CN113735079B - Method and production device for extracting ultra-high purity helium at normal temperature - Google Patents
Method and production device for extracting ultra-high purity helium at normal temperature Download PDFInfo
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- CN113735079B CN113735079B CN202011626608.7A CN202011626608A CN113735079B CN 113735079 B CN113735079 B CN 113735079B CN 202011626608 A CN202011626608 A CN 202011626608A CN 113735079 B CN113735079 B CN 113735079B
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- 239000001307 helium Substances 0.000 title claims abstract description 83
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 83
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 83
- 238000000034 method Methods 0.000 title claims abstract description 56
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 239000007789 gas Substances 0.000 claims abstract description 114
- 238000001179 sorption measurement Methods 0.000 claims abstract description 72
- 238000000926 separation method Methods 0.000 claims abstract description 71
- 239000012528 membrane Substances 0.000 claims abstract description 70
- 238000005262 decarbonization Methods 0.000 claims abstract description 28
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 28
- 230000023556 desulfurization Effects 0.000 claims abstract description 28
- 238000005516 engineering process Methods 0.000 claims abstract description 22
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 19
- 230000003197 catalytic effect Effects 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- 239000001257 hydrogen Substances 0.000 claims description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims description 14
- 238000003795 desorption Methods 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 7
- 150000002371 helium Chemical class 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims 2
- 230000005494 condensation Effects 0.000 claims 2
- 238000010438 heat treatment Methods 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 239000003345 natural gas Substances 0.000 description 9
- 238000006356 dehydrogenation reaction Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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- C01B23/001—Purification or separation processes of noble gases
- C01B23/0094—Combined chemical and physical processing
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- 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
- B01D53/04—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 with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- 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
- B01D53/225—Multiple stage diffusion
- B01D53/226—Multiple stage diffusion in serial connexion
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- 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
- B01D53/228—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 characterised by specific membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- 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
- B01D53/26—Drying gases or vapours
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/869—Multiple step processes
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- C01B2210/0043—Impurity removed
- C01B2210/0068—Organic compounds
- C01B2210/007—Hydrocarbons
Abstract
A method and a production device for extracting ultra-high purity helium at normal temperature belong to the technical field of petrochemical industry. According to the invention, membrane separation, pressure swing adsorption, low-temperature catalysis and desulfurization and decarbonization technologies are integrated, and when helium in raw material gas is purified, the raw material gas sequentially passes through a plurality of technology cluster systems such as desulfurization and decarbonization, membrane separation, pressure swing adsorption, low-temperature catalysis and the like according to the composition of the raw material gas, so that the helium product with the volume fraction of not less than 99.9999% is obtained. The process successfully breaks the development bottleneck of a single separation technology through mutual cooperation among multiple technologies, greatly improves the yield of helium product, reduces the investment and energy consumption in the helium production process, prolongs the service life of a separation system, and widens the available helium resource.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry. According to the invention, membrane separation, pressure swing adsorption, low-temperature catalysis and desulfurization and decarbonization technologies are integrated, and when helium in raw material gas is purified, the raw material gas sequentially passes through a plurality of technical cluster systems such as desulfurization and decarbonization, membrane separation, pressure swing adsorption, low-temperature catalysis and the like according to the composition of the raw material gas, so that qualified product helium is obtained. Besides helium and natural gas, the invention can also produce byproducts such as carbon dioxide, nitrogen and the like with higher purity according to the condition of raw materials.
Background
Helium has been derived mainly from helium-containing natural gas, and thus natural gas helium stripping technology has become the main research direction in the field of helium stripping.
The related patents related to helium recovery or helium production, which are referred to at present, mainly comprise two types, namely process tail gas purification and separation; the other type is natural gas or air separation tail gas helium extraction, in the patents, the majority is deep cooling or the combination of deep cooling and other technologies, the method can obtain a helium product with high purity, but the production energy consumption is higher, and the economy of the method can not meet the requirements under the working condition of not producing LNG as a byproduct; some are simple membrane methods or pressure/temperature swing adsorption technologies, and the method can obtain helium products with certain purity, but has a narrow application range, cannot obtain helium products with high purity and has low helium product yield; the method has the advantages that the method is simple in structure, low in cost and convenient to operate, and the method is simple in operation, and the method is convenient to use, and the method is simple in operation, and the method is easy to operate, and the method is suitable for the production of the hydrogen-containing helium.
