CN103994635B - The apparatus and method that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons - Google Patents
The apparatus and method that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons Download PDFInfo
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- CN103994635B CN103994635B CN201410191260.1A CN201410191260A CN103994635B CN 103994635 B CN103994635 B CN 103994635B CN 201410191260 A CN201410191260 A CN 201410191260A CN 103994635 B CN103994635 B CN 103994635B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
- F25J3/0214—Liquefied natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
Abstract
The present invention discloses the apparatus and method that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons, the LNG pressurizations in LNG storage tank are pumped out to LNG delivery trunk lines by the first force (forcing) pump, LNG is divided into two plumes by first flow distributor and separately flows into LNG the first pipelines of output and LNG the second pipelines of output；The LNG plumes that LNG is exported in the first pipeline are flowed into the top of domethanizing column by heat exchange the 3rd pipeline of output after being exchanged heat through First Heat Exchanger；The LNG plumes that LNG is exported in the second pipeline are flowed into the middle part of domethanizing column by heat exchange the 17th pipeline of output after being exchanged heat through the second heat exchanger；Domethanizing column carries out rectifying separation to the LNG plumes for flowing into portion region and central region thereon, and the tower top of domethanizing column produces lean gas, bottom of towe and obtains C2+；Lean gas is used for after First Heat Exchanger heat exchange condensation the output that exchanges heat again；C2+ feeding dethanizers are subjected to rectifying separation, the gas main component that the tower top of dethanizer is produced is ethane, bottom of towe obtains LPG, pressurized to pump out and be stored in LPG storage tanks.
Description
Technical field
It is same using cold energy of liquefied natural gas recovery lighter hydrocarbons in particular to one kind the present invention relates to lighter hydrocarbons recovery field
The apparatus and method of Shi Lengning lean gases.
Background technology
As the world is increasingly vigorous to the demand of the energy, traditional energy resource structure has been difficult to meet multiple demands, day
Right gas has turned into after the third-largest energy after coal, oil, and as a kind of high-quality, efficient, cleaning the energy, it is in Energy Mix
Shared ratio is increasingly improved.The liquefaction accumulating of natural gas is advantageously implemented distributing rationally for resource.Liquefied natural gas (LNG,
Liquefied Natural Gas) in addition to mainly containing methane, also a small amount of ethane, propane and butane are also possible in addition
Contain nitrogen.According to the difference of C2+ lighter hydrocarbons content in LNG, LNG can be divided into lean gas and rich gas.At present, international LNG in the markets have
Quite a few is rich gas (C2, C3 containing mass fraction more than 10%, and a small amount of C4 hydro carbons).C2+ lighter hydrocarbons in rich gas are
A kind of high-quality and widely used industrial chemicals, with very high added value, naphtha is replaced with it as the raw material energy of ethene
Enough reduce investment outlay 30%, ethylene unit energy consumption reduction by 30~40%, integrated cost reduction by 10% or so.
LNG under normal pressure is -161 DEG C of liquid, has contained the cold energy of a large amount of high-quality.LNG is being transported to pipe network user
Before need gasification, gasification is typically to be realized using seawater or air heating, although this method is simple directly, is wasted
The a large amount of valuable cold energy contained in LNG.The cold energy discharged when LNG under 0.1MPa is from -161 DEG C of re-heats to 27 DEG C is about
The huge high-quality cold energy that 950KJ/Kg, LNG contain will be great waste if not being subject to recycling.Therefore, using LNG certainly
The cold of body, is come out the lighter hydrocarbons resource separation in rich gas with relatively low cost, the synthesis for being advantageously implemented natural gas resource is excellent
Change and utilize.
Because the LNG industries of China are just at the early-stage, the current country rarely has the report of related LNG lighter hydrocarbons isolation technics, and
It is external just to have the technical literature that LNG lighter hydrocarbons are separated early in the sixties in last century.In the U.S., C2+ lighter hydrocarbons have been isolated from LNG
It is allowed to meet the important means of American National combustion gas standard as regulation heating value of natural gas.In recent years, LNG lighter hydrocarbons isolation technics exists
The states such as the U.S., Japan have got back significant progress and application, and this is China separates lighter hydrocarbons from the LNG rich gases of coastal introduction
To good directive function.With the foundation of China's relevant criterion and specification and sound, increasing certainly will be played by from LNG reclaiming lighter hydrocarbons
Plus LNG receiving stations operating flexibility, adapt to user's request diversity and improve many-sided demand of factory economy type.
The content of the invention
The present invention provides the apparatus and method that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons, to utilize LNG cold energy
Reclaiming LPG, (Liquefied Petroleum Gas, liquefied petroleum gas, abbreviation LPG, key component is propane and butane, i.e., gently
Hydrocarbon).
