CN219526260U - System for simultaneously extracting helium and hydrogen from BOG - Google Patents
System for simultaneously extracting helium and hydrogen from BOG Download PDFInfo
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- CN219526260U CN219526260U CN202320110250.5U CN202320110250U CN219526260U CN 219526260 U CN219526260 U CN 219526260U CN 202320110250 U CN202320110250 U CN 202320110250U CN 219526260 U CN219526260 U CN 219526260U
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- 239000001307 helium Substances 0.000 title claims abstract description 140
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 140
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 140
- 239000001257 hydrogen Substances 0.000 title claims abstract description 49
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 49
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 239000012528 membrane Substances 0.000 claims abstract description 206
- 238000000926 separation method Methods 0.000 claims abstract description 202
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 124
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- 238000012544 monitoring process Methods 0.000 claims description 31
- 238000004458 analytical method Methods 0.000 claims description 8
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- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a system for simultaneously extracting helium and hydrogen from BOG. The system comprises a first membrane separation system, a pressure swing adsorption purification system and a hydrogen adsorption system which are sequentially connected through pipelines; the first membrane separation system is configured to remove or partially remove the non-permeate gas in the BOG to obtain permeate gas; the pressure swing adsorption purification system is configured to treat the permeate gas to produce a resolved gas and a non-resolved gas; the hydrogen adsorption system is configured to treat the non-resolved gas to produce helium and hydrogen. The utility model perfectly combines membrane separation, pressure swing adsorption and hydrogen adsorption technologies to produce high-purity helium and high-purity hydrogen.
Description
Technical Field
The utility model belongs to the technical field of helium separation and purification, and relates to a system for simultaneously extracting helium and hydrogen from BOG.
Background
Helium (He) is a rare gas, colorless and odorless, and has inactive chemical properties, so that the helium is difficult to react with other substances in a general state; is one of the indispensable rare resources of national defense and military industry and high-tech industry development, is widely applied to the high-tech fields of semiconductor manufacture, aerospace, medical and health and the like, and the market demand is gradually expanded.
Helium is mainly distributed in the mantle, air, ore and natural gas. The helium content in the air is very small and is only 5ppm; in helium-enriched natural gas, the concentration of helium is 0.02% -5%, namely 200-50000 mmp. Thus, the extraction of helium from natural gas is a major industrial source thereof.
Liquefied natural gas (Liquefied Natural Gas, LNG for short) is a form of natural gas, the main component of which is methane, and is recognized as the cleanest fossil energy source on earth. Colorless, odorless, nontoxic and noncorrosive, and has a volume of about 1/625 of the volume of the same amount of gaseous natural gas, and the mass of liquefied natural gas is only about 45% of the same volume of water. During LNG production from LNG plants, a certain amount of Boil Off Gas (BOG) is produced. Helium is present in BOG at a higher concentration (up to 15%). The BOG mainly comprises He (boiling point: 268.9 ℃) and CH 4 (boiling point: 161.5 ℃ C.) N 2 (boiling point: 195.8 ℃ C.) H 2 (boiling point: 253 ℃ C.) O 2 (boiling point: minus 183 ℃ C.), ar (boiling point: minus 185.9 ℃ C.), etc.
Currently, the main methods for extracting helium from natural gas are a Pressure Swing Adsorption (PSA) method, an absorption method, a membrane separation method and a cryogenic method. The pressure swing adsorption method uses molecular sieve as adsorbent and adopts the principle of separating gas mixture by utilizing the difference of adsorption property of molecular sieve to different gas molecules. The membrane separation method utilizes the characteristic that some metal membranes or organic membranes have selective permeation and diffusion to some gas components to achieve the purposes of gas separation and purification. The method takes the partial pressure difference of the gases at two sides of the membrane as the driving force, and realizes the separation by the steps of dissolution, diffusion, permeation, desorption and the like to generate the difference of the transfer rates among the components. The cryogenic process, also called low temperature condensation adsorption process, is a process for extracting helium by cryogenic distillation, which is generally provided by atmospheric liquid nitrogen, and can produce helium with purity of 99.99%. The pressure swing adsorption method and the membrane separation method do not need low-temperature condensation and then gas separation, so the method is superior to the cryogenic method in energy consumption and material consumption.
Hydrogen (H) 2 ) Is a simple substance formed by hydrogen element, and the hydrogen gas is colorless, odorless, extremely easy to burn and difficult to dissolve in water at normal temperature and normal pressure. The industry generally produces hydrogen from natural gas or water gas without the use of high energy-consuming methods of water electrolysis.
