CN111847407A - Multi-stage helium extraction device and multi-stage helium extraction process - Google Patents
Multi-stage helium extraction device and multi-stage helium extraction process Download PDFInfo
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- 229910052734 helium Inorganic materials 0.000 title claims abstract description 107
- 239000001307 helium Substances 0.000 title claims abstract description 105
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 238000000605 extraction Methods 0.000 title claims abstract description 51
- 238000000926 separation method Methods 0.000 claims abstract description 190
- 239000012528 membrane Substances 0.000 claims abstract description 157
- 239000007789 gas Substances 0.000 claims abstract description 100
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 48
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000003345 natural gas Substances 0.000 claims abstract description 18
- 239000012466 permeate Substances 0.000 claims description 30
- 239000000047 product Substances 0.000 claims description 27
- 230000018044 dehydration Effects 0.000 claims description 20
- 238000006297 dehydration reaction Methods 0.000 claims description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 8
- 238000006392 deoxygenation reaction Methods 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 238000005265 energy consumption Methods 0.000 abstract description 13
- 238000001179 sorption measurement Methods 0.000 abstract description 9
- 230000007547 defect Effects 0.000 abstract description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 12
- 239000001257 hydrogen Substances 0.000 description 12
- 229910052739 hydrogen Inorganic materials 0.000 description 12
- 239000003949 liquefied natural gas Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
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- 230000008569 process Effects 0.000 description 2
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- 239000003054 catalyst Substances 0.000 description 1
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- 230000006835 compression Effects 0.000 description 1
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- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000004904 shortening 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
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B23/00—Noble gases; Compounds thereof
- C01B23/001—Purification or separation processes of noble gases
- C01B23/0094—Combined chemical and physical processing
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0003—Chemical processing
- C01B2210/0004—Chemical processing by oxidation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/001—Physical processing by making use of membranes
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Abstract
The invention provides a multistage helium extraction device and a multistage helium extraction process, and relates to the technical field of gas separation. The multistage helium extraction device is used for extracting helium from natural gas and comprises a multistage membrane separation unit and a dehydrogenation unit, wherein the multistage membrane separation unit comprises at least three stages of membrane separation groups from a first stage membrane separation group to an Nth stage membrane separation group, a permeation gas outlet of each stage of membrane separation group is communicated with a gas inlet of the next stage of membrane separation group, and the dehydrogenation unit is arranged between any two adjacent stages of membrane separation groups. The multi-stage helium extraction process adopts the multi-stage helium extraction device to purify helium, avoids the defects of high energy consumption, low product yield, low product purity and the like caused by cryogenic separation or pressure swing adsorption, effectively simplifies the operation of the device, and shortens the starting time of the device.
Description
Technical Field
The invention relates to the technical field of gas separation, in particular to a multistage helium extraction device and a multistage helium extraction process.
Background
Helium is an important strategic resource and is widely used in the fields of military industry, medical treatment, semiconductors, low-temperature superconduction, nuclear magnetic resonance, gas leakage detection and the like. Helium is relatively low in air and significantly higher in formations than air. Along with the rapid development of the exploration of the natural gas of China, the processing and the treatment of natural gas and shale gas of China are rapidly developed, the scale of the domestic natural gas consumption market is continuously enlarged, the natural gas contains a large amount of helium and has higher concentration, a large amount of emptying gas in an oil field associated natural gas and natural gas treatment factory is usually combusted through a factory boiler or a torch, the waste of a large amount of helium in the natural gas is caused, therefore, the research and development of a helium recovery device with lower investment cost and lower energy consumption can be urgently needed, the helium with higher concentration in the natural gas is recovered, the waste of the helium can be effectively avoided, and the storage of the domestic helium is increased.
The existing helium purification method generally adopts a cryogenic separation or pressure swing adsorption device, and the cryogenic separation helium device has the defects of large investment, long starting time, high energy consumption, low product purity and the like; the pressure swing adsorption device has the defects of large equipment volume, high noise, low helium yield and the like.
Disclosure of Invention
The invention aims to provide a multistage helium extraction device, which aims to reduce the energy consumption in the helium extraction process and ensure the purity and yield of products.
The invention also aims to provide a multistage helium extraction process, aiming at reducing the energy consumption of the process on the premise of improving the purity and yield of products.
