CN111847407B - Multistage helium extraction device and multistage helium extraction process - Google Patents
Multistage helium extraction device and multistage helium extraction process Download PDFInfo
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- CN111847407B CN111847407B CN202010894183.1A CN202010894183A CN111847407B CN 111847407 B CN111847407 B CN 111847407B CN 202010894183 A CN202010894183 A CN 202010894183A CN 111847407 B CN111847407 B CN 111847407B
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- 229910052734 helium Inorganic materials 0.000 title claims abstract description 104
- 239000001307 helium Substances 0.000 title claims abstract description 102
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 238000000605 extraction Methods 0.000 title claims abstract description 48
- 238000000926 separation method Methods 0.000 claims abstract description 186
- 239000012528 membrane Substances 0.000 claims abstract description 150
- 239000007789 gas Substances 0.000 claims abstract description 88
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 47
- 239000012466 permeate Substances 0.000 claims abstract description 42
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000000047 product Substances 0.000 claims abstract description 28
- 239000003345 natural gas Substances 0.000 claims abstract description 18
- 230000018044 dehydration Effects 0.000 claims description 17
- 238000006297 dehydration reaction Methods 0.000 claims description 17
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 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 8
- 208000005156 Dehydration Diseases 0.000 description 14
- 238000000034 method Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000003949 liquefied natural gas Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 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
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000005481 NMR spectroscopy Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000004065 semiconductor Substances 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
- 239000002699 waste material Substances 0.000 description 1
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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
- C01B23/00—Noble gases; Compounds thereof
- C01B23/001—Purification or separation processes of noble gases
- C01B23/0094—Combined chemical and physical processing
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
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, namely a first stage membrane separation group to an N stage membrane separation group, a permeate 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 multistage helium extraction process adopts the multistage 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 multi-stage helium extracting device and a multi-stage helium extracting process.
Background
Helium is widely used in the fields of military industry, medical treatment, semiconductors, low-temperature superconductivity, nuclear magnetic resonance, gas leakage detection and the like. Helium is present in relatively low levels in air and is present in the formation in significantly higher levels than air. With the rapid development of petroleum and natural gas exploration in China, the processing and treatment of natural gas and shale gas in China are rapidly developed, the domestic natural gas consumption market scale is continuously expanded, a large amount of helium is contained in natural gas, the concentration is higher, a large amount of discharged air in the oilfield associated natural gas and natural gas treatment factory is combusted usually through a factory boiler or a torch, so that a large amount of helium in the natural gas is wasted, and therefore a helium recovery device with low investment cost and low energy consumption is required to be developed urgently, the helium with higher concentration in the natural gas is recovered, the waste of the helium can be effectively avoided, and the domestic helium storage is increased.
The existing helium purifying method generally adopts a cryogenic separation or pressure swing adsorption device, and the cryogenic separation helium device has the defects of larger investment, longer starting time, higher energy consumption, low product purity and the like; the pressure swing adsorption device has the defects of large equipment volume, high noise, lower 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 further aims to provide a multistage helium extraction process, which aims to reduce the energy consumption of the process on the premise of improving the purity and yield of the product.
The invention is realized in the following way:
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 and an Nth stage membrane separation group, a permeate gas outlet of each stage of membrane separation group is communicated with an air 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-permeate gas outlet of the first stage of membrane separation group is communicated with a helium extraction tail gas exhaust port, and a permeate gas outlet of the Nth stage of membrane separation group is communicated with a helium product collecting port.
Further, in a preferred embodiment of the present invention, the multi-stage membrane separation unit includes at least four stage membrane separation groups, and the multi-stage helium extraction apparatus further includes a first pressurizing unit, an air inlet of the first pressurizing unit is communicated with the natural gas supply line, and an air outlet of the first pressurizing unit is communicated with an air inlet of the first stage membrane separation group.
Further, in a preferred embodiment of the present invention, a second pressurizing unit is provided between any adjacent two of the first to nth stage membrane separation groups.
Further, in a preferred embodiment of the present invention, a pressurizing unit is provided between any adjacent two of the first to nth stage membrane separation groups.
Further, in a preferred embodiment of the present invention, the non-permeate gas outlet of the second stage membrane separation group is in communication 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 all in communication with the gas inlet of the front end compressor.