Since helium and hydrogen can both be extracted from natural gas, there can be a system or method to simultaneously extract and separate the two gases from the natural gas byproduct BOG
Disclosure of Invention
In order to solve the technical problems, the utility model discloses a system for simultaneously extracting helium and hydrogen from BOG, which comprises a first membrane separation system, a pressure swing adsorption purification system and a hydrogen adsorption system which are sequentially connected through pipelines; the first membrane separation system is configured to remove or partially remove the non-permeate gas in the BOG to obtain permeate gas; the pressure swing adsorption purification system is configured to treat the permeate gas to produce a resolved gas and a non-resolved gas; the hydrogen adsorption system is configured to treat the non-resolved gas to produce helium and hydrogen.
In some embodiments, the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device, a secondary compressor connected in sequence by a conduit; the air inlet of the primary membrane separation device is used for accessing BOG to be processed; the air outlet of the secondary compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; the resolved gas outlet of the pressure swing adsorption purification system is connected with the gas inlet of the secondary membrane separation device through a pipeline.
In some embodiments, the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device, a secondary compressor, a tertiary membrane separation device, and a tertiary compressor connected in sequence by piping; the air inlet of the primary membrane separation device is used for accessing BOG to be processed; the air outlet of the three-stage compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; the non-permeate gas outlet of the three-stage membrane separation device is connected with the gas inlet of the two-stage membrane separation device through a pipeline; the resolved gas outlet of the pressure swing adsorption purification system is connected with the gas inlet of the three-stage membrane separation device through a pipeline.
In some embodiments, the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device, a secondary compressor, a tertiary membrane separation device, and a tertiary compressor, and a first valve, a second valve, a third valve, a fourth valve, and a fifth valve, connected in sequence by piping; the air inlet of the primary membrane separation device is used for accessing BOG to be processed; the air outlet of the three-stage compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; the non-permeate gas outlet of the three-stage membrane separation device is connected with the gas inlet of the two-stage membrane separation device through a pipeline and a first valve 4; the analytic gas outlet of the pressure swing adsorption purification system is connected with the gas inlet of the three-stage membrane separation device through a pipeline and a second valve 10; the resolved gas outlet of the pressure swing adsorption purification system is also connected with the gas inlet of the secondary membrane separation device through a pipeline and a third valve 11; the secondary membrane separation device is connected with the secondary compressor through a pipeline and a fourth valve 5; the second-stage membrane separation device is connected with the third-stage compressor through a pipeline and a fifth valve 7;
the workflow of the first membrane separation system is set to: under the condition that the helium concentration in the BOG is more than or equal to 50000mmp, the first valve 4, the fourth valve 5 and the second valve 10 are closed, the third valve 11 and the fifth valve 7 are opened, so that the permeate gas obtained by the secondary membrane separation device directly enters a tertiary compressor, and the permeate gas of the pressure swing adsorption purification system returns to the air inlet of the secondary membrane separation device for recycling and repeating treatment; under the condition that the helium concentration in the BOG is less than 50000mmp, the first valve 4, the fourth valve 5 and the second valve 10 are opened, the third valve 11 and the fifth valve 7 are closed, so that the permeate gas obtained by the secondary membrane separation device enters the secondary compressor, the non-permeate gas obtained by the tertiary membrane separation device returns to the air inlet of the secondary membrane separation device for recovery and reprocessing, and the analysis gas of the pressure swing adsorption purification system returns to the air inlet of the tertiary membrane separation device for recovery and reprocessing.
In some embodiments, a helium concentration monitoring system is also included for monitoring the concentration of helium in the BOG entering the primary membrane separation unit.
