CN220999250U - System for extracting helium - Google Patents
System for extracting helium Download PDFInfo
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- CN220999250U CN220999250U CN202322922513.5U CN202322922513U CN220999250U CN 220999250 U CN220999250 U CN 220999250U CN 202322922513 U CN202322922513 U CN 202322922513U CN 220999250 U CN220999250 U CN 220999250U
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- 239000001307 helium Substances 0.000 title claims abstract description 101
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 101
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 238000001179 sorption measurement Methods 0.000 claims abstract description 348
- 239000007789 gas Substances 0.000 claims abstract description 205
- 239000012528 membrane Substances 0.000 claims abstract description 90
- 239000012535 impurity Substances 0.000 claims abstract description 60
- 238000000926 separation method Methods 0.000 claims abstract description 39
- 238000000034 method Methods 0.000 claims abstract description 24
- 230000008569 process Effects 0.000 claims abstract description 17
- 238000012545 processing Methods 0.000 claims abstract description 11
- 239000001257 hydrogen Substances 0.000 claims description 35
- 229910052739 hydrogen Inorganic materials 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 19
- 150000002431 hydrogen Chemical class 0.000 claims description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 18
- 239000000956 alloy Substances 0.000 claims description 6
- 229910045601 alloy Inorganic materials 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000012621 metal-organic framework Substances 0.000 claims description 5
- 238000002203 pretreatment Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 230000008859 change Effects 0.000 abstract description 3
- 229920006395 saturated elastomer Polymers 0.000 description 12
- 238000007599 discharging Methods 0.000 description 11
- 239000003463 adsorbent Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 7
- 238000004140 cleaning Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000007781 pre-processing Methods 0.000 description 3
- 239000004693 Polybenzimidazole Substances 0.000 description 2
- 239000004642 Polyimide Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229920002480 polybenzimidazole Polymers 0.000 description 2
- 229920001721 polyimide Polymers 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000013110 organic ligand Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000013154 zeolitic imidazolate framework-8 Substances 0.000 description 1
- MFLKDEMTKSVIBK-UHFFFAOYSA-N zinc;2-methylimidazol-3-ide Chemical compound [Zn+2].CC1=NC=C[N-]1.CC1=NC=C[N-]1 MFLKDEMTKSVIBK-UHFFFAOYSA-N 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The embodiment of the application discloses a system for extracting helium, which comprises a pretreatment module, a control module and a control module, wherein the pretreatment module is used for receiving external mixed gas to be treated and carrying out pretreatment on the mixed gas to be treated; the membrane separation module is used for receiving the mixed gas pretreated by the pretreatment module and removing part of gas impurities in the mixed gas; at least one set of adsorption modules; the adsorption module comprises a first adsorption column and a second adsorption column which are arranged in parallel; the first adsorption column and the second adsorption column are configured to alternately receive the mixed gas output by the previous processing module and adsorb the remaining gas impurities in the received mixed gas. According to the system provided by the application, the pretreatment module, the membrane separation module and the adsorption module are used for separating, adsorbing and the like the mixed gas to be treated received from the outside, so that the high-purity helium is finally generated, no phase change exists in the whole process, the energy consumption is low, the efficiency is high, other gas impurities are not introduced, the purity of the generated helium can reach more than 5N, and the system is safe and reliable.
Description
Technical Field
The present application relates to the field of gas purification technology, and more particularly, to a system for extracting helium.
Background
Helium is colorless and odorless rare gas at normal temperature, has stable chemical property, has the characteristics of extremely low boiling point, extremely small molecular size, extremely low solubility in water, extremely high ionization energy, high specific heat, high thermal conductivity and the like, and is widely applied to the fields of high-tech product manufacture, aerospace, national defense, military industry, medical treatment and the like. Helium is rare on the earth, is widely distributed but is extremely uneven, and is a very lean country in China, helium resources are distributed and dispersed, the grade is low, helium content in natural gas is low, more than 95% of helium needs to be imported, the external dependence is extremely high, and the exploration of low-cost helium extracting technology facing low concentration is very important.
The existing helium extraction technology mainly comprises four methods of cryogenic method, adsorption separation, membrane separation and integrated helium extraction. Cryogenic processes are the most mainstream, but have the problems of high energy consumption and poor economy when the helium content is low. In addition, because the molecular size of hydrogen is similar to that of helium, the impurities are often difficult to remove by a membrane separation and physical adsorption method, and more methods are adopted at present, namely a catalytic dehydrogenation device is adopted, but oxygen impurities are introduced, and the safety problem of explosion can be possibly caused in subsequent treatment due to the existence of oxygen.
Disclosure of utility model
The object of the present utility model is to provide a system for extracting helium to solve at least one of the above technical problems.
