CN219199732U - High nitrogen BOG gas helium extraction system - Google Patents

High nitrogen BOG gas helium extraction system Download PDF

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Publication number
CN219199732U
CN219199732U CN202223286572.XU CN202223286572U CN219199732U CN 219199732 U CN219199732 U CN 219199732U CN 202223286572 U CN202223286572 U CN 202223286572U CN 219199732 U CN219199732 U CN 219199732U
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temperature
bog
catalytic dehydrogenation
low
helium extraction
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王怀昇
李维亚
王华霖
贾智利
唐英武
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Shanxi Tianhao Clean Energy Co ltd
Yichuan Tianyun Clean Energy Co ltd
Shanghai CIMC TZ Clean Energy Co Ltd
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Shanxi Tianhao Clean Energy Co ltd
Yichuan Tianyun Clean Energy Co ltd
Shanghai CIMC TZ Clean Energy Co Ltd
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/64—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end by pressure-swing adsorption [PSA] at the hot end
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Abstract

The utility model relates to the technical field of BOG gas recovery of natural gas liquefaction factories, in particular to a high-nitrogen BOG gas helium extraction system, which is used for carrying out catalytic dehydrogenation treatment on BOG gas at first, so that the problems of crude helium extraction by a cryogenic method and catalytic dehydrogenation are effectively solved, and the problems of higher hydrogen enrichment concentration and higher catalytic reaction temperature in the crude helium are solved. After catalytic dehydrogenation treatment, the low-temperature rectification crude helium extraction mechanism comprising two stages of rectification towers is used for low-temperature rectification, the concentration of crude helium obtained by the first rectification tower can reach more than 95%, the residual hydrogen and oxygen content are less, most nitrogen in the BOG gas can be removed by the second rectification tower, and a small amount of nitrogen can be further removed by the low-temperature PSA adsorption high-purity helium extraction mechanism, so that nitrogen is prevented from circulating in a liquefied system of LNG along with the BOG, and the energy consumption of the LNG liquefied system is further reduced.

Description

High nitrogen BOG gas helium extraction system
Technical Field
The utility model relates to the technical field of BOG gas recovery of natural gas liquefaction factories, in particular to a BOG gas helium extraction system with high nitrogen content.
Background
Helium (He) has a molecular weight of 4 and is colorless and odorless. Helium is very light, next to hydrogen, and has a density of 0.1786kg/m in standard conditions 3 Is 0.14 times of air density, has a boiling point of-268.9 ℃ and is close to absolute zero-273 ℃.
Helium is the second element of the second most abundant in the universe, but the reserves on earth are very rare, being buried mainly with natural gas in the ground and partially in the air.
In the natural gas industry, natural gas is often produced as liquefied natural gas (Liquefied Natural Gas, LNG) in a volume of about 1/600 of the original gaseous volume for ease of storage and transportation. In LNG production, it is necessary to reduce the liquefaction pressure to tank pressure through a final throttling valve. The boiling points of the components in natural Gas are different (helium: 4.22K, hydrogen: 20.28K, nitrogen: 77.36K, methane 111.7K) so that the throttling process corresponds to a simple evaporation of LNG at storage tank pressure, and the Gas molecules with lower boiling points are firstly escaped from LNG and are called flash gases (BOGs). Therefore, the BOG gas is the non-condensable gas which cannot be liquefied in the liquefied LNG production process or evaporated in the liquefied natural gas storage tank, and the maximum BOG gas flow can occupy about 8% of the raw gas flow, so that the LNG production process has a special recovery process for recovering the BOG gas.
The main components of BOG are methane and nitrogen, and some BOGs also contain a certain amount of helium, a very small amount of hydrogen and the like due to the different nature of natural gas in different areas. The concentration of helium in BOG is higher than that of raw natural gas, so that even a small amount of BOG has high utilization value.
