. The maximum advantage of the utility model is exactly that equipment investment cost is cheap, does not affect again LNG and normally uses, can extensively for the liquefaction in mini-gas source, and the BOG being especially applicable to LNG aerating reclaims.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model embodiment;
In figure: 1-low temperature cylinder; 2-nitrogen exhaust pipe; 3-Sweet natural gas input channel; 4-Sweet natural gas precool heat exchanger device; 5-intake pressure measuring instrument; 6-exhaust pressure measuring instrument; 7-controller; 8-vent valve; 9-intake valve; 10-control valve; 11-liquid nitrogen adds or LNG extracts pipeline out.
Embodiment
Below in conjunction with embodiment, the utility model is further elaborated, but the utility model is not formed any restriction by the present embodiment.
The present embodiment reclaims with the BOG of the LNG storage tank of LNG gas station and is described.
See Fig. 1, the low-temperature (low temperature) vessel in the present embodiment is special 450L low temperature cylinder 1, is filled with the liquid nitrogen of about the 0.3mpa of 90% volume before input; The pipe journey two ends of Sweet natural gas precool heat exchanger device 4 are connected on Sweet natural gas input channel 3, and the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device 4 pipe journey is equipped with intake valve 9 and intake pressure measuring instrument 5; Sweet natural gas input channel 3 is introduced in low temperature cylinder 1, and the exit end of its Sweet natural gas extends to the liquid nitrogen bottom in low temperature cylinder 1;
Being connected nitrogen exhaust pipe 2 between the shell side of Sweet natural gas precool heat exchanger device 4 and the gas-phase space of low temperature cylinder 1, the nitrogen inlet of Sweet natural gas precool heat exchanger device 4 shell side is equipped with vent valve 8 and exhaust pressure measuring instrument 6;
Liquid nitrogen adds or LNG extraction pipeline 11 is connected with the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device 4, and liquid nitrogen adds or on LNG extraction pipeline 11, control valve 10 is housed;
Intake valve 9 and intake pressure measuring instrument 5, vent valve 8 and exhaust pressure measuring instrument 6, control valve 10 are connected with controller 7.
Because the present embodiment is the BOG gas for reclaiming LNG storage tank, thus can closed control valve 10, it is even possible that do not establish liquid nitrogen to add or LNG extracts pipeline 11 and control valve 10 out; After BOG liquefaction is reclaimed, low temperature cylinder 1 can be carried out supercharging, it is pressurized in low temperature cylinder 1 pressure higher than, after LNG storage tank pressure, directly by the gas phase vapor pipe of Sweet natural gas input channel 3, intake valve 9 and LNG storage tank, being injected to storage tank from LNG storage tank top by low temperature LNG.
Intake valve 9 connects the gas phase exhaust line of gas station LNG storage tank, when LNG storage tank pressure arrival discharge BOG pressure or when needing to be convenient to back gas operation for storage tank reduction pressure, open intake valve 9, if when the force value of intake pressure measuring instrument 5 is worth higher than exhaust pressure measuring instrument 6, wouldn't be begun to rehearse air valve 8, if intake pressure measuring instrument 5 cuts exhaust pressure measuring instrument 6 pressure reduction lower than certain value, or when needing the force value of control in the low temperature cylinder 1 of exhaust pressure measuring instrument 6 pressure higher than setting, all open vent valve 8 what open intake valve 9 simultaneously, vent valve 8 adopts variable valve, the pressure that the pressure of low temperature cylinder 1 and exhaust pressure measuring instrument 6 show.
After intake valve 9 is opened, first BOG gas be passed into precooling in Sweet natural gas precool heat exchanger device 4, the Sweet natural gas input channel 3 of the BOG of precooling by connecting with low temperature cylinder 1, it is passed in the liquid nitrogen bottom the low temperature cylinder 1 of in-built liquid nitrogen, the Sweet natural gas that temperature is higher liquefies rapidly with very low temperature liquid direct heat exchange in container after entering liquid nitrogen, and the Sweet natural gas of liquefaction is stored in low temperature cylinder 1.
Meanwhile liquid nitrogen heat absorption can heat up vaporization, very low temperature nitrogen after vaporization is passed into Sweet natural gas precool heat exchanger device 4 from low temperature cylinder 1 top by nitrogen exhaust pipe 2 and vent valve 8, in Sweet natural gas precool heat exchanger device 4, nitrogen continues release cold energy, owing to Sweet natural gas precool heat exchanger device 4 Area comparison is big, in addition inner cryogenic nitrogen and the comparatively high temps BOG gas temperature difference are relatively big, can discharge after being reclaimed further by nitrogen cold energy rapidly.Owing to Sweet natural gas precool heat exchanger device 4 is arranged on low temperature cylinder 1 top, in Sweet natural gas precool heat exchanger device 4 by the small part Sweet natural gas of precooling and the few part LNG that may be taken out of by nitrogen in Sweet natural gas precool heat exchanger device 4 because of decrease in velocity, in Sweet natural gas precool heat exchanger device 4 under gas-liquid separation device and action of gravity, Sweet natural gas precool heat exchanger device 4 no matter shell side or the LNG liquid of Guan Chengzhong all can automatic back flow in low temperature cylinder 1.