Further, in a preferred embodiment of the present invention, the first pressurizing unit includes a compressor, a cooler, and a separation tank sequentially disposed, an air inlet of the compressor is communicated with the natural gas supply line, and a gas outlet of the separation tank is communicated with an air inlet of the first-stage membrane separation group.
Further, in a preferred embodiment of the present invention, the dehydrogenation unit includes a dehydrogenation tower, a deoxidization tower and a dehydration tower which are sequentially arranged, wherein an air inlet of the dehydrogenation tower is respectively communicated with a permeate air outlet of the membrane separation group and an oxygen supply pipeline, and an air outlet of the dehydration tower is communicated with an air inlet of another membrane separation group.
Further, in the preferred embodiment of the present invention, a cooling separation device is provided between the deoxidizing tower and the dehydrating tower; the cooling and separating device comprises a cooler for cooling the materials processed by the tower equipment and a separating tank for carrying out gas-liquid separation on the cooled materials.
Further, in a preferred embodiment of the present 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, helium product outlets are arranged between two adjacent membrane separation units in the multi-stage membrane separation units.
The beneficial effects of the invention are as follows: according to the multistage helium extraction device obtained through the design, helium is concentrated step by adopting at least three stages of membrane separation groups, the non-permeate gas of the membrane separation groups at the rear stage is returned to the inlet of the front compressor for pressurization, helium extraction tail gas is discharged from the non-permeate gas outlet of the first stage of membrane separation groups, and helium products are discharged from the permeate gas outlet of the N stage of membrane separation groups. The non-permeate gas of the membrane separation group at the rear stage is circulated to the inlet of the membrane separation group at the front stage, so that the helium component in the non-permeate gas at each stage is further extracted, and the product yield of the helium extracting device is effectively improved.
In addition, the treatment gas quantity of the first-stage to N-stage membrane separation groups is sequentially reduced, the helium concentration is sequentially increased, 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 deoxidization tower and the dehydration tower is arranged between the two adjacent membrane separation groups, so that the effective separation of helium and hydrogen is realized, and the defect of high energy consumption caused by cryogenic separation of helium and hydrogen is avoided. Meanwhile, a pressure swing adsorption device is not required to be arranged, and the investment and the operation difficulty of the device are effectively reduced on the basis of ensuring the purity and the yield of the product.
In particular, the non-permeate gas outlet of the rear membrane separation group of the multistage helium extracting device is communicated with the inlet of the compressor of a certain pressurizing unit at the front end according to the principle that the 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 critical, and the dehydrogenation unit is arranged between the two adjacent membrane separation groups, so that the defects of high energy consumption, low treatment precision and the like caused by the need of treating a large amount of raw gas in the dehydrogenation reaction under low concentration are avoided, and the equipment overtemperature risk caused by the dehydrogenation reaction (exothermic reaction) under the 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 the separation is carried out by the multistage membrane separation groups and the dehydrogenation units positioned between the adjacent two stages of 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 adopting 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 needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some examples of the present invention and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic view of a first configuration of a multi-stage helium extraction apparatus according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a second configuration of a multi-stage helium extraction apparatus according to an embodiment of the present invention;
FIG. 3 is a schematic view of a third configuration of a multi-stage helium extraction apparatus according to an embodiment of the present invention;
FIG. 4 is a schematic view of the structure of the dehydrogenation unit of FIG. 3;
FIG. 5 is a flow chart of a preferred embodiment of the present invention.
Icon: 100 a-a multi-stage helium extraction unit; 100 b-a multi-stage helium extraction unit; 100 c-a multistage helium extraction device; a 001-LNG storage tank; 002-helium collection tank; 110-a multistage membrane separation unit; 111-a first stage membrane separation group; 112-a second stage membrane separation group; 113-a 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-deoxidizing tower; 123-a dehydration tower; 124-cooling separation means; 1241-a cooler; 1242-separation tank; 1243-filter; 130-a first pressurizing unit; 131-a compressor; 132-a cooler; 133-a separator tank; 140-a third booster unit; 150-a second pressurizing unit.