In order to achieve at least one of the above objects, the present application adopts the following technical scheme:
The application provides a system for extracting helium gas, comprising a plurality of processing modules;
The plurality of processing modules comprises
The pretreatment module is used for receiving external mixed gas to be treated and carrying out pretreatment on the mixed gas to be treated;
The membrane separation module is used for receiving the mixed gas pretreated by the pretreatment module and removing part of gas impurities in the mixed gas;
At least one set of adsorption modules;
The adsorption module comprises
The first adsorption column and the second adsorption column are arranged in parallel;
the first adsorption column and the second adsorption column are configured to alternately receive the mixed gas output by the previous processing module and adsorb the remaining gas impurities in the received mixed gas.
Optionally, the adsorption modules are provided with two groups which are arranged in series, namely a first adsorption module and a second adsorption module;
The first adsorption column and the second adsorption column in the first adsorption module are respectively communicated with the membrane separation module and are used for alternately receiving the mixed gas output by the membrane separation module to generate hydrogen helium mixed gas;
The first adsorption column and the second adsorption column in the second adsorption module are respectively communicated with the first adsorption module and are used for alternately receiving the hydrogen helium mixed gas and adsorbing hydrogen in the hydrogen helium mixed gas to generate high-purity helium.
Optionally, the first adsorption column and the second adsorption column in the first adsorption module are MOFs adsorption columns;
the first adsorption column and the second adsorption column in the second adsorption module are hydrogen storage alloy adsorption columns.
Optionally, the adsorption module further comprises: a first gas-filling pipeline and a second gas-filling pipeline which are respectively communicated with one end of the first adsorption column and one end of the second adsorption column, wherein the first gas-filling pipeline is used for conveying high-purity helium to the first adsorption column, and the second gas-filling pipeline is used for conveying high-purity helium to the second adsorption column;
a first air outlet pipeline and a second air outlet pipeline which are respectively communicated with the other end of the first adsorption column and the other end of the second adsorption column;
when the first charging pipeline conveys high-purity helium to the first adsorption column, the gas impurities absorbed in the first adsorption column are output to the outside through the first air outlet pipeline;
when the second charging pipeline conveys the high-purity helium to the second adsorption column, the gas impurities absorbed in the second adsorption column are output to the outside through the second air outlet pipeline.
Optionally, two ends of the first adsorption column are respectively provided with a first switch, and two ends of the second adsorption column are respectively provided with a second switch;
The first charging line includes a first outlet located between and in communication with one of the two first switches and a first adsorption column;
the second charging pipeline comprises a second outlet, and the second outlet is positioned between one of the two second switches and a second adsorption column and is communicated with the second adsorption column;
The first air outlet pipeline comprises a first inlet which is positioned between the other first switch of the two switches and a first adsorption column and is communicated with the first adsorption column;
The second outlet pipe comprises a second inlet which is positioned between the other second switch of the two and the second adsorption column and is communicated with the second adsorption column.
Optionally, a third switch is respectively arranged on the first air charging pipeline and the first air outlet pipeline, and a fourth switch is respectively arranged on the second air charging pipeline and the second air outlet pipeline;
When the first adsorption column is in an adsorption state, the first switch and the fourth switch are in an open state, and the second switch and the third switch are in a closed state;
When the second adsorption column is in an adsorption state, the first switch and the fourth switch are in a closed state, and the second switch and the third switch are in an open state.
Optionally, the membrane separation module comprises
At least one primary membrane separator which is communicated with the pretreatment module and is used for receiving the mixed gas pretreated by the pretreatment module;
the second-stage membrane separator is communicated with the first-stage membrane separator through a compressor and is used for receiving the mixed gas output by the first-stage membrane separator;
The adsorption module is communicated with the secondary membrane separator and receives the mixed gas output by the secondary membrane separator.
Optionally, the tail gas output by the secondary membrane separator is input into the primary membrane separator again through a circulating pipeline.
Optionally, a preheater is disposed between the pretreatment module and the membrane separation module.
Optionally, the side walls of the first adsorption column and the second adsorption column are respectively provided with a heating belt.
The beneficial effects of the application are as follows:
Aiming at the problems in the prior art, the application provides a system for extracting helium, and the arrangement of a plurality of processing modules can sequentially purify mixed gas to be processed received by the system from the outside, so that high-purity helium is finally generated. Specifically, the mixed gas to be treated received from the outside can be subjected to acid removal, desulfurization, mercury removal, defogging and drying through the pretreatment module, the generated mixed gas is transmitted to the membrane separation module, the membrane separation module can remove most of gas impurities in the mixed gas output from the pretreatment module, such as CO 2、CH4 and N 2 in the mixed gas, after the most of gas impurities are removed through the membrane separation module, the volume fraction of helium in the mixed gas output from the membrane separation module can reach 85% -90%, and then the mixed gas is adsorbed by the first adsorption column and the second adsorption column in the adsorption module to finally form high-purity helium. The alternating use of first adsorption column and second adsorption column can make the adsorption module be in operating condition all the time, and work efficiency is high, when can not appear only an adsorption column, when the gas impurity of this adsorption column absorption reaches the condition that the saturation state needs the adsorption module to stop working to clear up it. In the use process of the adsorption module, when the gas impurities adsorbed by the first adsorption column reach a saturated state, the adsorption module is switched to the second adsorption column to adsorb, the first adsorption column can be cleaned at the moment, and when the gas impurities adsorbed by the second adsorption column reach the saturated state, the adsorption module is switched to the first adsorption column to adsorb, and the second adsorption column can be cleaned at the moment; according to the system provided by the application, the pretreatment module, the membrane separation module and the adsorption module are used for separating, adsorbing and the like the mixed gas to be treated received from the outside, so that the high-purity helium is finally generated, no phase change exists in the whole process, the energy consumption is low, the efficiency is high, other gas impurities are not introduced, the purity of the generated helium can reach more than 5N, and the system is safe and reliable.
