CN110469768A - A kind of CO of LNG cold energy use and hydrate exploitation2Capturing device and its capture method - Google Patents
A kind of CO of LNG cold energy use and hydrate exploitation2Capturing device and its capture method Download PDFInfo
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- CN110469768A CN110469768A CN201810452274.2A CN201810452274A CN110469768A CN 110469768 A CN110469768 A CN 110469768A CN 201810452274 A CN201810452274 A CN 201810452274A CN 110469768 A CN110469768 A CN 110469768A
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
- F17C7/02—Discharging liquefied gases
- F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
Abstract
The present invention relates to oil-gas storages and Transportation Engineering technical field, disclose the CO of a kind of LNG cold energy use and hydrate exploitation2Capturing device and its capture method, comprising: LNG vaporization system, BOG processing system and CO2Recovery system, the LNG vaporization system include the liquid phase region heating subsystem, Gas-liquid phase region heating subsystem and gas phase zone heating subsystem being sequentially connected, and Gas-liquid phase region heating subsystem is connected with the BOG processing system；The CO2Vaporization pressurization output system respectively with the BOG processing system and the CO2Recovery system is connected, so that the flue gas CO that the BOG processing system generates2It is injected into hydration reservoir to displace CH4Gas and partial fume CO2Gas is simultaneously transported to the CO2Recovery system does further recovery processing；The CO2Recovery system is connected with liquid phase region heating subsystem and Gas-liquid phase region heating subsystem respectively.The CO of the LNG cold energy use and hydrate exploitation2Capturing device has LNG cold energy use rate high and CO2The advantages of effectively being trapped.
Description
Technical field
The present invention relates to oil-gas storages and Transportation Engineering technical field, more particularly to a kind of LNG cold energy use and hydration
The CO of object exploitation2Capturing device and its capture method.
Background technique
LNG is -162 DEG C under normal pressure of cryogenic liquid mixtures, and when LNG gasification per ton can produce about 240kWh cold energy, is closed
Reason can produce considerable economic benefit using this part cold energy.Wherein, cold energy can be used to generate electricity, low-temperature cold store and ice storage
Equal fields.LNG temperature during cold energy discharges is increased to 10 DEG C from -162 DEG C, and temperature span range is larger, if therefore establishing
Single-stage Rankine cycle electricity generation system, the heat transfer temperature difference of Rankine cycle electricity generation system is larger, be easy to cause cold available energy loss larger, cold
Energy utilization efficiency is difficult to improve.
Hydrate replacement exploitation is to inject substitution gas into hydrate layer within the scope of certain temperature and pressure, set
Body of taking a breath is mainly CO2(carbon dioxide) gas.Substitution gas, which enters, closes object cage, displaces the CH in hydrate cage4(first
Alkane), to achieve the purpose that exploitation.CO2Gas can replacement exploitation of gas hydrate, be primarily due in identical pressure
Under the conditions of, CO2Hydrate ratio CH4Hydrate is more stable.Temperature and pressure is controlled in CO2Hydrate is stabilized, CH4Hydration
In the range of object cannot be stabilized, CO is then injected into stratum2, CO2The CH in hydrate cage can be displaced4。
In order to protect environment, the CO discharged in power production process is reduced2Gas, therefore, CO2Discharge at present also by
Concern.Therefore, CO2Trapping with seal up for safekeeping will become research emphasis.
Summary of the invention
(1) technical problems to be solved
The object of the present invention is to provide the CO of a kind of LNG cold energy use and hydrate exploitation2Capturing device and its trapping side
Method injects substitution gas, substitution gas into hydrate layer to solve in the prior art during hydrate replacement exploitation
It enters and closes object cage, displace the CH in hydrate cage4(methane), thus achieve the purpose that exploitation, in the process, existing skill
Art can not efficiently utilize the cold energy of LNG (liquefied natural gas), meanwhile, also BOG (boil-off gas) can not efficiently be utilized, and
To CO2It can not realize after being liquefied and preferably seal up for safekeeping.
(2) technical solution
In order to solve the above-mentioned technical problem, according to the first aspect of the invention, a kind of LNG cold energy use and hydrate are provided
The CO of exploitation2Capturing device, comprising: LNG vaporization system, BOG processing system and CO2Recovery system, the LNG vaporization system packet
Include the liquid phase region heating subsystem, Gas-liquid phase region heating subsystem and gas phase zone heating subsystem being sequentially connected, wherein described
The output end of gas phase zone heating subsystem exports gas product, and the Gas-liquid phase region heating subsystem and the BOG are handled
System is connected, described for the cryogenic natural gas obtained after Gas-liquid phase region heating subsystem heating vaporization to be delivered to
BOG processing system, to balance the material supply of the BOG processing system；CO2Vaporization pressurization output system, the CO2Vaporization adds
Pressure output system respectively with the BOG processing system and the CO2Recovery system is connected, so that the BOG processing system generates
Flue gas CO2It is injected into hydration reservoir to displace CH4Gas and partial fume CO2Gas is simultaneously transported to the CO2It returns
Receipts system does further recovery processing；Wherein, the CO2Recovery system heats up with the liquid phase region subsystem and the gas respectively
Liquid two-phase section heating subsystem is connected, so that the flue gas CO2It is recycled.