To reach above-mentioned purpose, the invention provides the device that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons, including
LNG storage tank, LPG storage tanks, First Heat Exchanger, the second heat exchanger, domethanizing column, dethanizer, poor air compressor, gas-liquid separation
Tank, surge tank, first flow distributor, the first force (forcing) pump, the second force (forcing) pump, the 3rd force (forcing) pump, the 4th force (forcing) pump, slender acanthopanax
Press pump, LNG delivery trunks line, LNG export the first pipeline, LNG and export the second pipeline, the 3rd pipeline of heat exchange output, methane gas phase
Export the 4th pipeline, methane gas-liquid mixed and export the 5th pipeline, the 6th pipeline of gas phase methane output, liquid phase methane the 7th pipe of output
Line, compressed methane export the 8th pipeline, gas phase heat exchange output the 9th pipeline, outer defeated tenth pipeline, heat exchange output the 17th pipeline,
C2+ exports the 11st pipeline, C2 and exports the 12nd pipeline, the 13rd pipeline of C2 heat exchange outputs, the 14th pipeline of C2 backflows, LPG
Store into the pipeline of tank the 16th, wherein
First force (forcing) pump is located in the LNG storage tank, described LNG delivery trunks line one end and first force (forcing) pump
Connection, the other end is connected with the first flow distributor, and the first flow distributor is managed with LNG outputs first
Line and the LNG export the connection of the second pipeline, and first force (forcing) pump pumps out the LNG pressurizations in the LNG storage tank to described
LNG delivery trunk lines, LNG is divided into two plumes by the first flow distributor and separately flows into the first pipeline of the LNG outputs
And the LNG exports the second pipeline；
The LNG exports the first pipeline and is connected with the first pipeline of the First Heat Exchanger, and the of the First Heat Exchanger
One pipeline is connected with the 3rd pipeline of the heat exchange output, and the top of heat exchange the 3rd pipeline of output and the domethanizing column connects
Connect, the LNG plumes that the LNG is exported in the first pipeline export the 3rd pipeline after being exchanged heat through the First Heat Exchanger by the heat exchange
Flow into the top of the domethanizing column；
The LNG exports the second pipeline and is connected with the first pipeline of second heat exchanger, and the of second heat exchanger
One pipeline is connected with the 17th pipeline of the heat exchange output, the middle part of heat exchange the 17th pipeline of output and the domethanizing column
Connection, the LNG plumes that the LNG is exported in the second pipeline export the 17th after being exchanged heat through second heat exchanger by the heat exchange
Pipeline flows into the middle part of the domethanizing column；
The domethanizing column carries out rectifying separation to the LNG plumes for flowing into portion region and central region thereon, through multistage gas
After liquid mass transfer, the tower top of the domethanizing column produces lean gas, bottom of towe and obtains C2+ (more than C2 gases)；
The top of the domethanizing column connects the methane gas phase and exports the 4th pipeline, and the methane gas phase output the 4th is managed
Line is connected with the second pipe of the First Heat Exchanger, and the second pipe of the First Heat Exchanger and the methane gas-liquid mixed are defeated
Go out one end connection of the 5th pipeline, the other end that the methane gas-liquid mixed exports the 5th pipeline is connected to the gas-liquid separation
Tank, one end that the liquid-phase outlet of the knockout drum exports the 7th pipeline with the liquid phase methane is connected, the gas-liquid separation
One end that the gaseous phase outlet of tank exports the 6th pipeline with the gas phase methane is connected；The liquid phase methane exports the 7th pipeline and institute
The top connection of domethanizing column is stated, second force (forcing) pump is located at the liquid phase methane and exported on the 7th pipeline；The gas phase first
The other end that alkane exports the 6th pipeline be connected with the poor air compressor, and the poor air compressor and the compressed methane export the
One end connection of eight pipelines, the 3rd pipeline of the other end and the First Heat Exchanger that the compressed methane exports the 8th pipeline connects
Connect, the 3rd pipeline of the First Heat Exchanger is connected with gas phase heat exchange the 9th pipeline of output；Gas phase heat exchange output the
Nine pipelines are connected with outer defeated tenth pipeline, and the 3rd force (forcing) pump is located on outer defeated tenth pipeline；
It is cold that the lean gas exports part after the 4th pipeline is exchanged heat into the First Heat Exchanger along the methane gas phase
Solidifying to form gas-liquid two-phase, the lean gas of gas-liquid two-phase exports the 5th pipeline into the gas-liquid point through the methane gas-liquid mixed
Gas phase and liquid phase separation are carried out from tank；The lean gas of liquid phase exports the 7th pipeline through the liquid phase methane and enters the demethanation
The top of tower constitutes the liquid phase plume for flowing back and providing needed for the domethanizing column progress rectifying separation；The lean gas warp of gas phase
The gas phase methane exports the 6th pipeline and enters the poor air compressor, and the poor air compressor adds the lean gas of gas phase
Pressure, the lean gas after pressurization exports the 3rd pipeline heat exchange that the 8th pipeline enters the First Heat Exchanger through the compressed methane
Exported to liquid phase and by gas phase heat exchange the 9th pipeline of output to outer defeated tenth pipeline, the 3rd force (forcing) pump is added
Press pump is defeated by user beyond going out；
The bottom of towe of the domethanizing column exports the 11st pipeline by the C2+ with the dethanizer and is connected, for inciting somebody to action
The C2+ that the bottom of towe of the domethanizing column is obtained sends into the dethanizer and carries out rectifying separation, described after multi-stage gas-liquid mass transfer
The gas main component that the tower top of dethanizer is produced is ethane, bottom of towe obtains LPG；
The tower top of the dethanizer exports the second pipe of the 12nd pipeline and second heat exchanger by the C2
One end connection, the other end of the second pipe of second heat exchanger passes through C2 heat exchange the 13rd pipeline of output and the buffering
Tank is connected, and the surge tank is connected by the C2 the 14th pipelines of backflow with the tower top of the dethanizer, and the described 4th adds
Press pump is located at the C2 and flowed back on the 14th pipeline, and the gas that the tower top of the dethanizer is produced passes through second heat exchanger
Liquid phase is condensed into after heat exchange into the surge tank, it is pumped out to the dethanizer by the 4th force (forcing) pump is pressurized
The top that tower top enters the dethanizer constitutes the liquid phase stock for flowing back and providing needed for the dethanizer progress rectifying separation
Stream；
The bottom of towe of the dethanizer is stored by the LPG and is connected into the pipeline of tank the 16th with the LPG storage tanks, described
5th force (forcing) pump is located at the LPG and stored on the pipeline of tank the 16th, and the 5th force (forcing) pump is by the bottom of towe of the dethanizer
The lighter hydrocarbons pressurization of generation pumps out and is stored in the LPG storage tanks.