Drawings
The following describes the embodiments of the present utility model in further detail with reference to the drawings.
Fig. 1 is a schematic view showing the overall structure of a system for extracting helium in one embodiment of the present application.
Detailed Description
In the following description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of one or more embodiments. It may be evident, however, that such embodiment(s) may be practiced without these specific details.
In the description of the present application, it should be noted that the azimuth or positional relationship indicated by the terms "upper", "lower", etc. are based on the azimuth or positional relationship shown in the drawings, and are merely for convenience of describing the present application and simplifying the description, and are not indicative or implying that the apparatus or element in question must have a specific azimuth, be constructed and operated in a specific azimuth, and thus should not be construed as limiting the present application. Unless specifically stated or limited otherwise, the terms "mounted," "connected," and "coupled" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art according to the specific circumstances.
It is further noted that in the description of the present application, relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises the element.
To solve the problems of the prior art, one embodiment of the present application provides a system for extracting helium gas, as shown in fig. 1, comprising a plurality of process modules; the plurality of processing modules comprise a preprocessing module 1, wherein the preprocessing module 1 can be a filter and is used for receiving external mixed gas to be processed and preprocessing the mixed gas to be processed; in the application, the mixed gas to be treated is exemplified by natural gas; the membrane separation module is used for receiving the mixed gas pretreated by the pretreatment module 1 and removing part of gas impurities in the mixed gas; further comprising at least one set of adsorption modules; the adsorption module comprises a first adsorption column 51 and a second adsorption column 52 which are arranged in parallel; the first adsorption column 51 and the second adsorption column 52 are configured to alternately receive the mixed gas outputted from the previous process module and adsorb the remaining gas impurities in the received mixed gas. The former process module herein refers to a process module adjacent to the adsorption module having the first adsorption column 51 and the second adsorption column 52, and the process module can transfer the output mixed gas to the adsorption module adjacent thereto; for example, if there are two adsorption modules, namely a first adsorption module and a second adsorption module, the mixed gas output by the membrane separation module is transmitted to the first adsorption module, and the membrane separation module corresponds to the last processing module of the first adsorption module; the mixed gas output by the first adsorption module is transmitted to the second adsorption module, and the first adsorption module is equivalent to the last processing module of the second adsorption module.
In the above embodiment of the present application, the plurality of processing modules may be configured to sequentially purify the mixed gas to be processed received by the system from the outside, and finally generate high purity helium gas. Specifically, the mixed gas to be treated received from the outside can be subjected to acid removal, desulfurization, mercury removal, defogging and drying through the pretreatment module 1, and the generated mixed gas is transmitted to the membrane separation module, wherein the membrane separation module can remove most of gas impurities, such as CO 2、CH4 and N 2, in the mixed gas output from the pretreatment module 1, after the most of gas impurities are removed through the membrane separation module, the volume fraction of helium in the mixed gas output from the membrane separation module can reach 85% -90%, and then the first adsorption column 51 and the second adsorption column 52 in the adsorption module adsorb other gas impurities in the mixed gas, so that the high-purity helium is finally formed. The alternating use of the first adsorption column 51 and the second adsorption column 52 can enable the adsorption module to be always in a working state, the working efficiency is high, and when only one adsorption column does not appear, when the gas impurities adsorbed by the adsorption column reach a saturation state, the adsorption module is required to stop working to clean the gas impurities. In the use process of the adsorption module, when the gas impurities adsorbed by the first adsorption column 51 reach a saturated state, the adsorption module is switched to the second adsorption column 52 for adsorption, the first adsorption column 51 can be cleaned at the moment, and when the gas impurities adsorbed by the second adsorption column 52 reach the saturated state, the adsorption module is switched to the first adsorption column 51 for adsorption, and the second adsorption column 52 can be cleaned at the moment; according to the system provided by the application, the pretreatment module 1, the membrane separation module and the adsorption module are used for separating, adsorbing and the like the mixed gas to be treated received from the outside, so that the high-purity helium is finally generated, no phase change exists in the whole process, the energy consumption is low, the efficiency is high, other gas impurities are not introduced, and the purity of the generated helium can reach more than 5N, so that the system is safe and reliable.