In some embodiments, the system further comprises a control system in communication with the helium concentration monitoring system, wherein the control system is configured to control opening and closing of the first valve, the second valve, the third valve, the fourth valve and the fifth valve according to the helium concentration in the BOG monitored by the helium concentration monitoring system, so as to help complete the workflow of the first membrane separation system, specifically:
under the condition that the helium concentration monitoring system monitors that the helium concentration in the BOG is more than or equal to 50000mmp, the control system closes the first valve 4, the fourth valve 5 and the second valve 10, and opens the third valve 11 and the fifth valve 7, so that the permeate gas obtained by the secondary membrane separation device directly enters the tertiary compressor, and the analysis gas of the pressure swing adsorption purification system returns to the air inlet of the secondary membrane separation device for recycling and repeating treatment; under the condition that the helium concentration monitoring system monitors that the helium concentration in the BOG is less than 50000mmp, the control system opens the first valve 4, the fourth valve 5 and the second valve 10, closes the third valve 11 and the fifth valve 7, so that the penetrating gas obtained by the secondary membrane separation device enters the secondary compressor, the non-penetrating gas obtained by the tertiary membrane separation device returns to the air inlet of the secondary membrane separation device for recycling and reprocessing, and the analyzing gas of the pressure swing adsorption purification system returns to the air inlet of the tertiary membrane separation device for recycling and reprocessing.
In some embodiments, a second membrane separation system and an LNG plant are also included; the second membrane separation system is connected with the first membrane separation system through the LNG factory, so that the helium-containing natural gas is concentrated through the second membrane separation system and then is subjected to BOG (boil off gas) treatment through the LNG factory for the first membrane separation system, the pressure swing adsorption purification system and the hydrogen adsorption system, namely, the BOG is a byproduct generated when the helium-containing natural gas is concentrated through the second membrane separation system and then is subjected to LNG preparation through the LNG factory.
In some embodiments, the second membrane separation system comprises a primary membrane separation system, a compressor of the second membrane separation system, and a secondary membrane separation system connected in sequence by piping, further comprising a sixth valve and a seventh valve; the sixth valve is arranged on a connecting pipeline between the primary membrane separation system and the LNG factory; the seventh valve is arranged on a connecting pipeline of the compressors of the first membrane separation system and the second membrane separation system;
the helium concentration monitoring system is also used for monitoring the concentration of helium in helium-containing natural gas entering the primary membrane separation system; the control system is also used for controlling the opening and closing of the sixth valve and the seventh valve according to the helium concentration in the helium-containing natural gas monitored by the helium concentration monitoring system, so as to help to complete the working flow of the second membrane separation system, and specifically comprises the following steps:
under the condition that the helium concentration monitoring system monitors that the helium concentration in the helium-containing natural gas is more than or equal to 500ppm, the control system closes the seventh valve and opens the sixth valve, so that the helium-containing natural gas directly enters the LNG factory through the primary membrane separation system; and under the condition that the helium concentration monitoring system monitors that the helium concentration in the helium-containing natural gas is greater than or equal to 200ppm and less than 500ppm, the control system closes the sixth valve and opens the seventh valve, so that the helium-containing natural gas enters the LNG factory through the first-stage membrane separation system and the second-stage membrane separation system through the compressor of the second-stage membrane separation system.
In some embodiments, the primary membrane separation system may concentrate helium from 5 to 10 times.
In some embodiments, the primary membrane separation system and the secondary membrane separation system cooperate to concentrate helium by a factor of 10 to 40.
In some embodiments, the compressor, primary compressor, secondary compressor, tertiary compressor of the second membrane separation system, respectively, may compress the gas such that the inlet pressure of the secondary membrane is 0.2MPa above the inlet pressure of the primary membrane, and so on.
The beneficial effects of the utility model include:
1. the utility model perfectly combines membrane separation, pressure swing adsorption and hydrogen adsorption technologies to produce high-purity helium and high-purity hydrogen.
2. Compared with the traditional technology, the technology has better economical efficiency, particularly under the condition of higher hydrogen concentration, avoids a plurality of unfavorable places of catalytic combustion dehydrogenation, burns off the hydrogen, and can produce high-purity helium and high-purity hydrogen.
3. The operation temperature of the membrane separation in the utility model is 40-60 ℃, preferably 50 ℃, the temperature is high in efficiency, the temperature is low, and the separation effect is good. The temperature is between 40 and 60 ℃, the temperature is mild, the control is easy, and the safety is ensured.
4. The helium concentration in the BOG and the helium concentration in the helium-containing natural gas are doubly selected, and the helium concentration monitoring system and the control system are arranged, so that the method can automatically treat different helium-containing natural gases and BOGs.
5. The concentration of helium in natural gas is increased by 5-10 times through primary membrane separation, the volume is reduced to 1/5-1/10 of the original volume, the natural gas is used as raw material gas to enter an LNG factory for producing LNG, and the BOG gas concentration is 5-10 times that of the natural gas directly used as the raw material.