Wherein, it is additionally provided with gas phase and exports the 9th looped pipeline line and gas phase regulating valve, the gas phase exports the one of the 9th looped pipeline line
End exports the 8th pipeline with the compressed methane and is connected, and its other end is connected with gas phase heat exchange the 9th pipeline of output, makes to add
A lean gas part after pressure exports the 9th looped pipeline line by the gas phase and flows directly into outer defeated tenth pipeline；The gas
Phase regulating valve is located at the gas phase and exported on the 9th looped pipeline line, and it is secondary that the gas phase governor valve control flows through the gas phase output the 9th
The flow of the lean gas of pipeline, the aperture of the gas phase regulating valve makes the first pipeline and the 3rd pipeline of the First Heat Exchanger
The temperature difference maintain between+25 DEG C~+30 DEG C.
Wherein, the bottom of towe of the domethanizing column and the bottom of towe of the dethanizer are respectively equipped with the first reboiler and second again
Device is boiled, for making the liquid of tower reactor in the domethanizing column and the dethanizer vaporize again.
Wherein, ethane storage tank, second flow distributor, C2+ is additionally provided with to store into the pipeline of tank the 15th and the 6th pressurization
Pump, the second flow distributor is connected to the surge tank and the 14th pipeline junction of C2+ backflows, for controlling
The liquid phase plume of the surge tank enters the flow of the de- ethene column overhead, and the 6th force (forcing) pump is located at the C2+ storages
Enter on the pipeline of tank the 15th, the ethane storage tank is connected to the C2+ and stores output end into the pipeline of tank the 15th.
Wherein, the First Heat Exchanger and second heat exchanger are that plate sticks up formula heat exchanger.
The present invention also provides a kind of method that device for reclaiming lighter hydrocarbons using above-mentioned cold energy of liquefied natural gas reclaims lighter hydrocarbons,
Comprise the following steps：
The LNG pressurizations in the LNG storage tank are pumped out to the LNG delivery trunks line, LNG by first force (forcing) pump
Two plumes are divided into by the first flow distributor and separately flow into LNG first pipelines of output and LNG outputs second
Pipeline；
The LNG plumes that the LNG is exported in the first pipeline exchanged heat through the First Heat Exchanger after by the heat exchange output the
Three pipelines flow into the top of the domethanizing column；
The LNG plumes that the LNG is exported in the second pipeline exchanged heat through second heat exchanger after by the heat exchange output the
17 pipelines flow into the middle part of the domethanizing column；
The domethanizing column carries out rectifying separation to the LNG plumes for flowing into portion region and central region thereon, through multistage gas
After liquid mass transfer, the tower top of the domethanizing column produces lean gas, bottom of towe and obtains C2+；
It is cold that the lean gas exports part after the 4th pipeline is exchanged heat into the First Heat Exchanger along the methane gas phase
Solidifying to form gas-liquid two-phase, the lean gas of gas-liquid two-phase exports the 5th pipeline through the methane gas-liquid mixed and enters knockout drum
Carry out gas phase and liquid phase separation；The lean gas of liquid phase exports the 7th pipeline through the liquid phase methane and enters the domethanizing column
Top constitutes the liquid phase plume for flowing back and providing needed for the domethanizing column progress rectifying separation；The lean gas of gas phase is through described
Gas phase methane exports the 6th pipeline and enters the poor air compressor, and the poor air compressor pressurizes the lean gas of gas phase, plus
The 3rd pipeline that the lean gas after pressure exports the 8th pipeline into the First Heat Exchanger through the compressed methane exchanges heat to liquid
Mutually and by gas phase heat exchange the 9th pipeline of output export to outer defeated tenth pipeline, the 3rd force (forcing) pump is by its force (forcing) pump
User is defeated by beyond going out；
The C2+ that the bottom of towe of the domethanizing column is obtained sends into the dethanizer and carries out rectifying separation, through multi-stage gas-liquid
After mass transfer, the gas main component that the tower top of the dethanizer is produced is ethane, bottom of towe obtains LPG；
The gas that the tower top of the dethanizer is produced is condensed into liquid phase after second heat exchanger heat exchange and enters institute
Surge tank is stated, it enters the dethanizer by pressurized pump out to the tower top of the dethanizer of the 4th force (forcing) pump
Top constitutes the liquid phase plume for flowing back and providing needed for the dethanizer progress rectifying separation；
The LPG pressurizations that 5th force (forcing) pump produces the bottom of towe of the dethanizer pump out and are stored in LPG storage tanks.
Wherein, it is 7.5 that the LNG, which exports the first pipeline and exports the plume mole ratio in the second pipeline with the LNG,:1
~9.0:1.
Wherein, the pump discharge pressure of first force (forcing) pump is 1.75MPaG~2.25MPaG.
Wherein, the outlet pressure of the poor air compressor is 2.9MPaG~3.3MPaG.
Wherein, the operating pressure of the dethanizer is 0.45MPaG~0.6MPaG.