In one embodiment, the membrane separation module comprises at least one primary membrane separator 21 in communication with the pretreatment module 1 and configured to receive the mixed gas pretreated by the pretreatment module 1; a second-stage membrane separator 22 which is communicated with the first-stage membrane separator 21 through a compressor 7 and is used for receiving the mixed gas output by the first-stage membrane separator 21; the adsorption module is communicated with the secondary membrane separator 22 and receives the mixed gas output by the secondary membrane separator 22. Polyimide (PI), polybenzimidazole (PBI), microporous Polymer (PIMs), carbon molecular sieve membrane (CMS), and the like can be added to the primary membrane separator 21 and the secondary membrane separator 22, and various materials can be combined.
The pretreatment module 1 removes acidity, desulphurizes, demercurations, demists and dries the mixed gas to be treated received from the outside, and then transmits the generated mixed gas to a first-stage membrane separator 21 of the membrane separation module, wherein when the number of the first-stage membrane separators 21 is multiple, the plurality of the first-stage membrane separators 21 are sequentially connected in series, the number of the first-stage membrane separators 21 is preferably three, and the first-stage membrane separators are set according to actual conditions; the first-stage membrane separator 21 separates the received mixed gas from the pretreatment module 1, mainly removes most of the gas impurities, the main components of the gas impurities are CH 4、N2、O2 and other various hydrocarbon gases, and the pressure of the residual mixed gas is greatly reduced after the removal, in order to improve the separation effect, the mixed gas output from the first-stage membrane separator 21 needs to be compressed by the compressor 7 until the pressure is similar to that of the mixed gas received by the first-stage membrane separator 21, the compressed mixed gas is generally compressed to 1.8Mpa to 2.2Mpa, the mixed gas enters the second-stage membrane separator 22 again, the second-stage membrane separator 22 further separates the mixed gas, and then removes part of the gas impurities, the main components of the gas impurities are CO 2, and simultaneously comprise CH 4 and N 2, and the volume fraction of helium in the mixed gas output by the second-stage membrane separator 22 can reach 85% -90%, and the second-stage membrane separator 22 transmits the output mixed gas to the adsorption module.
In practical application, the primary membrane separator 21 and the secondary membrane separator 22 both generate tail gas, and since the content of helium in the tail gas generated by the primary membrane separator 21 is extremely low and negligible, the tail gas can be directly discharged into the collecting device through the exhaust pipe 92, and the tail gas output by the secondary membrane separator 22 is input to the inlet of the primary membrane separator 21 again through the circulating pipeline 91, so that the tail gas is continuously separated, and the recovery rate of helium is improved. It should be noted that, if the pressure of the tail gas output by the second-stage membrane separator 22 is similar to the pressure of the mixed gas received by the first-stage membrane separator 21, the tail gas does not need to be compressed by the compressor 7, and if the pressure is small enough to affect the separation efficiency of the first-stage membrane separator 21 after entering the first-stage membrane separator 21, the tail gas needs to be compressed by the compressor and then enters the first-stage membrane separator 21.
In a specific embodiment, a preheater 8 is disposed between the pretreatment module 1 and the membrane separation module, and in particular, a preheater 8 is disposed between the pretreatment module 1 and the primary membrane separator 21. In order to enhance the separation effect of the mixed gas entering the primary membrane separator 21, the mixed gas needs to reach a certain temperature, typically 30-40 ℃; therefore, when the external environment temperature is lower than 30 ℃, the preheater 8 is started, and the mixed gas output by the pretreatment module 1 is heated by the preheater 8 and then enters the primary membrane separator 21.
In a specific embodiment, the adsorption modules have two groups, namely a first adsorption module 3 and a second adsorption module 4, which are arranged in series; the first adsorption column 51 and the second adsorption column 52 in the first adsorption module 3 are respectively communicated with the membrane separation module, and are used for alternately receiving the mixed gas output by the membrane separation module, namely, the mixed gas output by the secondary membrane separator 22, and the residual gas impurities in the mixed gas are absorbed through the first adsorption module 3 to generate hydrogen helium mixed gas; the first adsorption column 51 and the second adsorption column 52 in the second adsorption module 4 are respectively communicated with the first adsorption module 3, and are used for alternately receiving the hydrogen helium mixed gas and adsorbing hydrogen in the hydrogen helium mixed gas to generate high-purity helium gas. In this embodiment, the first adsorption module 3 can absorb the residual gas impurities in the mixed gas with the volume fraction of 85% -90% to generate a hydrogen helium mixed gas, wherein the gas impurities are for example O 2、CH4、CO、CO2、N2; the hydrogen in the hydrogen-helium mixed gas is absorbed by the second absorption module 4, and finally high-purity helium is formed.