In the prior art, a natural gas liquefaction plant is not provided with a feed gas denitrification device, but the nitrogen content is increased along with the change of the components of the feed gas, so that the nitrogen content in the BOG is accumulated to be 16-27% mol. The BOG gas is used as a fuel of a company, the rest BOG is returned to the LNG system for continuous liquefaction, and nitrogen in the BOG circulates in the liquefaction system, so that energy consumption is lost. In addition, the BOG in the liquefaction plant usually contains about 4% by mol of helium, and has helium extraction conditions. Therefore, helium is extracted and nitrogen in BOG is fractionated, so that the problems existing in the existing production are solved, and the purpose of extracting helium can be achieved.
In view of this, the utility model provides a novel high nitrogen BOG gas helium extraction system.
Disclosure of Invention
The utility model aims to provide a high nitrogen BOG gas helium extraction system which can fractionate nitrogen in BOG during helium extraction, so that the problems existing in the existing production are solved, the purpose of helium extraction can be achieved, and the system has the effects of simplicity in operation, stability and energy conservation.
The utility model provides a high nitrogen BOG gas helium extraction system which comprises a catalytic dehydrogenation mechanism, a low-temperature rectification crude helium extraction mechanism and a low-temperature PSA adsorption high-purity helium extraction mechanism which are connected in sequence.
Preferably, the catalytic dehydrogenation mechanism comprises a BOG gasifier, a liquid oxygen gasifier, a catalytic dehydrogenation reactor, a separation tank and an adsorption dryer, wherein the BOG gasifier and the liquid oxygen gasifier are respectively communicated with the top of the catalytic dehydrogenation reactor, and the catalytic dehydrogenation reactor, the separation tank and the adsorption dryer are sequentially communicated.
As the preferred mode of this technical scheme, catalytic dehydrogenation mechanism still includes first compressor, first forced air cooling machine and second forced air cooling machine, the BOG gasifier first compressor first forced air cooling machine with catalytic dehydrogenation reactor communicates in proper order, catalytic dehydrogenation reactor second forced air cooling machine with the knockout drum communicates in proper order.
As the technical scheme, preferably, the low-temperature rectification crude helium extraction mechanism comprises a high-temperature cold box, a low-temperature cold box, a first rectification tower and a second rectification tower which are sequentially communicated, wherein a gas outlet of the adsorption dryer is communicated with an inlet of the high-temperature cold box, and the tops of the first rectification tower and the second rectification tower are reversely communicated with the high-temperature cold box; and a coarse helium outlet of the high-temperature cold box is communicated with the low-temperature PSA adsorption high-purity helium extraction mechanism.
Preferably, the low-temperature rectification crude helium extraction mechanism further comprises a circulating refrigeration compressor, a heat exchanger and a refrigerator, wherein the refrigerant outlets of the circulating refrigeration compressor, the refrigerator and the high-temperature cold box are communicated with the heat exchanger; the refrigerator is communicated with the cold energy inlet of the high-temperature cold box.
As the technical scheme, preferably, the circulating refrigeration compressor comprises a second compressor, a third air cooler, a third compressor and a fourth air cooler which are communicated in sequence, wherein the fourth air cooler is communicated with the high-temperature inlet end of the heat exchanger, and the low-temperature outlet end of the heat exchanger is communicated with the refrigerator.
Preferably, a throttle valve is further arranged outside the low-temperature cold box, and a refrigerant outlet of the low-temperature cold box, the throttle valve and the low-temperature cold box are sequentially communicated.
Preferably, as the technical scheme, a baffle plate is arranged at the inlet of the separation tank, and a silk screen layer is arranged at the middle upper part of the separation tank.
Preferably, in the technical scheme, two adsorption dryers are arranged in parallel.
As the technical scheme, the nitrogen outlet containing a small amount of methane of the high-temperature cold box is communicated with the flare tower.