The invention is realized by the following steps:
the invention provides a multistage helium extraction device, which is used for extracting helium from natural gas and comprises a multistage membrane separation unit and a dehydrogenation unit, wherein the multistage membrane separation unit comprises at least three stages of membrane separation groups, namely a first stage membrane separation group to an Nth stage membrane separation group, a permeation gas outlet of each stage of membrane separation group is communicated with a gas inlet of the next stage of membrane separation group, the dehydrogenation unit is arranged between any two adjacent stages of membrane separation groups, a non-permeation gas outlet of the first stage of membrane separation group is communicated with a helium extraction tail gas exhaust port, and a permeation gas outlet of the Nth stage of membrane separation group is communicated with a helium product collection port.
Further, in a preferred embodiment of the present invention, the multistage membrane separation unit comprises at least four stages of membrane separation sets, the multistage helium extraction device further comprises a first pressurizing unit, a gas inlet of the first pressurizing unit is communicated with the natural gas supply pipeline, and a gas outlet of the first pressurizing unit is communicated with a gas inlet of the first stage of membrane separation set.
Further, in a preferred embodiment of the present invention, a second pressurizing unit is provided between any two adjacent membrane separation groups of the first-stage membrane separation group to the nth-stage membrane separation group.
Further, in a preferred embodiment of the present invention, a pressurizing unit is disposed between any two adjacent membrane separation groups from the first-stage membrane separation group to the nth-stage membrane separation group.
Further, in a preferred embodiment of the present invention, the non-permeate gas outlet of the second stage membrane separation group is communicated with the gas inlet of the compressor in the first pressurizing unit, and the non-permeate gas outlets from the third stage membrane separation group to the Nth stage membrane separation group are communicated with the gas inlet of the front-end compressor.
Further, in a preferred embodiment of the present invention, the first pressurizing unit comprises a compressor, a cooler and a separation tank which are arranged in sequence, wherein a gas inlet of the compressor is communicated with a natural gas supply pipeline, and a gas outlet of the separation tank is communicated with a gas inlet of the first-stage membrane separation group.
Further, in a preferred embodiment of the present invention, the dehydrogenation unit comprises a dehydrogenation tower, a deoxygenation tower and a dehydration tower arranged in sequence, wherein the gas inlet of the dehydrogenation tower is respectively communicated with the permeate gas outlet of the membrane separation group and the oxygen supply pipeline, and the gas outlet of the dehydration tower is communicated with the gas inlet of the other membrane separation group.
Further, in the preferred embodiment of the present invention, a cooling separation device is provided between the deoxygenation tower and the dehydration tower; the cooling and separating device comprises a cooler for cooling the materials processed by the tower type equipment and a separating tank for separating gas from liquid of the cooled materials.
Further, in a preferred embodiment of the invention, a filter is further included between the dehydration tower and the corresponding membrane separation group, and an air outlet of the filter is communicated with an air inlet of the membrane separation group.
The embodiment of the invention also provides a multistage helium extraction process which is carried out by applying the multistage helium extraction device;
preferably, a helium product outlet is arranged between two adjacent membrane separation units in the multistage membrane separation units.
The invention has the beneficial effects that: according to the multi-stage helium extraction device obtained through the design, at least three stages of membrane separation groups are adopted to gradually concentrate helium, non-permeation gas of the membrane separation group at the rear stage returns to the inlet of the front compressor to be pressurized, helium extraction tail gas is discharged from the non-permeation gas outlet of the first stage membrane separation group, and a helium product is discharged from the permeation gas outlet of the Nth stage membrane separation group. The non-permeable gas of the rear stage membrane separation group is circulated to the inlet of the front stage membrane separation group, so that the helium component in each stage of non-permeable gas is further extracted, and the product yield of the helium extraction device is effectively improved.
In addition, the treatment gas amount from the first-stage membrane separation group to the Nth-stage membrane separation group is reduced in sequence, the helium concentration is increased in sequence, the compression work of the compressor is effectively reduced, and the energy consumption of the device is reduced. In addition, the dehydrogenation unit comprising the dehydrogenation tower, the deoxygenation tower and the dehydration tower is arranged between the adjacent two-stage membrane separation groups, so that the helium and the hydrogen are effectively separated, and the defect of high energy consumption caused by cryogenic separation of the helium and the hydrogen is avoided. Meanwhile, a pressure swing adsorption device is not required, and the investment and the operation difficulty of the device are effectively reduced on the basis of ensuring the product purity and yield.