In a specific embodiment, the adsorption module further comprises: a first gas-filling pipe 53 and a second gas-filling pipe 54 respectively communicating with one end of the first adsorption column 51 and one end of the second adsorption column 52, the first gas-filling pipe 53 being used for transporting high-purity helium gas to the first adsorption column 51, the second gas-filling pipe 54 being used for transporting high-purity helium gas to the second adsorption column 52; a first air outlet pipe 55 and a second air outlet pipe 56 which are respectively communicated with the other end of the first adsorption column 51 and the other end of the second adsorption column 52; when the first gas-filling pipe 53 delivers high purity helium gas to the first adsorption column 51, the gas impurities absorbed in the first adsorption column 51 are outputted to the outside through the first gas-outlet pipe 55; when the second gas-filling pipe 54 delivers high purity helium gas to the second adsorption column 52, the gas impurities absorbed in the second adsorption column 52 are outputted to the outside through the second gas-outlet pipe 56. The arrangement of the first air charging pipeline 53, the second air charging pipeline 54, the first air outlet pipeline 55 and the second air outlet pipeline 56 realizes that the first adsorption column 51 and the second adsorption column 52 alternately receive the mixed gas output by the membrane separation module and adsorb gas impurities in the mixed gas.
When the gas impurities adsorbed by the first adsorption column 51 reach a saturated state, the adsorption process is switched to the second adsorption column 52 for adsorption, and high-purity helium is filled into the first adsorption column 51 through the first air charging pipeline 53 at this time so as to purge the gas impurities adsorbed in the first adsorption column 51 to the first air outlet pipeline 55, and the gas impurities are output to the outside through the first air outlet pipeline 55, so that the cleaning of the first adsorption column 51 is realized.
When the gas impurities adsorbed by the second adsorption column 52 reach a saturated state, the adsorption process is switched to the first adsorption column 51 for adsorption, and high-purity helium is filled into the second adsorption column 52 through the second air charging pipeline 54, so that the gas impurities adsorbed in the second adsorption column 52 can be purged to the second air outlet pipeline 56, and the gas impurities are output to the outside through the second air outlet pipeline 56, so that the second adsorption column 52 is cleaned.
Specifically, the end of the first air-charging pipe 53 far from the first adsorption column 51 can be communicated with the end of the second air-charging pipe 54 far from the second adsorption column 52, so that high-purity helium can be received through a receiving port; the end of the first air outlet pipeline 55 far away from the first adsorption column 51 and the end of the second air outlet pipeline 56 far away from the second adsorption column 52 can be communicated, so that the gas impurities absorbed in the first adsorption column 51 or the second adsorption column 52 can be discharged to the outside through one air outlet.
Here, the time for delivering high purity helium gas to the first adsorption column 51 or the second adsorption column 52 is smaller than the time for the first adsorption column 51 or the second adsorption column 52 to adsorb gas impurities, so as to ensure that the first adsorption column 51 or the second adsorption column 52 is in a completely cleaned state when switching to the first adsorption column 51 or the second adsorption column 52; the time for the first adsorption column 51 to adsorb the gas impurities and the time for purging by high purity helium gas are set according to practical conditions.
In a specific embodiment, the first switches 61 are respectively disposed at two ends of the first adsorption column 51, and the second switches 62 are respectively disposed at two ends of the second adsorption column 52; the first charge line 53 includes a first outlet located between one of the two first switches 61 and the first adsorption column 51 and communicating with the first adsorption column 51; the second charge line 54 includes a second outlet located between one of the two second switches 62 and the second adsorption column 52 and in communication with the second adsorption column 52; the first outlet pipe 55 comprises a first inlet located between the other of the two first switches 61 and the first adsorption column 51 and communicating with the first adsorption column 51; the second outlet line 56 includes a second inlet located between the other of the two second switches 62 and the second adsorption column 52 and in communication with the second adsorption column 52. When the first adsorption column 51 is in the adsorption state, the two first switches 61 are opened, the two second switches 62 are closed, the first air charging pipeline 53 is in a non-charging state, the second air charging pipeline 54 is in an air charging state, the first air discharging pipeline 55 is in a non-air discharging state, and the second air discharging pipeline 56 is in an air discharging state; that is, the first adsorption column 51 receives the mixed gas from the previous module, and the second adsorption column 52 is in a cleaning state; when the second adsorption column 52 is in the adsorption state, the two second switches 62 are opened, the two first switches 61 are closed, the second air-charging pipeline 54 is in a non-air-charging state, the first air-charging pipeline 53 is in an air-charging state, the second air-discharging pipeline 56 is in a non-air-discharging state, and the first air-discharging pipeline 55 is in an air-discharging state; that is, the second adsorption column 52 receives the mixed gas from the previous module, and the first adsorption column 51 is in a cleaning state; the use of two first switches 61 and two second switches 62 can realize that the first adsorption column 51 and the second adsorption column 52 alternately receive the mixed gas from the previous module, thereby improving the separation efficiency of the mixed gas.
