CN216472258U - Helium extraction system for geothermal well associated gas - Google Patents
Helium extraction system for geothermal well associated gas Download PDFInfo
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- CN216472258U CN216472258U CN202123250133.9U CN202123250133U CN216472258U CN 216472258 U CN216472258 U CN 216472258U CN 202123250133 U CN202123250133 U CN 202123250133U CN 216472258 U CN216472258 U CN 216472258U
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- geothermal well
- buffer tank
- extraction system
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- 239000007789 gas Substances 0.000 title claims abstract description 119
- 239000001307 helium Substances 0.000 title claims abstract description 50
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 50
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000000605 extraction Methods 0.000 title claims abstract description 23
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 239000012528 membrane Substances 0.000 claims description 64
- 239000012510 hollow fiber Substances 0.000 claims description 23
- 239000000428 dust Substances 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 14
- 230000007246 mechanism Effects 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 20
- 238000006477 desulfuration reaction Methods 0.000 abstract description 9
- 230000023556 desulfurization Effects 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 5
- 239000000112 cooling gas Substances 0.000 abstract description 2
- 150000002371 helium Chemical class 0.000 abstract 1
- 238000000746 purification Methods 0.000 description 9
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 8
- 238000006356 dehydrogenation reaction Methods 0.000 description 8
- 239000012466 permeate Substances 0.000 description 7
- 238000001179 sorption measurement Methods 0.000 description 7
- 239000003054 catalyst Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000005057 refrigeration Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 229910052763 palladium Inorganic materials 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 230000008595 infiltration Effects 0.000 description 3
- 238000001764 infiltration Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000007791 dehumidification Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000001680 brushing effect Effects 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
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Abstract
The utility model relates to a helium draws technical field, and disclose a helium extraction system for geothermal well associated gas, including the buffer tank, geothermal well's output is provided with the buffer tank, the output of buffer tank is connected with low pressure diaphragm compressor, the output of low pressure diaphragm compressor is connected with the digester, the output of digester is connected with the digester, this helium extraction system for geothermal well associated gas uses geothermal water as the carrier through geothermal well associated gas, after conveying to ground through the immersible pump, through the separation of gas-water separator, geothermal water gets into the heat supply heat transfer flow, geothermal well associated gas (helium content 2.5-3%) gets into the buffer tank, the main purpose of buffer tank is balanced air supply pressure fluctuation phenomenon and the effect of cooling gas, make extraction system work more steady, the water of buffer tank lower part is automatic control discharges by the liquid level, the gas that comes out from the buffer tank gets into low pressure diaphragm compressor entry, the compressor raises the micro-positive pressure gas to the operation pressure of 0.25-0.35MPa to purify the system for desulfurization.
Description
Technical Field
The utility model relates to a helium draws technical field, specifically is a helium extraction system for geothermal well associated gas.
Background
Helium is a rare gas, is a colorless and tasteless inert gas, is inactive in chemical property, is difficult to react with other substances under a general state, and is widely applied to the fields of medical treatment, electronics, national defense, military industry and the like as a nonrenewable rare gas along with the rapid development of modern science and technology.
The helium resource can be extracted from the geothermal well, but the conventional extraction process has huge energy consumption, and the extracted helium has impurities which are difficult to control.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
Not enough to prior art, the utility model provides a helium extraction system for geothermal well associated gas possesses the advantage of extracting helium in the geothermal well, and it is big to have solved current geothermal well energy consumption when extracting helium, has the problem of impurity moreover.
(II) technical scheme
In order to achieve the above object, the utility model provides a following technical scheme: the utility model provides a helium extraction system for geothermal well associated gas, including the buffer tank, geothermal well's output is provided with the buffer tank, the output of buffer tank is connected with low pressure diaphragm compressor, low pressure diaphragm compressor's output is connected with the digester, the output of digester is connected with the cold machine of doing, the output of cold machine of doing is connected with one section membrane group separator, the output of one section membrane group separator is connected with two-stage process membrane group separator and hollow fiber separation unit, the output of two-stage process membrane group separator is connected with tail gas treatment mechanism, hollow fiber separation unit's output is connected with piston compressor, piston compressor's output list is connected with VPSA, VPSA's output is connected with high-pressure diaphragm compressor two, the output list of high-pressure diaphragm compressor two is connected with product gas collection check group.
Preferably, the output ends of the two-stage membrane group separator and the VPSA are respectively connected with the input end of the buffer tank.