Particularly, the non-permeable gas outlet of the membrane separation group at the rear stage of the multi-stage helium extraction device is communicated with the compressor inlet of a certain pressurizing unit at the front end according to the principle that gas components are similar, so that separation work caused by back mixing of gases with different purities is avoided.
Particularly, the arrangement position of the dehydrogenation unit is more critical, and the dehydrogenation unit is arranged between the two adjacent stages of membrane separation groups, so that the defects of high energy consumption, low treatment precision and the like caused by the fact that a large amount of raw material gas needs to be treated in the dehydrogenation reaction under low concentration are overcome, and the equipment overtemperature risk caused by the fact that the dehydrogenation reaction (exothermic reaction) is carried out under over high concentration is also avoided.
The multistage helium extraction process provided by the invention is carried out by applying the multistage helium extraction device, and separation is carried out by the multistage membrane separation groups and the dehydrogenation unit positioned between the adjacent two-stage membrane separation groups, so that the problems of high energy consumption, long starting time, low product yield, low product purity and the like caused by cryogenic separation or pressure swing adsorption are avoided.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
Fig. 1 is a schematic view of a first structure of a multi-stage helium extraction device provided by an embodiment of the invention;
fig. 2 is a schematic diagram of a second structure of the multi-stage helium extracting device provided by the embodiment of the invention;
FIG. 3 is a schematic diagram of a third structure of a multi-stage helium extraction device provided by the embodiment of the invention;
FIG. 4 is a schematic diagram of the structure of the dehydrogenation unit of FIG. 3;
FIG. 5 is a flow chart of the preferred embodiment of the present invention.
Icon: 100 a-a multi-stage helium extraction device; 100 b-a multistage helium extraction device; 100 c-a multistage helium extraction device; 001-LNG storage tanks; 002-helium gas collection tank; 110-a multi-stage membrane separation unit; 111-first stage membrane separation group; 112-second stage membrane separation group; 113-third stage membrane separation group; 114-fourth stage membrane separation group; 115-nth stage membrane separation group; 120-a dehydrogenation unit; 121-a dehydrogenation column; 122-a deoxygenation column; 123-a dehydration column; 124-a cooling separation device; 1241-cooler; 1242-knockout drum; 1243-filter; 130-a first pressurizing unit; 131-a compressor; 132-a cooler; 133-a separation tank; 140-a third pressurizing unit; 150-a second pressurizing unit.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings of the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, the embodiment of the invention provides a multi-stage helium extraction apparatus 100a for extracting helium from natural gas, which includes a multi-stage membrane separation unit 110 and a dehydrogenation unit 120, wherein the dehydrogenation unit 120 is used for removing hydrogen from a mixed gas for the purpose of further purifying helium.
Specifically, the multistage membrane separation unit 110 includes at least three stages of membrane separation sets, which are a first stage membrane separation set 111 to an nth stage membrane separation set 115, respectively, a permeate gas outlet of each stage of membrane separation set is communicated with a gas inlet of a next stage of membrane separation set, and the hydrogen removal unit 120 is disposed between any two adjacent stages of membrane separation sets. As shown in fig. 1, a first stage membrane separation group 111, a second stage membrane separation group 112, a third stage membrane separation group 113, and an nth stage membrane separation group 115; the multistage helium extraction device 100b in fig. 2 shows the four-stage membrane separation group with the most practical value, namely the first-stage membrane separation group 111 to the fourth-stage membrane separation group 114. In fig. 2, the multistage membrane separation unit 110 is a four-stage membrane separation group, the treated gas inlet of the dehydrogenation unit 120 is communicated with the permeate gas outlet of the third-stage membrane separation group 113, and the treated gas outlet of the dehydrogenation unit 120 is communicated with the gas inlet of the fourth-stage membrane separation group 114. N in the embodiments of the present application means an integer of four or more.