Wherein, the liquid phase region heating subsystem includes liquid phase region heat exchanger, the liquid for being sequentially connected and being capable of forming circuit
Phase region circulatory mediator pump, liquid phase region circulatory mediator heat exchanger and liquid phase region expanding machine.
Wherein, the Gas-liquid phase region heating subsystem includes Gas-liquid phase region heat exchanger.
Wherein, the CO2Recovery system includes first-class heat exchanger and gas-liquid separator.
Wherein, the CO2Vaporization pressurization output system includes flue gas CO2Pump and with the flue gas CO2Pump the CO being connected2
Heat exchanger, wherein the CO2The output end of heat exchanger is extend into hydrate reservoir by injection well, is used for the hydration
Flue gas CO is injected in object reservoir2, to displace the CH in the hydrate reservoir4With partial fume CO2。
Wherein, the CO2Vaporization pressurization output system further includes CH4And CO2Separator, wherein the CH4And CO2Point
Entrance from device is connected to by the extraction well extending into hydrate reservoir, the CH4And CO2The outlet of separator and institute
State the entrance connection of first-class heat exchanger.
Wherein, the gas phase zone heating subsystem includes gas phase zone heat exchanger, the gas for being sequentially connected and being capable of forming circuit
Phase region circulatory mediator pump, gas phase zone circulatory mediator heat exchanger and gas phase zone expanding machine.
Wherein, the outlet of the first-class heat exchanger is connect with the entrance of the gas phase zone circulatory mediator heat exchanger.
Wherein, the BOG processing system includes combustion chamber and the flue gas of LNG fluid reservoir, BOG compressor, oxygen and BOG
Expanding machine.
According to a second aspect of the present application, the CO of a kind of LNG cold energy use and hydrate exploitation is also provided2Capture method,
It include: step S1, it is simultaneously outer defeated to obtain gas product to carry out gasification process to LNG；Step S2 burns to obtain to BOG
Obtain high temperature mixed flue gas；Step S3, to the CO in high temperature mixed flue gas2It is recycled.
Wherein, in step sl, the method also includes: by make LNG successively by liquid phase region heat up subsystem, gas
Liquid two-phase section heating subsystem and gas phase zone heating subsystem exchange heat to obtain the gas product.
Wherein, in the step S2, the method also includes: step S21, by pressurizeing to BOG, and will pressurization
BOG afterwards, which is transported in combustion chamber, to burn to generate high-temperature flue gas CO2And H2O。
Wherein, in the step S3, the method also includes step S31, pass through the high-temperature flue gas generated to reaction
CO2And H2O carries out gas-liquid separation, and to the high-temperature flue gas CO after separation2Carry out pressurized treatments.
Wherein, in the step S3, the method also includes step S32, by the high-temperature flue gas CO after pressurized treatments2
First-class heat exchanger, gas phase zone circulatory mediator heat exchanger, liquid phase region circulatory mediator heat exchanger and Gas-liquid phase region is sequentially sent to change
In hot device and carry out after heat exchange to form liquid CO2。
Wherein, in step s3, the method also includes step S33, to liquid CO2Pressurized treatments are carried out, and to pressurization
Liquid CO afterwards2It is vaporized processing, so that liquid CO2It is vaporized into CO2Gas.
Wherein, in step s3, the method also includes step S34, by CO2Gas injects in hydrate reservoir, and makes
Obtain CO2Hydrate in gas and hydrate reservoir reacts to displace CH4Mixed gas；Step S35, by CH4Gaseous mixture
CH in body4And CO2The CH for being separated, and being isolated4A part feeding natural gas output channel progress is outer defeated, will be another
Part CH4It is sent into combustion chamber and carries out circulating generation, meanwhile, by isolated CO2It is carried out in gas feeding first-class heat exchanger next
Secondary CO2Liquefaction processing.
(3) beneficial effect
The CO of LNG cold energy use provided by the invention and hydrate exploitation2Capturing device has compared with prior art
Following advantage:
The application is by making LNG fluid reservoir successively by liquid phase region heating subsystem, Gas-liquid phase region heating subsystem
After gas phase zone heating subsystem, more cold energy can be released, by carrying out segmentation utilization to LNG cold energy, and is made every
Circulatory mediator in Duan Xunhuan forms difference, so that refrigerant cooling curve and LNG evaporation curve reach of height
Match, further, greatly increases the exergy efficiencyX of LNG cold energy.
In addition, the BOG for utilizing LNG receiving station to generate by using power cycle is increased, to reach the efficient of BOG
It utilizes, and power supply can be provided for the whole audience, the greenhouse gases CO generated in the process2Also trapping has been obtained to seal up for safekeeping,
Environmental protection is achieved the effect that.
By to liquid CO2After carrying out pressurization vaporization, hydrate is exploited, energy consumption is lower, and realizes CO2Seal up for safekeeping.
Detailed description of the invention
Fig. 1 is the CO of LNG cold energy use and the hydrate exploitation of embodiments herein2The overall structure of capturing device is shown
It is intended to；
Fig. 2 is the CO of LNG cold energy use and the hydrate exploitation of embodiments herein2The step process of capture method is shown
It is intended to.