6. The helium concentration in the natural gas is increased by 10-40 times through the secondary membrane separation, the volume is reduced to 1/10-1/40 of the original volume, the natural gas is used as the raw material gas to enter an LNG factory for producing LNG, and the BOG gas concentration is 10-40 times that of the natural gas directly used as the raw material.
7. Compared with the technology of directly extracting helium from natural gas, the technology can greatly reduce helium extracting cost, and normal use of the original natural gas is not affected. Is suitable for the situation that the natural gas quantity is 5 to 10 times or 10 to 40 times larger than the treatment capacity of the LNG factory.
8. Once the technology is popularized, the problems of low helium concentration and high helium extraction cost in natural gas in China can be solved, and the technology is economically feasible for extracting helium from natural gas with helium concentration of more than 500ppm or more than 200ppm and less than 500 ppm.
9. The helium recovery rate of the utility model is more than 95%; the pressure of the natural gas is less than 10Mpa, and the pressure is 1.0-2.0 Mpa in the subsequent treatment process after BOG is formed; the flow rate is not limited.
LNG plants vary in LNG capacity depending on the scale, but have an upper limit ranging from 4 to 400 kilocubic meters per day, so the extraction of helium from natural gas is limited by LNG capacity. The utility model not only perfectly combines membrane separation, pressure swing adsorption and hydrogen adsorption technologies to produce high purity helium and high purity hydrogen, but also extracts helium from natural gas source, and skillfully combines with the downstream LNG factory, so that the natural gas treatment capacity is 5-10 times, even 10-40 times of the original LNG factory treatment capacity, and the efficiency is greatly improved.
The conception, specific structure, and technical effects of the present utility model will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present utility model.
Drawings
Fig. 1 is a schematic diagram of a system for simultaneously extracting helium and hydrogen from BOG according to embodiment 1 of the present utility model.
Fig. 2 is a schematic diagram of a system for simultaneously extracting helium and hydrogen from BOG according to embodiment 2 of the present utility model.
Detailed Description
The utility model is further described with reference to the following detailed description in order to make the technical means, the inventive features, the achieved objects and the effects of the utility model easy to understand. The present utility model is not limited to the following examples.
It should be understood that the structures, proportions, sizes, etc. shown in the drawings are for illustration purposes only and should not be construed as limiting the utility model to the extent that it can be practiced, since modifications, changes in the proportions, or otherwise, used in the practice of the utility model, are not intended to be critical to the essential characteristics of the utility model, but are intended to fall within the spirit and scope of the utility model.
"LNG" is natural gas that is generally known to include a high percentage of methane. LNG may also include trace amounts of other compounds or elements such as ethane, propane, butane, carbon dioxide, nitrogen, helium, hydrogen sulfide, or combinations thereof. LNG plants process natural gas to remove one or more components (e.g., helium) or impurities (e.g., water and/or heavy hydrocarbons) and then condense to a liquid by cooling at near atmospheric pressure when producing LNG.
"Natural gas" refers to a multi-component gas obtained from a crude oil well or a subterranean gas producing formation. The composition and pressure of natural gas can vary significantly. Typical natural gas contains methane as a major component, i.e. the methane content exceeds 50%. Natural gas may also contain ethane, higher molecular weight hydrocarbons (e.g., C 3 -C 20 Hydrocarbon), one or more acid gases (e.g., carbon dioxide or hydrogen sulfide), or any combination thereof. Natural gas may also include small amounts of magazines such as water, nitrogen, iron sulfide, wax, crude oil, or any combination thereof.
Example 1
Fig. 1 shows a system for simultaneously extracting helium and hydrogen from BOG of the present embodiment, which includes a first membrane separation system, a pressure swing adsorption purification system 12, and a hydrogen adsorption system 13, which are sequentially connected by pipes, and a helium concentration monitoring system and a control system in communication with the helium concentration monitoring system.
The first membrane separation system is configured to remove or partially remove the non-permeate gas in the BOG to obtain permeate gas; the pressure swing adsorption purification system 12 is configured to treat the permeate gas to produce a resolved gas and a non-resolved gas; the hydrogen adsorption system 13 is configured to treat the non-resolved gas to produce helium and hydrogen, i.e., high purity helium and high purity hydrogen in fig. 1.