It should be noted that, the membrane separation group cannot directly and effectively separate hydrogen from helium, and the hydrogen removal unit 120 is provided in the present application, and hydrogen is removed by using the principle that hydrogen and oxygen undergo an oxidation reaction under the action of a catalyst to generate water, and then oxygen and water are removed. This application sets up between suitable adjacent two-stage membrane separation group through the hydrogen concentration with dehydrogenation unit 120 according to membrane separation group permeate gas export at different levels, has both avoided carrying out dehydrogenation reaction under the low concentration and need handle a large amount of feed gases and the energy consumption that exists is high, the processing accuracy is low grade shortcoming, has also avoided carrying out dehydrogenation reaction under too high concentration and the overtemperature risk that exists. The arrangement of the dehydrogenation unit obviously improves the separation effect of hydrogen and helium, ensures the purity of the final helium, and avoids the defects of high energy consumption, long starting time, low product yield and the like caused by a cryogenic separation or pressure swing adsorption (or low temperature adsorption) process.
In the preferred embodiment of the present invention, the natural gas feedstock for helium separation is flash Boil Off Gas (BOG) of liquefied natural gas, the BOG being from LNG storage tank 001.
In some embodiments, referring to fig. 3-4, the multistage helium extraction apparatus 100c further includes a first pressure increasing unit 130, a gas inlet of the first pressure increasing unit 130 is communicated with the BOG gas supply line, and a gas outlet of the first pressure increasing unit 130 is communicated with a gas inlet of the first stage membrane separation group 111. The gas is pressurized by the first pressurizing unit 130, so that the gas has a larger pressure before membrane separation, and the pressure loss of the permeate gas is larger during membrane separation, and if pressurization is not performed, the inlet pressure of each membrane separation group is gradually reduced. Therefore, a second pressurizing unit (not shown) can be arranged between any two adjacent membrane separation groups from the second-stage membrane separation group 112 to the Nth-stage membrane separation group 115 according to requirements, so that the required pressure difference between the membrane separation modules is ensured, and gas confluence with similar helium concentrations at different pressures is realized.
Referring to fig. 5, in the preferred embodiment of the present invention, the non-permeate outlet of the second-stage membrane separation group 112 is communicated with the inlet of the compressor in the first pressure increasing unit 130, the non-permeate outlet of the third-stage membrane separation group 113 is communicated with the inlet of the compressor in the first pressure increasing unit 130, and the non-permeate outlet of the fourth-stage membrane separation group 114 is communicated with the inlet of the compressor in the second pressure increasing unit 150.
In a preferred embodiment of the present invention, the non-permeate gas outlets of the third-stage membrane separation group 113 to the nth-stage membrane separation group 115 are all communicated with the gas inlet of the membrane separation group with the helium concentration close to the front end through the compressor, so that the non-permeate gas at the rear end returns to the inlet of the membrane separation assembly with the helium concentration close to the front end (the non-permeate gas at the rear end returns to the inlet of the front-end compressor to return to the inlet of the front-end membrane separation assembly through the compressor), thereby realizing the confluence of gases with similar concentrations, saving the power consumption of the compressor, and improving the total yield of helium. It should be noted that the number of the compressors may be one or more, and a compressor may be provided between each stage of membrane separation, in which case the non-permeate gas outlet of each stage may be communicated with the gas inlet of the corresponding previous stage of membrane separation group and returned to the previous stage.
Further, the first pressurizing unit 130 includes a compressor 131, a cooler 132 and a separation tank 133 which are sequentially arranged, wherein an air inlet of the compressor 131 is communicated with a natural gas supply pipeline, and an air outlet of the separation tank 133 is communicated with an air inlet of the first-stage membrane separation group 111. The gas is pressurized by the compressor 131, cooled by the cooler 132, and then subjected to gas-liquid separation by the separation tank 133, thereby preventing liquid from being brought into the membrane separation stage.
And tail gas after helium extraction treatment is discharged from a non-permeate gas outlet of the first-stage membrane separation group, and a helium product is discharged from a permeate gas outlet of the Nth-stage membrane separation group. Of course, helium product outlets are arranged between two adjacent membrane separation units in the multistage membrane separation units, so that helium products with different purities can be obtained at each stage of outlet.
In some embodiments, a helium collecting tank 002 is provided for collecting the permeate gas of the nth membrane separation group 115, and a helium analyzer may be added to the front end of the helium collecting tank 002 to obtain helium with different concentrations for recycling.