In figure, 1:LNG intake pipeline；2:LNG high-pressure pump；3: high pressure LNG feed-line；4: liquid phase region heat exchanger；5: liquid
Phase region heat exchanger LNG outlet line；6: Gas-liquid phase region heat exchanger；7: Gas-liquid phase region heat exchanger exit pipeline；8: gas phase zone
Heat exchanger；9: natural gas export pipeline；10: liquid phase region heat exchanger circulatory mediator outlet line；11: liquid phase region circulatory mediator pump；
12: liquid phase region circulatory mediator heat exchanger inlet line；13: liquid phase region circulatory mediator heat exchanger；14: liquid phase region expanding machine air inlet pipe
Line；15: liquid phase region expanding machine；16: liquid phase region expander outlet pipeline；17: gas phase zone circulatory mediator pump；18: gas phase zone circulation
Medium pump outlet line；19: gas phase zone circulatory mediator heat exchanger；20: gas phase zone circulatory mediator expander inlet pipeline；21: gas
Phase region expanding machine；22: gas phase zone expander outlet pipeline；23: gas phase zone circulatory mediator pump inlet pipeline；24: oxygen intake pipe
Line；25: combustion chamber charge pipeline；26: combustion chamber；27: smoke gas turbine expanding machine admission line；28: smoke gas turbine expanding machine；
29: first-class heat exchanger；30: the exhanst gas outlet pipeline of first-class heat exchanger；31: gas phase zone circulatory mediator heat exchanger smoke outlet tube
Line；32: separator；33: liquid water separate pipeline；36: Gas-liquid phase region heat exchanger inlet line；37- flue gas CO2Compressor into
Mouth pipeline；38: Gas-liquid phase region heat exchanger exhanst gas outlet pipeline；39:CO2Heat exchanger；40: flue gas CO2Pump；41: flue gas CO2Pump
Outlet line；42: flue gas CO2Compressor；43: flue gas CO2Compressor outlet pipeline；44: flue gas CO2Recycle main pipe line；45: one
Grade heat exchanger flue gas CO2Outlet line；46:BOG intake pipeline；47:BOG compressor；48: methane afterburning gas line；49:CO2
Heat exchanger inlet line；50:CO2Heat exchanger exit pipeline；51: injection well；52: hydrate reservoir；53: extraction well；54:CH4With
CO2Separator；55: separating highly concentrated CH4Outlet line；56: natural gas export pipeline；57: extraction CO2Outlet line；58:CH4
Into combustion chamber pipeline；70:LNG fluid reservoir.
Specific embodiment
With reference to the accompanying drawings and examples, specific embodiments of the present invention will be described in further detail.Following instance
For illustrating the present invention, but it is not intended to limit the scope of the invention.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase
Even ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or be integrally connected；It can
To be mechanical connection, it is also possible to be electrically connected；It can be directly connected, can also can be indirectly connected through an intermediary
Connection inside two elements.For the ordinary skill in the art, above-mentioned term can be understood at this with concrete condition
Concrete meaning in invention.
Embodiment 1:
As shown in Figure 1, schematically showing what LNG (liquefied natural gas) cold energy use and hydrate were exploited in figure
CO2Capturing device includes LNG vaporization system, BOG (boil-off gas) processing system and CO2Recovery system.
In embodiments herein, which includes liquid phase region the heating subsystem, gas-liquid two being sequentially connected
Heat up subsystem for phase region heating subsystem and gas phase zone, wherein the output end output natural gas of gas phase zone heating subsystem produces
Product, Gas-liquid phase region heating subsystem are connected with the BOG processing system, for Gas-liquid phase region heating subsystem to heat up
The cryogenic natural gas obtained after vaporization is delivered to the BOG processing system, to balance the material supply of the BOG processing system.
The CO2Vaporization pressurization output system respectively with the BOG processing system and the CO2Recovery system is connected, so that the BOG
The flue gas CO that processing system generates2It is injected into hydration reservoir to displace CH4Gas and partial fume CO2Gas is simultaneously defeated by its
It send to the CO2Recovery system does further recovery processing.
The CO2Recovery system is connected with liquid phase region heating subsystem and Gas-liquid phase region heating subsystem respectively, with
Make flue gas CO2It is recycled.Specifically, the application is by making LNG fluid reservoir 70 successively by liquid phase region heating subsystem
After system, Gas-liquid phase region heating subsystem and gas phase zone heating subsystem, more cold energy can be released, by LNG cold energy
Carry out segmentation utilization, and make the circulatory mediator composition in every section of circulation different so that refrigerant cooling curve with
LNG evaporation curve reaches the matching of height, further, greatly increases the exergy efficiencyX of LNG cold energy.
In addition, the BOG for utilizing LNG receiving station to generate by using power cycle is increased, to reach the efficient of BOG
It utilizes, and power supply can be provided for the whole audience, the greenhouse gases CO generated in the process2Also trapping has been obtained to seal up for safekeeping,
Environmental protection is achieved the effect that.
By to liquid CO2After carrying out pressurization vaporization, hydrate is exploited, energy consumption is lower, and realizes CO2Seal up for safekeeping.