The first membrane separation system comprises a first-stage membrane separation device 1, a first-stage compressor 2, a second-stage membrane separation device 3, a second-stage compressor 6, a third-stage membrane separation device 8 and a third-stage compressor 9 which are sequentially connected through pipelines, and a first valve 4, a second valve 10, a third valve 11, a fourth valve 5 and a fifth valve 7. The air inlet of the primary membrane separation device 1 is used for accessing BOG to be processed; the air outlet of the three-stage compressor 9 is connected with the air inlet of the pressure swing adsorption purification system 12; the non-permeate gas outlet of the secondary membrane separation device 3 is connected with the gas inlet of the primary membrane separation device 1 through a pipeline; the non-permeate gas outlet of the three-stage membrane separation device 8 is connected with the gas inlet of the two-stage membrane separation device 3 through a pipeline and a first valve 4; the resolved gas outlet of the pressure swing adsorption purification system 12 is connected with the gas inlet of the three-stage membrane separation device 8 through a pipeline and a second valve 10; the resolved gas outlet of the pressure swing adsorption purification system 12 is also connected with the gas inlet of the secondary membrane separation device 3 through a pipeline and a third valve 11; the secondary membrane separation device 3 is connected with the secondary compressor 6 through a pipeline and a fourth valve 5; the secondary membrane separation device 3 is connected with the tertiary compressor 9 through a pipeline and a fifth valve 7.
And the helium concentration monitoring system is used for monitoring the concentration of helium in the BOG entering the primary membrane separation device. The control system is used for controlling the opening and closing of the first valve 4, the second valve 10, the third valve 11, the fourth valve 5 and the fifth valve 7 according to the helium concentration in the BOG monitored by the helium concentration monitoring system, so as to help to complete the working flow of the first membrane separation system, specifically:
under the condition that the helium concentration monitoring system monitors that the helium concentration in the BOG is more than or equal to 50000mmp, the control system closes the first valve 4, the fourth valve 5 and the second valve 10, and opens the third valve 11 and the fifth valve 7, so that the permeate gas obtained by the secondary membrane separation device 3 directly enters the tertiary compressor 9, and the analysis gas of the pressure swing adsorption purification system 12 returns to the air inlet of the secondary membrane separation device 3 for recycling and repeating treatment; under the condition that the helium concentration monitoring system monitors that the helium concentration in the BOG is less than 50000mmp, the control system opens the first valve 4, the fourth valve 5 and the second valve 10, closes the third valve 11 and the fifth valve 7, so that the permeate gas obtained by the secondary membrane separation device 3 enters the secondary compressor 6, the non-permeate gas obtained by the tertiary membrane separation device 8 returns to the air inlet of the secondary membrane separation device 3 for recovery and reprocessing, and the analysis gas of the pressure swing adsorption purification system 12 returns to the air inlet of the tertiary membrane separation device 8 for recovery and reprocessing.
Example 2
Fig. 2 shows the system of this embodiment for simultaneously extracting helium and hydrogen from BOG, including a second membrane separation system and LNG plant 14 in addition to the components included in embodiment 1; the second membrane separation system is connected with the first membrane separation system through the LNG factory 14, so that the helium-containing natural gas is concentrated through the second membrane separation system and then is subjected to BOG (boil off gas) treatment through the LNG factory 14 for the first membrane separation system, the pressure swing adsorption purification system 12 and the hydrogen adsorption system 13, namely, the BOG is a byproduct generated when the helium-containing natural gas is concentrated through the second membrane separation system and then is subjected to LNG preparation through the LNG factory 14.
The second membrane separation system comprises a first membrane separation system 19, a compressor 16 of the second membrane separation system and a second membrane separation system 15 which are sequentially connected through pipelines, and further comprises a sixth valve 18 and a seventh valve 17; a sixth valve 18 is provided on a connection pipe of the primary membrane separation system 19 and the LNG plant 14; the seventh valve 17 is arranged on a connecting pipeline between the first membrane separation system 19 and the compressor 16 of the second membrane separation system;
the helium concentration monitoring system is also used for monitoring the concentration of helium in helium-containing natural gas entering the primary membrane separation system; the control system is further configured to control opening and closing of the sixth valve 18 and the seventh valve 17 according to the helium concentration in the helium-containing natural gas monitored by the helium concentration monitoring system, so as to help complete the workflow of the second membrane separation system, specifically:
under the condition that the helium concentration monitoring system monitors that the helium concentration in the helium-containing natural gas is greater than or equal to 500ppm, the control system closes the seventh valve 17 and opens the sixth valve 18, so that the helium-containing natural gas directly enters the LNG plant 14 through the primary membrane separation system 19; in the case where the helium concentration monitoring system monitors that the helium concentration in the helium-containing natural gas is greater than or equal to 200ppm but less than 500ppm, the control system closes the sixth valve 18 and opens the seventh valve 17 so that the helium-containing natural gas enters the LNG plant 14 through the primary membrane separation system 19 via the compressor 16 of the secondary membrane separation system and the secondary membrane separation system 15.
