CN105971581A - Device and method for efficiently exploiting natural gas hydrate by adopting flue gas of power plant - Google Patents
Device and method for efficiently exploiting natural gas hydrate by adopting flue gas of power plant Download PDFInfo
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- CN105971581A CN105971581A CN201610501216.5A CN201610501216A CN105971581A CN 105971581 A CN105971581 A CN 105971581A CN 201610501216 A CN201610501216 A CN 201610501216A CN 105971581 A CN105971581 A CN 105971581A
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- hydrate
- gas
- hollow fiber
- flue gas
- fiber film
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 239000003546 flue gas Substances 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 38
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 title claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 58
- 239000012528 membrane Substances 0.000 claims abstract description 38
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 238000011084 recovery Methods 0.000 claims abstract description 23
- 238000005261 decarburization Methods 0.000 claims abstract description 13
- 238000002347 injection Methods 0.000 claims abstract description 6
- 239000007924 injection Substances 0.000 claims abstract description 6
- 239000012510 hollow fiber Substances 0.000 claims description 57
- 238000010521 absorption reaction Methods 0.000 claims description 24
- 238000005262 decarbonization Methods 0.000 claims description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 239000008246 gaseous mixture Substances 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 230000036772 blood pressure Effects 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000005204 segregation Methods 0.000 claims description 3
- 230000036571 hydration Effects 0.000 claims description 2
- 238000006703 hydration reaction Methods 0.000 claims description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 claims 1
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 230000008595 infiltration Effects 0.000 description 16
- 238000001764 infiltration Methods 0.000 description 16
- 239000000243 solution Substances 0.000 description 11
- 238000005065 mining Methods 0.000 description 10
- 150000004677 hydrates Chemical class 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 239000000835 fiber Substances 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 239000002912 waste gas Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- -1 gas-booster Chemical compound 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 229920000428 triblock copolymer Polymers 0.000 description 1
Classifications
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/30—Specific pattern of wells, e.g. optimising the spacing of wells
- E21B43/305—Specific pattern of wells, e.g. optimising the spacing of wells comprising at least one inclined or horizontal well
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/105—Removal of contaminants of nitrogen
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B41/00—Equipment or details not covered by groups E21B15/00 - E21B40/00
- E21B41/0099—Equipment or details not covered by groups E21B15/00 - E21B40/00 specially adapted for drilling for or production of natural hydrate or clathrate gas reservoirs; Drilling through or monitoring of formations containing gas hydrates or clathrates
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/01—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells specially adapted for obtaining from underwater installations
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/166—Injecting a gaseous medium; Injecting a gaseous medium and a liquid medium
- E21B43/168—Injecting a gaseous medium
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/295—Gasification of minerals, e.g. for producing mixtures of combustible gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
Landscapes
- Engineering & Computer Science (AREA)
- Geology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Mining & Mineral Resources (AREA)
- Geochemistry & Mineralogy (AREA)
- Fluid Mechanics (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a device for efficiently exploiting natural gas hydrate by adopting flue gas of a power plant. The device comprises a gas booster, an injection well, an overlying formation, an exploiting well, a turbine expansion device, a membrane separation device and a decarburization device, wherein the gas booster is connected with the injection well; the exploiting well is connected with the turbine expansion device, the membrane separation device and the decarburization device sequentially. With the adoption of the method for exploiting the hydrate, the recovery rate of methane is higher; the exploiting mode is more environment-friendly, and CO2 is sealed and stored while methane hydrate is exploited; energy consumption is lower.
Description
Technical field
The present invention relates to exploitation of gas hydrates field, particularly relate to power-plant flue gas efficiently, the economic exploitation gas water
The method of compound.
Background technology
Gas hydrates are widely present in land permafrost region and sea-bottom deposit nitride layer, are the next generations of a kind of great prospect
Energy resources.The most efficiently, the natural gas resource that mine reserves is huge from hydrate reservoir economically still faces lot of challenges.