As shown in Figure 1, at one of the application than in more preferably technical solution, liquid phase region heating subsystem include according to
Secondary connection is simultaneously capable of forming the liquid phase region heat exchanger 4 in circuit, liquid phase region circulatory mediator pump 11, liquid phase region circulatory mediator heat exchanger 13
And liquid phase region expanding machine 15.It should be noted that LNG fluid reservoir 70 is connect with LNG high-pressure pump 2, LNG high-pressure pump 2 and liquid phase
One of entrance of area's circulatory mediator heat exchanger 13 connects.Specifically, the LNG after the pressurization of LNG high-pressure pump 2 and Rankine cycle
The temperature of media for heat exchange, the outlet LNG of control liquid phase region circulatory mediator heat exchanger 13 is lower than the gasification temperature of LNG at this pressure
1 DEG C to 2 DEG C, gaseous Rankine cycle medium is cooled to liquid by LNG.
In one embodiment, the Rankine cycle medium of liquid phase region be a kind of organic circulation medium mixture, specific group
At as follows: methane 45-56%, ethane 30-50%, propane 10-20%, normal butane 5-7%, pentane 5-7%, this organic circulation
Evaporation curve of the cooling curve of medium just with LNG in liquid phase region matches, and the corresponding trend increased is presented.It is cooled down by LNG
Organic circulation medium be first sent into liquid phase region circulatory mediator pump 11 pressurization after, be re-fed into liquid phase region circulatory mediator heat exchanger 13 into
Row heat exchange, after industrial exhaust heat heats, which is vaporizated into after gaseous recycle medium that be admitted to liquid phase region swollen
It does work and generates electricity in swollen machine 15, be then re-fed into liquid phase region circulatory mediator heat exchanger 13 and carry out next Rankine cycle.
In one embodiment, Gas-liquid phase region heating subsystem includes Gas-liquid phase region heat exchanger 6.Specifically, by
The LNG that Gas-liquid phase region heat exchanger 6 is sent out after exchanging heat, which is sent in gas phase zone heat exchanger 8, to exchange heat, gaseous circulatory mediator
Liquid is cooled to by LNG, LNG is vaporizated into defeated outside natural gas.
In another embodiment, the CO2Recovery system includes first-class heat exchanger 29 and gas-liquid separator 32.It needs to illustrate
, by flue-gas expander 28 do work after flue gas enter in first-class heat exchanger 29 with circulatory mediator CO2It exchanges heat, with heating
Circulatory mediator CO2.Flue gas CO2It is sent into gas-liquid separator 32 after the heat exchange of gas phase zone circulatory mediator heat exchanger 19, by flue gas CO2
In liquid H2After O separation, it is sent into liquid phase region circulatory mediator heat exchanger 13.
As shown in Figure 1, also schematically showing the CO in figure2Vaporization pressurization output system includes flue gas CO2Pump 40 and with
Flue gas CO2The CO that pump 40 is connected2Heat exchanger 39, wherein the CO2The output end of heat exchanger 39 is extend by injection well 51
In hydrate reservoir 52, for injecting flue gas CO into the hydrate reservoir 522, to displace the CH in the hydrate reservoir 524
With partial fume CO2.Specifically, through liquefied CO2It is sent into flue gas CO2After pump 40 is pressurizeed, a part is through first-class heat exchanger 29
Enter in the combustion chamber 25 of oxygen and BOG after heating vaporization and CO is completed with further heating2Rankine cycle.Another part liquid
Change CO2It is admitted to CO2It exchanges heat in heat exchanger 39, using seawater to make heat exchange, liquefied CO2High pressure is vaporizated by heating of seawater
CO2.It will carry out the CO after pressurization vaporization2It is injected into hydrate reservoir 52 and is exploited by injection well 51, the CO of injection2Meeting
It is reacted with the hydrate in hydrate reservoir 52 to obtain containing CH4Gaseous mixture.Exploit obtained CH4And CO2Gaseous mixture
CH is sent to by producing well 534And CO2It is separated in separator 54.
As shown in Figure 1, one in the application is compared in more preferably technical solution, the CO2Vaporization pressurization output system is also
Including CH4And CO2Separator 54, wherein the CH4And CO2The entrance of separator 54 is by extending into hydrate reservoir 52
Extraction well 53 be connected to, the CH4And CO2The outlet of separator is connected to the entrance of the first-class heat exchanger 29.Specifically, it will open
The CH adopted4And CO2Gaseous mixture separated by the methods of hydrate embrane method or membrane separation process, to obtain high concentration
CH4And CO2.Isolated CH will be exploited4A part pressurize outer defeated, and another part can add to oxygen and BOG
Combustion power generation is carried out in combustion chamber 25.By isolated CO2It is sent to CO2In Rankine cycle, to continue next Rankine
Circulation.