In a specific embodiment, the first air-charging pipeline 53 and the first air-discharging pipeline 55 are respectively provided with a third switch 63, and the second air-charging pipeline 54 and the second air-discharging pipeline 56 are respectively provided with a fourth switch 64; when the first adsorption column 51 is in an adsorption state, the first switch 61 and the fourth switch 64 are in an open state, and the second switch 62 and the third switch 63 are in a closed state; when the second adsorption column 52 is in the adsorption state, the first switch 61 and the fourth switch 64 are in the closed state, and the second switch 62 and the third switch 63 are in the open state. The use of two third switches 63 may close or open the first outlet of the first air charge line 53 and the first inlet of the first air outlet line 55, and the use of two fourth switches 64 may close or open the second outlet of the second air charge line 54 and the first inlet of the second air outlet line 56, thereby effecting the alternate cleaning of the first and second adsorption columns 51, 52.
In a specific example, the side walls of the first adsorption column 51 and the second adsorption column 52 are respectively provided with a heating belt 511, and when the first adsorption column 51 or the second adsorption column 52 is filled with high-purity helium, the first adsorption column 51 or the second adsorption column 52 is heated to 100 ℃ to 150 ℃ by the heating belt 511, so that the temperature of the high-purity helium entering the adsorption column can reach 100 ℃ to 150 ℃, thereby improving the cleaning efficiency of the first adsorption column 51 or the second adsorption column 52. The temperature of the heating belt 511 may be controlled by a temperature programmable meter.
In practical application, the usage flow of the first adsorption module 3 is as follows: the first adsorption column 51 is operated first, and the second adsorption column 52 is operated later. The two first switches 61 are opened, the two second switches 62, the two third switches 63 and the two fourth switches 64 are closed, the first adsorption column 51 in the first adsorption module 3 starts to receive the mixed gas output from the second-stage membrane separator 22 and adsorbs gas impurities in the mixed gas, the generated hydrogen helium mixture is conveyed to the second adsorption module 4, the second adsorption column 52 is in a non-working state at this time, the heating belts 511 wrapped on the side walls of the first adsorption column 51 and the second adsorption column 52 are not working, when the first adsorption column 51 is in a saturated state, the two first switches 61 and the two fourth switches 64 are closed, the two second switches 62 and the two third switches 63 are both turned on, that is, the second adsorption column 52 starts to receive the mixed gas outputted from the second membrane separator 22 and adsorbs the gas impurities in the mixed gas, the generated hydrogen helium mixture is delivered to the second adsorption module 4, at this time, the heating belt 511 wrapped on the side wall of the second adsorption column 52 does not work, the heating belt 511 wrapped on the side wall of the first adsorption column 51 is heated to 100-150 ℃, the high purity helium gas is delivered to the first adsorption column 51 through the first gas-filling pipeline 53, so that the gas impurities absorbed in the first adsorption column 51 are outputted to the outside through the first gas-outlet pipeline 55, when the second adsorption column 52 is in a saturated state, the two first switches 61 and the two fourth switches 64 are opened, and the two second switches 62 and the two third switches 63 are closed, i.e. the first adsorption column 51 starts to receive the mixed gas output from the second membrane separator 22 and adsorb the gas impurities in the mixed gas, the generated hydrogen helium mixture is conveyed to the second adsorption module 4, at this time, the heating belt 511 wrapped on the side wall of the first adsorption column 51 does not work, the heating belt 511 wrapped on the side wall of the second adsorption column 52 is heated to 100-150 ℃, the high purity helium is conveyed to the second adsorption column 52 through the second air charging pipeline 54, so that the gas impurities absorbed in the second adsorption column 52 are outputted to the outside through the second gas outlet pipe 56; when the first adsorption column 51 adsorbs impurities in the mixed gas outputted from the second-stage membrane separator 22 and is in a saturated state, the two first switches 61 and the two fourth switches 64 are closed, and the two second switches 62 and the two third switches 63 are opened, i.e. the second adsorption column 52 starts to receive the mixed gas outputted from the second-stage membrane separator 22 and adsorbs gas impurities in the mixed gas, and the generated hydrogen helium mixture is delivered to the second adsorption module 4, at this time, the heating belt 511 wrapped on the side wall of the second adsorption column 52 does not work, the heating belt 511 wrapped on the side wall of the first adsorption column 51 is heated to 100-150 ℃, delivering high purity helium gas to the first adsorption column 51 through the first gas-filling pipe 53 so that the gas impurities absorbed in the first adsorption column 51 are outputted to the outside through the first gas-outlet pipe 55; similarly, the first adsorption column 51 and the second adsorption column 52 alternately receive the mixed gas outputted from the secondary membrane separator 22.