Detailed Description
For the purpose of making 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 clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, based on the embodiments of the invention, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the invention. Thus, the following detailed description of the embodiments of the invention, as 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, based on the embodiments of the invention, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
Referring to fig. 1, an embodiment of the present invention provides a multi-stage helium extracting 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 in a mixed gas, so as to further purify helium.
Specifically, the multistage membrane separation unit 110 includes at least three stages of membrane separation groups, that is, a first stage membrane separation group 111 to an nth stage membrane separation group 115, respectively, and a permeate 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 hydrogen removal unit 120 is disposed between any adjacent two stages of membrane separation groups. As 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 multi-stage helium extraction apparatus 100b in fig. 2 shows the most valuable four-stage membrane separation groups, i.e., 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. In the embodiment of the application, N refers to an integer of four or more.
It should be noted that the membrane separation group cannot directly and effectively separate hydrogen and helium, and the present application is provided with the hydrogen removal unit 120, and uses the principle that hydrogen and oxygen undergo oxidation reaction under the action of a catalyst to generate water to remove hydrogen, and then remove oxygen and water. According to the application, the dehydrogenation unit 120 is arranged between the two adjacent membrane separation groups according to the hydrogen concentration of the permeate gas outlet of each membrane separation group, so that the defects of high energy consumption, low treatment precision and the like caused by the need of treating a large amount of raw gas when the dehydrogenation reaction is carried out at low concentration are avoided, and the overtemperature risk caused by the dehydrogenation reaction carried out at too high concentration is also avoided. 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 the cryogenic separation or pressure swing adsorption (or low-temperature adsorption) process.
In a preferred embodiment of the invention, the natural gas feedstock for helium separation is flash gas of liquefied natural gas (BOG), BOG being from LNG storage tank 001.
In some embodiments, referring to fig. 3-4, multi-stage helium extraction apparatus 100c further comprises a first pressurizing unit 130, wherein an air inlet of first pressurizing unit 130 is in communication with the BOG air supply line, and an air outlet of first pressurizing unit 130 is in communication with an air inlet of first stage membrane separation group 111. The gas is pressurized by the first pressurizing unit 130, so that the gas has larger pressure before membrane separation, the pressure loss of permeation gas in the membrane separation process is larger, and if the pressurization is not performed, the inlet pressure of each stage of membrane separation group is gradually reduced. Therefore, a second pressurizing unit (not shown) may be provided between any two adjacent membrane separation groups of the second-stage membrane separation group 112 to the nth-stage membrane separation group 115 as needed, so that not only the pressure difference required between the membrane separation groups is ensured, but also the gas fusion of similar helium concentrations with different pressures is realized.
Referring to fig. 5, in a preferred embodiment of the present invention, the non-permeate outlet of the second stage membrane separation unit 112 is connected to the inlet of the compressor in the first pressurizing unit 130, the non-permeate outlet of the third stage membrane separation unit 113 is connected to the inlet of the compressor in the first pressurizing unit 130, and the non-permeate outlet of the fourth stage membrane separation unit 114 is connected to the inlet of the compressor in the second pressurizing unit 150.
In the preferred embodiment of the invention, the non-permeate gas outlets from the third stage membrane separation group 113 to the nth stage membrane separation group 115 are all communicated with the gas inlets of the membrane separation groups with similar helium concentration at 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 similar helium concentration at 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), the merging of the gases with similar concentration is realized, the power consumption of the compressor is saved, and the total helium yield is improved. It should be noted that the number of compressors may be one or more, and compressors may be disposed 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 upper stage of membrane separation group, and all the non-permeate gas outlets return to the upper stage.
Further, the first pressurizing unit 130 includes a compressor 131, a cooler 132, and a separation tank 133, which are sequentially disposed, an air inlet of the compressor 131 is communicated with a natural gas supply line, and a gas 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 separated into gas and liquid by the separator tank 133, thereby preventing the liquid from being carried into the membrane separation stage.
And the tail gas after helium extraction treatment is discharged from a non-permeate gas outlet of the first-stage membrane separation group, and helium products are 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 multi-stage membrane separation units, and helium products with different purities can be respectively obtained at the outlets of each stage.
