A device for tail gas treatment in a methanol steam reforming hydrogen production process

Abstract

The utility model belongs to tail gas treatment technical field, specifically disclose a kind of tail gas treatment device for hydrogen production in methanol steam reforming process, including the methanol steam reforming hydrogen production microreactor for preparing hydrogen gas, the purification device for H2 purification connected with methanol steam reforming hydrogen production microreactor, the H2 collection tank connected with purification device, and the N2 collection tank and CO2 collection tank connected with the tail gas outlet of purification device, the purification device is also connected with H2O adsorption and desorption module, H2O adsorption and desorption module is connected with buffer tank, buffer tank is connected with CO oxidation module, CO oxidation module is connected with CO2 collection tank;Nitrogen purging mechanism is connected on the H2O adsorption and desorption module and CO oxidation module. The tail gas treatment device modularization of the utility model is synergistically designed, optimizes tail gas treatment process, and improves processing efficiency.

Description

Technical Field

[0001] This utility model relates to the field of tail gas treatment technology, and in particular to a tail gas treatment device for the methanol steam reforming hydrogen production process. Background Technology

[0002] CO2 capture, absorption of harmful gases, and reduction of pollutant emissions have become crucial issues. Hydrogen energy, with its significant advantages of being clean and sustainable, is experiencing rapid development. Among various hydrogen production methods, methanol steam reforming exhibits the highest hydrogen production efficiency. Subsequently, the PSA (Power Suppression Allocation) principle is used to purify CO2 from hydrogen through automated adsorption. As the adsorption process continues, the adsorbent gradually approaches saturation. At this point, the adsorbent surface is adsorbed with a large amount of impurities other than H2, including CO2 and small amounts of CO and CH4. To enable the adsorbent to be recycled, a purging and desorption operation is required to remove surface impurities. The hydrogen purification tail gas obtained by nitrogen purging contains H2O, CO2, CO, and N2. This tail gas needs to be treated to obtain CO2 for storage.

[0003] I. Disadvantages of Existing Technologies

[0004] 1. H2O adsorption module

[0005] The adsorbent exhibits poor selectivity, readily adsorbing other gases (such as CO2 and CO), and its adsorption capacity decreases significantly under high humidity or high temperature. Regeneration methods are energy-intensive and easily shorten the adsorbent's lifespan. Insufficient humidity control and the lack of dynamic monitoring and switching mechanisms can lead to a sharp drop in treatment efficiency after the adsorbent becomes saturated.

[0006] 2. CO oxidation module

[0007] Catalysts are susceptible to poisoning, such as deactivation due to contamination by impurities like sulfur and halogens. The wide explosive range of CO and O2 mixtures, coupled with the lack of dynamic explosion-proof control in traditional systems, poses safety hazards. Fluctuations in reaction temperature can easily lead to catalyst sintering or decreased activity, affecting oxidation efficiency.

[0008] 3. CO2 compression and storage module

[0009] Traditional compressors are inefficient, and their energy consumption accounts for a large proportion of the total system energy consumption. Liquid or supercritical CO2 requires equipment with extremely high pressure resistance, and traditional storage tanks are prone to leakage or explosion, posing safety risks. Summary of the Invention

[0010] The purpose of this invention is to address the shortcomings of existing technologies and provide a tail gas treatment device for the methanol steam reforming hydrogen production process.

[0011] To achieve the above objectives, this utility model is implemented according to the following technical solution:

[0012] A tail gas treatment device for a methanol steam reforming hydrogen production process includes a methanol steam reforming hydrogen production microreactor for hydrogen production, a purification device for H2 purification connected to the methanol steam reforming hydrogen production microreactor, an H2 collection tank connected to the purification device, and an N2 collection tank and a CO2 collection tank connected to the tail gas outlet of the purification device. The purification device is also connected to an H2O adsorption-desorption module, which is connected to a buffer tank. The buffer tank is connected to a CO oxidation module, which is connected to a CO2 collection tank. Both the H2O adsorption-desorption module and the CO oxidation module are connected to a nitrogen purging mechanism.