As shown in Figure 1, also schematically showing gas phase zone heating subsystem in figure includes being sequentially connected and being capable of shape
At the gas phase zone heat exchanger 8 in circuit, gas phase zone circulatory mediator pump 17, gas phase zone circulatory mediator heat exchanger 19 and gas phase zone expansion
Machine 21.Specifically, the LNG sent out after the heat exchange of Gas-liquid phase region heat exchanger 6 is continued to be fed into and is carried out into gas phase zone heat exchanger 8
Heat exchange, gaseous circulatory mediator are cooled to liquid by LNG, and LNG is vaporizated into defeated outside natural gas.The organic circulation cooled down by LNG
Medium is sent in gas phase zone circulatory mediator pump 17 and pressurizes, and the LNG after pressurization is sent to gas phase zone circulatory mediator and is changed
It exchanges heat in hot device 19.Gas phase zone circulatory mediator is sent by the organic circulation medium after 17 pressurization of gas phase zone circulatory mediator pump to change
After in hot device 19, after industrial exhaust heat heating is vaporizated into gaseous recycle medium, it is sent into gas phase zone expanding machine 21.Circulatory mediator is logical
It crosses after the vaporization of gas phase zone circulatory mediator heat exchanger 19 heats up after being sent into the acting power generation of gas phase zone expanding machine 21, is sent into gas phase zone and exchanges heat
Next circulation is carried out in device 8.
It should be noted that the organic circulation medium in the Rankine cycle of gas phase zone is a kind of organic circulation medium mixture,
Its concrete composition is as follows: ethane 30-55%, propane 25-40%, pentane 30-40%, the cooling curve of this organic circulation medium
It matches with LNG in gas phase zone evaporation curve, the corresponding trend increased of approximately linear is presented.
In one embodiment, the outlet of the first-class heat exchanger 29 connects with the entrance of the gas phase zone circulatory mediator heat exchanger 19
It connects.
As shown in Figure 1, to advanced optimize the BOG processing system in above-mentioned technical proposal, in the base of above-mentioned technical proposal
On plinth, which includes combustion chamber 25 and the flue gas expansion of LNG fluid reservoir 70, BOG compressor 47, oxygen and BOG
Machine 28.Specifically, the BOG from LNG storage tank 70 is entered after BOG compressor 47 pressurizes to the combustion chamber 25 for being sent into oxygen and BOG
In burn, burning generate high temperature CO2And H2O.The high temperature CO that burning generates2And H2O enters flue-gas expander 28 and generates electricity
After acting, into heat exchange is carried out in first-class heat exchanger 29, to realize to CO2Cooling processing.
The CO of the LNG cold energy use of the application and hydrate exploitation2The connection relationship of each component part in capturing device
It is as follows:
LNG is directly connected the output end of LNG high-pressure pump 2 by LNG intake pipeline 1 after being exported by LNG fluid reservoir 70, LNG increases
After pressure, output end connects the input terminal of high pressure LNG feed-line 3, and the output end of high pressure LNG feed-line 3 connects liquid phase region
The liquid phase input terminal of heat exchanger 4, liquid phase region heat exchanger LNG outlet line 5 connect the input terminal of Gas-liquid phase region heat exchanger 6, liquid
Phase region heat exchanger circulatory mediator outlet line 10 connects the input terminal of liquid phase region circulatory mediator pump 11, liquid phase region circulatory mediator pump 11
Output end be connected with liquid phase region circulatory mediator heat exchanger inlet line 12, the output end of liquid phase region circulatory mediator heat exchanger 13
Liquid phase region expanding machine admission line 14 is connected, the outlet end of liquid phase region expanding machine 15 connects liquid phase region expander outlet pipeline 16,
Liquid phase region expander outlet pipeline 16 is connected with the gas phase input end of liquid phase region heat exchanger 4.Gas-liquid phase region heat exchanger 6 goes out
Mouth end is connected with Gas-liquid phase region heat exchanger exit pipeline 7, and an input end of gas phase zone heat exchanger 8 is changed with Gas-liquid phase region
Hot device outlet line 7 is connected, and natural gas export pipeline 9 is connected with the outlet end of gas phase zone heat exchanger 8.Gas phase zone heat exchanger
8 another liquid phase input terminal is connected with gas phase zone expander outlet pipeline 22, gas phase zone circulatory mediator pump inlet pipeline 23
It is connected with another outlet end of gas phase zone heat exchanger 8, the outlet end of gas phase zone circulatory mediator pump 17 and gas phase zone circulation are situated between
Matter pump discharge pipeline 18 is connected, the outlet end of gas phase zone circulatory mediator heat exchanger 19 and gas phase zone circulatory mediator expander inlet
Pipeline 20 is connected, and the outlet end of gas phase zone expanding machine 21 is connected with gas phase zone expander outlet pipeline 22, gas phase zone heat exchange
Another input end of device 8 is connected with gas phase zone expander outlet pipeline 22.The air inlet of oxygen intake pipe line 24 and combustion chamber
Pipeline 25 is connected, and the intake pipeline 46 of BOG is connected with the arrival end of BOG compressor 47, the outlet end of BOG compressor 47 with
The admission line 25 of combustion chamber is connected, and methane afterburning gas line 48 is connected with the admission line 25 of combustion chamber, combustion chamber
26 input terminal is connected with the admission line 25 of combustion chamber.Smoke gas turbine expanding machine admission line 27 and flue-gas expander 28
Input end is connected, and the output end of flue-gas expander 28 is connected with the input terminal of first-class heat exchanger 29, the cigarette of first-class heat exchanger
Gas outlet line 30 is connected with the input terminal of gas phase zone circulatory mediator heat exchanger 19, gas phase zone circulatory mediator heat exchanger flue gas
CO2Outlet line 31 is connected with the input terminal of separator 32, an output end of liquid water separate pipeline 33 and separator 32
It is connected, flue gas CO2Outlet line 34 is connected with the another output of separator 32.Liquid phase region circulatory mediator heat exchanger 13
Output end and liquid phase region circulatory mediator heat exchanger flue gas CO2Outlet line 35 is connected, Gas-liquid phase region heat exchanger inlet tube
Line 36 is connected with the input terminal of Gas-liquid phase region heat exchanger 6, the outlet of Gas-liquid phase region heat exchanger exhanst gas outlet pipeline 38 with
Flue gas CO2The input terminal of pump 40 is connected, flue gas CO2The one outlet pipeline CO of pump 402The inlet line 49 of heat exchanger 39 is connected
It connects, CO2The outlet line 50 of heat exchanger 39 is connected with the import of injection well 51, and the shaft bottom of injection well 51 and extraction well 53 is located at
Hydrate reservoir 52 produces outlet and the CH of well 534And CO2The entrance of separator 54 is connected, CH4And CO2Separator 54
Highly concentrated CH4Outlet 55 is connected with natural gas output channel 56, CH4And CO2The CO of separator 542Outlet 57 and flue gas CO2
The outlet line 43 of compressor is connected, flue gas CO2Compressor outlet pipeline 43 and flue gas CO2Pump discharge pipeline 41 and flue gas CO2
Circulation main pipe line 44 is connected, first-class heat exchanger flue gas CO2Outlet line 45 is connected with the outlet end of first-class heat exchanger 29, combustion
Burn the input end and first-class heat exchanger flue gas CO of room 252Outlet line 45 is connected.