In removal process, controller 7 detects the pressure in exhaust pressure measuring instrument 6 in real time, the aperture of control vent valve, make low temperature cylinder 1 inner control pressure between 0.41-0.5mpa gauge pressure, thus indirectly control fluid temperature in low temperature cylinder 1 and, at-181 to-179 degree, Sweet natural gas is only liquefied.
Leading in liquefaction process at Sweet natural gas, controller 7 is measured by intake pressure measuring instrument 5 and exhaust pressure measuring instrument 6 in real time and is changed into and out of low temperature cylinder 1 gas pressure change and pressure reduction, judges whether liquid nitrogen all vaporizes, completes to reclaim. Concrete grammar is: when vent valve 8, intake valve 9 aperture all do not change, before entering people's low temperature cylinder 1, intake pressure measuring instrument 5 is without under considerable change, inlet outlet pressure differential and between intake pressure measuring instrument 5, exhaust pressure measuring instrument 6 pressure obviously become big, and exhaust pressure measuring instrument 6 is reduced to close to (lower than 0.05mpa) when 0, can judge that liquid nitrogen has all been vaporized discharge, now must close rapidly vent valve 8, prevent from occurring in container negative pressure, by outside air intake.
After vent valve 8 is closed, now the LNG fluid temperature in low temperature cylinder 1 is still the supercooled liquid of about-180 degree left and right, and its saturation pressure is close to 0, still can absorb natural gas liquids in a large number, is now divided into two kinds of situations to carry out different process:
Directly the LNG of recovery is sent back in original LNG storage tank again, now by following operation:
(1) when continuing to lead to Sweet natural gas make pressure in low temperature cylinder 1 reach recovery that about 0.2mpa-0.4mpa (will lower than original LNG storage tank in pressure) namely can be considered a BOG, now can start low temperature cylinder 1 from supercharging system, or introduce pressurising medium from outside to the gas-phase space of low temperature cylinder.
(2) when (be namely equivalent to exhaust pressure measuring instrument 6 pressure higher than intake pressure measuring instrument 5 pressure after) after pressure in low temperature cylinder 1 is higher than LNG storage tank pressure, the LNG liquid in low temperature cylinder 1 can be back in LNG storage tank automatically from low temperature cylinder 1. Because the container inner pressure in the BOG recovery of control low temperature cylinder 1 is lower than the pressure of LNG storage tank, the temperature of low temperature cylinder 1 will lower than the BOG temperature in storage tank and in pipeline, like this in the LNG reflux course in low temperature cylinder 1, BOG gas in LNG storage tank and BOG pipeline will be reduced pressure by liquefaction, its effect is the LNG velocity of discharge that can accelerate in low temperature cylinder 1, effect two can be change in gas cylinder process prevent LNG storage tank superpressure after being reduction of the pressure of storage tank, and the recovery gas cylinder for more renewing provides sufficient surge time.
(3) after detecting that the LNG of recovery is substantially emptying by the liquidometer of installation in low temperature cylinder 1, or low temperature storage tank intake pressure 5 detected after equal with going out pressure 6 (after liquid all discharges, there is no liquid-flow, pressure balances very soon), intake valve 9 can be closed, complete the discharge of the LNG of post liquefaction. Then can open and add nitrogen control valve 10 and by Sweet natural gas input channel 3, liquid nitrogen is added in low temperature cylinder 1, when adding 95% capacity that liquid nitrogen arrives low temperature cylinder 1, can restart to open intake valve 9 and carry out new aerating and reclaim BOG process.
(4) the method and simple, only need the auxiliary instrument of the gas cylinder of an a few hectolitre and small part, valve, pipeline and a little type heat exchanger etc. just can complete whole removal process, its cost of investment less than existing recovery technology cost of investment three/once the recovery that can realize BOG.
In low temperature cylinder 1 liquid nitrogen all emptying, low temperature cylinder 1 internal pressure be close to 0, after closing vent valve 8, now also can carry out reclaimer operation by the method for the low temperature cylinder 1 more renewed, concrete steps are as follows:
(1) intake valve 9 is continued to open, close vent valve 8, continue through Sweet natural gas precool heat exchanger device 4 and Sweet natural gas is delivered to low temperature cylinder 1 by Sweet natural gas input channel 3, now in container, LNG fluid temperature can progressively raise, when being elevated to LNG boiling temperature, in low temperature cylinder 1, pressure can progressively rise, and controller 7 detects the pressure of exhaust pressure measuring instrument 6 namely when pressure in low temperature cylinder 1 reaches the settings of 0.5mpa-0.8mpa, close all valves, stop Sweet natural gas and reclaim.
(2) after having reclaimed, the low temperature cylinder 1(having reclaimed full low temperature cylinder 1 volume 80-90% volume was filled liquid nitrogen 90% time originally, pressure when different liquid nitrogen initial temperature reclaims with BOG is different, the LNG volume being recovered to is different, but arrive the packing volume of initial liquid nitrogen never) pull down, change the new low-temperature (low temperature) vessel filling liquid nitrogen 90% and just can re-start new BOG removal process.