The usage flow of the second adsorption module 4 is as follows: the first adsorption column 51 is operated first, and the second adsorption column 52 is operated later. The two first switches 61 are opened, the two second switches 62, the two third switches 63 and the two fourth switches 64 are closed, the first adsorption column 51 in the second adsorption module 4 starts to receive the mixed gas output by the first adsorption module 3 and adsorb gas impurities in the mixed gas, the generated high-purity helium gas is conveyed to the collector, the second adsorption column 52 is in a non-working state at the moment, the heating belts 511 wrapped on the side walls of the first adsorption column 51 and the second adsorption column 52 are not working, when the first adsorption column 51 is in a saturated state, the two first switches 61 and the two fourth switches 64 are closed, the two second switches 62 and the two third switches 63 are opened, namely the second adsorption column 52 starts to receive the hydrogen helium mixed gas output by the first adsorption module 3 and adsorb hydrogen in the hydrogen helium mixed gas, the generated high-purity helium gas is delivered to the collector, at this time, the heating belt 511 wrapped on the side wall of the second adsorption column 52 is not operated, the heating belt 511 wrapped on the side wall of the first adsorption column 51 is heated to 100-150 ℃, the high-purity helium gas is delivered to the first adsorption column 51 through the first gas-filling pipe 53, so that the hydrogen gas absorbed in the first adsorption column 51 is delivered to the outside through the first gas-discharging pipe 55, when the second adsorption column 52 is in a saturated state, the two first switches 61 and the two fourth switches 64 are both opened, the two second switches 62 and the two third switches 63 are both closed, i.e., the first adsorption column 51 starts to receive the hydrogen-helium mixed gas outputted from the first adsorption module 3 and adsorbs the hydrogen in the hydrogen-helium mixed gas, at this time, the generated high-purity helium gas is delivered to the collector, the heating belt 511 wrapped on the side wall of the first adsorption column 51 is not operated, the heating belt 511 wrapped on the side wall of the second adsorption column 52 is heated to 100-150 ℃, and high-purity helium gas is delivered to the second adsorption column 52 through the second gas-filling pipeline 54, so that hydrogen gas absorbed in the second adsorption column 52 is output to the outside through the second gas-outlet pipeline 56; when the first adsorption column 51 adsorbs hydrogen in the hydrogen helium mixed gas output by the first adsorption module 3 and is in a saturated state, the two first switches 61 and the two fourth switches 64 are closed, and the two second switches 62 and the two third switches 63 are opened, namely, the second adsorption column 52 starts to receive the hydrogen helium mixed gas output by the first adsorption module 3 and adsorbs gas impurities in the hydrogen helium mixed gas, generated high-purity helium gas is conveyed to a collector, at the moment, a heating belt 511 wrapped on the side wall of the second adsorption column 52 does not work, the heating belt 511 wrapped on the side wall of the first adsorption column 51 is heated to 100-150 ℃, and the high-purity helium gas is conveyed to the first adsorption column 51 through the first air charging pipeline 53, so that the hydrogen absorbed in the first adsorption column 51 is output to the outside through the first air outlet pipeline 55; similarly, the first adsorption column 51 and the second adsorption column 52 alternately receive the mixed gas outputted from the first adsorption module 3.
In a specific example, the first adsorption column 51 and the second adsorption column 52 in the first adsorption module 3 may be MOFs adsorption columns, and the MOFs adsorption columns are multiple in types, strong in functionality, capable of having a very large specific surface area and high porosity, capable of showing a relatively large adsorption capacity and a relatively good selective adsorption performance at normal temperature, capable of increasing open metal sites to improve selective adsorption thereof, and capable of adjusting pore diameters by changing the length of the organic ligands; for example, cu-BTC, ZIF-67, ZIF-8, uiO66 and the like can be added as adsorption substances to the adsorbent in the MOFs adsorption column, and chemical substances can be added to the adsorbent according to actual conditions so as to effectively adsorb CH 4 and N 2 in the mixed gas, and of course, other adsorption substances can be added according to actual conditions, the pore diameter and unsaturated metal sites of the material can be adjusted, and the adsorption and separation performance of the material can be optimized so as to improve the adsorption of gas impurities.
The first adsorption column 51 and the second adsorption column 52 in the second adsorption module 4 are hydrogen storage alloy adsorption columns, which can adsorb hydrogen in the received hydrogen-helium mixed gas, avoid introducing oxygen impurities by using a catalytic dehydrogenation device, and greatly improve the purity of the output helium. The hydrogen storage alloy in the hydrogen storage alloy adsorption column can be rare earth hydrogen storage alloy.
In practical application, the first adsorption column 51 and the second adsorption column 52 are stainless steel round adsorption columns, both ends of each column are filled with a certain amount of quartz sand, the middle of each column is filled with granular adsorbent, the amount of the adsorbent is determined according to the flow of mixed gas, the type of adsorbent material and other factors, and the adsorbent should be activated before use, so that the adsorption efficiency of the adsorbent is highest. After activation the first and second adsorption columns 51, 52 start to enter a normal operating state.