By adopting the scheme, the output ends of the two-section membrane group separator and the VPSA are respectively connected with the input end of the buffer tank, so that the gas with the helium content of more than ten percent generated by the two-section membrane group separator can be returned to the buffer tank for circulation, about one percent of the helium content of the analytic gas generated by the VPSA is returned to the buffer tank to be mixed with the associated gas of the second well at the wellhead and the two-section membrane group permeation gas, and the mixed gas is used as about three percent of the helium content of the feed gas and then enters the process again for separation.
Preferably, each separator is shut off or on by a valve.
Through adopting above-mentioned scheme, through cutting off or separating with the separator with the valve, the later stage is convenient for each unit isolated operation like this.
Preferably, the first-stage membrane group separator and the second-stage membrane group separator are respectively connected with a vacuum pump.
By adopting the scheme, the first-stage membrane component separator and the second-stage membrane component separator are respectively connected with the vacuum pump, so that the pressure difference between two sides of the hollow fiber separation unit can be increased by the permeation gas of the first-stage membrane component separator and the permeation gas of the second-stage membrane component separator, and the separation effect of the membrane separator can be increased.
Preferably, the output end of the hollow fiber separation unit is connected with a first high-pressure diaphragm compressor, the output end of the first high-pressure diaphragm compressor is connected with a permeation gas collection grid group, and the output end of the permeation gas collection grid group is connected with a piston compressor.
Through adopting above-mentioned scheme, through the output high pressure diaphragm compressor I at hollow fiber separating element, the output of high pressure diaphragm compressor I is connected with infiltration gas collection check group, the output of infiltration gas collection check group is connected with piston compressor, can store the gaseous of the helium content fifty percent that hollow fiber separating element produced in the steel bottle in infiltration gas collection check group like this to use when carrying out the purification for follow-up, when using, purify in with gas suction to VPSA through piston compressor.
Preferably, the air-cooler includes auxiliary assembly, auxiliary assembly includes the air-cooler, the positive top of air-cooler is provided with the controller, the front symmetry of air-cooler is provided with the fixed block, two slide one, two have been seted up to the opposite face one side symmetry of fixed block the inboard sliding connection of slide one has the dust screen.
Through adopting above-mentioned scheme, through two fixed blocks that set up in the front of air-cooler, the slide one of seting up in opposite face one side symmetry of fixed block sets up the dust screen in the inboard of slide one, and the later stage of being convenient for like this is dismantled the dust screen, avoids the later stage dust screen to take place to damage, leads to causing the influence to the cooling system of air-cooler.
Preferably, two slide two, two have been seted up to the inboard opposite face opposite side symmetry of fixed block the inboard sliding connection of slide two has the slide, the back of slide is provided with soft brush, two the positive top of fixed block is provided with the fixed plate, the top of fixed plate is provided with the movable rod, the one end of movable rod runs through the top of fixed plate and with the front of slide is connected.
Through adopting above-mentioned scheme, through the slide two of seting up at the opposite face opposite side of fixed block, at the slide that the inboard of slide two set up, what set up at the back of slide has soft brush, can clear up the surperficial dust of dust screen through removing the slide like this, be provided with the fixed plate in the front of fixed block, the top of fixed plate is provided with the movable rod and passes the fixed plate and connect the slide, can just can control soft brush and clear up the surface of dust screen through the pull movable rod like this.
Preferably, the movable rod is connected with the sliding plate through a bolt.
Through adopting above-mentioned scheme, through making movable rod and slide bolted connection, the later stage of being convenient for like this is changed soft brush.