The technology of offshore production gas hydrates typically comes from the conventional oil of industrial gas oil, gas exploitation skill at present
Art.These methods are all to utilize temperature, pressure different with chemical potential aspect driving force, thus significantly change hydrate reservoir district
Condition.Heat shock method is to cause hydrate reservoir temperature to change (Δ between generating and decomposingT)；Voltage drop method is to change reservoir
Pressure makes it below hydrate and generates pressure (ΔP)；Inhibitor is the chemical environment (Δ changing hydrateμ) thus hinder
The generation of gas hydrate.But, these methods are all built upon being likely to result on the basis of decomposition of hydrate serious
Consequence, such as submarine landslide and the destruction of benthic system.
Use flue gas (CO2With N2Gaseous mixture) to carry out exploitation of gas hydrate be a kind of potential lossless mining type, open
The process of adopting can form CO2Hydrate can play the effect of good ground.But owing to injecting N in gas2Content is higher, extraction
CH in gas4Content is the lowest and N2/CH4Difficult separation so that the total energy effect of whole process reduces, and exploited cost and increases, and caused acquisition
CH4Industrial application value is the highest.
During for flue gas production of water compound, output gas methane concentration is low, the shortcoming that recovery process efficiency is low, less economical,
The present invention propose power-plant flue gas efficiently, the method for the economic exploitation gas hydrates, on the one hand improve the concentration of output gas methane,
On the other hand consider from the flue gas whole flow process of replacement exploitation hydrate (from power-plant flue gas to final methane product gas), choose
Suitably operating condition and separating technology, thus improve economy and the efficiency of flue gas production of water compound process.
Summary of the invention
During for flue gas production of water compound, output gas methane concentration is low, the shortcoming that recovery process efficiency is low, less economical,
The present invention proposes the method for power-plant flue gas efficiently extracting natural gas hydrate.
The present invention is achieved through the following technical solutions:
The method of power-plant flue gas efficiently extracting natural gas hydrate, first gets out the horizontal well of more than two mouthfuls at hydrate reservoir；
Described horizontal well includes more than one injection well and more than one recovery well；Begin with blood pressure lowering mining type to open
Adopt, when 5% ~ 15% of hydrate phase balance pressure corresponding to hydrate reservoir pressure drop as little as reservoir temperature, by injecting well
Inject the flue gas higher than hydrate reservoir pressure 2 ~ 4 MPa to hydrate reservoir, be injected into flue gas and the hydrate reservoir on stratum
In hydrate react the gaseous mixture obtained containing methane, through recovery well, pipelined to turbine expansion device recoverer
Partial pressure energy, the gaseous mixture after turbine expansion device is delivered to membrane separation device and removes nitrogen, after membrane separation device processes
Gas be fed directly to decarbonization device by pipeline and carry out decarburization, finally give required product gas methane gas.
In said method, injecting flue gas to hydrate reservoir, power-plant flue gas directly carries out supercharging, injects without entering flue gas
Row separates, purified treatment；Flue gas after supercharging is directly injected into stratum without carrying out cooling process by injecting well.
In said method, the gaseous mixture after turbine expansion device is delivered to membrane separation device and removes nitrogen, described film
Segregation apparatus removes nitrogen and also includes using pressure-variable adsorption or hydration mode to remove nitrogen.
In said method, the described gas after membrane separation device process is fed directly to decarbonization device by pipeline to be carried out
Decarburization, decarburization mode herein can carry out decarburization to use ethanolamine absorption, hydrate, membrance separation, pressure-variable adsorption mode.
In said method, pressure is down to required for membrane separation device by extraction well gas out by turbine expansion device
Admission pressure simultaneously recovery section pressure energy.
The device of power-plant flue gas efficiently extracting natural gas hydrate, including gas-booster, injection well, superstratum, opens
Adopt well, turbine expansion device, membrane separation device and decarbonization device；
Described gas-booster is connected with injecting well；Described recovery well and turbine expansion device, membrane separation device and decarbonization device
It is sequentially connected with.