[0013] Furthermore, the H2O adsorption-desorption module includes a low-temperature constant-temperature reaction bath, within which a first 3A molecular sieve adsorption tube and a second 3A molecular sieve adsorption tube are installed. The top of the second 3A molecular sieve adsorption tube is connected to the exhaust gas outlet of the purification device via a pipeline. A first valve and a fourth valve are installed on the pipeline between the exhaust gas outlet of the purification device and the top of the second 3A molecular sieve adsorption tube. A first tee pipe is connected between the first valve and the fourth valve. A second valve is installed at the third port of the first tee pipe, which is then connected to the top of the first 3A molecular sieve adsorption tube via a pipeline. The bottom of the first 3A molecular sieve adsorption tube is connected to a second tee pipe via a pipeline. The second port of the first 3A molecular sieve adsorption tube is connected to the buffer tank via a pipeline after the third valve is installed. The third port of the second 3A molecular sieve adsorption tube is connected to the bottom of the condenser via a pipeline after the seventh valve is installed. The bottom of the second 3A molecular sieve adsorption tube is connected to the third 3A molecular sieve adsorption tube via a pipeline after the fifth valve is installed. The second port of the third 3A molecular sieve adsorption tube is connected to the bottom of the buffer tank via a pipeline after the fifth valve is installed. The third port of the third 3A molecular sieve adsorption tube is connected to the bottom of the condenser via a pipeline after the ninth valve is installed. The top of the condenser is connected to the N2 collection tank via a pipeline. The pipeline between the condenser and the N2 collection tank is equipped with the sixteenth valve. The tops of the first 3A molecular sieve adsorption tube and the second 3A molecular sieve adsorption tube are respectively connected to the inlet of the vacuum pump via pipelines.

[0014] Furthermore, the CO oxidation module includes a constant-temperature reaction bath, within which is a reactor filled with a Pt / Al2O3 honeycomb ceramic catalyst. The inlet of the reactor is connected to the top of a buffer tank via a pipeline, and a tenth valve is installed on the pipeline between the reactor and the top of the buffer tank. The inlet of the reactor is connected to an O2 storage tank via a pipeline, and a nineteenth valve is installed on the pipeline between the inlet of the reactor and the O2 storage tank. The outlet of the reactor is connected to a flame arrester via a pipeline, and an eleventh valve is installed on the pipeline between the flame arrester and the outlet of the reactor. The outlet of the flame arrester is connected to a CO2 collection tank via a pipeline. The top of the reactor is connected to an H2 storage tank via a pipeline, and a twelfth and eighteenth valves are installed on the pipeline between the H2 storage tank and the reactor. The outlet of the reactor is connected to an exhaust pipe, and a thirteenth valve is installed on the exhaust pipe.

[0015] Further, the nitrogen purging mechanism includes a first nitrogen purging mechanism, a second nitrogen purging mechanism, and a third nitrogen purging mechanism; the first nitrogen purging mechanism includes a first N2 storage tank, which is connected via a pipeline to the pipeline between the second valve and the top of the first 3A molecular sieve adsorption tube, and a sixth valve is provided on the pipeline between the first N2 storage tank and the top of the first 3A molecular sieve adsorption tube; the second nitrogen purging mechanism includes a second N2 storage tank, which is connected via a pipeline to the pipeline between the fourth valve and the top of the second 3A molecular sieve adsorption tube, and an eighth valve is provided on the pipeline at the outlet end of the second N2 storage tank; the third nitrogen purging mechanism includes a third N2 storage tank, which is connected via a pipeline between the twelfth valve and the eighteenth valve, and a seventeenth valve is provided on the pipeline at the outlet end of the third N2 storage tank.

[0016] Furthermore, the temperature inside the low-temperature constant-temperature reaction bath is 25-50℃.

[0017] Furthermore, the temperature inside the constant temperature reaction bath is 80-150℃.

[0018] Furthermore, a first flow meter is installed on the pipeline between the second valve and the first 3A molecular sieve adsorption tube, a second flow meter is installed on the pipeline between the second 3A molecular sieve adsorption tube and the fourth valve, and a third flow meter is installed on the pipeline between the tenth valve and the reactor.

[0019] Furthermore, both the first 3A molecular sieve adsorption tube and the second 3A molecular sieve adsorption tube are equipped with a pressure sensor, a temperature sensor, and a humidity sensor.