(III) advantageous effects
Compared with the prior art, the utility model provides a helium extraction system for geothermal well associated gas possesses following beneficial effect:
the helium extraction system for the geothermal well associated gas takes geothermal water as a carrier through the geothermal well associated gas, the geothermal water is separated by a gas-water separator after being pumped to the ground through a submersible pump, the geothermal water enters a heat supply and heat exchange process, the geothermal well associated gas (the content of the helium is 2.5-3 percent) enters a buffer tank, the main purpose of the buffer tank is to balance the pressure fluctuation phenomenon of a gas source and the effect of cooling the gas, so that the extraction system works more stably, the water at the lower part of the buffer tank is automatically discharged by liquid level control, the gas discharged from the buffer tank enters an inlet of a low-pressure diaphragm compressor, the compressor lifts the micro-positive pressure gas to the operation pressure of 0.25-0.35MPa to a purification system for desulfurization, dehydrogenation and dehumidification, the gas sequentially enters a desulfurization tank and a desulfurization tank, hydrogen sulfide in the gas is removed to 0.1ppm by direct contact with a desulfurizing agent in the tank, the desulfurized gas enters a dehydrogenation tank, a palladium catalyst is filled in the dehydrogenation tank, the palladium catalyst is one kind of catalyst used in chemical and chemical reaction process and is used in eliminating hydrogen from gas through oxygen adding and hydrogen eliminating process. The gas after desulfurization and dehydrogenation enters a refrigeration dryer, the refrigeration dryer utilizes a refrigerant to exchange heat with the gas, the temperature of the gas is reduced to the dew point temperature within the range of 2-10 ℃, water vapor in the gas is removed, so that the feed gas is prevented from generating water mist to influence the membrane separation performance after entering a membrane separator, liquid water formed by condensation is automatically discharged by a ball float valve in the refrigeration dryer, the purified gas enters a hollow fiber membrane separation unit, the hollow fiber membrane has high selectivity on helium, the separation is realized by taking partial pressure difference between the inner side and the outer side of the hollow fiber membrane as driving force through the steps of dissolution, diffusion, desorption and the like, the inner side of the hollow fiber membrane forms a helium-poor gas flow, the outer side forms a helium-rich gas flow, the former is called tail gas, the latter is called permeate gas, the gas firstly enters a section of membrane component separator for separation, the section of membrane component permeate gas is vacuumized by a vacuum pump to generate a component with the helium content of more than 50 percent and then enters a pressure swing adsorption process for purification, and (3) taking tail gas (the helium content is about 0.8%) of the first-stage membrane group as raw material gas of the second-stage membrane group separator, sending the tail gas of the second-stage membrane group separator to the second-stage membrane group separator, directly exhausting the tail gas of the second-stage membrane group separator, and taking permeation gas with the helium content of more than 50% as the raw material gas to enter a Vacuum Pressure Swing Adsorption (VPSA) process. The gas is lifted to the operating pressure of 0.8-1.0MPa by a piston compressor and then enters a VPSA adsorption tower for purification, and the product gas (the content of helium is more than 99 percent) is stored in a steel cylinder in a product gas collection grid group by a high-pressure compressor III.
Drawings
FIG. 1 is a schematic diagram of a geothermal well associated helium extraction process;
fig. 2 is a schematic structural view of the front side of the intercooler fan of the present invention;
fig. 3 is a schematic structural diagram of the top portions of two fixing blocks in the present invention.
In the figure:
1. an auxiliary component; 11. an air cooler; 12. a controller; 13. a fixed block; 131. a first slideway; 132. a second slideway; 14. a dust screen; 15. a slide plate; 16. soft brushing; 17. a fixing plate; 171. a movable rod.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example one
A helium extraction system for associated gas of a geothermal well comprises a buffer tank, wherein the output end of the geothermal well is provided with the buffer tank, the output end of the buffer tank is connected with a low-pressure diaphragm compressor, the output end of the low-pressure diaphragm compressor is connected with a desulfurizing tank, the output end of the desulfurizing tank is connected with a cooling and drying machine, the output end of the cooling and drying machine is connected with a first-section membrane group separator, the output end of the first-section membrane group separator is connected with a second-section membrane group separator and a hollow fiber separation unit, the output end of the second-section membrane group separator is connected with a tail gas treatment mechanism, the output end of the hollow fiber separation unit is connected with a piston compressor, an output unit of the piston compressor is connected with VPSA, the output end of the VPSA is connected with a second high-pressure diaphragm compressor, and an output unit of the second high-pressure diaphragm compressor is connected with a product gas collection grid group;
the output ends of the two-section membrane component separator and the VPSA are respectively connected with the input end of the buffer tank, each separator is cut off or connected through a valve, the one-section membrane component separator and the two-section membrane component separator are respectively connected with a vacuum pump, the output end of the hollow fiber separation unit is connected with a high-pressure membrane compressor I, the output end of the high-pressure membrane compressor I is connected with a permeate gas collection grid group, and the output end of the permeate gas collection grid group is connected with a piston compressor.