Disclosure of Invention
Aiming at the above situation, the invention adopts a secondary low-temperature catalysis technology to ensure the hydrogen removal effect, adopts constant-temperature dehydrogenation, and eliminates the influence of exothermic reaction in the dehydrogenation link; the invention also innovatively introduces a double-reflux pressure swing adsorption technology, and obviously reduces equipment investment and operation consumption under the condition of fully ensuring that the purity of helium can reach ultra-pure helium. Compared with the currently granted or published patent at home and abroad, the method has obvious innovation.
The double-reflux pressure swing adsorption technology is characterized in that three adsorption towers which are connected in parallel form are utilized to form a separation unit, the top and the bottom of the separation unit are respectively provided with a buffer tank, a compressor is connected between the buffer tank at the bottom and the bottoms of the three adsorption towers, the feeding position is arranged at the bottom of the adsorption towers, the difficult-to-adsorb gas is discharged to the light component buffer tank at the top of the separation unit, and the reflux operation of the light component flow in the three adsorption towers is realized through a control valve on a connecting pipe; the impurity gas is discharged to a heavy component buffer tank at the bottom of the separation unit, and the reflux operation of the heavy component flow in the three adsorption towers is realized through a compressor connected with the buffer tank and a control valve on a connecting pipeline. The gas realizes the high-precision separation of the light and heavy components in the raw material gas through repeated reflux between the top and the bottom of the adsorption tower which are connected in parallel in form.
The low-temperature catalytic technology is a technology which can still normally react when the temperature of oxidative dehydrogenation reaction is reduced to be lower than the reaction temperature in the absence of a catalyst by using palladium as a catalyst. In order to ensure the safety of the reaction device, a heat transfer device is additionally arranged in the reactor, and the reaction heat is timely transferred out through the heat transfer device additionally arranged in the reactor during reaction, so that the temperature of the system is always kept at a constant temperature.
A method for extracting ultra-high purity helium at normal temperature is a multi-technology cluster method, wherein the cluster technology comprises desulfurization and decarbonization, gas membrane separation, pressure swing adsorption and low-temperature catalysis technologies, and helium-containing raw gas enters a primary membrane separation process after desulfurization and decarbonization treatment; the helium-rich gas after membrane separation enters a low-temperature catalytic process for one time, and hydrogen components in the helium-rich gas are removed; the dehydrogenated helium-rich gas enters a secondary gas membrane separation process, and the helium-rich gas with higher helium concentration obtained after treatment is sent into a primary pressure swing adsorption process; obtaining relatively pure helium gas, and performing a secondary low-temperature catalysis process to remove trace hydrogen in the helium gas; the dehydrogenated helium enters a secondary pressure swing adsorption process; and sending qualified ultra-pure helium obtained after treatment out of the boundary.
The helium-lean tail gas of the secondary membrane separation returns to the primary membrane separation process inlet, the desorption gas of the primary pressure swing adsorption process returns to the secondary gas membrane separation inlet, the desorption gas of the secondary pressure swing adsorption process returns to the primary pressure swing adsorption process or the secondary gas membrane separation inlet, and the secondary pressure swing adsorption adopts double-reflux pressure swing adsorption.
The carbon dioxide volume content in the feed gas entering the primary or secondary membrane separation system is not higher than 20%, preferably not higher than 0.4%; the hydrogen volume content in the feed gas to the secondary pressure swing adsorption system is not higher than 0.08ppm, preferably not higher than 0.01ppm, and the helium volume content is not lower than 90%, preferably not lower than 99%, and most preferably not lower than 99.9%.
Pressurizing gas before the desulfurization and decarbonization process, and dehydrating gas after the desulfurization and decarbonization process; pressurizing gas before the low-temperature catalytic process, and dehydrating gas after the low-temperature catalytic process; carrying out gas pressurization and pretreatment before the gas membrane separation process; the pressure swing adsorption process is preceded by gas pressurization and pretreatment.