Compared with prior art, beneficial effects of the present invention are embodied in：
The apparatus and method that utilization cold energy of liquefied natural gas that the present invention is provided reclaims lighter hydrocarbons, by liquefied natural gas from storage tank
Middle pressurization is conveyed into two cold energy after pumping out and reclaimed in heat exchangers respectively, respectively with the lean gas after lighter hydrocarbons recovery and two column overheads
Gas phase is exchanged heat；By making liquefied natural gas endothermic gasification, the process of lean gas exothermic condensation completes the cold of liquefied natural gas
Recycle；Condensed lean gas is pressurized to ductwork pressure with pump and is transported to after gasifier gasification in pipe network pipeline, reclaims
Obtained lighter hydrocarbons are pumped in corresponding storage tank and stored；The present invention is using LNG itself cold with relatively low cost by rich gas
Lighter hydrocarbons resource separation come out, realize the comprehensive optimal control of natural gas resource, increase LNG receiving stations operating flexibility is adapted to
User's request diversity and the many-sided demand for improving factory economy type.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is the accompanying drawing used required in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, can be with
Other accompanying drawings are obtained according to these accompanying drawings.
Fig. 1 reclaims the device of lighter hydrocarbons for the utilization cold energy of liquefied natural gas of one embodiment of the invention and reclaims LPG using LNG
Flow chart.
Description of reference numerals：T1-LNG storage tanks；T2- ethane storage tanks；T3-LPG storage tanks；E1- First Heat Exchangers；E2- second
Heat exchanger；C1- domethanizing columns；C2- dethanizers；The poor air compressors of K1-；Q1- knockout drums；Q2- surge tanks；V1- gas phases
Regulating valve；L1- first flow distributors；L2- second flow distributors；The force (forcing) pumps of D1- first；The force (forcing) pumps of D2- second；
The force (forcing) pumps of D3- the 3rd；The force (forcing) pumps of D4- the 4th；The force (forcing) pumps of D5- the 5th；The force (forcing) pumps of D6- the 6th；The reboilers of M1- first；M2- second
Reboiler；100-LNG delivery trunk lines；101-LNG exports the first pipeline；102-LNG exports the second pipeline；103- heat exchange outputs
3rd pipeline；104- methane gas phase exports the 4th pipeline；105- methane gas-liquid mixed exports the 5th pipeline；106- gas phase methane is defeated
Go out the 6th pipeline；107- liquid phases methane exports the 7th pipeline；108- compressed methanes export the 8th pipeline；The heat exchange output of 109- gas phases
9th pipeline；Defeated tenth pipeline outside 110-；117- heat exchange the 17th pipelines of output；111-C2+ exports the 11st pipeline；112-C2
Export the 12nd pipeline；113-C2 heat exchange the 13rd pipelines of output；114-C2 the 14th pipelines of backflow；115-C2+ is stored into tank
15th pipeline；116-LPG is stored into the pipeline of tank the 16th.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation is described, it is clear that described embodiment is only a part of embodiment of the invention, rather than whole embodiments.It is based on
Embodiment in the present invention, it is every other that those of ordinary skill in the art are obtained under the premise of creative work is not paid
Embodiment, belongs to the scope of protection of the invention.
Referring to Fig. 1, Fig. 1 reclaims the device and profit of lighter hydrocarbons for the utilization cold energy of liquefied natural gas of one embodiment of the invention
LPG flow chart is reclaimed with LNG.
As shown in figure 1, the invention provides the device that a kind of utilization cold energy of liquefied natural gas reclaims lighter hydrocarbons, including LNG storages
Tank T1, LPG storage tank T3, First Heat Exchanger E1, the second heat exchanger E2, domethanizing column C1, dethanizer C2, poor air compressor K1,
Knockout drum Q1, surge tank Q2, first flow distributor L1, the first force (forcing) pump D1, the second force (forcing) pump D2, the 3rd force (forcing) pump
D3, the 4th force (forcing) pump D4, the 5th force (forcing) pump D5, the 6th force (forcing) pump D6, the first reboiler M1, second reboiler M2, LNG outputs are total
It is defeated that pipeline 100, LNG export the first pipeline 101, the second pipeline 102 of LNG outputs, the 3rd pipeline 103 of heat exchange output, methane gas phase
Go out the 4th pipeline 104, the 5th pipeline 105 of methane gas-liquid mixed output, the 6th pipeline 106 of gas phase methane output, liquid phase methane defeated
Go out the 7th pipeline 107, compressed methane and export the 8th pipeline 108, the 9th pipeline 109 of gas phase heat exchange output, outer defeated tenth pipeline
110th, the 17th pipeline 117 of heat exchange output, C2+ export the 11st pipeline 111, C2 and export the 12nd pipeline 112, C2 heat exchange outputs
13rd pipeline 113, the 14th pipeline 114 of C2 backflows, LPG are stored into the pipeline 116 of tank the 16th, wherein
First force (forcing) pump D1 is located in LNG storage tank T1, and one end of LNG delivery trunks line 100 is connected with the first force (forcing) pump D1,
The other end is connected with first flow distributor L1, and first flow distributor L1 and LNG exports the first pipeline 101 and LNG is defeated
Go out the second pipeline 102 to connect；
LNG exports the first pipeline 101 and is connected with First Heat Exchanger E1 the first pipeline, First Heat Exchanger E1 the first pipeline
It is connected with heat exchange the 3rd pipeline 103 of output, heat exchange the 3rd pipeline 103 of output is connected with domethanizing column C1 top；
LNG exports the second pipeline 102 and is connected with the second heat exchanger E2 the first pipeline, the second heat exchanger E2 the first pipeline
It is connected with heat exchange the 17th pipeline 117 of output, heat exchange the 17th pipeline 117 of output is connected with domethanizing column C1 middle part；
Domethanizing column C1 top connection methane gas phase exports the 4th pipeline 104, the pipeline 104 of methane gas phase output the 4th the