The primary membrane separation system 19 may concentrate helium by a factor of 5 to 10. The primary membrane separation system 19 and the secondary membrane separation system 15 cooperate to concentrate helium by a factor of 10 to 40. The compressor 16, the primary compressor 2, the secondary compressor 6, the tertiary compressor 9 of the second membrane separation system may compress the gas, respectively, such that the inlet pressure of the secondary membrane is 0.2MPa higher than the inlet pressure of the primary membrane, and so on.
Example 3
The embodiment relates to a method for simultaneously extracting helium and hydrogen from BOG, which comprises the following steps:
s1, introducing BOG into a primary membrane separation device to obtain permeation gas with non-permeation gas removed completely or partially;
s2, pressurizing the permeate gas obtained in the step S1 by using a first-stage compressor, and then enabling the permeate gas to enter a second-stage membrane separation device to obtain permeate gas and non-permeate gas separated by the second-stage membrane separation device;
s3, pressurizing the permeate gas separated by the secondary membrane separation device through a secondary compressor, and then entering the tertiary membrane separation device to obtain permeate gas and non-permeate gas separated by the tertiary membrane separation device; returning the non-permeate gas separated by the secondary membrane separation device to the air inlet of the primary membrane separation device in the step S1, and repeating the steps S1-S3;
s4, pressurizing the permeate gas separated by the three-stage membrane separation device by a three-stage compressor, and then enabling the permeate gas to enter a pressure swing adsorption purification system to obtain non-resolved gas and resolved gas; returning the analysis gas to the gas inlet of the three-stage membrane separation device in the step S3, and repeating the steps S3 and S4;
s5, separating helium and hydrogen from the non-resolved gas through a hydrogen adsorption system.
The method for acquiring the BOG comprises the following steps:
1) Concentrating helium-containing natural gas by membrane separation helium, and removing or partially removing non-permeable gas to obtain product gas;
2) The product gas obtained in the step 1) is used for LNG production in an LNG factory, and BOG is obtained;
step 1) two cases of treatment:
a) Under the condition that the helium concentration in the helium-containing natural gas is more than or equal to 500ppm, carrying out membrane separation and helium concentration on the helium-containing natural gas through a primary membrane separation system, and removing or partially removing non-permeable gas to obtain product gas;
b) Under the condition that the helium concentration in the helium-containing natural gas is more than or equal to 200ppm and less than 500ppm, removing or partially removing the non-permeable gas separated by the primary membrane separation system after the helium-containing natural gas passes through the primary membrane separation system, then compressing the non-permeable gas by a compressor of the secondary membrane separation system, and entering the secondary membrane separation system to perform membrane separation helium concentration to obtain product gas; and recycling the non-permeate gas separated by the primary membrane separation system and re-entering the primary membrane separation system for treatment.
The compressor, the primary compressor, the secondary compressor and the tertiary compressor of the second membrane separation system can compress the gas respectively, so that the inlet pressure of the secondary membrane is 0.2MPa higher than the inlet pressure of the primary membrane, and so on. The helium recovery of this example was greater than 95%; the pressure of the natural gas is less than 10Mpa, and the pressure is 1.0-2.0 Mpa in the subsequent treatment process after BOG is formed; the operation temperature is about 50 ℃; the flow rate is not limited.
The foregoing describes in detail preferred embodiments of the present utility model. It should be understood that numerous modifications and variations can be made in accordance with the concepts of the utility model without requiring creative effort by one of ordinary skill in the art. Therefore, all technical solutions which can be obtained by logic analysis, reasoning or limited experiments based on the prior art by the person skilled in the art according to the inventive concept shall be within the scope of protection defined by the claims.
Claims (8)
1. The system for simultaneously extracting helium and hydrogen from BOG is characterized by comprising a first membrane separation system, a pressure swing adsorption purification system and a hydrogen adsorption system which are sequentially connected through pipelines; the first membrane separation system is configured to remove or partially remove the non-permeate gas in the BOG to obtain permeate gas; the pressure swing adsorption purification system is configured to treat the permeate gas to produce a resolved gas and a non-resolved gas; the hydrogen adsorption system is configured to treat the non-resolved gas to produce helium and hydrogen.