It is 4MPa with LNG evaporating pressure in a specific example, Rankine cycle medium in liquid phase region is methane 45%,
Ethane 40%, propane 7%, normal butane 5%, pentane 3%, gas phase zone Rankine cycle medium be ethane 40%, propane 30%, just
Pentane 30% carries out process operation operation.
As shown in Figure 1, supplying the natural gas of 4MPa, mole group of LNG for high-pressure natural gas user in certain LNG receiving station
At as follows: methane 88.77%, ethane 7.54%, propane 2.59%, iso-butane 0.45%, normal butane 0.56%, nitrogen
0.08%.Equipped with 2 16*104m3The LNG storage tank of (cubic meter), boiling point is -162 DEG C under LNG normal pressure, density 456kg/m3
For (kilogram every cubic metre), the warehousing total amount of each LNG liquid storage flow container 70 is (assuming that storage tank is canful) 72960t (ton).
The operating pressure of LNG liquid storage flow container 70 is 0.150MPa (megapascal), and the outer throughput rate of LNG is 200t/h (tph), and LNG is through low
Press pump is pressurized to 4MPa, after being warming up to 159.8 DEG C enter liquid phase region heat exchanger 4, with Rankine cycle media for heat exchange after temperature rise to-
It 93 DEG C, after feeding liquid phase region circulatory mediator pump 11 is forced into 5MPa after Rankine cycle medium is cooled to -142.1 DEG C by LNG, is sent into
It is heated in liquid phase region circulatory mediator heat exchanger 13 by industrial exhaust heat, after temperature is upgraded to 23 DEG C, is sent into liquid phase region expanding machine 15 and expands
To 200kPa (kPa), temperature is reduced to -70.29 DEG C afterwards, is sent into liquid phase region circulatory mediator heat exchanger 13 and carries out next circulation.
Temperature is upgraded to -83 DEG C by -93 DEG C after LNG feeding Gas-liquid phase region heat exchanger 6.4MPa, -83 DEG C of LNG are sent into
Gas phase zone heat exchanger 8 is directly outer defeated after being warming up to 15 DEG C, after gas phase zone Rankine cycle medium is cooled to -66.3 DEG C by LNG, is sent into
After gas phase zone circulatory mediator pump 17 is forced into 4MPa by 150kPa, it is sent into gas phase zone circulatory mediator heat exchanger 19 and is added by industrial exhaust heat
Heat 130 DEG C after be sent into gas phase zone expanding machine 21 be expanded to 150kPa acting after be sent into gas phase zone heat exchanger 8 continue it is next
Circulation.
The BOG evaporated by LNG fluid reservoir 70 is forced into 2.5MPa by 0.15MPa through BOG compressor 47, with high pressure O2It is mixed
The combustion chamber 25 of oxygen and BOG is sent into after conjunction, and the methane gas of afterburning is sent into oxygen together and the combustion chamber 25 of BOG generates
Be sent into flue-gas expander 28 after 800 DEG C to 900 DEG C of high-temperature flue gas and be expanded to 600kpa, temperature be reduced to 600-650 DEG C after with follow
The CO of ring2After temperature is reduced to 200-250 DEG C after being exchanged heat, it is sent into gas phase zone circulatory mediator heat exchanger 19 and heats gas phase zone circulation
After temperature is reduced to 30-80 DEG C after medium, the liquid H in flue gas is isolated into gas-liquid separator 322Liquid phase region circulation is sent into after O
In media heat exchanger 13, liquid phase region circulatory mediator is heated, flue gas CO is made2After further precooling temperature is reduced to -30 DEG C to -45 DEG C,
A part is sent into Gas-liquid phase region heat exchanger 6, flue gas CO2It is cooled to liquid CO herein2Afterwards, liquid CO2Through flue gas CO2Pump
40 are forced into 7MPa, most enters CO2Heat exchanger 39 is vaporized into 20 DEG C of gases, when being reduced to 3MPa through recovery pressure, by CO2
Gas injects into well, CO2It reacts with hydrate, displaces CH4, by obtained gaseous mixture through defeated, feeding outside extraction well 53
CH4And CO2Separator 54 carries out isolated highly concentrated CH4And CO2, the CH that will obtain4It is most of to be sent into natural gas efferent duct
Road carries out outer defeated, the progress of combustion chamber 25 circulating generation of a part feeding oxygen and BOG, by isolated CO2It is sent into next
A CO2Rankine cycle.The flue gas CO cooled down by liquid phase region circulatory mediator2Another part is sent directly into flue gas CO2Pump 40 is forced into
The combustion chamber 25 for being sent into oxygen and BOG after 2.5MPa after the heating of first-class heat exchanger 29 carries out next circulation.