One heat exchanger E1 second pipe connection, First Heat Exchanger E1 second pipe and methane gas-liquid mixed export the 5th pipeline 105
One end connection, methane gas-liquid mixed export the 5th pipeline 105 the other end be connected to knockout drum Q1, knockout drum Q1
Liquid-phase outlet and liquid phase methane export one end of the 7th pipeline 107 and be connected, knockout drum Q1 gaseous phase outlet and gas phase first
Alkane exports one end connection of the 6th pipeline 106；Liquid phase methane exports the 7th pipeline 107 and is connected with domethanizing column C1 top, the
Two force (forcing) pump D2 are located at liquid phase methane and exported on the 7th pipeline 107；Gas phase methane exports the other end and lean gas of the 6th pipeline 106
Compressor K1 connections, one end that poor air compressor K1 exports the 8th pipeline 108 with compressed methane is connected, compressed methane output the 8th
The other end of pipeline 108 is connected with First Heat Exchanger E1 the 3rd pipeline, and First Heat Exchanger E1 the 3rd pipeline and gas phase exchange heat
Export the 9th pipeline 109 to connect, in one embodiment of the invention, be additionally provided with gas phase and export the 9th looped pipeline line and gas phase regulation
Valve V1, the gas phase exports one end of the 9th looped pipeline line and compressed methane exports the 8th pipeline 108 and is connected, its other end and gas phase
Heat exchange the 9th pipeline 109 of output is connected, and the part of the lean gas after pressurization is exported the 9th looped pipeline line by the gas phase and is directly flowed
Enter outer defeated tenth pipeline 110；Gas phase heat exchange the 9th pipeline 109 of output is connected with outer defeated tenth pipeline 110, and the 3rd force (forcing) pump D3 is set
Outside on defeated tenth pipeline；
Domethanizing column C1 bottom of towe exports the 11st pipeline 110 by C2+ with dethanizer C2 and is connected；
Dethanizer C2 tower top exports one end of the 12nd pipeline 112 and the second heat exchanger E2 second pipe by C2
Connection, the other end of the second heat exchanger E2 second pipe is connected by C2 heat exchange the 13rd pipelines 113 of output with surge tank Q2,
Surge tank Q2 is connected by C2 the 14th pipelines 114 of backflow with dethanizer C2 tower top, and the 4th force (forcing) pump D4 is located at C2 backflows
On 14th pipeline 114.In one embodiment of the invention, ethane storage tank T2, second flow distributor L2, C2 are additionally provided with
+ store into the pipeline 115 of tank the 15th and the 6th force (forcing) pump D6, second flow distributor L2 is connected to surge tank Q2 and C2+ and returned
The junction of the 14th pipeline 114 is flowed, the 6th force (forcing) pump D6 is located at C2+ and stored on the pipeline 115 of tank the 15th.
Dethanizer C2 bottom of towe is stored by LPG and is connected into the pipeline 116 of tank the 16th with LPG storage tanks T3, the 5th pressurization
Pump D5 is located at LPG and stored on the pipeline 116 of tank the 16th.
When it is implemented, the first force (forcing) pump D1 pumps out the LNG pressurizations in LNG storage tank T1 to LNG delivery trunks line 100,
Wherein, the first force (forcing) pump D1 pump discharge pressure is 1.75MPaG~2.25MPaG (MPaG, meter reading pressure).LNG is by first
Flow distribution device L1 is divided to separately flows into LNG the first pipelines 101 of output and LNG the second pipelines 102 of output for two plumes.Wherein,
It is 7.5 that LNG, which exports the first pipeline and exports the plume mole ratio in the second pipeline with LNG,:1~9.0：1.LNG outputs first are managed
LNG plumes in line 101 flow into the upper of domethanizing column C1 after being exchanged heat through First Heat Exchanger E1 by heat exchange the 3rd pipeline 103 of output
Portion；Wherein, the plume of the 3rd pipeline 103 of heat exchange output is with -85 DEG C or so of temperature, and about 0.75~0.85 rate of gasification is to enter
Domethanizing column C1 top.The LNG plumes that LNG is exported in the second pipeline 102 are exported after being exchanged heat through the second heat exchanger E2 by heat exchange
17th pipeline 117 flows into domethanizing column C1 middle part.Domethanizing column C1 is to flowing into the LNG stocks of portion region and central region thereon
Stream carries out rectifying separation, after multi-stage gas-liquid mass transfer, and domethanizing column C1 tower top produces lean gas, bottom of towe and obtains C2+.Lean gas is along first
Alkane gas phase exports partial condensation formation gas-liquid two-phase, gas-liquid two-phase after the 4th pipeline 104 is exchanged heat into First Heat Exchanger E1
Lean gas through methane gas-liquid mixed export the 5th pipeline 105 and enter knockout drum Q1 and carry out gas phase and liquid phase separation；Liquid phase
The top composition that lean gas exports the 7th pipeline 107 into domethanizing column C1 through liquid phase methane flows back and provides domethanizing column C1 and carries out
Liquid phase plume needed for rectifying separation；The lean gas of gas phase exports the 6th pipeline 106 through gas phase methane and enters poor air compressor K1, poor
Air compressor K1 pressurizes the lean gas of gas phase, wherein, poor air compressor K1 outlet pressure is 2.9MPaG~3.3MPaG.Pressurization
The 3rd pipeline that the compressed methane of lean gas afterwards exports the 8th pipeline 108 into First Heat Exchanger E1 exchanges heat to liquid phase and by gas phase
Heat exchange the 9th pipeline 109 of output is exported to outer defeated tenth pipeline 110, and gas phase regulating valve V1 is located at the gas phase and exports the 9th looped pipeline
On line, the flow that the gas phase exports the lean gas of the 9th looped pipeline line is flowed through in gas phase regulating valve V1 controls, and gas phase regulating valve V1's opens
Degree makes First Heat Exchanger E1 the first pipeline and the temperature difference of the 3rd pipeline maintain between+25 DEG C~+30 DEG C；3rd force (forcing) pump D3