The high nitrogen BOG gas helium extraction system provided by the utility model has at least the following effects:
the high nitrogen BOG gas helium extraction system comprises a catalytic dehydrogenation mechanism, a low-temperature rectification crude helium extraction mechanism and a low-temperature PSA adsorption high-purity helium extraction mechanism which are connected in sequence. Firstly, the BOG gas is subjected to catalytic dehydrogenation treatment, at the moment, hydrogen in the BOG gas is not enriched, the concentration is low and is only about 0.4% (v/v), so that the temperature during catalytic dehydrogenation is about 80 ℃, the operation of a catalytic dehydrogenation reactor is more beneficial, and the problems that crude helium is extracted by a cryogenic method and then catalytic dehydrogenation is carried out, and the concentration of hydrogen in the crude helium is high and the catalytic reaction temperature is high are effectively solved. After catalytic dehydrogenation treatment, the low-temperature rectification crude helium extraction mechanism comprising two stages of rectification towers is used for carrying out low-temperature rectification, the concentration of crude helium obtained by the first rectification tower can reach more than 95%, the residual hydrogen and oxygen content are less and can be lower than 0.1ppm (volume content), the method is more beneficial to extracting helium with higher purity, most nitrogen in BOG gas can be removed by the second rectification tower, and a small part of nitrogen can be further removed by the low-temperature PSA adsorption high-purity extraction mechanism, so that nitrogen is prevented from circulating in a liquefied system of LNG along with BOG, and the energy consumption of the LNG liquefied system is further reduced. Therefore, the high nitrogen BOG gas helium extraction system can extract helium and fractionate nitrogen in BOG, solves the problems existing in the existing production, can achieve the purpose of extracting helium, and has the effects of simplicity in operation, stability and energy conservation.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present utility model, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic illustration of a catalytic dehydrogenation mechanism according to the present utility model;
FIG. 2 is a schematic diagram of a cryogenic rectification crude helium extraction mechanism of the present utility model;
FIG. 3 is a flow chart of the helium extraction of the high nitrogen BOG gas of the present utility model.
Reference numerals illustrate:
1: a BOG gasifier; 2: a liquid oxygen gasifier; 3: a catalytic dehydrogenation reactor; 4: a separation tank; 5: an adsorption dryer; 6: a first compressor; 7: a first air cooling machine; 8: a second air cooling machine; 9: a high temperature cold box; 10: a low-temperature cold box; 11: a first rectifying column; 12: a second rectifying column; 13: a low temperature PSA adsorption high purity helium extraction mechanism; 14: a heat exchanger; 15: a refrigerating machine; 16: a second compressor; 17: a third air cooling machine; 18: a third compressor; 19: a fourth air cooling machine; 20: a throttle valve; 21: and a flare stack.
Detailed Description
The technical solutions of the present utility model will be clearly and completely described in connection with the embodiments, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
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 of the described features. In the description of the present utility model, the meaning of "a plurality" is two or more, unless explicitly defined otherwise. Furthermore, the terms "mounted," "connected," "coupled," and "connected" 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 utility model will be understood in specific cases by those of ordinary skill in the art.
As shown in fig. 1-3, the present embodiment provides a high nitrogen BOG gas helium extraction system comprising a catalytic dehydrogenation mechanism, a low temperature rectification crude helium extraction mechanism and a low temperature PSA adsorption high purity helium extraction mechanism 13 connected in sequence.
Firstly, the catalytic dehydrogenation mechanism is used for carrying out catalytic dehydrogenation treatment on the BOG gas, at the moment, hydrogen in the BOG gas is not enriched yet, the concentration is low and is only about 0.4% (v/v), so that the temperature during catalytic dehydrogenation is about 80 ℃, the operation of the catalytic dehydrogenation reactor 3 is more beneficial, and the problems that crude helium is extracted by a deep cooling method and then catalytic dehydrogenation is carried out, and the concentration of hydrogen in the crude helium is high and the catalytic reaction temperature is high are effectively solved.
After catalytic dehydrogenation treatment, the low-temperature rectification crude helium extraction mechanism comprising two stages of rectification towers is used for low-temperature rectification, the concentration of crude helium obtained by the first rectification tower 11 can reach more than 95%, the residual hydrogen and oxygen content is less and can be lower than 0.1ppm (volume content), the method is more beneficial to extracting helium with higher purity, most nitrogen in BOG gas can be removed by the second rectification tower 12, and a small part of nitrogen can be further removed by the low-temperature PSA adsorption high-purity helium extraction mechanism 13, so that nitrogen is prevented from circulating in a liquefied system of LNG along with BOG, and the energy consumption of the LNG liquefied system is further reduced.