In some embodiments, a helium gas collection tank 002 is provided for collecting permeation gas of the nth membrane separation group 115, and helium gas with different concentrations can be recovered by adding a helium gas analyzer to the front end of the helium gas collection tank 002.
Further, referring to fig. 3 and 4, the dehydrogenation unit 120 includes a dehydrogenation tower 121, a deoxidizing tower 122 and a dehydration tower 123 sequentially arranged, wherein an air inlet of the dehydrogenation tower 121 is respectively communicated with a permeate air outlet of the 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, and the dehydrogenation tower 121 removes hydrogen using the principle of reaction of hydrogen and oxygen, and the deoxidization tower 122 and the dehydration tower 123 perform oxygen and water removal, respectively. The number of the dehydrogenation columns 121, the deoxidizing columns 122 and the dehydration columns 123 is not limited, and may be 1 to 3. The dehydration column 123 is also called a drying column, and the drying column removes moisture by using a desiccant, and can be dried by molecular sieve dehydration.
In some embodiments, the concentration of the gas phase oxygen separated by the separation tank 1242 between the dehydrogenation tower 121 and the deoxygenation tower 122 may be detected by an oxygen analyzer, indirectly analyzing whether the dehydrogenation is complete, and directing the adjustment of the flow of oxygen or air to the dehydrogenation tower 121.
In the preferred embodiment of the present invention, a cooling separation device 124 is provided between the deoxidizing column 122 and the dehydrating column 123; the cooling separation device 124 comprises a cooler 1241 for cooling the material processed by the tower equipment and a separation tank 1242 for separating gas from liquid of the cooled material. The reaction in the tower equipment is often accompanied with heat release, and the reaction is cooled by a cooler 1241 and then subjected to gas-liquid separation by a separation tank 1242, so that the generation of liquid is prevented from being carried to the next process.
In a preferred embodiment of the present invention, a filter 1243 is further included between the dehydration column 123 and the corresponding membrane separation group, an air inlet of the filter 1243 is communicated with the air outlet of the dehydration column 123, and an air outlet of the filter 1243 is communicated with the air inlet of the membrane separation group. The filter 1243 filters impurities such as dust to protect the back end membrane separation group from the impurities.
In the preferred embodiment of the present invention, the third pressurizing unit 140 is disposed between the membrane separation unit and the dehydrogenation unit, and the third pressurizing unit 140 may be disposed as required to prevent the adverse dehydrogenation separation process due to the too low pressure after the dehydrogenation unit 120.
The embodiment of the invention also provides a multistage helium extraction process, which is performed by using the multistage helium extraction device, and is performed by purifying through the multistage membrane separation unit 110 and the dehydrogenation unit 120, and improving the position of the dehydrogenation unit 120 to further improve the purification effect.
Preferably, helium product outlets are arranged between two adjacent membrane separation units in the multistage membrane separation units, helium products with different concentrations can be taken out from different positions between stages, and helium products with various purities can be produced, and the lower the purity is, the higher the yield is.
Carrying out multistage helium extraction by adopting the device in FIG. 3, pressurizing BOG of the LNG storage tank 001 to 3MPa-10MPa by a compressor of a first pressurizing unit, separating the BOG by a cooler, and then entering a first-stage membrane separation assembly, wherein non-permeate gas of the first-stage membrane separation assembly is returned to a factory as helium extraction tail gas (the main components are methane and nitrogen), and permeate gas of the first-stage membrane separation assembly enters a second-stage membrane separation assembly; the non-permeate gas of the second-stage membrane separation assembly returns to the inlet of the compressor of the first pressurizing unit, the permeate gas is pressurized to 3-6MPa by the compressor of the second pressurizing unit and then enters the dehydrogenation unit, and after dehydrogenation, deoxidation and dehydration treatment, the permeate gas enters the third-stage membrane separation assembly. The non-permeate gas of the third-stage membrane separation assembly is returned to the inlet of the compressor of the first pressurizing unit, and the permeate gas enters the fourth-stage membrane separation assembly. The non-permeate gas of the fourth-stage membrane separation assembly is returned to the inlet of the compressor of the second pressurizing unit, and the permeate gas is taken as product helium gas to enter the helium gas collecting device.