Further, referring to fig. 3 and 4, the dehydrogenation unit 120 includes a dehydrogenation tower 121, a deoxygenation tower 122, and a dehydration tower 123 sequentially disposed, wherein an air inlet of the dehydrogenation tower 121 is respectively communicated with a permeate gas outlet of a membrane separation group and an oxygen supply pipeline, and an air outlet of the dehydration tower 123 is communicated with an air inlet of another membrane separation group. Specifically, the oxygen supply line is used to supply oxygen or air, the dehydrogenation tower 121 removes hydrogen by using the principle of reaction between hydrogen and oxygen, and the deoxidation tower 122 and the dehydration tower 123 remove oxygen and water, respectively. The number of the dehydrogenation column 121, the deoxygenation column 122, and the dehydration column 123 is not limited, and may be 1 to 3. The dehydration tower 123 is also called a drying tower, and the drying tower removes moisture by using a drying agent and can dry the moisture by using a molecular sieve dehydration method.
In some embodiments, the concentration of the gas-phase oxygen separated in the separation tank 1242 between the dehydrogenation tower 121 and the dehydrogenation tower 122 may be detected by an oxygen analyzer, indirectly analyze whether the dehydrogenation is complete, and guide the adjustment of the flow rate of the oxygen or air input to the dehydrogenation tower 121.
In the preferred embodiment of the present invention, a cooling and separating device 124 is provided between the deoxidation tower 122 and the dehydration tower 123; the cooling and separating device 124 comprises a cooler 1241 for cooling the material processed by the tower type equipment and a separating tank 1242 for gas-liquid separation of the cooled material. The reaction in the column apparatus is often accompanied by heat generation, and the reaction product is cooled by the cooler 1241 and then subjected to gas-liquid separation in the separation tank 1242, thereby preventing the generation of liquid and bringing the liquid to the next step.
In the preferred embodiment of the present invention, a filter 1243 is further included between the dehydration tower 123 and the corresponding membrane separation group, an air inlet of the filter 1243 is communicated with an air outlet of the dehydration tower 123, and an air outlet of the filter 1243 is communicated with an air inlet of the membrane separation group. Impurities such as dust are filtered by the filter 1243 to protect the rear membrane separation group from being damaged by the impurities.
In the preferred embodiment of the present invention, a third pressurizing unit 140 is disposed between the membrane separation group and the dehydrogenation unit, and the third pressurizing unit 140 may be disposed as needed to prevent the dehydrogenation separation process from being adversely affected by too low a pressure after the dehydrogenation unit 120.
The embodiment of the invention also provides a multistage helium extraction process which is carried out by applying the multistage helium extraction device, carries out purification through the multistage membrane separation unit 110 and the dehydrogenation unit 120, and improves the position of the dehydrogenation unit 120 so as to further improve the purification effect.
Preferably, a helium product outlet is arranged between two adjacent membrane separation units in the multistage membrane separation unit, helium products with different concentrations can be taken out from different interstage positions, helium products with various purities can be produced, and the lower the purity is, the higher the yield is.
The device in FIG. 3 is used for multi-stage helium extraction, the BOG of the LNG storage tank 001 is pressurized to 3MPa-10MPa by a first pressurizing unit compressor, then enters a first-stage membrane separation assembly after being cooled and separated, the non-permeation gas of the first-stage membrane separation assembly is used as helium extraction tail gas (the main components are methane and nitrogen) and returns to a factory, and the permeation gas of the first-stage membrane separation assembly enters a second-stage membrane separation assembly; and the non-permeate gas of the second-stage membrane separation component returns to the inlet of the compressor of the first pressurizing unit, and the permeate gas enters the dehydrogenation unit after being pressurized to 3-6MPa by the compressor of the second pressurizing unit, and enters the third-stage membrane separation component after being subjected to dehydrogenation, deoxidation and dehydration. And the non-permeate gas of the third-stage membrane separation assembly returns to the inlet of the compressor of the first pressurizing unit, and the permeate gas enters the fourth-stage membrane separation assembly. And the non-permeate gas of the fourth-stage membrane separation component returns to the inlet of the compressor of the second pressurizing unit, and the permeate gas enters the helium collecting device as product helium.
In the specific embodiment of FIG. 3In the examples, the feed gas composition is: CH (CH)472.16％，N222.31％，He 4.31％，H21.22% and a flow rate of 1000m3H is used as the reference value. The flow rate of the tail gas after four-stage helium extraction separation is 945.71m3H, the components are as follows: CH (CH)476.30％，N223.59％，He 0.07％，H20.04%, helium product purity of 99.999% and flow rate of 42.45m3The product yield is 98.49 percent, the product purity is high, and the yield is high.