Finally, the crude helium is further purified using a low temperature PSA adsorption high purity helium extraction mechanism 13 to extract high purity helium.
Therefore, the high nitrogen BOG gas helium extraction system can extract helium and fractionate nitrogen in BOG, solves the problems existing in the existing production, can achieve the purpose of extracting helium, and has the effects of simplicity in operation, stability and energy conservation.
As shown in fig. 1, the catalytic dehydrogenation mechanism specifically includes a BOG gasifier 1, a liquid oxygen gasifier 2, a catalytic dehydrogenation reactor 3, a separation tank 4 and an adsorption dryer 5, wherein the BOG gasifier 1 and the liquid oxygen gasifier 2 are respectively communicated with the top of the catalytic dehydrogenation reactor 3, and the catalytic dehydrogenation reactor 3, the separation tank 4 and the adsorption dryer 5 are sequentially communicated.
In the catalytic dehydrogenation mechanism of this embodiment, BOG raw gas from the original BOG fuel gas pipeline is mixed with a proper amount of oxygen and then enters the catalytic dehydrogenation reactor 3, so that hydrogen in the BOG gas is completely reacted, components in the gas after the catalytic reaction include methane, helium, a very small amount of oxygen, water and nitrogen, the gas after the catalytic reaction is cooled and enters the separation tank 4 for gas-liquid separation, and finally enters the adsorption dryer 5 for dehydration.
The temperature of the BOG gas generated in the LNG storage tank is lower and can reach 160 ℃ below zero, so that the temperature of the BOG gas needs to be raised to be more than 5 ℃ through the BOG gasifier 1, and the BOG compressor is prevented from being damaged due to low medium temperature. Similarly, the liquid oxygen is gasified to 5 ℃ or higher by using the liquid oxygen gasifier 2.
On the basis of the technical scheme, the catalytic dehydrogenation mechanism further comprises a first compressor 6, a first air cooling machine 7 and a second air cooling machine 8, wherein the BOG gasifier 1, the first compressor 6, the first air cooling machine 7 and the catalytic dehydrogenation reactor 3 are sequentially communicated, and the catalytic dehydrogenation reactor 3, the second air cooling machine 8 and the separation tank 4 are sequentially communicated.
The BOG gas gasified by the BOG gasifier 1 is pressurized to about 8bar by the first compressor 6, then is processed to the ambient temperature by the first air cooler 7, and finally the pretreated BOG gas and oxygen enter the catalytic dehydrogenation reactor 3 together. In the catalytic dehydrogenation reactor 3 of the present embodiment, the catalytic dehydrogenation temperature is around 80 ℃, which is more advantageous for the operation of the catalytic dehydrogenation reactor 3. The components in the gas after dehydrogenation reaction comprise methane, helium, a very small amount of oxygen, water and nitrogen, the mixed gas is cooled by an air cooler and enters a separation tank 4 for gas-liquid separation, and finally enters an adsorption dryer 5 for dehydration.
The utility model does not strictly limit the specific structure of the separating tank 4, but in order to effectively separate gas from liquid and improve the gas-liquid separation effect, a baffle plate can be arranged at the inlet of the separating tank 4, and a silk screen layer is arranged at the middle upper part of the separating tank 4 so as to realize primary water removal.
The utility model is not strictly limited to the specific type of the adsorption dryer 5, and specifically can adopt a 4A molecular sieve for adsorption and dehydration, so that the water content is reduced to below 1ppm (volume content), and the dew point is less than-76 ℃. In order to facilitate continuous operation of the system, two adsorption dryers 5 may be arranged in parallel, and when one is in dehydration, the other may be subjected to molecular sieve regeneration at about 200 ℃.
As shown in fig. 2, the cryogenic rectification crude helium extraction mechanism of the present embodiment includes a high-temperature cold box 9, a cryogenic cold box 10, a first rectification tower 11 and a second rectification tower 12 which are sequentially communicated, a gas outlet of the adsorption dryer 5 is communicated with an inlet of the high-temperature cold box 9, and tops of the first rectification tower 11 and the second rectification tower 12 are reversely communicated with the high-temperature cold box 9; the crude helium outlet of the high temperature cold box 9 is communicated with the low temperature PSA adsorption high purity helium extraction mechanism 13.