Claims (5)
1. the efficient recovery device of liquefied of Sweet natural gas, it is characterised in that, comprising:
Low-temperature (low temperature) vessel, fills liquid nitrogen in low-temperature (low temperature) vessel, gas-phase space is arranged at the liquid nitrogen top in low-temperature (low temperature) vessel;
Sweet natural gas precool heat exchanger device (4), the pipe journey two ends of Sweet natural gas precool heat exchanger device (4) are connected on Sweet natural gas input channel (3), and the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device (4) Guan Cheng is equipped with intake valve (9) and intake pressure measuring instrument (5); Sweet natural gas input channel (3) is introduced in low-temperature (low temperature) vessel, and the exit end of its Sweet natural gas extends to the liquid nitrogen bottom in low-temperature (low temperature) vessel;
Being connected nitrogen exhaust pipe (2) between the shell side of Sweet natural gas precool heat exchanger device (4) and the gas-phase space of low-temperature (low temperature) vessel, the nitrogen inlet of Sweet natural gas precool heat exchanger device (4) shell side is equipped with vent valve (8) and exhaust pressure measuring instrument (6);
Liquid nitrogen adds or LNG extraction pipeline (11) is connected with the Sweet natural gas air inlet end of Sweet natural gas precool heat exchanger device (4), and liquid nitrogen adds or on LNG extraction pipeline (11), control valve (10) is housed;
Intake valve (9) and intake pressure measuring instrument (5), vent valve (8) and exhaust pressure measuring instrument (6), control valve (10) are connected with controller (7).
2. the efficient recovery device of liquefied of Sweet natural gas according to claim 1, it is characterised in that: nitrogen exhaust pipe (2) internal diameter sectional area is greater than the internal diameter cross-sectional area of Sweet natural gas input channel (3).
3. the efficient recovery device of liquefied of Sweet natural gas according to claim 1, it is characterized in that: Sweet natural gas input channel (3) is one or more, the liquid nitrogen bottom immediate vicinity introduced from low-temperature (low temperature) vessel top and extend perpendicularly in low-temperature (low temperature) vessel, the exit end of Sweet natural gas arranges guiding device.
4. the efficient recovery device of liquefied of Sweet natural gas according to claim 1, it is characterised in that: Sweet natural gas precool heat exchanger device (4) is vertical or is inclined and mounted on the top of low-temperature (low temperature) vessel.
5. the efficient recovery device of liquefied of Sweet natural gas according to claim 1, it is characterised in that: low-temperature (low temperature) vessel is 450L low temperature cylinder.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201521066993.9U CN205316815U (en) | 2015-12-21 | 2015-12-21 | High -efficient liquefaction recovery unit of natural gas |
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| CN201521066993.9U CN205316815U (en) | 2015-12-21 | 2015-12-21 | High -efficient liquefaction recovery unit of natural gas |
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| CN205316815U true CN205316815U (en) | 2016-06-15 |
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| CN201521066993.9U Expired - Fee Related CN205316815U (en) | 2015-12-21 | 2015-12-21 | High -efficient liquefaction recovery unit of natural gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108413245A (en) * | 2018-05-24 | 2018-08-17 | 浙江智海化工设备工程有限公司 | Compressed gas recovery system and recovery method in a kind of cryogenic liquid transport tank car |
| CN108870867A (en) * | 2018-09-05 | 2018-11-23 | 上海宝钢气体有限公司 | A kind of liquefying plant and its application method using liquid nitrogen high efficiente callback high value residual air |
| 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 |
| CN112272768A (en) * | 2018-06-08 | 2021-01-26 | 欧姆龙株式会社 | Micro-hotplate and MEMS gas sensor |
| CN113984827A (en) * | 2021-10-25 | 2022-01-28 | 重庆科技学院 | Simulation experiment device and method for natural gas liquefaction performance by supersonic nozzle |
| 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 |
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2015
- 2015-12-21 CN CN201521066993.9U patent/CN205316815U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108413245A (en) * | 2018-05-24 | 2018-08-17 | 浙江智海化工设备工程有限公司 | Compressed gas recovery system and recovery method in a kind of cryogenic liquid transport tank car |
| CN112272768A (en) * | 2018-06-08 | 2021-01-26 | 欧姆龙株式会社 | Micro-hotplate and MEMS gas sensor |
| CN108870867A (en) * | 2018-09-05 | 2018-11-23 | 上海宝钢气体有限公司 | A kind of liquefying plant and its application method using liquid nitrogen high efficiente callback high value residual air |
| 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 |
| CN113984827A (en) * | 2021-10-25 | 2022-01-28 | 重庆科技学院 | Simulation experiment device and method for natural gas liquefaction performance by supersonic nozzle |
| CN113984827B (en) * | 2021-10-25 | 2023-11-21 | 重庆科技学院 | Device and method for simulating natural gas liquefaction performance of supersonic jet pipe |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160615 Termination date: 20181221 |
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| CF01 | Termination of patent right due to non-payment of annual fee |