In the specific example of fig. 3, the feed gas composition is: CH 4 72.16％,N2 22.31％,He 4.31％,H2 1.22.22% and a flow of 1000m 3/h. The tail gas flow rate after four-stage helium extraction and separation is 945.71m 3/h, and the components are as follows: CH 476.30％,N2 23.59％,He 0.07％,H2 is 0.04%, the purity of helium is 99.999%, the flow is 42.45m 3/h, the product yield is 98.49%, and the product purity and the yield are high.
In summary, the invention provides a multistage helium extraction device, which adopts at least three stages of membrane separation groups to carry out multistage membrane separation, and a dehydrogenation unit is arranged between two adjacent stages of membrane separation groups, so that the defects of high energy consumption, low product yield, low product purity and the like caused by cryogenic separation or pressure swing adsorption are avoided, and the starting time of the device is effectively shortened.
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 units positioned between the adjacent two stages of 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 adopting cryogenic separation or pressure swing adsorption are avoided.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. The multistage helium extraction device is used for extracting helium from natural gas and is characterized by comprising a multistage membrane separation unit and a dehydrogenation unit, wherein the multistage membrane separation unit comprises at least four stages of membrane separation groups, namely a first stage membrane separation group and an Nth stage membrane separation group, a permeate 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-permeate gas outlet of the first stage of membrane separation group is communicated with a helium extraction tail gas outlet, and a permeate gas outlet of the Nth stage of membrane separation group is communicated with a helium product collection port; the hydrogen removal unit removes hydrogen by adopting the principle that hydrogen and oxygen are subjected to oxidation reaction under the action of a catalyst to generate water, and then oxygen and water are removed; the dehydrogenation unit comprises a dehydrogenation tower, a deoxidization tower and a dehydration tower which are sequentially arranged, wherein an air inlet of the dehydrogenation tower is respectively communicated with a permeation gas outlet of the membrane separation group and an oxygen supply pipeline, and an air outlet of the dehydration tower is communicated with an air inlet of the other group of membrane separation group;
The multistage helium extraction device further comprises a first pressurizing unit, an air inlet of the first pressurizing unit is communicated with a natural gas supply pipeline, and an air outlet of the first pressurizing unit is communicated with an air inlet of the first stage membrane separation group;
a second pressurizing unit is arranged between any two adjacent membrane separation groups from the first-stage membrane separation group to the N-stage membrane separation group; or, 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;
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 N-stage membrane separation group are all communicated with the gas inlet of the front-end compressor.
2. The multi-stage helium extraction unit according to claim 1, wherein the first pressurizing unit comprises a compressor, a cooler and a separation tank which are sequentially arranged, an air inlet of the compressor is communicated with the natural gas supply pipeline, and a gas outlet of the separation tank is communicated with an air inlet of the first-stage membrane separation group.
3. The multi-stage helium extraction apparatus according to claim 1, wherein a cooling separation device is provided between the deoxidizing column and the dehydrating column;
The cooling and separating device comprises a cooler for cooling the materials processed by the tower equipment and a separating tank for carrying out gas-liquid separation on the cooled materials.
4. A multi-stage helium extraction unit according to claim 3, further comprising a filter between the dehydration column and the corresponding membrane separation group, the outlet of the filter being in communication with the inlet of the membrane separation group.
5. A multistage helium extraction process, characterized in that it is carried out using a multistage helium extraction device according to any one of claims 1 to 4.
6. The multi-stage helium extraction process of claim 5, wherein helium product outlets are provided between two adjacent membrane separation units in the multi-stage membrane separation unit.
7. The multistage helium extraction process according to claim 5, wherein 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 the compressor of a certain pressurizing unit at the front end according to the principle that gas components are similar.
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| CN115845572B (en) * | 2021-09-26 | 2025-09-19 | 中国石油化工股份有限公司 | Method and system for purifying helium by combining two-stage polymer membrane separation with palladium membrane separation |
| CN117720955B (en) * | 2023-11-14 | 2025-01-28 | 中国石油天然气集团有限公司 | A system and method for extracting helium from natural gas |
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| CN212292809U (en) * | 2020-08-31 | 2021-01-05 | 成都赛普瑞兴科技有限公司 | Multistage helium extraction device and helium separation system |
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