The system adopts a process of continuously rectifying two towers of a two-stage cold box with one-stage throttling and depressurization after the single-cycle mixed refrigerant is combined with the pre-cooling of the refrigerator 15, so that the cold quantity of distillate is recycled, and the system is simple in operation, stable and energy-saving.
The temperature of the high-temperature cold box 9 is about-150 ℃ to-155 ℃, the temperature of the low-temperature cold box 10 is about-160 ℃ to-165 ℃, cold energy in two temperature intervals is fully utilized according to a temperature gradient, the temperature of the BOG gas is changed, and finally the BOG gas subjected to cooling treatment sequentially enters the first rectifying tower 11 and the second rectifying tower 12.
The concentration of the crude helium obtained by the treatment of the first rectifying tower 11 can reach more than 95%, the content of residual hydrogen and oxygen is less, and the content of residual hydrogen and oxygen can be lower than 0.1ppm (volume content), thereby being more beneficial to extracting helium with higher purity. In the prior art, the catalytic dehydrogenation is carried out after the low-temperature rectification, the hydrogen content is lower than 1ppm (volume content), but the hydrogen content cannot reach the content of the utility model, and the residual content of oxygen is higher and higher along with the lower hydrogen content, thus providing a barrier for the subsequent low-temperature PSA extraction of helium with higher purity.
The second rectifying tower 12 is used for removing most of nitrogen in the BOG gas, and most of nitrogen containing a small amount of methane has low recycling value and can be directly sent to the flare tower 21 for burning; and a small amount of nitrogen can be further removed by the low-temperature PSA adsorption high-purity helium extraction mechanism 13, so that nitrogen is prevented from being recycled with the BOG back to the LNG liquefaction system, and the energy consumption of the LNG liquefaction system is further reduced.
On the basis of the above technical solution, it is further preferred that the cryogenic rectification crude helium extraction mechanism further includes a circulating refrigeration compressor, a heat exchanger 14 and a refrigerator 15 to continuously provide cold for the high-temperature cold box 9 and the low-temperature cold box 10, specifically, refrigerant outlets of the circulating refrigeration compressor, the refrigerator 15 and the high-temperature cold box 9 are all communicated with the heat exchanger 14; the refrigerator 15 is communicated with a cold energy inlet of the high-temperature cold box 9. The circulating refrigeration compressor specifically comprises a second compressor 16, a third air cooler 17, a third compressor 18 and a fourth air cooler 19 which are sequentially communicated, the fourth air cooler 19 is communicated with the high-temperature inlet end of the heat exchanger 14, and the low-temperature outlet end of the heat exchanger 14 is communicated with the refrigerator 15.
When in use, the refrigerant is compressed and cooled by the second compressor 16, the third air cooler 17, the third compressor 18 and the fourth air cooler 19 in sequence, enters the heat exchanger 14, exchanges heat with the refrigerant returned by the high-temperature cold box 9, enters the refrigerator 15 for precooling, and then enters the high-temperature cold box 9 and the low-temperature cold box 10 for providing cold energy for the high-temperature cold box 9 and the low-temperature cold box 10. When the cold energy is used up, the refrigerant enters the heat exchanger 14 from the outlet of the high-temperature cold box 9 to carry out heat exchange with the compressed refrigerant, after heat exchange, the refrigerant enters the circulating refrigeration compressor again to repeat the process.
On the basis of the above technical solution, more preferably, a throttle valve 20 is further disposed outside the cryocooler 10, and the refrigerant outlet of the cryocooler 10, the throttle valve 20, and the cryocooler 10 are sequentially connected. That is, after the refrigerant is used by the cryocooler 10, the refrigerant is depressurized and cooled by the throttle valve 20 and then returns to the cryocooler 10, and the pressure and the temperature of the refrigerant during the return are reduced to a greater extent, so that more cold energy can be provided for the cryocooler 10. The refrigerant used by the low-temperature cold box 10 can also be returned to the high-temperature cold box 9 for recycling, so that the low-temperature cold box 10 is reversely communicated with the high-temperature cold box 9.