It should be understood that the foregoing examples of the present utility model are provided merely for clearly illustrating the present utility model and are not intended to limit the embodiments of the present utility model, and that various other changes and modifications may be made therein by one skilled in the art without departing from the spirit and scope of the present utility model as defined by the appended claims.
Claims (10)
1. A system for extracting helium gas comprising a plurality of process modules;
The plurality of processing modules comprises
The pretreatment module is used for receiving external mixed gas to be treated and carrying out pretreatment on the mixed gas to be treated;
The membrane separation module is used for receiving the mixed gas pretreated by the pretreatment module and removing part of gas impurities in the mixed gas;
At least one set of adsorption modules;
The adsorption module comprises
The first adsorption column and the second adsorption column are arranged in parallel;
the first adsorption column and the second adsorption column are configured to alternately receive the mixed gas output by the previous processing module and adsorb the remaining gas impurities in the received mixed gas.
2. The system for extracting helium gas of claim 1, wherein the adsorption module has two groups arranged in series, a first adsorption module and a second adsorption module, respectively;
The first adsorption column and the second adsorption column in the first adsorption module are respectively communicated with the membrane separation module and are used for alternately receiving the mixed gas output by the membrane separation module to generate hydrogen helium mixed gas;
The first adsorption column and the second adsorption column in the second adsorption module are respectively communicated with the first adsorption module and are used for alternately receiving the hydrogen helium mixed gas and adsorbing hydrogen in the hydrogen helium mixed gas to generate high-purity helium.
3. The system for extracting helium of claim 2, wherein the first adsorption column and the second adsorption column in the first adsorption module are MOFs adsorption columns;
the first adsorption column and the second adsorption column in the second adsorption module are hydrogen storage alloy adsorption columns.
4. The system for extracting helium of claim 1, wherein the adsorption module further comprises: a first gas-filling pipeline and a second gas-filling pipeline which are respectively communicated with one end of the first adsorption column and one end of the second adsorption column, wherein the first gas-filling pipeline is used for conveying high-purity helium to the first adsorption column, and the second gas-filling pipeline is used for conveying high-purity helium to the second adsorption column;
a first air outlet pipeline and a second air outlet pipeline which are respectively communicated with the other end of the first adsorption column and the other end of the second adsorption column;
when the first charging pipeline conveys high-purity helium to the first adsorption column, the gas impurities absorbed in the first adsorption column are output to the outside through the first air outlet pipeline;
when the second charging pipeline conveys the high-purity helium to the second adsorption column, the gas impurities absorbed in the second adsorption column are output to the outside through the second air outlet pipeline.
5. The system for extracting helium of claim 4, wherein a first switch is provided at both ends of the first adsorption column, and a second switch is provided at both ends of the second adsorption column, respectively;
The first charging line includes a first outlet located between and in communication with one of the two first switches and a first adsorption column;
the second charging pipeline comprises a second outlet, and the second outlet is positioned between one of the two second switches and a second adsorption column and is communicated with the second adsorption column;
The first air outlet pipeline comprises a first inlet which is positioned between the other first switch of the two switches and a first adsorption column and is communicated with the first adsorption column;
The second outlet pipe comprises a second inlet which is positioned between the other second switch of the two and the second adsorption column and is communicated with the second adsorption column.
6. The system for extracting helium of claim 5, wherein a third switch is provided on each of the first inflation line and the first outlet line, and a fourth switch is provided on each of the second inflation line and the second outlet line;
When the first adsorption column is in an adsorption state, the first switch and the fourth switch are in an open state, and the second switch and the third switch are in a closed state;
When the second adsorption column is in an adsorption state, the first switch and the fourth switch are in a closed state, and the second switch and the third switch are in an open state.
7. The system for extracting helium of claim 1, wherein the membrane separation module comprises
At least one primary membrane separator which is communicated with the pretreatment module and is used for receiving the mixed gas pretreated by the pretreatment module;
the second-stage membrane separator is communicated with the first-stage membrane separator through a compressor and is used for receiving the mixed gas output by the first-stage membrane separator;
The adsorption module is communicated with the secondary membrane separator and receives the mixed gas output by the secondary membrane separator.
8. The system for extracting helium of claim 7, wherein the tail gas output from the secondary membrane separator is re-input to the primary membrane separator through a recycle line.
9. The system for extracting helium of claim 1, wherein a pre-heater is disposed between the pre-treatment module and the membrane separation module.
10. The system for extracting helium of claim 1, wherein heating strips are provided on sidewalls of the first and second adsorption columns, respectively.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202322922513.5U CN220999250U (en) | 2023-10-30 | 2023-10-30 | System for extracting helium |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202322922513.5U CN220999250U (en) | 2023-10-30 | 2023-10-30 | System for extracting helium |
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