In summary, the present invention provides a multi-stage helium extraction apparatus, which uses at least three membrane separation sets to perform multi-stage membrane separation, and arranges a dehydrogenation unit between two adjacent membrane separation sets, thereby avoiding the disadvantages of high energy consumption, low product yield, low product purity, etc. caused by cryogenic separation or pressure swing adsorption, and effectively shortening the start-up time of the apparatus.
The invention also provides a multistage helium extraction process which is carried out by applying the multistage helium extraction device, and the multistage membrane separation groups and the dehydrogenation unit positioned between the adjacent two-stage membrane separation groups are used for separation, so that the problems of high energy consumption, low product yield, low product purity, long starting time and the like caused by cryogenic separation or pressure swing adsorption are solved.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes may be made to the present invention by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The utility model provides a multistage helium device of carrying for draw helium in the follow natural gas, its characterized in that, including multistage membrane separation unit and dehydrogenation unit, multistage membrane separation unit includes at least tertiary membrane separation group, is first order membrane separation group to nth stage membrane separation group respectively, and the permeate gas export of each stage membrane separation group communicates with the air inlet of next stage membrane separation group, the dehydrogenation unit sets up between arbitrary adjacent two-stage membrane separation group, and the non-permeate gas export of first order membrane separation group with carry helium tail gas vent intercommunication, the permeate gas export of nth stage membrane separation group and helium product collection mouth intercommunication.
2. The multi-stage helium stripping plant of claim 1, wherein the multi-stage membrane separation unit comprises at least four stages of membrane separation banks, the multi-stage helium stripping plant further comprising a first pressure boosting unit, the first pressure boosting unit having a gas inlet in communication with a natural gas supply line and a gas outlet in communication with a gas inlet of the first stage membrane separation bank.
3. The multistage helium extraction device according to claim 2, wherein a second pressurization unit is provided between any two adjacent membrane separation groups of the first-stage membrane separation group to the nth-stage membrane separation group.
4. The multistage helium extraction device according to claim 2, wherein a pressurizing unit is arranged between any two adjacent membrane separation groups from the first stage membrane separation group to the Nth stage membrane separation group.
5. The multi-stage helium extraction plant of any one of claims 2-4, wherein the non-permeate outlet of the second stage membrane separation bank is in communication with the inlet of the compressor in the first pressure increasing unit, and the non-permeate outlets from the third stage membrane separation bank to the Nth stage membrane separation bank are in communication with the inlet of the front-end compressor.
6. The multi-stage helium extraction plant of claim 2, wherein the first pressure increasing unit comprises a compressor, a cooler and a separation tank arranged in sequence, wherein a gas inlet of the compressor is communicated with the natural gas supply pipeline, and a gas outlet of the separation tank is communicated with a gas inlet of the first stage membrane separation group.
7. The multistage helium extraction device as claimed in claim 1, wherein the dehydrogenation unit comprises a dehydrogenation tower, a deoxygenation tower and a dehydration tower which are arranged in sequence, wherein the gas inlet of the dehydrogenation tower is respectively communicated with the permeation gas outlet of the membrane separation group and the oxygen supply pipeline, and the gas outlet of the dehydration tower is communicated with the gas inlet of another membrane separation group.
8. The multi-stage helium extraction plant of claim 7, wherein a cooling separation device is provided between the deoxygenator column and the dehydration column;
the cooling and separating device comprises a cooler for cooling the materials processed by the tower type equipment and a separating tank for separating gas from liquid of the cooled materials.
9. The multi-stage helium extraction device of claim 8, further comprising a filter between the dehydration tower and the corresponding membrane separation group, wherein a gas outlet of the filter is communicated with a gas inlet of the membrane separation group.
10. A multistage helium extraction process, which is carried out by using the multistage helium extraction device of any one of claims 1 to 9;
preferably, a helium product outlet is arranged between two adjacent membrane separation units in the multistage membrane separation units;
preferably, the non-permeate gas outlets of the second-stage membrane separation group to the Nth-stage membrane separation group are communicated with the inlet of a compressor of a front-end pressurizing unit according to the principle that gas components are similar.
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