CN205014753U - Liquefaction recovery unit of LNG container evaporation gas - Google Patents
Liquefaction recovery unit of LNG container evaporation gas Download PDFInfo
- Publication number
- CN205014753U CN205014753U CN201520708720.3U CN201520708720U CN205014753U CN 205014753 U CN205014753 U CN 205014753U CN 201520708720 U CN201520708720 U CN 201520708720U CN 205014753 U CN205014753 U CN 205014753U
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- gas
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- lng
- container
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- 238000011084 recovery Methods 0.000 title claims abstract description 24
- 230000008020 evaporation Effects 0.000 title abstract 8
- 238000001704 evaporation Methods 0.000 title abstract 8
- 239000003507 refrigerant Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 11
- 238000009434 installation Methods 0.000 claims description 5
- 238000005057 refrigeration Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 84
- 239000003949 liquefied natural gas Substances 0.000 description 65
- 238000000034 method Methods 0.000 description 20
- 230000006835 compression Effects 0.000 description 19
- 238000007906 compression Methods 0.000 description 19
- 230000008569 process Effects 0.000 description 7
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005429 filling process Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
Abstract
The utility model provides a liquefaction recovery unit of LNG container evaporation gas for retrieve evaporation in the LNG container after the gas -liquidization to the LNG container in. Recovery unit includes delivery line, heat exchanger, recovery pipeline and refrigerating plant, delivery line one end communicate in the output interface of LNG container, the other end is connected to the heat exchanger, the switch -on of heat exchanger input delivery line, the heat exchanger output is connected retrieve the pipeline, it is connected to to retrieve pipeline one end the output of heat exchanger, the other end communicates extremely the recovery interface of LNG container, refrigerating plant is the mixed refrigerant refrigeration cycle device. Before being liquefied, evaporation gas need not pressurize to evaporation gas through pressurized equipment, come control evaporation gas place container pressure through the pressure before the control evaporation gas -liquidization, the LNG container is got back to in the dead weight of liquefied evaporation gas accessible, needn't establish the container in addition.
Description
Technical field
The utility model relates to the boil-off gas treatment technology of LNG, particularly relates to the recovery device of liquefied of the LNG container boil-off gas that a kind of structure is simple, energy consumption is low.
Background technology
In liquefied natural gas (LNG) transporting procedures, the boil-off gas (BOG) produced due to heat input needs process, and boil-off gas Producing reason and source may comprise:
1, LNG basin heat input.LNG basin is fully heat insulation, and due to economy and reasons in structure, the day vaporization rate of LNG basin design is about 0.05% (in pure CH4) of total capacity.
2, due to the input of SAPMAC method facility heat.The LNG come from basin is by pipeline continuous circulation, and object guarantees that pipeline is not the used time is in low-temperature condition.Circulation LNG will obtain heat, the heat that the low-lift pump work that these heats use from circulation time produces and the heat absorbed from surrounding environment.The LNG stream of endothermic heat returns LNG basin can increase boil-off gas generation.
3, high-pressure pump and the input of pipeline heat.The boil-off gas produced in high pressure pump barrel because of heat leakage is sent back in boil-off gas treatment system or LNG basin;
4, discharging operations.During discharging, the LNG on ship enters basin, and due to the input of heat, and the LNG liquid phase that gas-phase space is transfused to occupies, and can produce a large amount of flashed vapours.
5, due to rolling that LNG layering causes;
6, the boil-off gas that LNG storage and transportation equipment produces in filling process flows back into storage
General boil-off gas can be accommodated in the position such as gas-phase space and boil-off gas house steward of storage tank.According to different to natural gas vaporization gas disposal mode, boil-off gas process is divided into direct output method and condensation method two kinds again.
Direct output method, after boil-off gas is compressed to outer output pressure, directly delivers to gas line network.
Condensation method boil-off gas is compressed to lower pressure (being generally 0.7MPa) again, and the LNG sent from LNG storage tank by LNG low-pressure delivery pump mixes condenser again.Owing to being in supercooled state after LNG pressurization, can make boil-off gas condensation again, condensed LNG is after the pressurization of LNG high-pressure delivery pump, outer defeated through vaporizing.Condensation method can utilize the cold of LNG again, and reduces the consumption of boil-off gas work done during compression.