In order to achieve the above purpose, the invention provides a production device for extracting ultra-high purity helium at normal temperature, which comprises a desulfurization and decarbonization system, a low-temperature catalysis system, a gas membrane separation system and a pressure swing adsorption system; the system comprises a primary membrane separation system, a secondary membrane separation system, a primary pressure swing adsorption system, a secondary pressure swing adsorption system, a primary membrane separation system, a secondary low-temperature catalytic system, a secondary pressure swing adsorption system and a secondary pressure swing adsorption system, wherein a purified gas outlet pipeline of the desulfurization and decarbonization system is connected with an inlet pipeline of the primary membrane separation system, a helium-rich gas outlet pipeline of the primary membrane separation system is connected with an inlet pipeline of the primary low-temperature catalytic system, a dry dehydrogenization outlet pipeline of the primary catalytic system is connected with an inlet pipeline of the secondary pressure swing adsorption system. The raw material gas firstly enters a desulfurization and decarbonization system;
the desulfurization and decarbonization system comprises a compressor, a cooler, a desulfurization and decarbonization tower, a regeneration tower and a dehydration tower, wherein the equipment which are sequentially connected is the compressor, the cooler, the desulfurization and decarbonization tower and the dehydration tower, a rich liquid outlet pipeline of the desulfurization and decarbonization tower is connected with an inlet pipeline of the regeneration tower, and a lean liquid outlet pipeline of the regeneration tower is connected with a lean liquid inlet pipeline of the desulfurization and decarbonization tower; the low-temperature catalytic system comprises a compressor, a cooler, a low-temperature catalytic tower and a drying tower, and the equipment sequentially connected is the compressor, the cooler, the low-temperature catalytic tower and the drying tower; the gas membrane separation system comprises a compressor, a condenser, a gas-liquid separator, a heater and a membrane component, and the equipment which is connected in sequence comprises the compressor, the condenser, the gas-liquid separator, the heater and the membrane component; the pressure swing adsorption system comprises a compressor, a condenser, a gas-liquid separator and a pressure swing adsorption tower group, and the equipment which is connected in sequence comprises the compressor, the condenser, the gas-liquid separator and the pressure swing adsorption tower group; the lean helium gas outlet pipeline of the gas membrane separation system is directly out of the boundary, the desorption gas outlet pipeline of the primary pressure swing adsorption system is connected with the compressor inlet pipeline of the gas membrane separation system, and the desorption gas outlet pipeline of the secondary pressure swing adsorption system is connected with the compressor inlet pipeline of the primary pressure swing adsorption system.
Drawings
The invention is further described below with reference to the drawings and the detailed description.
FIG. 1 is a flow chart of the present invention and is a schematic process flow diagram of example 1. FIG. 2 is a flow chart of the process of the invention for the extraction of helium from non-hydrogen containing natural gas and is a schematic process flow diagram of example 2. FIG. 3 is a flow chart of the process of the invention for the extraction of helium from non-sulfur containing carbon containing natural gas and is a schematic process flow diagram of example 3.
Detailed Description
Example 1
For an understanding of this embodiment, refer to fig. 1. The figure shows the main equipment and the mutual connection relation of the main equipment.
The helium-containing raw gas I enters a primary membrane separation system after desulfurization and decarbonization treatment. The membrane module operating pressure was 2.90MPag and operating temperature was 60 ℃. After the treatment by the gas separation membrane, the helium-removed tail gas is sent out of the boundary, and the concentrated hydrogen-containing raw gas is sent into a primary low-temperature catalytic system. The dehydrogenation feed gas after dehydrogenation treatment by the primary low-temperature catalytic system is sent to a secondary membrane separation system. The membrane module operating pressure was 2.90MPag and operating temperature was 60 ℃. After being treated by the gas separation membrane, the helium-removed tail gas returns to the inlet of the primary membrane separation system, and the raw gas with high helium content is sent to the primary pressure swing adsorption system, and the pressure swing adsorption tower has the operating pressure of 2.9MPag and the operating temperature of 30 ℃. After primary pressure swing adsorption treatment, the desorption gas of the primary pressure swing adsorption system returns to the inlet of the secondary membrane separation system, the concentration of the extracted helium reaches 99.9%, and the helium is sent to the secondary low-temperature catalytic system for continuous dehydrogenation. The dehydrogenated helium enters a secondary pressure swing adsorption system, the operating pressure of the secondary pressure swing adsorption system is 1.0MPag, and the operating temperature is 30 ℃. The helium concentration of the product after secondary purification reaches more than 99.9999mol percent, and is sent out of the boundary, and the desorption gas returns to the inlet of the primary pressure swing adsorption system.
The specific process flow parameters for this example are shown in table 1.
TABLE 1 data sheet for purifying and recovering hydrogen-containing and carbon-containing natural gas helium
In this embodiment, the total recovery of cluster technology helium was 92.7%.