Further, described membrane separation device includes first order hollow fiber film assembly, second level hollow fiber film assembly
With third level hollow fiber film assembly；Described first order hollow fiber film assembly oozes vent outlet with outlet of oozing residual air respectively with the
The entrance of two grades of hollow fiber film assemblies and third level hollow fiber film assembly connects；Described second level hollow fiber film assembly oozes
The air inlet oozing vent outlet and first order hollow fiber film assembly of residual air outlet and third level hollow fiber film assembly is even
Connect.
Further, described decarbonization device includes absorption tower, tube bundle heat exchanger, centrifugal pump and desorber；Described absorption
The outlet at bottom of tower is connected with tube bundle heat exchanger left hand inlet port, tube bundle heat exchanger right-side outlet connects desorber top and enters
Mouthful；The outlet at bottom of described desorber is connected with centrifugal pump inlet, the bottom inlet of outlet of centrifugal pump and tube bundle heat exchanger
It is connected；The upper outlet of described tube bundle heat exchanger is connected with the top entry on absorption tower；CH4Arranged by absorption tower tower top outlet
Go out, CO2Discharged by desorber tower top outlet.
Compared with prior art, present invention have an advantage that
Using this method production of water compound, the response rate of methane is higher；Mining type is more environmentally friendly, is exploiting the same of methane hydrate
Time sealed CO up for safekeeping2；Energy consumption is lower simultaneously.
Accompanying drawing explanation
Fig. 1 be power-plant flue gas efficiently, the schematic diagram of the method for the economic exploitation gas hydrates；
Fig. 2 is the structural representation of membrane separation device；
Fig. 3 is the structural representation of decarbonization device.
In figure, all parts is as follows:
Gas-booster 1, inject well 2, under cover stratum 3, hydrate layer 4, superstratum 5, recovery well 6, turbine expansion device 7,
In membrane separation device 8, decarbonization device 9, first order hollow fiber film assembly 10, second level hollow fiber film assembly 11, the third level
Hollow fiber membrane module 12, absorption tower 13, tube bundle heat exchanger 14, centrifugal pump 15, desorber 16.
Detailed description of the invention
Being described in further detail the goal of the invention of the present invention with specific embodiment below in conjunction with the accompanying drawings, embodiment is not
Can repeat one by one at this, but the most therefore embodiments of the present invention are defined in following example.
Below in conjunction with the accompanying drawings and embodiment the invention will be further described.
The device of power-plant flue gas efficiently extracting natural gas hydrate, including gas-booster 1, inject well 2, superstratum 5,
Recovery well 6, turbine expansion device 7, membrane separation device 8 and decarbonization device 9；Described gas-booster 1 is connected with injecting well 2；Institute
State recovery well 6 to be sequentially connected with turbine expansion device 7, membrane separation device 8 and decarbonization device 9.Described membrane separation device 8 includes
One-level hollow fiber film assembly 10, second level hollow fiber film assembly 11 and third level hollow fiber film assembly 12；Described first
Level hollow fiber film assembly 10 ooze vent outlet with ooze residual air outlet respectively with second level hollow fiber film assembly 11 and the third level
The entrance of hollow fiber film assembly 12 connects；Described second level hollow fiber film assembly 11 oozes residual air outlet and third level hollow is fine
The vent outlet that oozes of dimension membrane module 12 is connected with the air inlet of first order hollow fiber film assembly 10.Described decarbonization device 9 wraps
Include absorption tower 13, tube bundle heat exchanger 14, centrifugal pump 15 and desorber 16；The outlet at bottom on described absorption tower 13 changes with bundled tube
Hot device 14 left hand inlet port connects, tube bundle heat exchanger 14 right-side outlet connects desorber 16 upper entrance；Described desorber 16
The bottom inlet that outlet at bottom is connected with centrifugal pump 15 entrance, centrifugal pump 15 exports with tube bundle heat exchanger 14 is connected；Described
The upper outlet of tube bundle heat exchanger 14 is connected with the top entry on absorption tower 13；CH4Discharged by absorption tower 13 tower top outlet,
CO2Discharged by desorber 16 tower top outlet.