During direct output method uses, if gas line network does not run for a long time, LNG gas in container can not be arranged outward in time, when gas pressure exceeds peak, can only carry out Stress control with the method for direct outer row.There is the problem of environmental pollution and energy waste.
And when adopting compression method to reclaim, can compress after general boil-off gas also will recover normal temperature, this also result in cold energy waste, and, in compression method, need to adopt compression device, cooling heat exchange equipment etc., equipment is numerous and flow process is loaded down with trivial details, and wherein compression step and cooling step need power consumption.
In a word, in prior art LNG container boil-off gas recovery process in, all reckon without the pressure and low temperature that utilize boil-off gas, but go adopt LNG produce Technologies And Conceptions and technique carry out liquefaction recovery.
Utility model content
For solving the above-mentioned problems in the prior art, the purpose of this utility model is to provide a kind of recovery device of liquefied of LNG container boil-off gas.
There is provided a kind of recovery device of liquefied of LNG container boil-off gas, reclaimed by boil-off gas post liquefaction in LNG container so far in LNG container, described retracting device comprises output pipe, heat exchanger, reclaim line and refrigerating plant; Described output pipe one end is communicated in the output interface of described LNG container, the described heat exchanger that the other end is connected to; Described heat exchanger input connects described output pipe, and described heat exchanger output connects described reclaim line; Described reclaim line one end is connected to the output of described heat exchanger, and the other end is communicated to the recovery interface of described LNG container; Described refrigerating plant is mix refrigerant refrigerating circulatory device.
According to an embodiment, described heat exchanger installation site is higher than the highest liquid level of described LNG container; Described recovery interface is lower than described output interface.
According to an embodiment, described reclaim line installs liquor pump additional, with liquor pump, post liquefaction boil-off gas is delivered to described LNG container through described reclaim line.
According to an embodiment, described boil-off gas directly enters described heat exchanger by described LNG container, the cold liquefaction utilizing described refrigerating plant to provide with described heat exchanger.Described boil-off gas is not pressurizeed.
The beneficial effects of the utility model are: do not need before boil-off gas is liquefied to be pressurizeed to boil-off gas by pressurized equipment; Control boil-off gas container pressure by the pressure before controlling boil-off gas liquefaction, reduce superpressure possibility, reduce unnecessary externally diffusing; The boil-off gas of liquefaction gets back to LNG container by deadweight, separately need not establish container;
The beneficial effects of the utility model are again: self cold energy that can make full use of boil-off gas, overcome Normal practice in boil-off gas pressure process, because boil-off gas self-temperature is lower, the heat produced in pressure process is not easily transferred, cause boil-off gas temperature to raise, add this unfavorable phenomenon of power consumption when boil-off gas is liquefied; The present invention can make boil-off gas liquefaction power consumption cost greatly reduce;
By boil-off gas container controlled pressure, the boil-off gas Stress control that can simplify in the boil-off gas liquefaction flow path newly increased drops into.
Accompanying drawing explanation
Fig. 1 is the recovery device of liquefied structural representation of LNG container boil-off gas in the utility model embodiment.
Description of reference numerals:
LNG container 1, output interface 11, recovery interface 12, output pipe 2, valve 21, articulation 22, heat exchanger 3, reclaim line 4, refrigerating plant 5, first compression set 51, radiator 52, second compression set 53, refrigerant circulation line 54.
Detailed description of the invention
The exemplary embodiments embodying the utility model feature & benefits will describe in detail in the following description.Be understood that the utility model can have various changes in different embodiments, it neither departs from scope of the present utility model, and explanation wherein and to be shown in be use when explain in essence, and be not used to limit the utility model.
As shown in Figure 1, the utility model embodiment provides a kind of recovery device of liquefied of LNG container boil-off gas, to be reclaimed by boil-off gas post liquefaction in LNG container 1 so far in LNG container 1, retracting device can comprise output pipe 2, heat exchanger 3, reclaim line 4 and refrigerating plant 5.