The utility model does not strictly limit the composition of the refrigerant, and the mixed gas of methane and nitrogen with the volume ratio of 7:3 is preferable, so that compared with the traditional 100 percent nitrogen or methane, the mixed gas has more remarkable effect. Meanwhile, the circulating refrigerant is precooled by combining the refrigerator 15, so that the pressure of the refrigerator 15 is only 13bar, and the BOG gas from catalytic dehydrogenation is only about 6bar, thereby effectively reducing the power consumption of the compressor.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.

Claims (8)

1. The high nitrogen BOG gas helium extraction system is characterized by comprising a catalytic dehydrogenation mechanism, a low-temperature rectification crude helium extraction mechanism and a low-temperature PSA adsorption high-purity helium extraction mechanism (13) which are connected in sequence;
the catalytic dehydrogenation mechanism comprises a BOG gasifier (1), a liquid oxygen gasifier (2), a catalytic dehydrogenation reactor (3), a separation tank (4) and an adsorption dryer (5),
the BOG gasifier (1) and the liquid oxygen gasifier (2) are respectively communicated with the top of the catalytic dehydrogenation reactor (3), and the catalytic dehydrogenation reactor (3), the separation tank (4) and the adsorption dryer (5) are sequentially communicated;
the low-temperature rectification crude helium extraction mechanism comprises a high-temperature cold box (9), a low-temperature cold box (10), a first rectification tower (11) and a second rectification tower (12) which are sequentially communicated;
the gas outlet of the adsorption dryer (5) is communicated with the inlet of the high-temperature cold box (9), and the tops of the first rectifying tower (11) and the second rectifying tower (12) are reversely communicated with the high-temperature cold box (9); the crude helium outlet of the high-temperature cold box (9) is communicated with the low-temperature PSA adsorption high-purity helium extraction mechanism (13).
2. The helium extraction system of claim 1, wherein the catalytic dehydrogenation mechanism further comprises a first compressor (6), a first air cooler (7) and a second air cooler (8),
BOG gasifier (1) first compressor (6) first forced air cooling machine (7) with catalytic dehydrogenation reactor (3) communicate in proper order, catalytic dehydrogenation reactor (3) second forced air cooling machine (8) with knockout drum (4) communicate in proper order.
3. The high nitrogen BOG gas helium extraction system of claim 2, wherein the cryogenic rectification crude helium extraction mechanism further comprises a cyclic refrigeration compressor, a heat exchanger (14) and a refrigerator (15);
the refrigerant outlets of the circulating refrigeration compressor, the refrigerator (15) and the high-temperature cold box (9) are communicated with the heat exchanger (14); the refrigerator (15) is communicated with a cold energy inlet of the high-temperature cold box (9).
4. A high nitrogen BOG gas helium extraction system according to claim 3, wherein said cyclic refrigeration compressor comprises a second compressor (16), a third air cooler (17), a third compressor (18), a fourth air cooler (19) in communication in sequence;
the fourth air cooler (19) is communicated with the high-temperature inlet end of the heat exchanger (14), and the low-temperature outlet end of the heat exchanger (14) is communicated with the refrigerator (15).
5. The high nitrogen BOG gas helium extraction system of claim 4, wherein a throttle valve (20) is further arranged outside said cryogenic refrigerator (10), and a refrigerant outlet of said cryogenic refrigerator (10), said throttle valve (20) and said cryogenic refrigerator (10) are sequentially communicated.
6. The high nitrogen BOG gas helium extraction system according to claim 1, wherein a baffle plate is arranged at the inlet of the separation tank (4), and a wire mesh layer is arranged at the middle upper part of the separation tank (4).
7. The high nitrogen BOG gas helium extraction system according to claim 1, wherein the adsorption dryer (5) is provided with two in parallel.
8. Helium extraction system according to claim 1, characterized in that the low methane nitrogen outlet of the high temperature cold box (9) is in communication with a flare stack (21).
CN202223286572.XU 2022-12-07 2022-12-07 High nitrogen BOG gas helium extraction system Active CN219199732U (en)

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