User is defeated by beyond the LNG pressurizations for flowing to outer defeated tenth pipeline 110 are pumped out.11st pipeline 110 is by domethanizing column C1 tower
The C2+ feedings dethanizer C2 that bottom is obtained carries out rectifying separation, wherein, dethanizer C2 operating pressure for 0.45MPaG~
0.6MPaG, after multi-stage gas-liquid mass transfer, the gas main component that dethanizer C2 tower top is produced is ethane, bottom of towe is obtained
LPG.The gas that dethanizer C2 tower top is produced is condensed into liquid phase after the second heat exchanger E2 heat exchange and enters surge tank Q2, its
Constituted by the pressurized tops pumped out to dethanizer C2 tower top into dethanizer C2 of the 4th force (forcing) pump D4 and flow back and carry
The liquid phase plume needed for rectifying separation is carried out for dethanizer C2；Second flow distributor L2 control surge tanks Q2 liquid phase stock
The flow for entering de- ethylene column C2 tower tops is flowed, it is required that surge tank Q2 liquid phase plume is separated into dethanizer C2 progress rectifying separation
Liquid phase plume after redundance import ethane storage tank T2 storage.The lighter hydrocarbons that dethanizer C2 bottom of towe is produced are by the 5th pressurization
Pump D5 pressurizations are pumped out and are stored in LPG storage tanks T3, realize that lighter hydrocarbons recovery is stored.In one embodiment of the invention, obtain
The molar concentrations of LPG products be not less than 98%.
In one embodiment of the invention, domethanizing column C1 bottom of towe is provided with the first reboiler M1, dethanizer C2's
Bottom of towe is provided with the second reboiler M2, is respectively used to make the liquid of tower reactor in domethanizing column C1 and dethanizer C2 vaporize again.
Wherein, in order that maximum heat transfer, in one embodiment of the invention, First Heat Exchanger E1 and the second heat exchanger
E2 is that plate sticks up formula heat exchanger.
One of ordinary skill in the art will appreciate that：Accompanying drawing be module in the schematic diagram of one embodiment, accompanying drawing or
Flow is not necessarily implemented necessary to the present invention.
One of ordinary skill in the art will appreciate that：The module in device in embodiment can be according to embodiment description point
It is distributed in the device of embodiment, respective change can also be carried out and be disposed other than in one or more devices of the present embodiment.On
The module for stating embodiment can be merged into a module, can also be further split into multiple submodule.
Finally it should be noted that：The above embodiments are merely illustrative of the technical solutions of the present invention, rather than its limitations；Although
The present invention is described in detail with reference to the foregoing embodiments, it will be understood by those within the art that：It still may be used
To be modified to the technical scheme described in previous embodiment, or equivalent substitution is carried out to which part technical characteristic；And
These modifications are replaced, and the essence of appropriate technical solution is departed from the spirit and model of technical scheme of the embodiment of the present invention
Enclose.
Claims (10)
1. a kind of utilization cold energy of liquefied natural gas reclaims the device of lighter hydrocarbons, it is characterised in that including LNG storage tank, LPG storage tanks, the
One heat exchanger, the second heat exchanger, domethanizing column, dethanizer, poor air compressor, knockout drum, surge tank, first flow point
With device, the first force (forcing) pump, the second force (forcing) pump, the 3rd force (forcing) pump, the 4th force (forcing) pump, the 5th force (forcing) pump, LNG delivery trunks line,
LNG exports the first pipeline, LNG and exports the second pipeline, the 3rd pipeline of heat exchange output, the 4th pipeline of methane gas phase output, methane gas
The 5th pipeline of liquid mixing output, gas phase methane export the 6th pipeline, liquid phase methane and export the 7th pipeline, compressed methane output the 8th
Pipeline, gas phase heat exchange output the 9th pipeline, outer defeated tenth pipeline, heat exchange output the 17th pipeline, C2+ export the 11st pipeline,
C2 exports the 12nd pipeline, the 13rd pipeline of C2 heat exchange outputs, the 14th pipeline of C2 backflows, LPG and stored into the pipeline of tank the 16th,
Wherein
First force (forcing) pump is located in the LNG storage tank, and described LNG delivery trunks line one end connects with first force (forcing) pump
Connect, the other end is connected with the first flow distributor, the first flow distributor exports the first pipeline with the LNG
And the LNG exports the connection of the second pipeline, first force (forcing) pump pumps out the LNG pressurizations in the LNG storage tank to the LNG
Delivery trunk line, LNG is divided into two plumes by the first flow distributor and separately flows into LNG first pipelines of output and institute
State LNG and export the second pipeline；
The LNG exports the first pipeline and is connected with the first pipeline of the First Heat Exchanger, the first pipe of the First Heat Exchanger
Road is connected with the 3rd pipeline of the heat exchange output, and the 3rd pipeline of the heat exchange output is connected with the top of the domethanizing column, institute
State after the LNG plumes in LNG the first pipelines of output exchange heat through the First Heat Exchanger and the inflow of the 3rd pipeline is exported by the heat exchange
The top of the domethanizing column；
The LNG exports the second pipeline and is connected with the first pipeline of second heat exchanger, the first pipe of second heat exchanger
Road is connected with the 17th pipeline of the heat exchange output, and the 17th pipeline of the heat exchange output in the middle part of the domethanizing column with connecting
Connect, the LNG plumes that the LNG is exported in the second pipeline export the 17th by the heat exchange after being exchanged heat through second heat exchanger and managed
Line flows into the middle part of the domethanizing column；