Referring to fig. 1-3, geothermal well associated gas uses geothermal water as a carrier, the geothermal water is separated by a gas-water separator after being pumped to the ground by a submersible pump, the geothermal water enters a heat supply and heat exchange process, the geothermal well associated gas (with the helium content of 2.5-3%) enters a buffer tank, the main purpose of the buffer tank is to balance the pressure fluctuation phenomenon of a gas source and the effect of cooling gas, so that the work of an extraction system is more stable, the water at the lower part of the buffer tank is automatically discharged by liquid level control, the gas discharged from the buffer tank enters an inlet of a low-pressure diaphragm compressor, the compressor lifts the micro-positive pressure gas to the operation pressure of 0.25-0.35MPa to a purification system for desulfurization, dehydrogenation and dehumidification, the gas sequentially enters a desulfurization tank and a desulfurization tank, hydrogen sulfide in the gas is removed to 0.1ppm by direct contact with a desulfurizing agent in the tank, the desulfurized gas enters a dehydrogenation tank, a palladium catalyst is filled in the dehydrogenation tank, the palladium catalyst is one kind of catalyst used in chemical and chemical reaction process and is used in eliminating hydrogen from gas through oxygen adding and hydrogen eliminating process. The gas after desulfurization and dehydrogenation enters a refrigeration dryer, the refrigeration dryer utilizes a refrigerant to exchange heat with the gas, the temperature of the gas is reduced to the dew point temperature within the range of 2-10 ℃, water vapor in the gas is removed, so that the feed gas is prevented from generating water mist to influence the membrane separation performance after entering a membrane separator, liquid water formed by condensation is automatically discharged by a ball float valve in the refrigeration dryer, the purified gas enters a hollow fiber membrane separation unit, the hollow fiber membrane has high selectivity on helium, the separation is realized by taking partial pressure difference between the inner side and the outer side of the hollow fiber membrane as driving force through the steps of dissolution, diffusion, desorption and the like, the inner side of the hollow fiber membrane forms a helium-poor gas flow, the outer side forms a helium-rich gas flow, the former is called tail gas, the latter is called permeate gas, the gas firstly enters a section of membrane component separator for separation, the section of membrane component permeate gas is vacuumized by a vacuum pump to generate a component with the helium content of more than 50 percent and then enters a pressure swing adsorption process for purification, tail gas (the content of helium is about 0.8%) of the first-stage membrane group is used as raw material gas of the second-stage membrane group separator and is sent to the second-stage membrane group separator, the tail gas of the second-stage membrane group separator is lean helium and is directly exhausted, and permeation gas with the content of helium of more than 50% is used as the raw material gas and enters a Vacuum Pressure Swing Adsorption (VPSA) process. The gas is lifted to the operating pressure of 0.8-1.0MPa by a piston compressor and then enters a VPSA adsorption tower for purification, product gas (the content of helium is more than 99 percent) is stored in steel cylinders in a product gas collection grid group by a high-pressure compressor, VPSA is vacuum pressure swing adsorption, the partial pressure of the adsorbed components is reduced by a vacuumizing method, the adsorbed components are desorbed under negative pressure, the gas with the content of helium more than ten percent generated by a two-section membrane group separator can return to a buffer tank for circulation by respectively connecting the output ends of the two-section membrane group separator and the VPSA with the input end of the buffer tank, about one percent of the content of helium of desorption gas generated by the VPSA also returns to the buffer tank to be mixed with second well head gas and second-section membrane group permeation gas, is used as about three percent of helium content, and enters the process again for separation, the separator is cut off or separated by a valve, so that each unit can independently operate conveniently at the later stage, the first-stage membrane component separator and the second-stage membrane component separator are respectively connected with a vacuum pump, so that the pressure difference between two sides of the hollow fiber separation unit can be increased by the permeation gas of the first-stage membrane component separator and the permeation gas of the second-stage membrane component separator, the separation effect of the membrane separators can be increased, by connecting the output end of the high-pressure diaphragm compressor I with the permeation gas collection grid group at the output end of the hollow fiber separation unit, connecting the output end of the permeation gas collection grid group with the piston compressor, this allows fifty percent of the helium content gas produced by the hollow fiber separation unit to be stored in cylinders within the permeate gas collection cell, when the purification device is used, gas is pumped into the VPSA by the piston compressor for purification.
Example two
The auxiliary assembly 1 is added on the basis of the first embodiment.
The air cooler comprises an auxiliary assembly 1, the auxiliary assembly 1 comprises an air cooler 11, a controller 12 is arranged at the top of the front face of the air cooler 11, the front face of the air cooler 11 is symmetrically provided with fixing blocks 13, one sides of opposite faces of the two fixing blocks 13 are symmetrically provided with first slide ways 131, the inner sides of the first slide ways 131 are connected with a dust screen 14 in a sliding manner, the other sides of the opposite faces of the inner sides of the two fixing blocks 13 are symmetrically provided with second slide ways 132, the inner sides of the second slide ways 132 are connected with a sliding plate 15 in a sliding manner, the back of the sliding plate 15 is provided with a soft brush 16, the top of the front of the two fixed blocks 13 is provided with a fixed plate 17, the top of the fixed plate 17 is provided with a movable rod 171, one end of the movable rod 171 penetrates through the top of the fixed plate 17 and is connected with the front surface of the sliding plate 15, and the movable rod 171 is connected with the sliding plate 15 through a bolt.