Example two
For an understanding of this embodiment, refer to fig. 2. The figure shows the main equipment and the mutual connection relation of the main equipment.
Helium-containing feed gas II enters a membrane separation system. The membrane module operating pressure was 6.90MPag and the operating temperature was 70 ℃. After the gas separation membrane treatment, the helium-removed tail gas is sent out of the boundary, and the raw gas with high helium content is sent into a primary pressure swing adsorption system, and the pressure swing adsorption tower has the operating pressure of 2.9MPag and the operating temperature of 30 ℃. After primary pressure swing adsorption treatment, the desorption gas of the primary pressure swing adsorption system returns to the inlet of the membrane separation system, the concentration of the proposed helium gas reaches 99.9%, and the helium gas enters the secondary pressure swing adsorption system, wherein the operation pressure of the secondary pressure swing adsorption system is 0.9MPag, and the operation temperature is 30 ℃. The helium gas secondary concentration of the product after secondary purification reaches more than 99.9999mol percent, and is sent out of the boundary, and the desorption gas returns to the inlet of the primary pressure swing adsorption system.
The specific parameters of this example are shown in Table 2.
TABLE 2 helium purification recovery data table for helium-containing natural gas
In this embodiment, the total recovery of cluster technology helium is 96.88%.
Example III
For an understanding of this embodiment, refer to fig. 3. The figure shows the main equipment and the mutual connection relation of the main equipment.
Helium-containing feed gas III enters a primary membrane separation system. The membrane module operating pressure was 2.90MPag and the operating temperature was 70 ℃. After the treatment by the gas separation membrane, the helium-removed tail gas is sent out of the boundary, and the concentrated hydrogen-containing raw gas is sent into a primary low-temperature catalytic system. The dehydrogenation feed gas after dehydrogenation treatment by the primary low-temperature catalytic system is sent to a secondary membrane separation system. The membrane module operating pressure was 2.90MPag and the operating temperature was 70 ℃. After the gas separation membrane treatment, the helium-removed tail gas returns to the inlet of the primary membrane separation system, and the raw gas with high helium content is sent into the secondary low-temperature catalytic system for continuous dehydrogenation. The dehydrogenated helium enters a pressure swing adsorption system, the operating pressure of the pressure swing adsorption system is 1.9MPag, and the operating temperature is 30 ℃. The three concentration of the purified helium gas reaches more than 99.9999mol percent, and the helium gas is sent out of the boundary, and the desorption gas returns to the inlet of the secondary membrane separation system.
The specific parameters of this example are shown in Table 2.
TABLE 2 helium purification recovery data table for helium-containing natural gas
In this embodiment, the total recovery of cluster technology helium was 97.38%.
Claims (7)
1. A method for extracting ultra-high purity helium at normal temperature is characterized by comprising the following steps: comprises desulfurization and decarbonization, gas membrane separation, pressure swing adsorption and low-temperature catalysis technology, wherein helium-containing raw gas firstly enters a primary membrane separation process after desulfurization and decarbonization treatment; the helium-rich gas after membrane separation enters a low-temperature catalytic process for one time, and hydrogen components in the helium-rich gas are removed; the dehydrogenated helium-rich gas enters a secondary membrane separation process, and the helium-rich gas with higher helium concentration obtained after treatment is sent into a primary pressure swing adsorption process; obtaining relatively pure helium gas, and performing a secondary low-temperature catalysis process to remove trace hydrogen in the helium gas; the dehydrogenated helium enters a secondary pressure swing adsorption process; sending qualified ultra-pure helium obtained after treatment out of the boundary, wherein the primary low-temperature catalysis process and the secondary low-temperature catalysis process are kept at constant temperature;
the low-temperature catalysis technology is a technology which can still normally react when the temperature of oxidative dehydrogenation reaction is reduced to be lower than the reaction temperature in the absence of a catalyst by using palladium as a catalyst; in order to ensure the safety of the reaction device, a heat transfer device is additionally arranged in the reactor, and the reaction heat is timely transferred out through the heat transfer device additionally arranged in the reactor during reaction, so that the temperature of the system is always kept at a constant temperature; the helium concentration of the product after secondary purification reaches more than 99.9999mol percent;
the helium-lean tail gas of the secondary membrane separation returns to the primary membrane separation inlet, the desorption gas of the primary pressure swing adsorption process returns to the secondary membrane separation inlet, the desorption gas of the secondary pressure swing adsorption process returns to the primary pressure swing adsorption process or the secondary membrane separation inlet, and the secondary pressure swing adsorption adopts double-reflux pressure swing adsorption.