The turbine expansion device 7 of the present invention uses the turbine expansion electromotor that Xida Low Temperature Equipment Co., Ltd., Suzhou produces
Group one.
The attachment structure of the present invention is as follows:
As it is shown in figure 1, power-plant flue gas is efficient, the method for the economic exploitation gas hydrates, first get out two mouthfuls of water horizontal wells, level
Well 2 and horizontal well 6, use blood pressure lowering mining type to exploit；When hydrate reservoir pressure drop as little as reservoir temperature correspondence is hydrated
On phase balance pressure 5% ~ 15%, power-plant flue gas passes through pressurizer 1 supercharging, then injects flue gas to injecting well 2；Extraction well
6 mined gases first pass through turbine expansion device 7 recovery section pressure energy, and the gaseous mixture after turbine expansion device is defeated
Delivering to membrane separation device 8 and remove nitrogen, the gas after membrane separation device process is fed directly to decarbonization device 9 by pipeline to be carried out
Decarburization, finally gives required product gas methane gas.
Turbine expansion device can use the turbine expansion generating set one that Xida Low Temperature Equipment Co., Ltd., Suzhou produces；Film
Segregation apparatus is made up of first order hollow fiber film assembly, second level hollow fiber film assembly, third level hollow fiber film assembly,
The hollow-fibre membrane of hollow fiber film assembly can use s-B-S (SBS) triblock copolymer film；Decarburization
The absorbent of device uses methyl diethanolamine (MDEA) solution.
Fig. 2 is the structural representation of membrane separation device 8, and specific embodiment is as follows: will under turbo-expander pressure
Gaseous mixture to 2MPa is delivered to the first order hollow fiber film assembly 10 of membrane separation device.First order hollow fiber film assembly
Infiltration gas enters second level hollow fiber film assembly 11, oozes residual air and enters third level hollow fiber film assembly 12；Third level hollow
Fiber film component infiltration gas is back to first order hollow fiber film assembly, oozes residual air and is directly vented；Second level hollow-fibre membrane group
Part oozes residual air and is back to first order hollow fiber film assembly, and infiltration gas is fed directly to decarbonization device.
Fig. 3 is the structural representation of decarbonization device 9, and specific embodiment is as follows: membrane separation device second level hollow is fine
Dimension membrane module infiltration gas is directly inputted into the absorption tower 13 of decarbonization device, injects MDEA solution from top, absorption tower, from suction simultaneously
Receiving column overhead and obtain required product gas methane gas, the absorbing liquid at the bottom of tower is (containing CO2MDEA solution) through tube bundle heat exchanger
14 enter desorber 16 desorbing, and tower top discharges CO2Waste gas, the lean solution centrifugal pump 15 at the bottom of tower is back to through tube bundle heat exchanger
Absorption tower.
Embodiment 1
The present embodiment provides a kind of power-plant flue gas high-efficiency mining reservoir conditions to be 4 DEG C, the side of the gas hydrates of 12MPa
Method, its operating process is as follows:
First, in the middle part of hydrate reservoir and edge respectively bores water horizontal well, begin with blood pressure lowering mining type and exploit.When
During hydrate reservoir pressure drop as little as 4.3MPa, (volume fraction is 0.16CO to inject 8MPa flue gas to hydrate reservoir2+
0.84N2).It is injected into the flue gas on stratum and the hydrate in hydrate reservoir to react the gaseous mixture obtained containing methane, passes through
Recovery well, pipeline are fed directly to turbo-expander recovery section pressure energy, and mixture pressure is down to 2MPa and is delivered to membrance separation
The first order hollow fiber film assembly of device.The infiltration gas of first order hollow fiber film assembly enters second level hollow-fibre membrane group
Part, oozes residual air and enters third level hollow fiber film assembly；Third level hollow fiber film assembly infiltration gas is back to first order hollow
Fiber film component, oozes residual air and is directly vented；Second level hollow fiber film assembly oozes residual air and is back to first order hollow-fibre membrane group
Part, infiltration gas is fed directly to decarbonization device.The infiltration gas entering decarbonization device absorbs through absorption tower, obtains required from tower top
Product gas methane gas.Absorbing liquid at the bottom of tower is (containing CO2MDEA solution) through tube bundle heat exchanger enter desorber desorbing, tower top
Discharge CO2Waste gas, the lean solution centrifugal pump at the bottom of tower is back to absorption tower through tube bundle heat exchanger.