Referring to fig. 1 to 3, two fixed blocks 13 are arranged on the front surface of the air cooler 11, a first slideway 131 is symmetrically arranged on one side of the opposite surface of the fixed block 13, a dust screen 14 is arranged on the inner side of the first slideway 131, so that the dust screen 14 can be conveniently detached in the later period, and the influence on the heat dissipation system of the air cooler 11 caused by the damage of the dust screen 14 in the later period is avoided, a second slideway 132 is arranged on the other side of the opposite surface of the fixed block 13, a sliding plate 15 is arranged on the inner side of the second slideway 132, a soft brush 16 is arranged on the back surface of the sliding plate 15, so that the dust on the surface of the dust screen 14 can be cleaned by moving the sliding plate 15, a fixed plate 17 is arranged on the front surface of the fixed block 13, a movable rod 171 is arranged on the top of the fixed plate 17 and penetrates through the fixed plate 17 and is connected with the sliding plate 15, so that the surface of the dust screen 14 can be cleaned by pulling the movable rod 171, by bolting the movable rod 171 to the slide plate 15, it is possible to facilitate the replacement of the soft brush 16 at a later stage.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (8)
1. A helium extraction system for geothermal well associated gas, characterized by: the device comprises a buffer tank, the output of geothermal well is provided with the buffer tank, the output of buffer tank is connected with low pressure diaphragm compressor, low pressure diaphragm compressor's output is connected with the digester, the output of digester is connected with cold machine of doing, the output of cold machine of doing is connected with one section membrane group separator, the output of one section membrane group separator is connected with two-stage process membrane group separator and hollow fiber separation unit, the output of two-stage process membrane group separator is connected with tail gas treatment mechanism, hollow fiber separation unit's output is connected with piston compressor, piston compressor's output list is connected with VPSA, VPSA's output is connected with high-pressure diaphragm compressor two, the output list of high-pressure diaphragm compressor two is connected with product gas collection check group.
2. A helium extraction system for geothermal well associated gas according to claim 1, wherein: the output ends of the two-section membrane group separator and the VPSA are respectively connected with the input end of the buffer tank.
3. A helium extraction system for geothermal well associated gas according to claim 2, wherein: each separator is shut off or connected by a valve.
4. A helium extraction system for geothermal well associated gas according to claim 3, wherein: the first-stage membrane group separator and the second-stage membrane group separator are respectively connected with a vacuum pump.
5. A helium extraction system for geothermal well associated gas according to claim 4, wherein: the output end of the hollow fiber separation unit is connected with a first high-pressure diaphragm compressor, the output end of the first high-pressure diaphragm compressor is connected with a permeation gas collection grid group, and the output end of the permeation gas collection grid group is connected with a piston compressor.
6. A helium extraction system for geothermal well associated gas according to claim 1, wherein: the air-cooler includes auxiliary assembly (1), auxiliary assembly (1) includes air-cooler (11), the front top of air-cooler (11) is provided with controller (12), the front symmetry of air-cooler (11) is provided with fixed block (13), two slide one (131), two have been seted up to the opposite face one side symmetry of fixed block (13) the inboard sliding connection of slide one (131) has dust screen (14).
7. A helium extraction system for geothermal well associated gas according to claim 6, wherein: two slide two (132), two have been seted up to the inboard opposite face opposite side symmetry of fixed block (13) the inboard sliding connection of slide two (132) has slide (15), the back of slide (15) is provided with soft brush (16), two the front top of fixed block (13) is provided with fixed plate (17), the top of fixed plate (17) is provided with movable rod (171), the one end of movable rod (171) is run through the top of fixed plate (17) and with the front of slide (15) is connected.
8. A helium extraction system for geothermal well associated gas according to claim 7, wherein: the movable rod (171) is connected with the sliding plate (15) through a bolt.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123250133.9U CN216472258U (en) | 2021-12-22 | 2021-12-22 | Helium extraction system for geothermal well associated gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123250133.9U CN216472258U (en) | 2021-12-22 | 2021-12-22 | Helium extraction system for geothermal well associated gas |
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| CN216472258U true CN216472258U (en) | 2022-05-10 |
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| CN202123250133.9U Expired - Fee Related CN216472258U (en) | 2021-12-22 | 2021-12-22 | Helium extraction system for geothermal well associated gas |
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