2. A method for extracting ultra-high purity helium gas at normal temperature according to claim 1, wherein: the volume content of carbon dioxide in the feed gas entering the primary or secondary membrane separation system is not higher than 20%, the volume content of hydrogen in the feed gas entering the secondary pressure swing adsorption system is not higher than 0.08ppm, and the volume content of helium is not lower than 90%.
3. A method of extracting ultra-high purity helium gas at ambient temperature according to claim 2, wherein: the volume content of carbon dioxide in the feed gas entering the primary or secondary membrane separation system is not higher than 0.4%; the volume content of hydrogen in the feed gas entering the secondary pressure swing adsorption system is not higher than 0.01ppm, and the volume content of helium is not lower than 99%.
4. A method of extracting ultra-high purity helium gas at ambient temperature according to claim 3, wherein: the volume content of carbon dioxide in the feed gas entering the primary or secondary membrane separation system is not higher than 0.4%; the volume content of hydrogen in the feed gas entering the secondary pressure swing adsorption system is not higher than 0.01ppm, and the volume content of helium is not lower than 99.9%.
5. A method for extracting ultra-high purity helium gas at normal temperature according to claim 1, wherein: pressurizing gas before the desulfurization and decarbonization process, and dehydrating gas after the desulfurization and decarbonization process; pressurizing gas before the low-temperature catalytic process, and dehydrating gas after the low-temperature catalytic process; the gas membrane separation process is preceded by gas pressurization, condensation, gas-liquid separation and heating; the pressure swing adsorption process is preceded by gas pressurization, condensation, and gas-liquid separation.
6. An apparatus for use in the production method for extracting ultra-high purity helium gas at normal temperature according to claim 1, wherein: the device comprises a desulfurization and decarbonization system, a low-temperature catalysis system, a gas membrane separation system and a pressure swing adsorption system; the system comprises a primary membrane separation system, a secondary membrane separation system, a primary pressure swing adsorption system, a secondary low-temperature catalysis system, a secondary pressure swing adsorption system, a secondary low-temperature catalysis system and a low-temperature catalysis system, wherein a purified gas outlet pipeline of the desulfurization and decarbonization system is connected with an inlet pipeline of the primary membrane separation system, a helium-rich gas outlet pipeline of the primary membrane separation system is connected with an inlet pipeline of the primary membrane separation system, a dry dehydrogenization outlet pipeline of the primary membrane separation system is connected with an inlet pipeline of the primary low-temperature catalysis system, and the low-temperature catalysis is kept at a constant temperature.
7. A production apparatus for extracting ultra-high purity helium gas at normal temperature according to claim 6, wherein: the desulfurization and decarbonization system comprises a compressor, a cooler, a desulfurization and decarbonization tower, a regeneration tower and a dehydration tower, wherein the equipment which are sequentially connected is the compressor, the cooler, the desulfurization and decarbonization tower and the dehydration tower, a rich liquid outlet pipeline of the desulfurization and decarbonization tower is connected with an inlet pipeline of the regeneration tower, and a lean liquid outlet pipeline of the regeneration tower is connected with a lean liquid inlet pipeline of the desulfurization and decarbonization tower; the low-temperature catalytic system comprises a compressor, a cooler, a low-temperature catalytic tower and a drying tower, and the equipment sequentially connected is the compressor, the cooler, the low-temperature catalytic tower and the drying tower; the gas membrane separation system comprises a compressor, a condenser, a gas-liquid separator, a heater and a membrane component, and the equipment which is connected in sequence comprises the compressor, the condenser, the gas-liquid separator, the heater and the membrane component; the pressure swing adsorption system comprises a compressor, a condenser, a gas-liquid separator and a pressure swing adsorption tower group, and the equipment which is connected in sequence comprises the compressor, the condenser, the gas-liquid separator and the pressure swing adsorption tower group; the low-temperature catalytic tower is characterized in that a lean helium gas outlet pipeline of the gas membrane separation system is directly out of the boundary, a desorption gas outlet pipeline of the primary pressure swing adsorption system is connected with a compressor inlet pipeline of the gas membrane separation system, a desorption gas outlet pipeline of the secondary pressure swing adsorption system is connected with a compressor inlet pipeline of the primary pressure swing adsorption system, and a heat transfer device is additionally arranged in the low-temperature catalytic tower.
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