Embodiment 2
The present embodiment provides a kind of power-plant flue gas high-efficiency mining reservoir conditions to be 1 DEG C, the side of the gas hydrates of 12MPa
Method, its operating process is as follows:
First, in the middle part of hydrate reservoir and edge respectively bores water horizontal well, begin with blood pressure lowering mining type and exploit.When
During hydrate reservoir pressure drop as little as 3.3MPa, (volume fraction is 0.16CO to inject 7MPa flue gas to hydrate reservoir2+
0.84N2).It is injected into the flue gas on stratum and the hydrate in hydrate reservoir to react the gaseous mixture obtained containing methane, passes through
Recovery well, pipeline are fed directly to turbo-expander recovery section pressure energy, and mixture pressure is down to 2MPa and is delivered to membrance separation
The first order hollow fiber film assembly of device.The infiltration gas of first order hollow fiber film assembly enters second level hollow-fibre membrane group
Part, oozes residual air and enters third level hollow fiber film assembly；Third level hollow fiber film assembly infiltration gas is back to first order hollow
Fiber film component, oozes residual air and is directly vented；Second level hollow fiber film assembly oozes residual air and is back to first order hollow-fibre membrane group
Part, infiltration gas is fed directly to decarbonization device.The infiltration gas entering decarbonization device absorbs through absorption tower, obtains required from tower top
Product gas methane gas.Absorbing liquid at the bottom of tower is (containing CO2MDEA solution) through tube bundle heat exchanger enter desorber desorbing, tower top
Discharge CO2Waste gas, the lean solution centrifugal pump at the bottom of tower is back to absorption tower through tube bundle heat exchanger.
Embodiment 3
The present embodiment provides a kind of power-plant flue gas high-efficiency mining reservoir conditions to be 1 DEG C, the side of the gas hydrates of 10MPa
Method, its operating process is as follows:
First, in the middle part of hydrate reservoir and edge respectively bores water horizontal well, begin with blood pressure lowering mining type and exploit.When
During hydrate reservoir pressure drop as little as 3.3MPa, (volume fraction is 0.16CO to inject 6MPa flue gas to hydrate reservoir2+
0.84N2).It is injected into the flue gas on stratum and the hydrate in hydrate reservoir to react the gaseous mixture obtained containing methane, passes through
Recovery well, pipeline are fed directly to turbo-expander recovery section pressure energy, and mixture pressure is down to 2MPa and is delivered to membrance separation
The first order hollow fiber film assembly of device.The infiltration gas of first order hollow fiber film assembly enters second level hollow-fibre membrane group
Part, oozes residual air and enters third level hollow fiber film assembly；Third level hollow fiber film assembly infiltration gas is back to first order hollow
Fiber film component, oozes residual air and is directly vented；Second level hollow fiber film assembly oozes residual air and is back to first order hollow-fibre membrane group
Part, infiltration gas is fed directly to decarbonization device.The infiltration gas entering decarbonization device absorbs through absorption tower, obtains required from tower top
Product gas methane gas.Absorbing liquid at the bottom of tower is (containing CO2MDEA solution) through tube bundle heat exchanger enter desorber desorbing, tower top
Discharge CO2Waste gas, the lean solution centrifugal pump at the bottom of tower is back to absorption tower through tube bundle heat exchanger.