Embodiment 2:
The present embodiment is substantially the same manner as Example 1, brief for description, during the description of the present embodiment, no longer
Technical characteristic same as Example 1 is described, only illustrates the present embodiment difference from Example 1:
As shown in Fig. 2, according to a second aspect of the present application, also providing the CO of a kind of LNG cold energy use and hydrate exploitation2
Capture method includes the following steps:
Step S1, it is simultaneously outer defeated to obtain gas product to carry out gasification process to LNG.
Step S2 burns to BOG to obtain high temperature mixed flue gas.
Step S3, to the CO in high temperature mixed flue gas2It is recycled.
In a preferred embodiment, in step sl, this method further include: by making LNG successively pass through liquid phase
Area's heating subsystem, Gas-liquid phase region heating subsystem and gas phase zone heating subsystem exchange heat to obtain the natural gas and produce
Product.
In a preferred embodiment, in the step S2, this method further include:
Step S21 by pressurizeing to BOG, and the BOG after pressurization is transported in combustion chamber and is burnt to generate
High-temperature flue gas CO2And H2O。
In one embodiment, in step S3, this method further include:
Step S31 passes through the high-temperature flue gas CO generated to reaction2And H2O carries out gas-liquid separation, and to the high temperature after separation
Flue gas CO2Carry out pressurized treatments.
In a preferred embodiment, in the step S3, this method further include:
Step S32, by the high-temperature flue gas CO after pressurized treatments2It is sequentially sent to first-class heat exchanger 29, gas phase zone circulatory mediator
In heat exchanger 19, liquid phase region circulatory mediator heat exchanger 13 and Gas-liquid phase region heat exchanger 6 and carry out after heat exchange to form liquid
Body CO2。
In another preferred embodiment, in step s3, this method further include:
Step S33, to liquid CO2Pressurized treatments are carried out, and to the liquid CO after pressurization2It is vaporized processing, so that liquid
Body CO2It is vaporized into CO2Gas.
In another embodiment, in step s3, the method also includes:
Step S34, by CO2Gas injects in hydrate reservoir, and makes CO2Hydrate in gas and hydrate reservoir
It reacts to displace CH4Mixed gas；
Step S35, by CH4CH in mixed gas4And CO2The CH for being separated, and being isolated4A part is sent into day
Right gas output channel progress is outer defeated, by another part CH4It is sent into combustion chamber and carries out circulating generation, meanwhile, by isolated CO2
Gas is sent into first-class heat exchanger 29 CO carried out next time2Liquefaction processing.
In conclusion the application is by making LNG fluid reservoir 70 successively by liquid phase region heating subsystem, Gas-liquid phase region
It heats up after subsystem and gas phase zone heating subsystem, more cold energy can be released, by carrying out segmentation utilization to LNG cold energy,
And make the circulatory mediator composition in every section of circulation different, so that refrigerant cooling curve is reached with LNG evaporation curve
To the matching of height, further, the exergy efficiencyX of LNG cold energy is greatly increased.
In addition, the BOG for utilizing LNG receiving station to generate by using power cycle is increased, to reach the efficient of BOG
It utilizes, and power supply can be provided for the whole audience, the greenhouse gases CO generated in the process2Also trapping has been obtained to seal up for safekeeping,
Environmental protection is achieved the effect that.
By to liquid CO2After carrying out pressurization vaporization, hydrate is exploited, energy consumption is lower, and realizes CO2Seal up for safekeeping.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (16)
1. the CO of a kind of LNG cold energy use and hydrate exploitation2Capturing device characterized by comprising
LNG vaporization system, BOG processing system and CO2Recovery system,
The LNG vaporization system includes liquid phase region heating subsystem, Gas-liquid phase region heating subsystem and the gas phase being sequentially connected
Heat up subsystem in area, wherein the output end of the gas phase zone heating subsystem exports gas product, the Gas-liquid phase region liter
Warm subsystem is connected with the BOG processing system, for what is obtained after vaporizing Gas-liquid phase region heating subsystem heating
Cryogenic natural gas is delivered to the BOG processing system, to balance the material supply of the BOG processing system；
CO2Vaporization pressurization output system, the CO2Vaporization pressurization output system respectively with the BOG processing system and the CO2
Recovery system is connected, so that the flue gas CO that the BOG processing system generates2It is injected into hydration reservoir to displace CH4Gas and
Partial fume CO2Gas is simultaneously transported to the CO2Recovery system does further recovery processing；
Wherein, the CO2Heat up respectively with liquid phase region subsystem and the Gas-liquid phase region of recovery system heats up subsystem phase
Even, so that the flue gas CO2It is recycled.