The domethanizing column carries out rectifying separation to the LNG plumes for flowing into portion region and central region thereon, is passed through multi-stage gas-liquid
After matter, the tower top of the domethanizing column produces lean gas, bottom of towe and obtains C2+；
The top of the domethanizing column connects the methane gas phase and exports the 4th pipeline, the methane gas phase export the 4th pipeline with
The second pipe connection of the First Heat Exchanger, the second pipe of the First Heat Exchanger and the methane gas-liquid mixed output the
One end connection of five pipelines, the other end that the methane gas-liquid mixed exports the 5th pipeline is connected to the knockout drum, institute
The liquid-phase outlet for stating knockout drum is connected with one end that the liquid phase methane exports the 7th pipeline, the gas of the knockout drum
Mutually outlet is connected with one end that the gas phase methane exports the 6th pipeline；The liquid phase methane exports the 7th pipeline and the piptonychia
The top connection of alkane tower, second force (forcing) pump is located at the liquid phase methane and exported on the 7th pipeline；The gas phase methane output
The other end of 6th pipeline is connected with the poor air compressor, and the poor air compressor exports the 8th pipeline with the compressed methane
One end connection, the other end that the compressed methane exports the 8th pipeline is connected with the 3rd pipeline of the First Heat Exchanger, institute
The 3rd pipeline for stating First Heat Exchanger is connected with gas phase heat exchange the 9th pipeline of output；Gas phase heat exchange the 9th pipeline of output
It is connected with outer defeated tenth pipeline, the 3rd force (forcing) pump is located on outer defeated tenth pipeline；
The lean gas exports partial condensation shape after the 4th pipeline is exchanged heat into the First Heat Exchanger along the methane gas phase
Into gas-liquid two-phase, the lean gas of gas-liquid two-phase exports the 5th pipeline through the methane gas-liquid mixed and enters the knockout drum
Carry out gas phase and liquid phase separation；The lean gas of liquid phase exports the 7th pipeline through the liquid phase methane and enters the domethanizing column
Top constitutes the liquid phase plume for flowing back and providing needed for the domethanizing column progress rectifying separation；The lean gas of gas phase is through described
Gas phase methane exports the 6th pipeline and enters the poor air compressor, and the poor air compressor pressurizes the lean gas of gas phase, plus
The 3rd pipeline that the lean gas after pressure exports the 8th pipeline into the First Heat Exchanger through the compressed methane exchanges heat to liquid
Mutually and by gas phase heat exchange the 9th pipeline of output export to outer defeated tenth pipeline, the 3rd force (forcing) pump is by its force (forcing) pump
User is defeated by beyond going out；
The bottom of towe of the domethanizing column exports the 11st pipeline by the C2+ with the dethanizer and is connected, for by described in
The C2+ that the bottom of towe of domethanizing column is obtained sends into the dethanizer and carries out rectifying separation, after multi-stage gas-liquid mass transfer, the de- second
The gas main component that the tower top of alkane tower is produced is ethane, bottom of towe obtains LPG；
The tower top of the dethanizer exports the one of the 12nd pipeline and the second pipe of second heat exchanger by the C2
End connection, the other end of the second pipe of second heat exchanger is connected by C2 heat exchange the 13rd pipeline of output and the surge tank
Connect, the surge tank is connected by the C2 the 14th pipelines of backflow with the tower top of the dethanizer, the 4th force (forcing) pump
It is located at the C2 to flow back on the 14th pipeline, the gas that the tower top of the dethanizer is produced exchanges heat by second heat exchanger
After be condensed into liquid phase into the surge tank, it is pumped out to the tower top of the dethanizer by the 4th force (forcing) pump is pressurized
Constituted into the top of the dethanizer and flow back and provide the dethanizer progress rectifying separation required liquid phase plume；
The bottom of towe of the dethanizer is stored by the LPG and is connected into the pipeline of tank the 16th with the LPG storage tanks, and the described 5th
Force (forcing) pump is located at the LPG and stored on the pipeline of tank the 16th, and the 5th force (forcing) pump produces the bottom of towe of the dethanizer
Lighter hydrocarbons pressurization pump out and be stored in the LPG storage tanks.
2. utilization cold energy of liquefied natural gas according to claim 1 reclaims the device of lighter hydrocarbons, it is characterised in that be additionally provided with gas
Mutually output the 9th looped pipeline line and gas phase regulating valve, the gas phase exports one end of the 9th looped pipeline line and compressed methane output the
Eight pipelines are connected, and its other end is connected with gas phase heat exchange the 9th pipeline of output, makes the part of the lean gas after pressurization logical
Cross the 9th looped pipeline line of the gas phase output and flow directly into outer defeated tenth pipeline；It is defeated that the gas phase regulating valve is located at the gas phase
Go out on the 9th looped pipeline line, the gas phase governor valve control flows through the flow that the gas phase exports the lean gas of the 9th looped pipeline line,
The aperture of the gas phase regulating valve make the first pipeline of the First Heat Exchanger and the temperature difference of the 3rd pipeline maintain+25 DEG C~+
Between 30 DEG C.
3. utilization cold energy of liquefied natural gas according to claim 1 reclaims the device of lighter hydrocarbons, it is characterised in that the piptonychia
The bottom of towe of alkane tower and the bottom of towe of the dethanizer are respectively equipped with the first reboiler and the second reboiler, for making the demethanation
The liquid of tower reactor is vaporized again in tower and the dethanizer.