LNG container 1 can be LNG container on general LNG storage tank, vehicle-mounted LNG container or ship, and it is supporting has and unload liquid pipeline and other pipeline accordingly, repeats no more in the utility model.
Output pipe 2 one end is communicated in the output interface 11 of LNG container 1, and the other end is connected to heat exchanger 3; Output pipe 2 can be provided with valve 21, and to control the open and close of output pipe 2, valve 21 can be automatically controlled or instrument control valve, so that carry out Automated condtrol.Output pipe 2 also can arrange an articulation 22, so that carry out the flexible connection of output pipe 2.
Heat exchanger 3 input connects output pipe 2, and heat exchanger 3 output connects reclaim line 4; Heat exchanger 3 can flexible choice for use existing equipment as required.Heat exchanger 3 installation site can be selected higher than the highest liquid level in LNG container 1; And the recovery interface 12 of LNG container 1 will lower than output interface 11.
Reclaim line 4 one end is connected to the output of heat exchanger 3, and the other end is communicated to the recovery interface 12 of LNG container 1; Reclaim line 4 can be provided with valve 21, and to control the open and close of reclaim line 4, valve 21 can be Electromagnetic Control or instrument control valve, so that carry out Automated condtrol.In another embodiment, reclaim line 4 also can install liquor pump additional, with liquor pump, post liquefaction boil-off gas is delivered to LNG container 1 through reclaim line 4.
Refrigerating plant 5 is mix refrigerant refrigerating circulatory device.Mix refrigerant refrigerating circulatory device comprises the first compression set 51, radiator 52, second compression set 53 and refrigerant circulation line 54, above each device is connected in series with refrigerant circulation line 54, first compression set 51 is near the refrigerant outlet of heat exchanger 3, second compression set 53 is near heat exchanger 3 refrigerant inlet, and heat exchanger 3 is between the first compression set 51 and the second compression set 53.Also configurable hybrid refrigeration agent container on refrigerant cycle pipeline 54, wherein mix refrigerant can select Four composition azeotrope.
With reference to shown in Fig. 1, the liquefaction recovery method of LNG container 1 boil-off gas that the utility model embodiment provides, comprises the following steps:
The gas compartment of a, LNG container 1 is communicated to the input of a heat exchanger 3 by output pipe 2, heat exchanger 3 output is communicated to the liquid Space of LNG container 1 by reclaim line 4;
In step a, between LNG container 1 and heat exchanger 3, boil-off gas is flowed by pressure reduction, pressure reduction come from boil-off gas be liquefied in heat exchanger 3 pressure reduce and produce.Boil-off gas keeps temperature when gasifying substantially when entering into heat exchanger, substantially not with extraneous heat exchange, also not have in Normal practice the boil-off gas temperature rising condition that causes to boil-off gas compression, this flow process can make full use of boil-off gas cold energy inherently;
When the gas compartment of b, LNG container 1 reaches setting pressure, such as boil-off gas gas pressure reaches after setting value is about 0.6-0.8MPa, starts a refrigerating plant 5, reduces heat exchanger 3 temperature;
In step b, refrigerating plant 5 adopts azeotrope kind of refrigeration cycle to provide cold for whole liquefaction system; Azeotrope kind of refrigeration cycle can realize the cold required for boil-off gas liquefaction.
After boil-off gas is down to corresponding temperature by c, heat exchanger 3, boil-off gas is liquefied; Boil-off gas temperature in heat exchanger 3 can reach condensing temperature and liquefy, and the boil-off gas of post liquefaction becomes LNG.
In step c, as long as azeotrope kind of refrigeration cycle runs well, the heat exchanger 3 passed through in boil-off gas will reach boil-off gas condensing temperature, boil-off gas post liquefaction, will with liquid form outflow heat exchanger 3, make heat exchanger 3 place gas pressure lower than the pressure of LNG container 1, and the boil-off gas that in LNG container 1, pressure is higher will flow to heat exchanger 3 because of differential pressure action, formation boil-off gas does not have orderly liquidization and flow when extraneous compression power consumption.This is also the energy-conservation major reason of the utility model, is a main aspect of innovation;
The boil-off gas of d, liquefaction is flow automatically or is back to the liquid Space of LNG container 1 by liquor pump.