2. the CO of LNG cold energy use according to claim 1 and hydrate exploitation2Capturing device, which is characterized in that described
Liquid phase region heating subsystem includes the liquid phase region heat exchanger for being sequentially connected and being capable of forming circuit, liquid phase region circulatory mediator pump, liquid
Phase region circulatory mediator heat exchanger and liquid phase region expanding machine.
3. the CO of LNG cold energy use according to claim 2 and hydrate exploitation2Capturing device, which is characterized in that described
Gas-liquid phase region heating subsystem includes Gas-liquid phase region heat exchanger.
4. the CO of LNG cold energy use according to claim 1 and hydrate exploitation2Capturing device, which is characterized in that described
CO2Recovery system includes first-class heat exchanger and gas-liquid separator.
5. the CO of LNG cold energy use according to claim 4 and hydrate exploitation2Capturing device, which is characterized in that described
CO2Vaporization pressurization output system includes flue gas CO2Pump and with the flue gas CO2Pump the CO being connected2Heat exchanger, wherein the CO2
The output end of heat exchanger is extend into hydrate reservoir by injection well, for injecting flue gas CO into the hydrate reservoir2,
To displace the CH in the hydrate reservoir4With partial fume CO2。
6. the CO of LNG cold energy use according to claim 5 and hydrate exploitation2Capturing device, which is characterized in that described
CO2Vaporization pressurization output system further includes CH4And CO2Separator, wherein the CH4And CO2The entrance of separator is by stretching
Enter the extraction well connection into hydrate reservoir, the CH4And CO2The outlet of separator and the entrance of the first-class heat exchanger
Connection.
7. the CO of LNG cold energy use according to claim 4 and hydrate exploitation2Capturing device, which is characterized in that described
Gas phase zone heating subsystem includes the gas phase zone heat exchanger for being sequentially connected and being capable of forming circuit, gas phase zone circulatory mediator pump, gas
Phase region circulatory mediator heat exchanger and gas phase zone expanding machine.
8. the CO of LNG cold energy use according to claim 7 and hydrate exploitation2Capturing device, which is characterized in that described
The outlet of first-class heat exchanger is connect with the entrance of the gas phase zone circulatory mediator heat exchanger.
9. the CO of LNG cold energy use according to claim 1 and hydrate exploitation2Capturing device, which is characterized in that described
BOG processing system includes combustion chamber and the flue-gas expander of LNG fluid reservoir, BOG compressor, oxygen and BOG.
10. the CO of a kind of LNG cold energy use and hydrate exploitation2Capture method characterized by comprising
Step S1, it is simultaneously outer defeated to obtain gas product to carry out gasification process to LNG；
Step S2 burns to BOG to obtain high temperature mixed flue gas；
Step S3, to the CO in high temperature mixed flue gas2It is recycled.
11. according to the method described in claim 10, it is characterized in that, in step sl, the method also includes:
By making LNG successively by liquid phase region heating subsystem, Gas-liquid phase region heating subsystem and gas phase zone heating subsystem
System exchanges heat to obtain the gas product.
12. according to the method described in claim 10, it is characterized in that, in the step S2, the method also includes:
Step S21 by pressurizeing to BOG, and the BOG after pressurization is transported in combustion chamber and is burnt to generate high temperature
Flue gas CO2And H2O。
13. according to the method for claim 12, which is characterized in that in the step S3, the method also includes:
Step S31 passes through the high-temperature flue gas CO generated to reaction2And H2O carries out gas-liquid separation, and to the high-temperature flue gas after separation
CO2Carry out pressurized treatments.
14. according to the method for claim 13, which is characterized in that in the step S3, the method also includes:
Step S32, by the high-temperature flue gas CO after pressurized treatments2Be sequentially sent to first-class heat exchanger, gas phase zone circulatory mediator heat exchanger,
In liquid phase region circulatory mediator heat exchanger and Gas-liquid phase region heat exchanger and carry out after heat exchange to form liquid CO2。
15. according to the method for claim 14, which is characterized in that in step s3, the method also includes:
Step S33, to liquid CO2Pressurized treatments are carried out, and to the liquid CO after pressurization2It is vaporized processing, so that liquid
CO2It is vaporized into CO2Gas.
16. according to the method for claim 15, which is characterized in that in step s3, the method also includes:
Step S34, by CO2Gas injects in hydrate reservoir, and makes CO2Hydrate in gas and hydrate reservoir occurs
Reaction is to displace CH4Mixed gas；
Step S35, by CH4CH in mixed gas4And CO2The CH for being separated, and being isolated4It is defeated that a part is sent into natural gas
Pipeline carries out outer defeated out, by another part CH4It is sent into combustion chamber and carries out circulating generation, meanwhile, by isolated CO2Gas is sent
Enter the CO carried out in first-class heat exchanger next time2Liquefaction processing.
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Effective date of registration: 20230906 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |