System for extracting hydrogen from BDO production discharge flare gas

Abstract

The utility model relates to a flare gas hydrogen extraction system for BDO production and emission, which comprises a BDO flare gas pipeline, a high-purity hydrogen pipeline, a hydrogen-poor retentate gas pipeline, and a buffer tank, a cyclone separator, a high-efficiency coalescer, a membrane separator and a PSA (Pressure Swing Adsorption) device which are sequentially communicated through pipelines to form a circulation loop, one end of the BDO torch gas pipeline is communicated with a pipeline communicated between the buffer tank and the PSA device; one end of the high-purity hydrogen pipeline is communicated with the bottom of the PSA device, and the other end is communicated with a hydrogen net; one end of the hydrogen-poor retentate gas pipeline is communicated with the top of the membrane separator, and the other end of the hydrogen-poor retentate gas pipeline is communicated with a gas pipe network. The device has the beneficial effects that the structure is simple, the design is reasonable, the flare gas is subjected to a combined process of coarse separation of the buffer tank, the cyclone separator, the coalescer, the membrane separator and PSA (Pressure Swing Adsorption) purification, high-purity hydrogen which can be used for producing and recycling is finally recovered, the hydrogen concentration of the flare gas is reduced, and the safety risk of flare combustion is further reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of hydrogen recovery, in particular to a hydrogen extraction system for the flare gas discharged in BDO production. Background Technique

[0002] At present, most of the BDO production gases are directly sent to the flare for combustion due to the reduction of hydrogen content (volume fraction is 30%-40%, the same below). Because hydrogen is easy to explode, there are safety risks when sent to the flare for co-combustion; secondly, hydrogen is a high-quality energy source that can be utilized. If it can be recovered to the greatest extent, it will greatly save production costs.

[0003] The main processes for hydrogen purification include membrane separation, PSA, cryogenic separation, etc. Among them, membrane separation and PSA are more widely used. The biggest advantage of PSA is that it can produce high-purity hydrogen, and the hydrogen purity can reach more than 99.99%. However, its hydrogen recovery rate is relatively low, and the hydrogen content in the desorbed gas is usually higher than 40.00%, and sometimes as high as 60.00%. The high-concentration hydrogen in the desorbed gas is discharged into the gas network, resulting in a large waste of hydrogen resources. The membrane separation technology is simple and flexible in operation, has a relatively wide selectivity for raw materials, and can process hydrogen with a hydrogen content of 20.00%-90.00% in the raw materials. However, due to the limitation of membrane performance, when the raw material hydrogen purity is relatively low, the product gas purity is difficult to meet the purity requirements of the refinery hydrogen network.

[0004] A single hydrogen recovery technology often fails to achieve the purpose of high efficiency and high recovery rate. It is necessary to combine the characteristics of various hydrogen recovery technologies, and through two or more recovery technologies, carry out cascade separation on the refinery hydrogen-rich gas to achieve efficient and high-recovery hydrogen purification and recovery. Content of the Utility Model

[0005] The utility model provides a hydrogen extraction system for the flare gas discharged in BDO production, aiming to solve the problems in the prior art.

[0006] The technical solution of the utility model to solve the above technical problems is as follows:

[0007] A hydrogen extraction system for the flare gas discharged in BDO production includes a BDO flare gas pipeline, a high-purity hydrogen pipeline, a hydrogen-depleted permeate pipeline, and a buffer tank, a cyclone separator, a high-efficiency coalescer, a membrane separator, and a PSA device that are sequentially connected through pipelines to form a circulation loop. One end of the BDO flare gas pipeline is connected to the pipeline communicating between the buffer tank and the PSA device; one end of the high-purity hydrogen pipeline is connected to the bottom of the PSA device, and the other end is used to connect to the hydrogen network; one end of the hydrogen-depleted permeate pipeline is connected to the top of the membrane separator, and the other end is used to connect to the gas network.

[0008] The beneficial effects of the present utility model are as follows: During the treatment process, the flare gas discharged from BDO production (containing a certain amount of water and oil) and the desorbed gas discharged from the PSA unit are homogenously mixed through a buffer tank; the mixed gas is sent to a cyclone separator to preliminarily remove larger water and oil droplets, and then to a high-efficiency coalescer to effectively remove the fine water and oil mists entrained in the gas; after the high-efficiency coalescer, it enters a membrane separator. After the mixed gas passes through membrane separation, the lean hydrogen retentate gas is sent to the gas network flare for combustion, and the permeate gas after rough separation by the membrane is sent to the PSA unit for hydrogen purification; after being treated by the PSA unit, high-purity hydrogen is sent to the hydrogen network for recovery, and the desorbed gas is sent to the buffer tank to be mixed with the flare gas.

[0009] The structure of the present utility model is simple and the design is reasonable. The flare gas undergoes a combined process of buffer tank + cyclone separator + coalescer + rough separation by membrane separator + PSA purification, and finally high-purity hydrogen that can be used for production reuse is recovered, reducing the hydrogen concentration in the flare gas and further reducing the safety risk of flare combustion.

[0010] On the basis of the above technical solution, the present utility model can also be improved as follows.

[0011] Further, a PSA inlet compressor is fixedly installed on the pipeline connecting the membrane separator and the PSA unit.

[0012] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The PSA inlet compressor is used to boost the mixed gas to meet the PSA inlet pressure condition.

[0013] Further, a permeate gas cooler is also fixedly installed on the pipeline connecting the membrane separator and the PSA unit, and the permeate gas cooler is located between the membrane separator and the PSA inlet compressor.

[0014] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The permeate gas cooler is used to cool the permeate gas to below 40°C.

[0015] Further, a mixed gas compressor is fixedly installed on the pipeline connecting the buffer tank and the cyclone separator.

[0016] The beneficial effect of adopting the above further solution is that the mixed gas compressor boosts the mixed gas to a set pressure to meet the treatment conditions.

[0017] Further, the mixed gas compressor boosts the mixed gas to 1.0 - 4.0 MPa.

[0018] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The mixed gas compressor boosts the mixed gas to a set pressure.

[0019] Further, an intake air heater is fixedly installed on the pipeline connecting the high-efficiency coalescer and the membrane separator.

[0020] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. An intake air heater is arranged after the high-efficiency coalescer, so that the mixed gas entering the membrane separator is far from the dew point, further ensuring that the water and oil mist that are not completely separated are condensed on the membrane surface, causing permanent damage to the membrane, and improving the separation performance of the membrane.

[0021] Further, the intake air heater heats the mixed gas to 73 - 93 °C.

[0022] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The temperature of the mixed gas is heated to 73 - 93 °C, so that the mixed gas entering the membrane separator is far from the dew point, further ensuring that the water and oil mist that are not completely separated are condensed on the membrane surface, causing permanent damage to the membrane, and improving the separation performance of the membrane.

[0023] Further, a raffinate cooler is fixedly installed on the pipeline of the lean hydrogen raffinate gas.

[0024] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The raffinate cooler cools the raffinate gas to below 40 °C.

[0025] Further, the raffinate cooler cools the permeate gas to below 40 °C.

[0026] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The raffinate cooler cools the raffinate gas to below 40 °C.

[0027] Further, an analysis gas compressor is fixedly installed on the pipeline connecting the buffer tank and the PSA device.

[0028] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The PSA analysis gas compressor boosts the analysis gas to the set pressure, that is, the same pressure as the BDO flare gas. Description of the Drawings

[0029] Figure 1 It is a structural schematic diagram of the present utility model.

[0030] In the drawings, the list of components represented by each reference numeral is as follows:

[0031] 1. Buffer tank; 2. Mixed gas compressor; 3. Cyclone separator; 4. High-efficiency coalescer; 5. Intake air heater; 6. Membrane separator; 7. Raffinate cooler; 8. Permeate cooler; 9. PSA intake compressor; 10. PSA device; 11. Analysis gas compressor; 12. BDO flare gas pipeline; 13. High-purity hydrogen gas pipeline; 14. Lean hydrogen raffinate gas pipeline. Detailed implementation manners

[0032] It should be noted that, without conflict, the embodiments in the present utility model and the features in the embodiments may be combined with each other.

[0033] In the description of the present utility model, it should be understood that the orientation or positional relationship indicated by the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation to the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first", "second", etc. may explicitly or implicitly include one or more of such features. In the description of the present utility model, unless otherwise specified, the meaning of "a plurality" is two or more.

[0034] In the description of the present utility model, it should be noted that unless otherwise clearly specified and defined, the terms "installation", "connection", and "connection" should be understood in a broad sense. For example, it may be a fixed connection, a detachable connection, or an integral connection; it may be a mechanical connection or an electrical connection; it may be directly connected, or indirectly connected through an intermediate medium, and it may be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present utility model can be understood through specific situations.

[0035] The present utility model will be described in detail below with reference to the drawings and in combination with embodiments.

[0036] Embodiment 1

[0037] As Figure 1 shown, this embodiment provides a hydrogen stripping system for BDO production discharge flare gas, including a BDO flare gas pipeline 12, a high-purity hydrogen gas pipeline 13, a hydrogen-deficient raffinate gas pipeline 14, and a buffer tank 1, a cyclone separator 3, a high-efficiency coalescer 4, a membrane separator 6, and a PSA device 10 that are connected in sequence through pipelines to form a circulation loop. One end of the BDO flare gas pipeline 12 is connected to the pipeline communicating between the buffer tank 1 and the PSA device 10; one end of the high-purity hydrogen gas pipeline 13 is connected to the bottom of the PSA device 10, and the other end is used to connect to the hydrogen network; one end of the hydrogen-deficient raffinate gas pipeline 14 is connected to the top of the membrane separator 6, and the other end is used to connect to the gas pipeline network.

[0038] During the treatment process, the flare gas discharged from BDO production (containing a certain amount of water and oil) and the desorbed gas discharged from the PSA unit are homogenously mixed through the buffer tank 1; the mixed gas is sent to the cyclone separator 3 to preliminarily remove larger water and oil droplets, and then the fine water and oil mists entrained in the gas are effectively removed by the high-efficiency coalescer 4; after the high-efficiency coalescer 4, it enters the membrane separator 6. After the mixed gas passes through membrane separation, the lean hydrogen retentate gas is sent to the gas network flare through the BDO flare gas pipeline 12 for combustion, and the permeate gas after rough membrane separation is sent to the PSA unit 10 for hydrogen purification; after being treated by the PSA unit 10, the high-purity hydrogen is sent to the hydrogen network for recovery through the high-purity hydrogen pipeline 13, and the desorbed gas is sent to the buffer tank to be mixed with the flare gas.

[0039] In the chemical field, BDO refers to 1,4-butanediol (Butane-1,4-diol), whose chemical formula is C4H 10 O2, and its molecular weight is 90.12. BDO is an important basic organic chemical raw material with a wide range of uses, including but not limited to the production of spandex, cosmetics, biodegradable materials, lithium battery solvents and other products.

[0040] Flare gas refers to the flammable and explosive gas generated during the chemical production process. These gases cannot be directly utilized during normal production and need to be treated through the flare system. The main purpose of the flare system is to safely burn and discharge these gases into the atmosphere to prevent their accumulation from causing safety accidents.

[0041] It should be noted that the above buffer tank 1, cyclone separator 3, high-efficiency coalescer 4, membrane separator 6 and PSA unit 10 respectively adopt existing technologies, and their specific structures and principles will not be elaborated here.

[0042] Preferably, in this embodiment, the filter element of the above high-efficiency coalescer 4 adopts a cylindrical fiber structure, with a total of 9 layers from the inside to the outside in the gas flow direction. The pores of the 1st to 2nd layers are relatively large, the pores of the 3rd to 7th layers are relatively small, and the 8th to 9th layers are similar to the 1st to 2nd layers. The filtration accuracy requirement of the high-efficiency coalescer 4 reaches 0.01μm, and the residual oil content is less than 0.01mg / m 3 .

[0043] Preferably, in this embodiment, the membrane separator 6 can be an organic polymer membrane, with a material of polyimide, and the separation performance, mechanical performance and chemical stability of the membrane are relatively high.

[0044] In this embodiment, taking the hydrogen content in the raw material as 40%, the hydrogen content in the permeate gas is more than 90%, and the hydrogen content in the retentate gas is about 20%. The permeate gas recovery rate (permeate gas hydrogen amount / raw material gas hydrogen amount) is more than 63%.

[0045] Preferably, in this embodiment, the PSA device 10 is used to increase the hydrogen concentration in the membrane permeate gas. The high-purity hydrogen is sent to the hydrogen network for recovery. After the desorbed gas is pressurized by a compressor, it is sent to the buffer tank to be mixed with the flare gas. The hydrogen concentration can reach over 99% after PSA purification.

[0046] The structure of this embodiment is simple and reasonably designed. The flare gas passes through a combined process of buffer tank + cyclone separator + coalescer + rough separation by membrane separator + PSA purification, and finally high-purity hydrogen that can be used for production reuse is recovered, reducing the hydrogen concentration in the flare gas and further reducing the safety risk of flare combustion.

[0047] Embodiment 2

[0048] Based on Embodiment 1, in this embodiment, a PSA inlet compressor 9 is fixedly installed on the pipeline connecting the membrane separator 6 and the PSA device 10.

[0049] This solution has a simple structure and is reasonably designed. The PSA inlet compressor 9 is used to pressurize the mixed gas to meet the PSA inlet pressure conditions.

[0050] Based on the above solution, the full name of the above PSA is: Pressure Swing Adsorption, and its Chinese meaning is: Pressure Swing Adsorption. PSA is a new gas separation technology.

[0051] It should be noted that the above PSA inlet compressor 9 adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0052] Embodiment 3

[0053] Based on Embodiment 2, in this embodiment, a permeate gas cooler 8 is also fixedly installed on the pipeline connecting the membrane separator 6 and the PSA device 10, and the permeate gas cooler 8 is located between the membrane separator 6 and the PSA inlet compressor 9.

[0054] This solution has a simple structure and is reasonably designed. The permeate gas cooler 8 is used to cool the permeate gas to below 40°C.

[0055] Preferably, in this embodiment, the permeate gas cooler 8 cools the permeate gas to below 40°C.

[0056] It should be noted that the above permeate gas cooler 8 adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0057] Embodiment 4

[0058] Based on the above embodiments, in this embodiment, a mixed gas compressor 2 is fixedly installed on the pipeline connecting the buffer tank 1 and the cyclone separator 3.

[0059] The mixed gas compressor boosts the mixed gas to a set pressure to meet the processing conditions.

[0060] It should be noted that the above-mentioned mixed gas compressor 2 adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0061] Example 5

[0062] Based on Example 4, in this example, the mixed gas compressor 2 boosts the mixed gas to 1.0 - 4.0 MPa.

[0063] This solution has a simple structure and reasonable design. The mixed gas compressor 2 boosts the mixed gas to the set pressure.

[0064] Preferably, in this example, the above-mentioned mixed gas compressor 2 boosts the mixed gas to 2.5 MPa.

[0065] Example 6

[0066] Based on the above embodiments, in this example, an intake air heater 5 is fixedly installed on the pipeline connecting the high-efficiency coalescer 4 and the membrane separator 6.

[0067] This solution has a simple structure and reasonable design. The intake air heater 5 is arranged after the high-efficiency coalescer 4, so that the mixed gas entering the membrane separator 6 is far from the dew point, further ensuring that the unseparated water and oil mist are condensed on the membrane surface to cause permanent damage to the membrane, and improving the separation performance of the membrane.

[0068] It should be noted that the above-mentioned intake air heater 5 adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0069] Example 7

[0070] Based on Example 6, in this example, the intake air heater 5 heats the mixed gas to 73 - 93 °C.

[0071] This solution has a simple structure and reasonable design. The mixed gas is heated to 73 - 93 °C, so that the mixed gas entering the membrane separator 6 is far from the dew point, further ensuring that the unseparated water and oil mist are condensed on the membrane surface to cause permanent damage to the membrane, and improving the separation performance of the membrane.

[0072] Example 8

[0073] Based on the above embodiments, in this example, a raffinate gas cooler 7 is fixedly installed on the raffinate gas pipeline 14.

[0074] This solution has a simple structure and reasonable design. The raffinate gas cooler cools the raffinate gas to below 40 °C.

[0075] It should be noted that the raffinate gas cooler 7 described above adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0076] In addition, the above-mentioned lean hydrogen raffinate gas refers to the gas that fails to pass through the membrane and is retained on the high-pressure side during the membrane separation process.

[0077] Example 9

[0078] Based on Example 8, in this example, the raffinate gas cooler 7 cools the permeate gas to below 40°C.

[0079] This solution has a simple structure and reasonable design. The raffinate gas cooler 7 cools the raffinate gas to below 40°C.

[0080] Example 10

[0081] Based on the above-mentioned various examples, in this example, an analysis gas compressor 11 is fixedly installed on the pipeline connecting the buffer tank 1 and the PSA device 10.

[0082] This solution has a simple structure and reasonable design. The PSA analysis gas compressor 11 pressurizes the analysis gas to the set pressure, that is, the same pressure as the BDO flare gas.

[0083] It should be noted that the above-mentioned analysis gas compressor 11 adopts the existing technology, and its specific structure and principle will not be elaborated here.

[0084] The working principle of the present utility model is as follows:

[0085] BDO production discharge flare gas (containing a certain amount of water and oil) and the analysis gas discharged from the PSA device 10 are homogenously mixed through the buffer tank 1; after the mixed gas is pressurized by the mixed gas compressor 2, it is sent to the cyclone separator 3 to preliminarily remove larger water and oil droplets, and then the fine water and oil mists entrained in the gas are effectively removed by the high-efficiency coalescer 4; an intake heater 5 is arranged after the high-efficiency coalescer 4 to make the mixed gas entering the membrane separator 6 far from the dew point, further ensuring that the water and oil mists that are not completely separated condense on the membrane surface and cause permanent damage to the membrane, and improving the separation performance of the membrane. After the mixed gas passes through the membrane separation, the lean hydrogen raffinate gas is cooled by the raffinate gas cooler 7 and then sent to the gas network flare for combustion. The permeate gas after rough membrane separation is cooled by the permeate gas cooler 8, pressurized by the PSA intake compressor 9, and then sent to the PSA device 10 for hydrogen purification; after being processed by the PSA device 10, high-purity hydrogen is sent to the hydrogen network for recovery, and the analysis gas is pressurized by the PSA analysis gas compressor 11 and then sent to the buffer tank 1 to be mixed with the flare gas.

[0086] The utility model relates to a hydrogen extraction system for BDO production discharge flare gas. Through this system, high-purity hydrogen that can be used for production reuse is finally recovered, the hydrogen concentration in the flare gas is reduced, and thus the safety risk of flare combustion is reduced. Its characteristic is to use a combined process system of buffer tank + cyclone separator + coalescer + membrane separator rough separation + PSA purification for hydrogen purification and recovery of BDO flare gas. The hydrogen extraction system for flare gas mainly includes a buffer tank, a compressor, a cyclone separator, a coalescer, a heater, a membrane separator, a cooler, a PSA, pipelines, a control system, etc. The high-purity hydrogen after PSA treatment is sent to the hydrogen network for recovery, and the PSA desorbed gas is returned to the front end of the process to be mixed with the flare gas; the hydrogen-depleted retentate gas separated by the membrane system is sent to the gas network flare for combustion.

[0087] Compared with the current wastewater treatment technologies at home and abroad, the hydrogen extraction system provided by the utility model has the following advantages and positive effects:

[0088] (1) The combined process of cyclone separator + high-efficiency coalescer before the membrane system can minimize the water and oil content in the flare gas and ensure the stable operation of the subsequent process system.

[0089] (2) A single hydrogen recovery technology often fails to achieve the purpose of high efficiency and high recovery rate. It is necessary to combine the characteristics of various hydrogen recovery technologies and perform cascade separation of refinery hydrogen-rich gas through two or more recovery technologies. The combined use of membrane separation and PSA technology can achieve high-efficiency and high-recovery hydrogen purification and recovery, with obvious advantages.

[0090] (3) Calculated based on the hydrogen content in the raw material being 40%, the hydrogen content in the permeate gas of the membrane system is above 90%, the hydrogen content in the retentate gas is about 20%, and the permeate gas recovery rate (permeate gas hydrogen volume / raw material gas hydrogen volume) is above 63%; the hydrogen concentration can reach above 99% after PSA purification, fully meeting the production use.

[0091] (4) The hydrogen membrane separation technology has the advantages of small floor area, moderate investment, simple operation, low operating cost, etc. With the membrane separator placed in front, it has the characteristics of simple and flexible operation and relatively wide selectivity for raw materials, and can process mixed gases with a hydrogen content of 20.00% - 90.00% in the raw material gas. Therefore, it is suitable for hydrogen recovery of mixed gases with a relatively low hydrogen content in similar BDO flare gas.

[0092] (5) PSA is widely used in industries such as chemical production. For example, the existing PSA device has design margin that can be utilized. The hydrogen content in the PSA desorbed gas is usually higher than 40.00%. In this process scheme, the desorbed gas is returned to the front end of the process to be mixed with the flare gas to ensure the maximum recovery of hydrogen.

[0093] It should be noted that all the electronic components involved in the present utility model adopt the prior art, and the above-mentioned components are electrically connected to the controller, and the control circuit between the controller and each component is the prior art.

[0094] For those skilled in the art, it is obvious that the present utility model is not limited to the details of the above-mentioned exemplary embodiments, and without departing from the spirit or basic characteristics of the present utility model, the present utility model can be implemented in other specific forms. Therefore, from any point of view, the embodiments should be regarded as exemplary and non-restrictive. The scope of the present utility model is defined by the appended claims rather than the above description. Therefore, all changes falling within the meaning and scope of the equivalent elements of the claims are intended to be included in the present utility model. Any reference signs in the claims should not be regarded as limiting the claimed rights.

[0095] In addition, it should be understood that although this specification is described according to the embodiments, not every embodiment only contains an independent technical solution. This narrative way of the specification is only for clarity. Those skilled in the art should regard the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

[0096] The above are only the preferred embodiments of the present utility model and are not intended to limit the present utility model. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present utility model shall be included in the protection scope of the present utility model.

Claims

1. A hydrogen stripping system for the flare gas discharged in BDO production, characterized in that: It includes a BDO flare gas pipeline (12), a high-purity hydrogen gas pipeline (13), a hydrogen-depleted raffinate gas pipeline (14), and a buffer tank (1), a cyclone separator (3), a high-efficiency coalescer (4), a membrane separator (6), and a PSA unit (10) that are connected in sequence through pipelines to form a circulation loop. One end of the BDO flare gas pipeline (12) is connected to the pipeline that communicates between the buffer tank (1) and the PSA unit (10); one end of the high-purity hydrogen gas pipeline (13) is connected to the bottom of the PSA unit (10), and the other end is used to connect to the hydrogen network; one end of the hydrogen-depleted raffinate gas pipeline (14) is connected to the top of the membrane separator (6), and the other end is used to connect to the gas pipeline network.

2. The hydrogen stripping system for the flare gas discharged in BDO production according to claim 1, wherein: A PSA inlet compressor (9) is fixedly installed on the pipeline that communicates between the membrane separator (6) and the PSA unit (10).

3. The hydrogen stripping system for BDO production exhaust flare gas according to claim 2, characterized in that: An permeate gas cooler (8) is also fixedly installed on the pipeline that communicates between the membrane separator (6) and the PSA unit (10), and the permeate gas cooler (8) is located between the membrane separator (6) and the PSA inlet compressor (9).

4. The hydrogen stripping system for the BDO production exhaust flare according to any one of claims 1 to 3, characterized in that: A mixed gas compressor (2) is fixedly installed on the pipeline that communicates between the buffer tank (1) and the cyclone separator (3).

5. The hydrogen stripping system for the flare gas discharged in BDO production according to claim 4, wherein: The mixed gas compressor (2) pressurizes the mixed gas to 1.0 - 4.0 MPa.

6. The hydrogen stripping system for the flare gas discharged from BDO production according to any one of claims 1-3, characterized in that: An inlet gas heater (5) is fixedly installed on the pipeline that communicates between the high-efficiency coalescer (4) and the membrane separator (6).

7. The hydrogen stripping system for the BDO production exhaust flare according to claim 6, wherein: The inlet gas heater (5) heats the mixed gas to 73 - 93 °C.

8. The hydrogen stripping system for the flare gas discharged during BDO production according to any one of claims 1-3, characterized in that: A raffinate gas cooler (7) is fixedly installed on the hydrogen-depleted raffinate gas pipeline (14).

9. The hydrogen stripping system for the flare gas discharged during BDO production according to claim 8, characterized in that: The raffinate gas cooler (7) cools the permeate gas to below 40 °C.

10. The hydrogen stripping system for the flare gas discharged during BDO production according to any one of claims 1-3, characterized in that: An analytical gas compressor (11) is fixedly installed on the pipeline that communicates between the buffer tank (1) and the PSA unit (10).

Images