4. utilization cold energy of liquefied natural gas according to claim 1 reclaims the device of lighter hydrocarbons, it is characterised in that be additionally provided with second
Alkane storage tank, second flow distributor, C2+ are stored into the pipeline of tank the 15th and the 6th force (forcing) pump, the second flow distribution dress
Put and be connected to the surge tank and the 14th pipeline junction of C2+ backflows, the liquid phase plume for controlling the surge tank
Into the flow of the de- ethene column overhead, the 6th force (forcing) pump is located at the C2+ and stored on the pipeline of tank the 15th, described
Ethane storage tank is connected to the C2+ and stores output end into the pipeline of tank the 15th.
5. utilization cold energy of liquefied natural gas according to claim 1 reclaims the device of lighter hydrocarbons, it is characterised in that described first
Heat exchanger and second heat exchanger are that plate sticks up formula heat exchanger.
6. a kind of cold energy of liquefied natural gas of any one of utilization Claims 1 to 55 reclaims the method that the device of lighter hydrocarbons reclaims lighter hydrocarbons,
It is characterised in that it includes following steps：
The LNG pressurizations in the LNG storage tank are pumped out to the LNG delivery trunks line by first force (forcing) pump, LNG is by institute
State first flow distributor and be divided into two plumes and separately flow into that the LNG exports the first pipeline and the LNG exports the second pipeline；
The LNG plumes that the LNG is exported in the first pipeline export the 3rd by the heat exchange after being exchanged heat through the First Heat Exchanger and managed
Line flows into the top of the domethanizing column；
The LNG plumes that the LNG is exported in the second pipeline export the 17th after being exchanged heat through second heat exchanger by the heat exchange
Pipeline flows into the middle part of the domethanizing column；
The domethanizing column carries out rectifying separation to the LNG plumes for flowing into portion region and central region thereon, is passed through multi-stage gas-liquid
After matter, the tower top of the domethanizing column produces lean gas, bottom of towe and obtains C2+；
The lean gas exports partial condensation shape after the 4th pipeline is exchanged heat into the First Heat Exchanger along the methane gas phase
Into gas-liquid two-phase, the lean gas of gas-liquid two-phase exports the 5th pipeline through the methane gas-liquid mixed and carried out into knockout drum
Gas phase and liquid phase separation；The lean gas of liquid phase exports the top that the 7th pipeline enters the domethanizing column through the liquid phase methane
Constitute and flow back and provide the domethanizing column progress rectifying separation required liquid phase plume；The lean gas of gas phase is through the gas phase
Methane exports the 6th pipeline and enters the poor air compressor, and the poor air compressor pressurizes the lean gas of gas phase, after pressurization
The lean gas through the compressed methane export the 8th pipeline enter the First Heat Exchanger the 3rd pipeline exchange heat to liquid phase simultaneously
By the gas phase heat exchange output the 9th pipeline export to outer defeated tenth pipeline, the 3rd force (forcing) pump pressurizeed pump out with
It is defeated by user outside；
The C2+ that the bottom of towe of the domethanizing column is obtained sends into the dethanizer and carries out rectifying separation, through multi-stage gas-liquid mass transfer
Afterwards, the gas main component that the tower top of the dethanizer is produced is ethane, bottom of towe obtains LPG；
The gas that the tower top of the dethanizer is produced is condensed into liquid phase after second heat exchanger heat exchange and enters described slow
Tank is rushed, it is by the pressurized top pumped out to the tower top of the dethanizer into the dethanizer of the 4th force (forcing) pump
Constitute and flow back and provide the dethanizer progress rectifying separation required liquid phase plume；
The LPG pressurizations that 5th force (forcing) pump produces the bottom of towe of the dethanizer pump out and are stored in LPG storage tanks.
7. the method according to claim 6 for reclaiming lighter hydrocarbons, it is characterised in that the LNG export the first pipeline with it is described
The plume mole ratio that LNG exports in the second pipeline is 7.5:1~9.0:1.
8. the method according to claim 6 for reclaiming lighter hydrocarbons, it is characterised in that the pump discharge pressure of first force (forcing) pump
For 1.75MPaG~2.25MPaG.
9. the method according to claim 6 for reclaiming lighter hydrocarbons, it is characterised in that the outlet pressure of the poor air compressor is
2.9MPaG~3.3MPaG.
10. the method according to claim 6 for reclaiming lighter hydrocarbons, it is characterised in that the operating pressure of the dethanizer is
0.45MPaG~0.6MPaG.
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| CN105783421B (en) * | 2016-04-07 | 2018-09-14 | 成都赛普瑞兴科技有限公司 | A kind of method and device of natural gas lighter hydrocarbons recovery |
| CN105733721B (en) * | 2016-04-14 | 2018-09-25 | 北京安珂罗工程技术有限公司 | A kind of method and system removing heavy hydrocarbon from natural gas |
| CN105779052B (en) * | 2016-04-14 | 2019-01-04 | 北京安珂罗工程技术有限公司 | The method and system of heavy hydrocarbon is recycled in a kind of liquefied natural gas (LNG) production |
| CN106247759B (en) * | 2016-08-15 | 2019-04-16 | 中国海洋石油集团有限公司 | A kind of method of LNG receiving station recycling lighter hydrocarbons |
| CN108507277A (en) * | 2018-04-28 | 2018-09-07 | 中国石油工程建设有限公司 | A kind of the cold comprehensive utilization device and method of natural gas ethane recovery |
| CN110590490B (en) * | 2018-06-13 | 2022-05-24 | 中国石化工程建设有限公司 | System and method for recovering hydrocarbons in liquefied natural gas |
| CN110144238B (en) * | 2019-05-24 | 2021-03-16 | 西南石油大学 | Liquefied natural gas light hydrocarbon recovery method |
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