[0020] Furthermore, the reactor is equipped with pressure sensors and temperature sensors.

[0021] Furthermore, a fifteenth valve is installed on the pipeline between the purification device and the H2 collection tank.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] 1. Modular collaborative design optimizes the exhaust gas treatment process and improves treatment efficiency.

[0024] 2. Setting up two H2O adsorption towers can enable the adsorption process to proceed continuously.

[0025] 3. The modular integrated structure and the low pressure loss of the honeycomb ceramic catalyst significantly reduce energy consumption.

[0026] 4. Explosion-proof design and emergency pressure relief mechanism ensure high safety.

[0027] 5. The buffer tank and back pressure valve are linked to effectively absorb pressure fluctuations between upstream and downstream, improving stability. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of the structure of this utility model. Detailed Implementation

[0029] To make the objectives, technical solutions, and advantages of this utility model clearer, the following detailed description is provided in conjunction with the accompanying drawings and embodiments. The specific embodiments described herein are for illustrative purposes only and are not intended to limit the scope of the utility model.

[0030] like Figure 1 As shown in the figure, this embodiment exemplarily demonstrates a tail gas treatment device for a methanol steam reforming hydrogen production process, including a methanol steam reforming hydrogen production microreactor 1 for hydrogen production, a purification device 2 for H2 purification connected to the methanol steam reforming hydrogen production microreactor 1, an H2 collection tank 3 connected to the purification device 2, a fifteenth valve 1015 provided on the pipeline between the purification device 2 and the H2 collection tank 3, and an N2 collection tank 4 and a CO2 collection tank 5 connected to the tail gas outlet of the purification device 2. The purification device 2 is also connected to an H2O adsorption-desorption module, the H2O adsorption-desorption module is connected to a buffer tank 8, the buffer tank 8 is connected to a CO oxidation module, and the CO oxidation module is connected to the CO2 collection tank 5; both the H2O adsorption-desorption module and the CO oxidation module are connected to a nitrogen purging mechanism.

[0031] Specifically, the H2O adsorption-desorption module includes a low-temperature constant-temperature reaction bath 6. The low-temperature constant-temperature reaction bath 6 contains a first 3A molecular sieve adsorption tube 13 and a second 3A molecular sieve adsorption tube 14. Both the first 3A molecular sieve adsorption tube 13 and the second 3A molecular sieve adsorption tube 14 are equipped with a pressure sensor 10, a temperature sensor 11, and a humidity sensor 12. The top of the second 3A molecular sieve adsorption tube 14 is connected to the exhaust gas outlet of the purification device 2 via a pipeline. A first valve 101 and a fourth valve 104 are installed on the pipeline between the exhaust gas outlet of the purification device 2 and the top of the second 3A molecular sieve adsorption tube 14. A first tee pipe connects the pipeline between the first valve 101 and the fourth valve 104. A second valve 102 is installed at the third port of the first tee pipe, which is then connected to the top of the first 3A molecular sieve adsorption tube 13 via a pipeline. The bottom of adsorption tube 13 is connected to a second three-way pipe via a pipeline. A third valve 103 is installed at the second port of the second three-way pipe, which is then connected to a buffer tank 8 via a pipeline. A seventh valve 107 is installed at the third port of the second three-way pipe, which is then connected to the bottom of the condenser 7 via a pipeline. The bottom of the second 3A molecular sieve adsorption tube 14 is connected to a third three-way pipe via a pipeline. A fifth valve is installed at the second port of the third three-way pipe, which is then connected to the bottom of the buffer tank 8 via a pipeline. A ninth valve 109 is installed at the third port of the third three-way pipe, which is then connected to the bottom of the condenser 7 via a pipeline. The top of the condenser 7 is connected to the N2 collection tank 4 via a pipeline. A sixteenth valve 1 is installed on the pipeline between the condenser 7 and the N2 collection tank 4. The tops of the first 3A molecular sieve adsorption tube 13 and the second 3A molecular sieve adsorption tube 14 are respectively connected to the inlet of the vacuum pump 17 via pipelines. The reaction conditions for the H2O adsorption process in the H2O adsorption-desorption module are as follows:

[0032] 1. Temperature requirement: 25-50℃: Avoid high temperatures that reduce adsorption capacity;

[0033] 2. Pressure requirement: Atmospheric pressure - 0.3 MPa;

[0034] 3. Flow control: ① Space velocity (GHSV: gas volumetric flow rate / adsorbent volume): 500-2000 / h; ② Flow velocity: 0.2-0.5m / s.

[0035] The reaction conditions for the H2O desorption process in the H2O adsorption-desorption module are as follows:

[0036] 1. Introduce desorption gas (nitrogen) at a flow rate of 1 L / min;

[0037] 2. Pressure control is under vacuum, and reaction tube temperature is controlled between 50 and 150°C;

[0038] 3. Real-time detection of exhaust gas using mass spectrometry and gas detection tube (adjust the flow rate of the lower valve of the furnace to 20 ml / min, and detect with a soap bubble flow meter). Desorption is complete when the moisture content is less than 500 ppm.

[0039] The CO oxidation module includes a constant-temperature reaction bath 18, within which is a reactor 19 filled with a Pt / Al2O3 honeycomb ceramic catalyst 15. The reactor 19 is equipped with a pressure sensor 10 and a temperature sensor 11. The inlet of the reactor 19 is connected to the top of a buffer tank 8 via a pipeline. A tenth valve 1010 is installed on the pipeline between the reactor 19 and the top of the buffer tank 8. The inlet of the reactor 19 is connected to an O2 storage tank 16 via a pipeline. A valve is installed on the pipeline between the inlet of the reactor 19 and the O2 storage tank 16. Nineteenth valve 1019; The outlet of reactor 19 is connected to flame arrester 20 via a pipeline. An eleventh valve 1011 is installed on the pipeline between flame arrester 20 and the outlet of reactor 19. The outlet of flame arrester 20 is connected to CO2 collection tank 5 via a pipeline. An H2 storage tank 21 is connected to the top of reactor 19 via a pipeline. Twelfth valve 1012 and eighteenth valve 1018 are installed on the pipeline between H2 storage tank 21 and reactor 19. An exhaust pipe is connected to the outlet of reactor 19, and a thirteenth valve 1013 is installed on the exhaust pipe. The reaction conditions in the CO oxidation module are:

[0040] 1. Temperature requirement: 80-150℃;

[0041] 2. Pressure requirement: Atmospheric pressure - 0.5 MPa;

[0042] 3. Supplement O2: Control the O2 / CO2 ratio to 1.2-1.5;

[0043] 4. Flow control: ① Air velocity: 10000-20000 / h; ② Flow velocity: 1-3m / s.

[0044] Pressure sensor 10 can detect pressure changes in the adsorption tube and oxidation tube, and timely adjustments can be made based on changes in the pressure sensor reading; temperature sensor 11 can detect temperature changes in the adsorption tube and oxidation tube, and timely adjustments can be made based on changes in the temperature sensor reading; humidity sensor 12 can detect changes in the adsorption capacity of 3A molecular sieve in the adsorption tube, thereby enabling timely adjustments to the opening and closing of the valve to ensure the continuous operation of the adsorption process.

[0045] Furthermore, the nitrogen purging mechanism includes a first nitrogen purging mechanism, a second nitrogen purging mechanism, and a third nitrogen purging mechanism; the first nitrogen purging mechanism includes a first N2 storage tank 22, which is connected via a pipeline to the pipeline between the second valve 102 and the top of the first 3A molecular sieve adsorption tube 13, and a sixth valve 106 is provided on the pipeline between the first N2 storage tank 22 and the top of the first 3A molecular sieve adsorption tube 13; the second nitrogen purging mechanism includes a second N2 storage tank 23, which is connected via a pipeline to the pipeline between the fourth valve 104 and the top of the second 3A molecular sieve adsorption tube 14. On the pipeline, an eighth valve 108 is installed at the outlet end of the second N2 storage tank 23; the third nitrogen purging mechanism includes a third N2 storage tank 24, which is connected to the pipeline between the twelfth and eighteenth valves via a pipeline, and a seventeenth valve 1017 is installed at the outlet end of the pipeline of the third N2 storage tank 24; a first flow meter 9 is installed on the pipeline between the second valve 102 and the first 3A molecular sieve adsorption tube 13; a second flow meter 25 is installed on the pipeline between the second 3A molecular sieve adsorption tube 14 and the fourth valve 104; and a third flow meter 26 is installed on the pipeline between the tenth valve and the reactor 19. The flow meters are used to control the gas flow rate, thereby ensuring that H2O in the mixed gas is fully adsorbed or CO is completely oxidized.

[0046] It should be noted that the valves in this embodiment include, but are not limited to, ball valves, butterfly valves, gate valves, safety valves, needle valves, angle valves, and pressure reducing valves.

[0047] When using the apparatus of this embodiment to treat the tail gas (mainly containing: H2O, CO2, CO, N2) generated from the reaction product gas of methanol steam reforming for hydrogen production processed by purification unit 2 for H2 purification, the specific process is as follows:

[0048] The product gas from the methanol steam reforming hydrogen production microreactor 1 is passed into a purification unit 2 based on PSA technology for H2 purification, yielding hydrogen with a purity of 99.999%, which is stored in an H2 collection tank 3. In the desorption stage, N2 purging is used to blow out the impurity gases (containing H2O, CO2, and CO) adsorbed by the adsorbent in the PSA unit. The mixed gas (containing H2O, CO2, CO, and N2) enters the tail gas treatment unit through the first valve 101 to begin tail gas treatment.

[0049] The entire adsorption and oxidation process:

[0050] In this exhaust gas treatment device, two 3A molecular sieve adsorption tubes are installed, namely the first 3A molecular sieve adsorption tube 13 and the second 3A molecular sieve adsorption tube 14, which can realize the continuous adsorption process. When adsorption begins, the first valve 101, the second valve 102, the third valve 103, the fourth valve 104, the fifth valve 105, the tenth valve 1010, and the eleventh valve 1011 are opened. After the exhaust gas passes through the first valve 101, it is divided into two paths. One path of gas enters the first 3A molecular sieve adsorption tube 13 through the second valve 102, and the other path of gas enters the second 3A molecular sieve adsorption tube 14 through the fourth valve 104. After the mixed gas is adsorbed by the 3A molecular sieve in the adsorption tower, it enters the buffer tank 8 (a buffer tank is added between the dehydration module and the catalytic oxidation module to absorb instantaneous pressure fluctuations). Then, it enters the CO oxidation module through the tenth valve 1010. After oxidation by the Pt / Al2O3 honeycomb ceramic catalyst 15, it enters the CO2 collection tank 5 through the eleventh valve 1011.

[0051] Because 3A molecular sieves have a certain adsorption capacity, this technology employs a two-adsorption-tube approach to ensure continuous adsorption, save time and costs, and improve processing efficiency. During operation, a humidity detector monitors the changes in adsorption capacity between the two tubes. If the 3A molecular sieve in the first 3A molecular sieve adsorption tube 13 reaches approximately 80% of its adsorption capacity, the second valve 102 and the third valve 103 are closed, while the sixth valve 106 and the seventh valve 107 are opened. The vacuum pump 17 is then activated to create a vacuum, and N2 from the first N2 storage tank 22 is introduced into the first 3A molecular sieve adsorption tube 13 at a specific flow rate and velocity to purge the 3A molecular sieve and regenerate the adsorbent. If the 3A molecular sieve in the second 3A molecular sieve adsorption tube 14 reaches approximately 80% of its adsorption capacity, the second valve 102 and the third valve 103 are closed, while the sixth valve 106 and the seventh valve 107 are opened. The vacuum pump 17 is then activated to create a vacuum, and N2 from the first N2 storage tank 22 is introduced into the first 3A molecular sieve adsorption tube 13 at a specific flow rate and velocity to purge the 3A molecular sieve and regenerate the adsorbent. When the adsorption capacity is around 80%, the fourth valve 104 and the fifth valve 105 can be closed and the eighth valve 108 and the ninth valve 109 can be opened. The vacuum pump 17 is turned on to draw a vacuum, and the N2 in the second N2 storage tank 23 is passed to the second 3A molecular sieve adsorption tube 14 at a certain flow rate and velocity to purge the 3A molecular sieve and achieve the purpose of adsorbent regeneration. The gas after N2 purging passes through the seventh valve 107 and the ninth valve 109 respectively, and H2O is removed by the condenser 7. The pure N2 can then be stored in the collection tank 4 to achieve the purpose of recycling.

[0052] After the Pt / Al2O3 honeycomb ceramic catalyst 15 has been catalyzing the oxidation of CO for a certain period of time, it needs to be reduced so that it can be reused. The specific operation method is as follows: close the tenth valve 1010 and the eleventh valve 1011, and open the twelfth valve 1012, the thirteenth valve 1013, and the eighteenth valve 1018, allowing H2 from the H2 storage tank 21 to enter the reactor 19 and reduce the Pt / Al2O3 honeycomb ceramic catalyst 15 in the reactor 19. The reduced gas can be discharged through the thirteenth valve 1013. In addition, to ensure that there is still unreacted CO in the Pt / Al2O3 honeycomb ceramic catalyst 15 when it is disassembled, this technology adopts N2 purging to purge the gas in the Pt / Al2O3 honeycomb ceramic catalyst 15. The specific operation method is as follows: close the tenth valve 1010 and the eleventh valve 1011 and open the twelfth valve 1012, the thirteenth valve 1013 and the seventeenth valve 1017, so that N2 in the third N2 storage tank 24 enters the reactor 19 to purge the Pt / Al2O3 honeycomb ceramic catalyst 15 in the reactor 19.

[0053] To ensure the efficient and orderly operation of the adsorption, desorption, and CO oxidation processes, it is necessary to conduct rigorous monitoring of the adsorption and oxidation tubes, including temperature, pressure, humidity, and flow rate.

[0054] The technical solution of this utility model is not limited to the specific embodiments described above. All technical modifications made based on the technical solution of this utility model shall fall within the protection scope of this utility model.

Claims

1. A tail gas treatment device for a methanol steam reforming hydrogen production process, comprising a methanol steam reforming hydrogen production microreactor (1) for hydrogen production, a purification device (2) connected to the methanol steam reforming hydrogen production microreactor (1) for H2 purification, an H2 collection tank (3) connected to the purification device (2), and an N2 collection tank (4) and a CO2 collection tank (5) connected to the tail gas outlet of the purification device (2), characterized in that: The purification device (2) is also connected to an H2O adsorption-desorption module, which is connected to a buffer tank (8). The buffer tank (8) is connected to a CO oxidation module, which is connected to a CO2 collection tank (5). Both the H2O adsorption-desorption module and the CO oxidation module are connected to a nitrogen purging mechanism.

2. The tail gas treatment device for methanol steam reforming to hydrogen production according to claim 1, characterized in that: The H2O adsorption-desorption module includes a low-temperature constant-temperature reaction bath (6). The low-temperature constant-temperature reaction bath (6) contains a first 3A molecular sieve adsorption tube (13) and a second 3A molecular sieve adsorption tube (14). The top of the second 3A molecular sieve adsorption tube (14) is connected to the tail gas outlet of the purification device (2) via a pipeline. A first valve (101) and a fourth valve (104) are installed on the pipeline between the tail gas outlet of the purification device (2) and the top of the second 3A molecular sieve adsorption tube (14). The pipeline between the fourth valve (104) is connected to the first tee pipe. The third port of the first tee pipe is connected to the top of the first 3A molecular sieve adsorption tube (13) through a pipeline after the second valve (102) is installed. The bottom of the first 3A molecular sieve adsorption tube (13) is connected to the second tee pipe through a pipeline. The second port of the second tee pipe is connected to the buffer tank (8) through a pipeline after the third valve (103) is installed. The third port of the second tee pipe is connected to the bottom of the condenser (7) through a pipeline after the seventh valve (107) is installed. The bottom of the second 3A molecular sieve adsorption tube (14) is connected to a third three-way pipe via a pipeline. The second port of the third three-way pipe is equipped with a fifth valve (105) and then connected to the bottom of the buffer tank (8) via a pipeline. The third port of the third three-way pipe is equipped with a ninth valve (109) and then connected to the bottom of the condenser (7) via a pipeline. The top of the condenser (7) is connected to the N2 collection tank (4) via a pipeline. A sixteenth valve (1016) is provided on the pipeline between the condenser (7) and the N2 collection tank (4). The tops of the first 3A molecular sieve adsorption tube (13) and the second 3A molecular sieve adsorption tube (14) are respectively connected to the air inlet of the vacuum pump (17) via pipelines.

3. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 2, characterized in that: The CO oxidation module includes a constant temperature reaction bath (18), and a reactor (19) filled with Pt / Al2O3 honeycomb ceramic catalyst (15) is provided in the constant temperature reaction bath (18). The inlet end of the reactor (19) is connected to the top of the buffer tank (8) through a pipeline. A tenth valve (1010) is provided on the pipeline between the top of the reactor (19) and the top of the buffer tank (8). The inlet end of the reactor (19) is connected to an O2 storage tank (16) through a pipeline. A nineteenth valve (1019) is provided on the pipeline between the inlet end of the reactor (19) and the O2 storage tank (16). The outlet end of the reactor (19) is connected to the flame arrester (20) through a pipeline. An eleventh valve (1011) is provided on the pipeline between the flame arrester (20) and the outlet end of the reactor (19). The outlet end of the flame arrester (20) is connected to the CO2 collection tank (5) through a pipeline. The top of the reactor (19) is connected to the H2 storage tank (21) through a pipeline. A twelfth valve (1012) and an eighteenth valve (1018) are provided on the pipeline between the H2 storage tank (21) and the reactor. The outlet end of the reactor (19) is connected to the exhaust pipe. A thirteenth valve (1013) is provided on the exhaust pipe.

4. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 3, characterized in that: The nitrogen purging mechanism includes a first nitrogen purging mechanism, a second nitrogen purging mechanism, and a third nitrogen purging mechanism; the first nitrogen purging mechanism includes a first N2 storage tank (22), which is connected to the pipeline between the second valve (102) and the top of the first 3A molecular sieve adsorption tube (13) via a pipeline, and a sixth valve (106) is provided on the pipeline between the first N2 storage tank (22) and the top of the first 3A molecular sieve adsorption tube (13); the second nitrogen purging mechanism includes a second N2 storage tank (23), the first N2 storage tank (22) is connected to the second valve (102) and the third nitrogen purging mechanism; the first nitrogen purging mechanism includes a first N2 storage tank (22), the second nitrogen purging mechanism includes a second N2 storage tank (23), the third nitrogen purging mechanism includes a second nitrogen storage tank (23), the second ... The second N2 storage tank (23) is connected to the pipeline between the fourth valve (104) and the top of the second 3A molecular sieve adsorption tube (14) via a pipeline. The pipeline at the outlet end of the second N2 storage tank (23) is provided with an eighth valve (108). The third nitrogen purging mechanism includes a third N2 storage tank (24). The third N2 storage tank (24) is connected to the pipeline between the twelfth valve (1012) and the eighteenth valve (1018) via a pipeline. The pipeline at the outlet end of the third N2 storage tank (24) is provided with a seventeenth valve (1017).

5. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 2, characterized in that: The temperature inside the low-temperature constant temperature reaction bath (6) is 25-50℃.

6. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 3, characterized in that: The temperature inside the constant temperature reaction bath is 80-150℃.

7. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 4, characterized in that: A first flow meter (9) is provided on the pipeline between the second valve (102) and the first 3A molecular sieve adsorption tube (13), a second flow meter (25) is provided on the pipeline between the second 3A molecular sieve adsorption tube (14) and the fourth valve (104), and a third flow meter (26) is provided on the pipeline between the tenth valve (1010) and the reactor (19).

8. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 4, characterized in that: The first 3A molecular sieve adsorption tube (13) and the second 3A molecular sieve adsorption tube (14) are each equipped with a pressure sensor (10), a temperature sensor (11) and a humidity sensor (12).

9. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 3, characterized in that: The reactor (19) is equipped with a pressure sensor (10) and a temperature sensor (11).

10. The tail gas treatment device for methanol steam reforming to produce hydrogen according to claim 1, characterized in that: A fifteenth valve (1015) is provided on the pipeline between the purification device (2) and the H2 collection tank (3).

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