Claims (7)
1. the method for power-plant flue gas efficiently extracting natural gas hydrate, it is characterised in that first get out two mouthfuls at hydrate reservoir
Above horizontal well；Described horizontal well includes more than one injection well and more than one recovery well；Begin with blood pressure lowering to open
The mode of adopting is exploited, when corresponding to hydrate reservoir pressure drop as little as reservoir temperature the 5% ~ 15% of hydrate phase balance pressure
Time, inject the flue gas higher than hydrate reservoir pressure 2 ~ 4 MPa by injecting well to hydrate reservoir, be injected into the flue gas on stratum
React the gaseous mixture obtained containing methane with the hydrate in hydrate reservoir, swollen to turbine through recovery well, pipelined
Swollen device recovery section pressure energy, the gaseous mixture after turbine expansion device is delivered to membrane separation device and removes nitrogen, and film divides
Gas after device processes is fed directly to decarbonization device by pipeline and carries out decarburization, finally gives required product gas first
Alkane gas.
The method of power-plant flue gas efficiently extracting natural gas hydrate the most according to claim 1, it is characterised in that Jing Guotou
Gaseous mixture after flat expansion gear is delivered to membrane separation device and removes nitrogen, and described membrane separation device removes nitrogen and also includes using
Pressure-variable adsorption or hydration mode remove nitrogen.
The method of power-plant flue gas efficiently extracting natural gas hydrate the most according to claim 1, it is characterised in that described film
Gas after segregation apparatus process is fed directly to decarbonization device by pipeline and carries out decarburization, and decarburization mode herein can use second
Hydramine absorption, hydrate, membrance separation, pressure-variable adsorption mode carry out decarburization.
The method of power-plant flue gas efficiently extracting natural gas hydrate the most according to claim 1, it is characterised in that extraction well goes out
Recovery section pressure while that pressure being down to the admission pressure required for membrane separation device by turbine expansion device by the gas come
Energy.
5. the device of power-plant flue gas efficiently extracting natural gas hydrate, it is characterised in that include
Gas-booster (1), injection well (2), superstratum (5), recovery well (6), turbine expansion device (7), membrane separation device
And decarbonization device (9) (8)；
Described gas-booster (1) is connected with injecting well (2)；Described recovery well (6) and turbine expansion device (7), membrance separation dress
Put (8) and decarbonization device (9) is sequentially connected with.
The device of power-plant flue gas efficiently extracting natural gas hydrate the most according to claim 5, it is characterised in that described film divides
Include that first order hollow fiber film assembly (10), second level hollow fiber film assembly (11) and third level hollow are fine from device (8)
Dimension membrane module (12)；Described first order hollow fiber film assembly (10) ooze vent outlet with ooze residual air outlet respectively with in the second level
The entrance of hollow fiber membrane module (11) and third level hollow fiber film assembly (12) connects；Described second level hollow fiber film assembly
(11) ooze residual air outlet and third level hollow fiber film assembly (12) oozes vent outlet and first order hollow fiber film assembly
(10) air inlet connects.
The device of power-plant flue gas efficiently extracting natural gas hydrate the most according to claim 5, it is characterised in that described decarburization
Device (9) includes absorption tower (13), tube bundle heat exchanger (14), centrifugal pump (15) and desorber (16)；Described absorption tower (13)
Outlet at bottom be connected with tube bundle heat exchanger (14) left hand inlet port, tube bundle heat exchanger (14) right-side outlet connect desorber
(16) upper entrance；The outlet at bottom of described desorber (16) is connected with centrifugal pump (15) entrance, centrifugal pump (15) outlet with
The bottom inlet of tube bundle heat exchanger (14) is connected；The upper outlet of described tube bundle heat exchanger (14) and the top on absorption tower (13)
Portion's entrance connects；CH4Discharged by absorption tower (13) tower top outlet, CO2Discharged by desorber (16) tower top outlet.
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