CN110144238A - A kind of liquefied natural gas methods of light hydrocarbon recovery - Google Patents
A kind of liquefied natural gas methods of light hydrocarbon recovery Download PDFInfo
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- CN110144238A CN110144238A CN201910441855.0A CN201910441855A CN110144238A CN 110144238 A CN110144238 A CN 110144238A CN 201910441855 A CN201910441855 A CN 201910441855A CN 110144238 A CN110144238 A CN 110144238A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- 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
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Abstract
The invention discloses a kind of liquefied natural gas methods of light hydrocarbon recovery, this method has product design high, system power dissipation is lower, the high advantage of heat exchange property, the ethane product and LPG product isolated are low-pressure low-temperature form, easily stored and transport, when the recycling yield of liquid-phase product is larger, remarkable in economical benefits, simultaneously using the methane gas liquefaction of part abjection as deposit peak regulation gas source, the gas supply anxiety situation for alleviating Natural Gas Demand vigorous period, significantly improves the economic benefit and the efficiency of management of LNG receiving station.
Description
Technical field
The invention belongs to process for recovering light hydrocarbon more particularly to a kind of novel lighter hydrocarbons suitable for liquefied natural gas receiving station to return
Receiving method.
Background technique
Liquefied natural gas (LNG) is that the world today increases swift and violent clean energy resource, is played to the energy-saving and emission-reduction of countries in the world
Good facilitation.From the point of view of the status of domestic import foreign countries LNG, domestic imported L NG total amount in 2017 is up to 37,890,000
Ton, estimates the year two thousand twenty country for import 310 × 108~560 × 108m3, 2025 by import 130 × 108~560 × 108m3.Entirely
Ball LNG production capacity steadily improves, i.e., will enter production capacity and concentrate acquisition time.
Currently, whole world LNG trade is concentrated mainly on the Asian-Pacific area.It is counted according to international natural gas alliance, Asia-Pacific in 2017
Area's LNG import volume accounts for the 50.3% of the whole world, wherein Japan, China, South Korea occupy LNG global import amount front three.Due to different productions
Its makings of the LNG on ground composition is different, and the LNG of China's import is broadly divided into poor LNG and two kinds of LNG of richness, general C2+ content compared with
More LNG is richness LNG, and poor is poor LNG.Wherein, it is domestic from Australia, Qatar, Algeria etc. it is national and
The middle C2+ component of the LNG of regional import is generally higher, and some Imported LNG product ethane molar constituent can reach 9% or more, C2+
Content may be up to 12% or more.However, ethane plays important work as a kind of good ethylene raw in national product
With.According to data, end 2014, up to 35%, the year two thousand twenty is expected to reach the specific gravity of ethane cracking ethylene in world wide
To 40%；And the domestic ratio for utilizing lighter hydrocarbons ethylene only has 14%, differs farther out with the level of world's lightweight material ethylene,
Wherein one of critically important reason is exactly that the country pays little attention to the recycling of light hydrocarbon in natural gas.If the rich LNG of domestic import
User is supplied after direct boiling, can not only run to LNG and sale enterprise causes no small economic loss, but also can be to domestic second
Alkane ethylene industry causes bigger raw material to bear, and national product and national energy security strategic is made to face bigger safety
Hidden danger and challenge.
It is analyzed from the calorific value regulation of domestic natural gas, the minimum 31.4MJ/ of the higher calorific value of China's civil natural gas
m3, but when light hydrocarbon component is higher in imported L NG, calorific value may be up to 40MJ/m3Or more, calorific value deviation is up to 27.3% or more.
In the case that calorific value in combustion gas is excessively high and user's total heat duties are constant, the tolerance run in pipe network can also be reduced, directly
Connect the safe and efficient operation that threaten gas distributing system.In addition, domestic gas equipment generally has the use calorific value of design, calorific value
After promotion, certain variation can occur for equipment combustion conditions, may make domestic gas incomplete combustion, and calorific value cannot be sufficient
It utilizes, it is also possible to cause other destructions to environment.Therefore, lighter hydrocarbons are recycled from domestic import richness LNG, to the safety of the LNG energy,
Effective use also important in inhibiting.
Development abroad LNG lighter hydrocarbons recovery technology is more early than domestic, as the U.S. begins to recycle gently from LNG in nineteen sixty
Hydrocarbon, and devise numerous LNG lighter hydrocarbons recovery processes, as US3837172, US5114451, US5588308, US6604380B1,
US6907752B2 etc..In addition, the also Japan and Australia etc. of the related isolation technics of external relatively early research LNG are national, and
Achieve preferable research achievement.With being stepped up for domestic LNG import volume, domestic scholars also separate skill to the lighter hydrocarbons of LNG
Art has carried out a large amount of research, achieves biggish breakthrough, the achievement in terms of the cascade utilization of the heat exchange optimization of equipment and cold energy
Significantly.But in conjunction with the lighter hydrocarbons Separation Research status of domestic and international LNG, the LNG lighter hydrocarbons recovery technology in China also occur it is some not
Foot place, main problem have:
(1) part LNG lighter hydrocarbons recovery process use more compressor apparatus, increase recovery process complexity and
Overall flow operation energy consumption makes more difficult to control on process parameter.
(2) the leaner natural gas of makings and C2+ product are only isolated in the process of part, although can reduce to a certain extent
Product calorific value, but ethane and LPG product are not efficiently separated, it is difficult to direct marketing and utilization lead to economic benefit not
Obviously.
(3) heat-exchange network in the process of part is more single, does not sufficiently cause stream using the design principle being thermally integrated
The cooling capacity utilization rate difference and heat energy consumption of journey are excessive, and the economic benefit generated to process causes large effect.
(4) all gas phases of methane product separated in the process of part, when natural gas demand increases, peak modulation capacity
Natural gas peak-shaving is not caught up with or can not carry out.
(5) ethane or LPG product are gas phase mostly in the process of part, need additional energy consumption that product could liquefy, no
It further stores or sells conducive to product.
Summary of the invention
There is provided a kind of methods of light hydrocarbon recovery of novel liquefied natural gas, it is light mainly to solve current LNG by the present invention
Some shortcomings in hydrocarbon isolation technics.This method mainly has following characteristics: it is few that process is heated and pressurizeed equipment, sets in process
Standby parameter is easily controllable；Based on the thought being thermally integrated, cold energy obtains sufficient cascade utilization；Ethane and LPG in the process
Recycling purity and the rate of recovery it is all very high, remarkable in economical benefits.
In order to achieve the above object, technical solution of the present invention is realized by following proposal:
The preheating of first part, raw material LNG:
A, raw material LNG passes through LNG booster pump first and is pressurized to 1.2MPa, after boost in pressure with separated in domethanizing column
The low temperature methane gas shunted afterwards carries out first time heat exchange, and liquefied low temperature methane gas.
B, raw material LNG exchanges heat with the ethane gas of deethanizer overhead again after the preheating of a step.After heat exchange,
Deethanizer overhead gas phase ethane is liquefied by LNG feedstock portions.Raw material LNG enters domethanizing column after being further heated.
Second part, demethanation:
C, raw material LNG enters domethanizing column after two-stage preheats, and the methane gas that tower top comes out is split device and is divided into two strands
Logistics, one logistics for accounting for 20% enter LNG storage tank by reducing pressure by regulating flow after raw material LNG liquefaction and are stored, and in addition one is accounted for
80% logistics then passes through heat exchanger and exchanges heat with step b without complete liquefied ethane logistics, by the second of partial liquefaction
Alkane product liquefies completely.The C2+ product stream of demethanizer bottom is complete with one after throttle valve reduces pressure to 0.83MPa
Low temperature ethane product logistics after full liquefaction exchanges heat, and C2+ stream temperature enters deethanization after being further reduced to -21 DEG C
Tower.
Part III, deethanization:
D, the demethanizer bottom C2+ logistics by step c cooling processing enters the separation that dethanizer carries out ethane, second
Alkane comes out from deethanizer overhead, and C3+ product comes out from dethanizer tower bottom.Effect is detached from order to enhance the ethane of dethanizer
Fruit, pressurization enters deethanizer reflux after the liquid phase ethane logistics in step c are split out one.
The heat exchange of Part IV, product:
E, the low temperature methane after being liquefied in step a by raw material LNG is other than into tank storage, it is also necessary in the natural gas peak-shaving phase
Between vaporize after transport to gas trunklines participate in peak regulation.
F, the ethane product after liquefying completely in step c is split device and is split into two streams, one accounts for 65% logistics
It exchanges heat with the C2+ component after demethanizer bottom throttling cooling, liquid is still kept after heat exchange；Another stock accounts for 35% logistics
0.78MPa is then pressurized to by ethane booster pump and enters deethanizer reflux.
G, in step d dethanizer tower bottom C3+ product stream throttling after by heat exchanger with it is in step c that ethane is complete
Liquefied low temperature methane gas logistics exchanges heat, and is finally fully liquefied into the atmospheric low-temperature LPG product convenient for storage and transport.
Beneficial effects of the present invention: the methane, ethane and LPG of high-purity can be obtained from raw material LNG, methane purity can
Up to 97.54%, the rate of recovery is up to 99.99%；Ethane product purity is up to 98.78%, and ethane recovery is up to 97.72%, LPG
Product recovery rate is up to 98.86%；The flow system uses and is thermally integrated thought, takes full advantage of the cold energy of LNG for each product
Liquefaction, part demethanation gas are used as peak regulation to lay in gas source, the gas supply in Natural Gas Demand vigorous period can be effectively relieved after being liquefied
Nervous situation；Based on cold energy cascade utilization and the maximized principle of system benefit, a kind of efficient heat-exchange network is devised, is made whole
A lighter hydrocarbons recovery process reaches maximum economic benefit with the smallest operation energy consumption.
Detailed description of the invention
Fig. 1 is process equipment flow diagram of the invention.
Wherein, title corresponding to the appended drawing reference in attached drawing are as follows: P1 is LNG booster pump, and E1 is the heat exchange of low temperature methane gas
Device, E2 are ethane heat exchanger, and T1 is domethanizing column, and VLV1 is throttle valve, and E3 is C2+ steam heat exchanger, and T2 is dethanizer, E4
For ethane heat exchanger, TEE1 is methane gas current divider, and TEE2 liquid phase ethane splitter, P2 liquid phase ethane booster pump, E5 is LPG production
Product heat exchanger, VLV2 are liquid phase methane throttle valve, and VLV3 is C3+ logistics throttle valve, and V1 is poor LNG peak regulation storage tank, and M1 is outer defeated
Mixer for natural gas in use.
Specific embodiment
The present invention is further detailed in conjunction with attached drawing and specific case study on implementation.
As shown in Figure 1, a kind of novel liquefied natural gas methods of light hydrocarbon recovery, comprising the following steps:
A, the preheating of unstripped gas: raw material LNG is pressurized to after 1.2MPa by booster pump P1 in the de- of heat exchanger E1 and 20%
Methane overhead gas stream exchanges heat, and the temperature of the raw material LNG after heat exchange is increased to -141~-137 DEG C；Raw material LNG is by de-
It enters heat exchanger E2 after methane gas heat exchange to exchange heat with the gas phase ethane at the top of dethanizer, the temperature of raw material LNG increases
Enter domethanizing column T1 after to -122 DEG C.
B, demethanation: after raw material LNG enters domethanizing column T1, tower top pressure 1.075MPa, tower bottom pressure is
1.175MPa；Methane gas is separated from tower top, is then split into two streams, and wherein one logistics accounts for 20%；Demethanation
The C2+ product stream of tower bottom is cooled to -21 DEG C by liquid phase ethane product after throttling to 0.83MPa and enters dethanizer.
C, deethanization: after C2+ logistics enters dethanizer, tower top pressure 0.8MPa, tower bottom pressure 0.9MPa are theoretical
The number of plates is 15, and 5th block column plate of the liquid phase ethane since tower top that flow back enters；Gas phase ethane from tower top deviate from, C3+ product from
Tower bottom abjection.
D, the heat exchange of product: 20% logistics being diverted from demethanizer overhead methane gas by raw material LNG liquefy to-
137~-125 DEG C, enters storage tank V1 as peak regulation by expenditure and pressure to 0.6MPa and use.The gas deviate from the top of from dethanizer
Phase ethane continues 80% logistics being diverted with demethanizer overhead methane gas after being liquefied by raw material LNG portion and exchanges heat, complete
Full liquefaction is to -60~-50 DEG C.From Deethanizer bottom come out C3+ product reducing pressure by regulating flow after with ethane is liquefied completely after
Methane gas logistics heat exchange is liquefied as LPG product and carries out atmospheric low-temperature storage.
Experimental example one
Treating capacity is 440.5t/h, -162 DEG C of the material temperature of LNG, pressure 0.12MPa, molar content situation are as follows: methane
81.0%, ethane 11.0%, propane 4.1%, normal butane 2.4%, pentane 0.6%, nitrogen 0.9%.
A, the preheating of unstripped gas: the temperature of raw material LNG is -162 DEG C, and pressure 0.12MPa first passes around LNG booster pump
P1 is pressurized to 1.2MPa, the logistics for the 58.1t/h being diverted after pressurization by heat exchanger E1 and demethanizer overhead methane gas
Heat exchange, the temperature of LNG rise to -141.7 DEG C.Raw material LNG is after first time exchanges heat again by heat exchanger E2 and deethanization tower top
The heat exchange of portion's gas phase ethane, temperature enter domethanizing column after being increased to -122 DEG C.
B, demethanation: after raw material LNG enters domethanizing column, tower top methane gas flow is 290.6t/h, and pressure is
1.075MPa, temperature are -118.5 DEG C；The flow of demethanizer bottom C2+ logistics is 149.8t/h, pressure 1.175MPa, temperature
- 8.6 DEG C of degree, pressure reduction is exchanged heat to 0.83MPa by heat exchanger E3 and liquid phase ethane product after throttle valve VLV1 throttling
Temperature afterwards is reduced to -21 DEG C, finally enters dethanizer.
C, deethanization: after C2+ logistics enters dethanizer, the flow of dethanizer top gas phase ethane is 109.8t/h,
Temperature is -37.9 DEG C, pressure 0.8MPa；The C3+ product flow of Deethanizer bottom is 78.4t/h, pressure 0.9MPa, temperature
Degree is 40.6 DEG C, is decompressed to 150kPa by throttle valve VLV3 and low temperature methane gas exchanges heat；The return flow of liquid phase ethane product
For 38.4t/h, return pressure 0.78MPa, temperature is -49.9 DEG C.
D, the heat exchange of product: 20% methane gas logistics being diverted from demethanizer overhead methane gas is fully liquefied
To -125 DEG C, it is decompressed to the laggard tank of 0.6MPa after throttle valve VLV2 throttling and saves as the use of peak regulation gas.Deethanization tower top
By partial liquefaction to -40.7 DEG C of temperature, pressure 0.75MPa after the gas phase ethane in portion and the heat exchange of LNG raw material, gas phase score 0.44,
80% logistics being diverted again with demethanizer overhead methane gas exchanges heat, and is fully liquefied to -50 DEG C of temperature, pressure
0.73MPa.Ethane completely after liquefaction is split into two strands again, one accounting is 65%, flow 71.4t/h, with demethanation
Temperature is -42.8 DEG C after C2+ logistics heat exchange after tower bottom throttling, and pressure 0.715MPa can still keep liquid phase to be stored
And transport.By being liquefied after heat exchanger E5 and the heat exchange of low temperature methane gas after the C3+ product throttling that Deethanizer bottom comes out
It is 0.12MPa at pressure, the atmospheric low-temperature LPG product that temperature is -40 DEG C is stored and sold.
Process for recovering light hydrocarbon logistics analog result is as shown in table 1.
Process for recovering light hydrocarbon logistics analog result in 1 experimental example one of table
Continued 1
Table 2 show the energy consumption of the entire each equipment of lighter hydrocarbons recovery process and the total energy consumption of whole flow process, system total energy
Consumption is calculated as 59160.3kW, and wherein the higher equipment of energy consumption is domethanizing column and dethanizer, mentions with the current other scholars in the country
Lighter hydrocarbons recovery process out is compared, and the energy consumption of the flow system is lower, can be applicable in the LNG lighter hydrocarbons recovery of most domestic well
It stands.
The equipment total energy consumption of lighter hydrocarbons recovery in 2 experimental example one of table
| Unit title | Power (kW) |
| Domethanizing column T1 | 44520.4 |
| Dethanizer T2 | 14285.6 |
| LNG booster pump P1 | 352.9 |
| Liquid phase ethane booster pump P2 | 1.4 |
| The energy consumption of whole system | 59160.3 |
Above-mentioned process has carried out the design and optimization of heat-exchange network to LNG process for recovering light hydrocarbon, using the thought being thermally integrated
Heat-exchange system is optimized, is all liquefied as storing in the form of low-pressure low-temperature by ethane and LPG product by lower energy consumption, in liquid
Economic benefit is obvious when phase light hydrocarbon product separation yield is more, and the methane gas of part abjection is liquefied as poor LNG as peak regulation
Gas source generates huge positive effect to the peak regulation of gas.By this process, the operation of the lighter hydrocarbons recovery of LNG receiving station is passed through
Ji property can significantly improve, and the efficiency of management can also be greatly improved.
The relevant technologies worker of this field may be aware that case as described herein preferably can help reader to manage
Solve the principle of the patent of invention, it should be understood that protection scope of the present invention does not limit to this case.The relevant technologies of this neighborhood
Worker disclosed the technical disclosures can make some groups for not departing from substantive other deformations of the invention according to the present invention
Collaborate journey, but the version of these processes is still fallen within the protection scope of the present invention.
Claims (5)
1. a kind of liquefied natural gas methods of light hydrocarbon recovery, it is characterised in that:
A, raw material LNG first passes through methane gas heat exchanger E1 and demethanizer overhead methane gas point after LNG booster pump P1 pressurization
The logistics flowed out exchanges heat, and the methane gas of shunting is liquefied completely, then passes through ethane heat exchanger E2 and dethanizer top
Ethane gas exchange heat, by gas phase ethane partial liquefaction；
B, raw material LNG enters domethanizing column T1 after two-stage exchanges heat, and is split device TEE1 after tower top abjection methane gas and is split into
Two strands, one is depressurized into storage tank V1 by throttle valve VLV2 as peak regulation natural gas, another burst of low temperature first after being liquefied by raw material LNG
Alkane gas then participates in the heat exchange of other products, and the logistics of demethanizer bottom passes through heat exchanger after throttle valve VLV1 throttling cooling
E3 exchanges heat with liquefaction low temperature ethane product, and temperature enters dethanizer T2 after being reduced to a certain range；
C, other than logistics enters dethanizer T2 in step b, the liquid phase ethane after being fully liquefied there are also one is split device
TEE2, which is shunted, to flow back with after liquid phase ethane booster pump P2 pressurization into dethanizer T2, and gas phase second is deviate from the top of dethanizer
Alkane exchanges heat after the C3+ stream product throttling of bottom abjection with low temperature methane gas；
D, in step b not as the low temperature methane gas logistics of peak regulation gas will by ethane heat exchanger E4 and step a not by
The completely liquefied ethane logistics of raw material LNG exchange heat, and ethane logistics are liquefied completely, then are exchanged heat by heat exchanger E5 by step
C3+ product liquefaction in c is LPG, outer defeated after mixing finally by mixer M1 with the peak regulation natural gas after vaporization.
2. a kind of liquefied natural gas methods of light hydrocarbon recovery according to claim 1, it is characterised in that: raw material LNG in step a
1.2MPa can be pressurized to by LNG booster pump P1, the temperature that the raw material LNG after two-stage preheating enters domethanizing column is -122
℃。
3. a kind of liquefied natural gas methods of light hydrocarbon recovery according to claim 1, it is characterised in that: demethanizer bottom
Pressure is 1175kPa, and the pressure at top is 1075kPa, and demethanizer bottom logistics throttles to 830kPa, by heat exchanger E3 with
Temperature is down to -21 DEG C into dethanizer after the heat exchange of liquid phase ethane product.
4. a kind of liquefied natural gas methods of light hydrocarbon recovery according to claim 1, it is characterised in that: liquid phase second in step c
Alkane is split into two strands, and 35% logistics is pressurized to after 780kPa by ethane booster pump P2 flows back into dethanizer, and in addition one
The logistics that stock accounts for 65% still keeps liquid phase after exchanging heat with demethanizer bottom logistics, and the pressure at the top of dethanizer is 800kPa,
Base pressure is 900kPa.
5. liquefied natural gas methods of light hydrocarbon recovery according to claim 1, it is characterised in that: account for domethanizing column in step d
The low temperature methane gas at top 80% liquefies ethane logistics completely to -50~-60 DEG C.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111732983A (en) * | 2020-06-22 | 2020-10-02 | 西安石油大学 | LNG light hydrocarbon recovery system and method |
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|---|---|---|---|---|
| US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
| CN1821352A (en) * | 2006-01-20 | 2006-08-23 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN103994635A (en) * | 2014-05-07 | 2014-08-20 | 中国寰球工程公司 | Device and method for recovering light hydrocarbon through cold energy of LNG |
| CN105074370A (en) * | 2012-12-28 | 2015-11-18 | 林德工艺装置股份有限公司 | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) |
| CN107082736A (en) * | 2017-04-06 | 2017-08-22 | 西南石油大学 | A kind of liquefied natural gas methods of light hydrocarbon recovery |
-
2019
- 2019-05-24 CN CN201910441855.0A patent/CN110144238B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
| CN1821352A (en) * | 2006-01-20 | 2006-08-23 | 华南理工大学 | Light hydrocarbon separating method for liquefied natural gas with peak regulating function |
| CN105074370A (en) * | 2012-12-28 | 2015-11-18 | 林德工艺装置股份有限公司 | Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas) |
| CN103994635A (en) * | 2014-05-07 | 2014-08-20 | 中国寰球工程公司 | Device and method for recovering light hydrocarbon through cold energy of LNG |
| CN107082736A (en) * | 2017-04-06 | 2017-08-22 | 西南石油大学 | A kind of liquefied natural gas methods of light hydrocarbon recovery |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111732983A (en) * | 2020-06-22 | 2020-10-02 | 西安石油大学 | LNG light hydrocarbon recovery system and method |
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