2. The system for simultaneously extracting helium and hydrogen from BOG according to claim 1, wherein the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device and a secondary compressor which are sequentially connected through pipelines; the air inlet of the primary membrane separation device is used for accessing the BOG to be processed; the air outlet of the secondary compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; and an analysis gas outlet of the pressure swing adsorption purification system is connected with a gas inlet of the secondary membrane separation device through a pipeline.
3. The system for simultaneously extracting helium and hydrogen from BOG according to claim 1, wherein the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device, a secondary compressor, a tertiary membrane separation device and a tertiary compressor which are sequentially connected through pipes; the air inlet of the primary membrane separation device is used for accessing the BOG to be processed; the air outlet of the three-stage compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; the non-permeate gas outlet of the three-stage membrane separation device is connected with the gas inlet of the two-stage membrane separation device through a pipeline; and an analysis gas outlet of the pressure swing adsorption purification system is connected with a gas inlet of the three-stage membrane separation device through a pipeline.
4. The system for simultaneously extracting helium and hydrogen from BOG according to claim 1, wherein the first membrane separation system comprises a primary membrane separation device, a primary compressor, a secondary membrane separation device, a secondary compressor, a tertiary membrane separation device, and a tertiary compressor, and a first valve, a second valve, a third valve, a fourth valve, and a fifth valve, which are sequentially connected through pipes; the air inlet of the primary membrane separation device is used for accessing the BOG to be processed; the air outlet of the three-stage compressor is connected with the air inlet of the pressure swing adsorption purification system; the non-permeate gas outlet of the secondary membrane separation device is connected with the gas inlet of the primary membrane separation device through a pipeline; the non-permeate gas outlet of the three-stage membrane separation device is connected with the gas inlet of the two-stage membrane separation device through a pipeline and the first valve; the analytic gas outlet of the pressure swing adsorption purification system is connected with the gas inlet of the three-stage membrane separation device through a pipeline and a second valve; the resolved gas outlet of the pressure swing adsorption purification system is also connected with the gas inlet of the secondary membrane separation device through a pipeline and a third valve; the secondary membrane separation device is connected with the secondary compressor through a pipeline and the fourth valve; the secondary membrane separation device is connected with the tertiary compressor through a pipeline and the fifth valve.
5. The system for simultaneously extracting helium and hydrogen from BOG of claim 4, further comprising a helium concentration monitoring system for monitoring the concentration of helium in BOG entering said primary membrane separation unit.
6. The system for simultaneously extracting helium and hydrogen from BOG of claim 5, further comprising a control system in communication with said helium concentration monitoring system for controlling the opening and closing of said first valve, said second valve, said third valve, said fourth valve and said fifth valve based on the concentration of helium in BOG monitored by said helium concentration monitoring system to thereby assist in completing the workflow of said first membrane separation system.
7. The system for simultaneously extracting helium and hydrogen from BOG of claim 6, further comprising a second membrane separation system and an LNG plant; the second membrane separation system is connected with the first membrane separation system through the LNG factory, so that helium-containing natural gas is concentrated by the second membrane separation system and then passes through the LNG factory to obtain the BOG for treatment by the first membrane separation system, the pressure swing adsorption purification system and the hydrogen adsorption system, namely the BOG is a byproduct generated when the helium-containing natural gas is concentrated by the second membrane separation system and then passes through the LNG factory to prepare LNG.
8. The system for simultaneously extracting helium and hydrogen from BOG according to claim 7, wherein the second membrane separation system comprises a primary membrane separation system, a compressor of the second membrane separation system and a secondary membrane separation system which are sequentially connected through a pipeline, and further comprises a sixth valve and a seventh valve; the sixth valve is arranged on a connecting pipeline between the primary membrane separation system and the LNG factory; the seventh valve is arranged on a connecting pipeline of the compressor of the first membrane separation system and the second membrane separation system;
the helium concentration monitoring system is also used for monitoring the concentration of helium in helium-containing natural gas entering the primary membrane separation system; the control system is also used for controlling the opening and closing of the sixth valve and the seventh valve according to the helium concentration in the helium-containing natural gas monitored by the helium concentration monitoring system, so as to help to complete the working flow of the second membrane separation system.
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