In steps d, heat exchanger 3 installation site is higher than the highest liquid level of LNG container 1, and post liquefaction boil-off gas because liquid level difference automatic back flow LNG container 1, can reduce flow sheet equipment link; If do not possess the condition of installation site higher than the highest liquid level, by installing liquor pump or post liquefaction boil-off gas is delivered to LNG container 1 by other mode of movement in reclaim line 4.
The utility model embodiment is at least also relative to the beneficial effect of prior art:
1, boil-off gas is directly liquefied without compression, decreases boil-off gas and is compressed link;
2, boil-off gas is directly liquefied without compression, can make full use of boil-off gas self cold energy, reduces liquefaction power consumption;
3, azeotrope flow process can reach or more lower than boil-off gas liquefaction required for low temperature;
4, boil-off gas post liquefaction utilizes deadweight backflow LNG container, can reduce flow sheet equipment link;
5, utilize LNG upper vessel portion gas-phase space, need not separately establish boil-off gas buffer container;
Boil-off gas is directly liquefied without compression, avoids boil-off gas compression power consumption, decreases liquefaction power consumption; Recovery process more simplifies, and do not need buffer container before boil-off gas liquefaction, boil-off gas post liquefaction does not need newly-increased liquid storage vessel.
Unless limited otherwise, the utility model term used is the implication that those skilled in the art understand usually.Embodiment described by the utility model is only for exemplary purpose; and be not used to limit protection domain of the present utility model; those skilled in the art can make other replacements various, changes and improvements in scope of the present utility model; thus; the utility model is not limited to above-mentioned embodiment, and is only defined by the claims.
Claims (3)
1. a recovery device of liquefied for LNG container boil-off gas, reclaimed by boil-off gas post liquefaction in LNG container so far in LNG container, it is characterized in that, described retracting device comprises output pipe, heat exchanger, reclaim line and refrigerating plant;
Described output pipe one end is communicated in the output interface of described LNG container, and the other end is connected to described heat exchanger;
Described heat exchanger input connects described output pipe, and described heat exchanger output connects described reclaim line;
Described reclaim line one end is connected to the output of described heat exchanger, and the other end is communicated to the recovery interface of described LNG container;
Described refrigerating plant is mix refrigerant refrigerating circulatory device.
2. the recovery device of liquefied of LNG container boil-off gas according to claim 1, is characterized in that, described heat exchanger installation site is higher than the highest liquid level of described LNG container.
3. the recovery device of liquefied of LNG container boil-off gas according to claim 1, is characterized in that, described boil-off gas directly enters described heat exchanger by described LNG container, the cold liquefaction utilizing described refrigerating plant to provide with described heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520708720.3U CN205014753U (en) | 2015-09-14 | 2015-09-14 | Liquefaction recovery unit of LNG container evaporation gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520708720.3U CN205014753U (en) | 2015-09-14 | 2015-09-14 | Liquefaction recovery unit of LNG container evaporation gas |
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| Publication Number | Publication Date |
|---|---|
| CN205014753U true CN205014753U (en) | 2016-02-03 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201520708720.3U Active CN205014753U (en) | 2015-09-14 | 2015-09-14 | Liquefaction recovery unit of LNG container evaporation gas |
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| CN (1) | CN205014753U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105927848A (en) * | 2016-04-20 | 2016-09-07 | 中国石油化工股份有限公司 | Small device and method for rapidly re-liquefying and recovering liquefied natural gas vapour |
| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
-
2015
- 2015-09-14 CN CN201520708720.3U patent/CN205014753U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
| CN105927848A (en) * | 2016-04-20 | 2016-09-07 | 中国石油化工股份有限公司 | Small device and method for rapidly re-liquefying and recovering liquefied natural gas vapour |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |