Hydrogen production equipment and hydrogen production process based on AEM technology

Abstract

The invention provides hydrogen production equipment based on an AEM technology, the hydrogen production equipment comprises a first electrolysis module, a second electrolysis module, cleaning assemblies, a condensation module and a purging assembly, the first electrolysis module and the second electrolysis module form a complete bipolar liquid inlet electrolysis system, the first electrolysis module is connected with one cleaning assembly through a pipeline, and the other cleaning assembly is connected with the condensation module through a pipeline. The invention further provides a hydrogen production process based on the AEM technology, and compared with the prior art, the hydrogen production process based on the AEM technology has the following beneficial effects that the first electrolysis module and the second electrolysis module are arranged, so that the cathode and the anode of the electrolytic bath are each provided with an independent liquid inlet structure, the single-pole liquid inlet mode of an existing AEM water electrolysis hydrogen production technology is changed, and the hydrogen production efficiency is improved; and the bipolar liquid inlet mode can be switched among a cathode liquid inlet mode, an anode liquid inlet mode and a cathode liquid inlet mode, so that the condition that electrolysis can be normally carried out on the other side under the condition that one side breaks down can be effectively ensured, and the shutdown time is shortened.

Description

Technical Field

[0001] The present invention belongs to the technical field of electrolytic hydrogen production equipment, and in particular relates to a hydrogen production equipment and a hydrogen production process based on AEM technology. Background Art

[0002] Existing electrolytic hydrogen production equipment based on AEM (anion exchange membrane) technology has significant shortcomings in the monopolar liquid inlet system, that is, once the liquid inlet fails, the equipment is prone to long-term shutdown, affecting the overall production efficiency. This shortcoming mainly stems from the limitations of the monopolar liquid inlet design. In this design, the liquid enters the electrolyzer only through one liquid inlet. If the liquid inlet pipeline is blocked, leaked, or the pump fails, the entire electrolysis process will be forced to interrupt. This characteristic of relying on a single liquid inlet path leads to fragility in the event of failure, especially under high-load operation, and the lag in monitoring and maintenance may make the problem worse.

[0003] To solve this problem, the conventional method is to increase the multi-way liquid inlet design or improve the intelligence of the monitoring system to facilitate timely detection and repair of faults. However, these methods are not perfect. Although the multi-way liquid inlet design can increase redundancy, it will also increase the complexity and failure points of the equipment, which may lead to an increase in the maintenance cost of the system and increase the failure rate of the overall equipment. Therefore, we hope to design a new structure based on AEM hydrogen production equipment to solve this problem. Summary of the invention

[0004] In view of the deficiencies in the prior art, the object of the present invention is to provide a hydrogen production equipment and a hydrogen production process based on AEM technology to solve the problems raised in the above background technology.

[0005] The present invention is implemented through the following technical solutions: A hydrogen production device based on AEM technology, comprising: an electrolysis module 1, an electrolysis module 2, a cleaning component, a condensation module and a purge component, wherein the electrolysis module 1 and the electrolysis module 2 form a complete bipolar liquid-inlet electrolysis system, the electrolysis module 1 is connected to a group of cleaning components through a pipeline, and the electrolysis module 2 is connected to another group of cleaning components through a pipeline;

[0006] One group of cleaning components is connected to one group of condensing modules through pipelines, and another group of cleaning components is connected to another group of condensing modules through pipelines;

[0007] The ends of the purge assembly are respectively communicated with the exhaust pipes of the two condensation modules.

[0008] As a preferred embodiment, the electrolysis module 1 includes an electrolytic cell, a cathode circulation tank, a condensation pump 1 and an instant heater, and the cathode circulation tank is connected to the condensation pump 1 through a pipeline;

[0009] The condensation pump 1 is connected to the pressure transmitter 1 through a pipeline, the pressure transmitter 1 is connected to the instant heater through a pipeline, the instant heater is close to the electrolytic cell, and a temperature measuring element is installed on the pipeline between the instant heater and the electrolytic cell, and the cathode liquid inlet of the electrolytic cell is connected to the temperature measuring element through a pipeline;

[0010] The temperature measuring element is connected to the internal temperature control component signal of the instant heater through a wireless signal, the cathode exhaust port of the electrolytic cell is connected to the air inlet of the cathode circulation tank through a pipeline, and the instant heater is an 800W heater that is resistant to alkali corrosion.

[0011] As a preferred embodiment, the electrolysis module 2 includes an anode circulation tank, which is connected to the anode liquid inlet of the electrolytic cell through a pipeline, a condensation pump 1, a pressure transmitter 1, an instant heater and a temperature measuring element. The anode exhaust port of the electrolytic cell is connected to the air inlet of the anode circulation tank through a pipeline. In actual use, the electrolysis module 1 has one more electrolysis cell than the electrolysis module 2. Apart from this, the rest of the structures are all the same. The specific structural arrangement can be set according to actual use requirements. The instant heaters on the pipelines connecting the cathode and anode of the electrolytic cell to the anode circulation tank and the cathode circulation tank are close to each other, which can reduce heat loss and ensure that the temperature control error is within a smaller range.

[0012] As a preferred embodiment, the cleaning assembly includes a cleaning device and a pure water delivery pipe, and the two groups of cleaning components have the same structure, the upper side of the cleaning device is connected to the pure water delivery pipe, the pure water delivery pipe is connected to an external pure water supply device, and the tops of the two groups of cleaning devices are equipped with delivery air pipes;

[0013] An overflow port is provided on the side of the cleaning device. The overflow ports on the two groups of cleaning devices are respectively connected to the upper sides of the sides of the cathode circulation tank and the anode circulation tank through pipelines, and the height of the overflow port is greater than the height of the cathode circulation tank and the anode circulation tank.

[0014] As a preferred embodiment, the condensing module includes a heat exchanger, an air cooler, a gas-liquid separation tank, a cold water tank and a condenser. The two groups of condensing modules have the same structure, and the heat source inlets of the heat exchangers on the two groups of condensing modules are respectively connected to the conveying air pipes on the tops of the two washers;

[0015] The heat source outlet of the heat exchanger is connected to the low-level inlet of the gas-liquid separation tank through a pipeline, and the bottoms of the gas-liquid separation tubes on the two groups of condensation modules are respectively connected to the anode circulation tank and the cathode circulation tank through pipelines;

[0016] The cold source inlet of the heat exchanger is connected to the condensation pump 2 through a pipeline, a flow meter, and a pressure transmitter 3. The condensation pump 2 is connected to the cold water tank through a pipeline. The cold source outlet of the heat exchanger is connected to the air cooler through a pipeline. The air cooler is connected to the cold water tank through a pipeline.

[0017] As a preferred embodiment, the purge assembly includes a pressure reducing valve, a pressure gauge, a float flowmeter and a pressure transmitter 2, and an external nitrogen delivery pipe is connected to the pressure reducing valve;

[0018] The pressure reducing valve is connected to a pressure gauge, a float flowmeter and a second pressure transmitter through pipelines, and the second pressure transmitter is connected to two sets of purge pipelines;

[0019] The two groups of purge pipelines are both installed with solenoid valves and check valves, and the ends of the two groups of purge pipelines are both provided with a purge port, and the two purge ports are respectively connected to the exhaust pipes on the upper sides of the two gas-liquid separation tanks.

[0020] The present invention also relates to a hydrogen production process based on AEM technology, comprising the following steps:

[0021] a. Before the electrolyte is introduced into the anion and anode electrolyzers, the alkali solution is heated in each channel by an 800W alkali corrosion-resistant instant heater. The real-time temperature is detected by the temperature measuring element in front of the electrolyte inlet to control the electrolysis temperature of each cell individually. Different channels can be heated to different temperatures according to needs, which is convenient for observing and testing electrolysis performance and has a significant experimental effect on membrane electrode performance analysis;

[0022] At the same time, it is only necessary to heat the anode circulation tank and the cathode circulation tank to a moderate temperature (40-50°C), without heating to the actual electrolysis temperature, which improves the overall heating time. The heater is arranged near the entrance of the electrolytic cell, and the water pipe is short and the heat dissipation is reduced, so the final temperature entering the cell can be controlled within ±0.5°C of the user-set temperature.

[0023] b. The hydrogen and oxygen generated by the electrolysis of the cathode and cathode are respectively refluxed to the anode circulation tank and the cathode circulation tank through corresponding pipelines. After being cleaned by the liquid in the anode circulation tank and the cathode circulation tank, the water vapor contained in them is preliminarily removed, and then the preliminarily treated hydrogen and oxygen are transported to the two cleaning devices through pipelines;

[0024] Two 2L washers are used to wash the alkaline substances in hydrogen and oxygen with pure water. In the initial state, pure water is added to the washers. The gas generated after electrolysis passes through the outlet of the anode circulation tank and the cathode circulation tank and then enters from the low water level of the washers. The alkali solution is diluted in pure water, and the gas is discharged through the exhaust port above.

[0025] An online alkali concentration detector is used on the circulating water outlet pipes of the anode circulating tank and the cathode circulating tank. A concentration range can be set on the host computer. If it exceeds the range, the user will be prompted to replace the alkali solution or dilute it. It is simple and practical. At the same time, there is a self-overflow port leading to the circulating liquid tank on the side of the washer. When the water level of the washer reaches the self-overflow port position, the liquid flows into the circulating liquid tank through the liquid level difference. The amount of water consumed during electrolysis is consistent with the amount of water added, and the alkali concentration in the entire circulation system is within a balanced range.

[0026] During the installation process, the height of the cleaning device must be maintained at least above the horizontal height of the anode circulation tank and the cathode circulation tank to prevent the liquid from the overflow port of the cleaning device from failing to reach the circulation tank through the liquid level difference (liquid level sensors are installed inside the anode circulation tank and the cathode circulation tank. When the liquid level is lower than the set value, new pure water will be injected into the cleaning device, and the consumed water will be replenished into the anode circulation tank and the cathode circulation tank through the overflow port to ensure that the alkali concentration in the entire circulation system is within a balanced range);

[0027] c. Use a heat exchanger (plate heat exchanger) with a maximum volume flow of 4m3 / h to heat and cool the hydrogen and oxygen produced by the electrolyzer, and then use the gas-liquid separation tank for efficient and safe gas-liquid separation; use an air cooler with a rated flow of 25L / min to cool the cooling water after heat exchange to ensure that the cooling water in the cooling system can be maintained at a temperature within a specific range; at the same time, the inlet and outlet of the heat exchanger use adjustable flow meters to adjust the heat exchange efficiency as needed;

[0028] d. After the electrolytic cell is stopped, in order to prevent the internal water channel of the electrolytic cell from being blocked due to the crystallization of the alkali solution at low temperature, the electrolytic cell needs to be flushed with alkali solution. A 5.3L / min diaphragm pump is used to extract pure water from the cooling water tank and flush the electrolytic cell and the subsequent pipes from the water inlet of the cathode and anode at the same time, which can not only cool down but also clean the electrolytic cell with alkali solution;

[0029] e. When the electrolysis stops or there is a large gas leakage, the hydrogen and oxygen in the pipeline need to be purged to prevent leakage into the laboratory or factory air and cause safety accidents; before the nitrogen enters the test system, the pressure reducing valve with a maximum output pressure of 0.3Mpa is adjusted, and the flow of nitrogen is controlled by a float flowmeter with a range of 0.25-2.5L / min to prevent the intake pressure and flow from being too large, which may damage the instruments in the system. The air intake of the purge pipeline is controlled by the solenoid valve alone to control the pipeline that needs to be purged. At the same time, the pressure transmitter and the solenoid valve form a chain control. The solenoid valve can only be opened when the pressure transmitter has a reading to prevent the solenoid valve from opening without pressure and causing air to enter the electrolytic cell.

[0030] After adopting the above technical scheme, the beneficial effects of the present invention are as follows: by setting the electrolysis module 1 and the electrolysis module 2, the cathode and the anode of the electrolytic cell have independent liquid inlet structures, which changes the existing AEM water electrolysis hydrogen production technology using a single-pole liquid inlet mode, and the bipolar liquid inlet mode can be switched among the cathode, anode, and anode and cathode liquid inlet modes, which can effectively ensure that in the case of a fault on one side, the other side can also perform electrolysis normally, thereby shortening the downtime;

[0031] By adding instant heaters and temperature measuring elements near the cathode and anode of the electrolytic cell in the electrolytic module 1 and the electrolytic module 2, the electrolyte temperature of each channel can be controlled separately, and the problem of large electrolyte temperature hysteresis in the electrolytic cell can be effectively solved, avoiding the problem of different electrolysis efficiencies of each channel due to temperature when other parameters are the same;

[0032] By setting an overflow port on the cleaner and directing the overflow water into the anode circulation tank and the cathode circulation tank through the corresponding pipeline, the liquid flows into the circulating liquid tank through the liquid level difference, so that the amount of water consumed during electrolysis is consistent with the amount of water added, and the alkali concentration in the whole circulation system is within a balanced range. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0034] Figure 1 This is a schematic diagram of the overall structure of a hydrogen production device based on AEM technology in the present invention.

[0035] Figure 2 This is a schematic diagram of the structure of a purge assembly of a hydrogen production equipment based on AEM technology according to the present invention.

[0036] Figure 3 This is a schematic diagram of the structure of electrolysis module 1 and electrolysis module 2 of a hydrogen production device based on AEM technology in the present invention.

[0037] Figure 4 This is a schematic diagram of a clear component structure of a hydrogen production device based on AEM technology of the present invention.

[0038] Figure 5 This is a schematic diagram of the condensing module structure of a hydrogen production equipment based on AEM technology in the present invention.

[0039] In the figure, 100-electrolysis module 1, 110-electrolysis cell, 120-cathode circulation tank, 130-condensation pump 1, 140-pressure transmitter 1, 150-instant heater, 160-temperature measuring element;

[0040] 200-cleaning assembly, 210-cleaner, 220-pure water delivery pipe, 230-overflow port;

[0041] 300-condensing module, 310-heat exchanger, 320-air cooler, 330-gas-liquid separation tank, 340-cold water tank, 350-condensing pump 2, 360-pressure transmitter 3, 370-flow meter;

[0042] 400-purge assembly, 410-pressure reducing valve, 420-pressure gauge, 430-float flowmeter, 440-pressure transmitter II, 450-solenoid valve, 460-check valve, 470-purge port;

[0043] 500-electrolysis module 2, 510-anode circulation tank. DETAILED DESCRIPTION

[0044] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0045] See also Figures 1 to 5 The present invention provides a technical solution: a hydrogen production device based on AEM technology, comprising: an electrolysis module 100, an electrolysis module 2 500, a cleaning component 200, a condensation module 300 and a purge component 400, wherein the electrolysis module 100 and the electrolysis module 2 500 form a complete bipolar liquid-inlet electrolysis system, the electrolysis module 100 is connected to a group of cleaning components 200 through a pipeline, and the electrolysis module 2 500 is connected to another group of cleaning components 200 through a pipeline;

[0046] One set of cleaning components 200 is connected to one set of condensing modules 300 through pipelines, and another set of cleaning components 200 is connected to another set of condensing modules 300 through pipelines;

[0047] The ends of the purge assembly 400 are respectively communicated with the exhaust pipes of the two condensation modules 300 .

[0048] See also Figure 1 , Figure 3 as well as Figure 4The electrolysis module 100 includes an electrolytic cell 110, a cathode circulation tank 120, a condensation pump 130 and an instant heater 150, and the cathode circulation tank 120 is connected to the condensation pump 130 through a pipeline;

[0049] The condensation pump 130 is connected to the pressure transmitter 140 through a pipeline, and the pressure transmitter 140 is connected to the instant heater 150 through a pipeline. The instant heater 150 is close to the electrolytic cell 110, and a temperature measuring element 160 is installed on the pipeline between the instant heater 150 and the electrolytic cell 110. The cathode liquid inlet of the electrolytic cell 110 is connected to the temperature measuring element 160 through a pipeline;

[0050] The temperature measuring element 160 is connected to the internal temperature control component signal of the instant heater 150 via a wireless signal. The cathode exhaust port of the electrolytic cell 110 is connected to the air inlet of the cathode circulation tank 120 via a pipeline. The instant heater 150 is an 800W alkali corrosion-resistant heater.

[0051] The electrolysis module 2 500 includes an anode circulation tank 510, which is connected to the anode liquid inlet of the electrolytic cell 110 through a pipeline, a condensation pump 130, a pressure transmitter 360, an instant heater 150 and a temperature measuring element 160. The anode exhaust port of the electrolytic cell 110 is connected to the air inlet of the anode circulation tank 510 through a pipeline. In actual use, the electrolysis module 100 has one more electrolytic cell 110 than the electrolysis module 2 500. Apart from this, the rest of the structures are all the same. The specific structural arrangement can be set according to actual use requirements. The instant heater 150 on the pipeline connecting the cathode and anode of the electrolytic cell 110 to the anode circulation tank 510 and the cathode circulation tank 120 is close to each other, which can reduce heat loss and ensure that the temperature control error is within a smaller range.

[0052] The cleaning assembly 200 includes a cleaning device 210 and a pure water delivery pipe 220, and the two cleaning devices 200 have the same structure. The upper side of the cleaning device 210 is connected to the pure water delivery pipe 220, and the pure water delivery pipe 220 is connected to an external pure water supply device. The tops of the two cleaning devices 210 are equipped with delivery air pipes.

[0053] An overflow port 230 is provided on the side of the cleaning device 210 . The overflow ports 230 on the two groups of cleaning devices 210 are respectively connected to the upper sides of the cathode circulation tank 120 and the anode circulation tank 510 through pipelines, and the height of the overflow port 230 is greater than the height of the cathode circulation tank 120 and the anode circulation tank 510 .

[0054] As the first embodiment of the present invention, before the negative and positive double-sided electrolytic cells 110 are filled with liquid, the alkali solution is heated on each channel by an instant heater 150 with a power of 800W and resistant to alkali solution corrosion. The real-time temperature is detected by a temperature measuring element 160 in front of the liquid inlet of the electrolytic cell 110 to individually control the electrolysis temperature of each cell. It is only necessary to heat the anode circulation tank 510 and the cathode circulation tank 120 to a moderate temperature (40-50°C), and there is no need to heat to the actual electrolysis temperature. The final temperature entering the cell can be controlled within ±0.5°C of the user-set temperature. The hydrogen and oxygen generated by the electrolysis of the positive and negative electrodes are respectively refluxed to the anode circulation tank 510 and the cathode circulation tank 120 through the corresponding pipelines. After the liquid in the anode circulation tank 510 and the cathode circulation tank 120 is cleaned, the water vapor contained in the other is preliminarily removed, and then the preliminarily treated hydrogen and oxygen are transported to the two washers 210 through pipelines, and the alkaline substances in the hydrogen and oxygen are cleaned with pure water;

[0055] In the initial state, pure water is added to the cleaning device 210. The gas generated after electrolysis passes through the gas outlets of the anode circulation tank 510 and the cathode circulation tank 120 and then enters from the low water level of the cleaning device 210. The alkali solution is diluted in the pure water, and the gas is discharged through the exhaust port on the top. There is a self-overflow port leading to the circulating liquid tank on the side of the cleaning device 210. When the water level of the cleaning device 210 reaches the self-overflow port position, the liquid flows into the circulating liquid tank through the liquid level difference (the height of the cleaning device 210 must be maintained at least above the horizontal height of the anode circulation tank 510 and the cathode circulation tank 120 to prevent the liquid from the self-overflow port of the cleaning device 210 from failing to reach the circulating liquid tank through the liquid level difference). The amount of water consumed during electrolysis is consistent with the amount of water added, and the alkali concentration in the entire circulation system is in a balanced range.

[0056] By providing the electrolysis module 100 and the electrolysis module 2 500, the cathode and the anode of the electrolyzer 110 have independent liquid inlet structures, which changes the existing AEM water electrolysis hydrogen production technology using a single-pole liquid inlet method, and the bipolar liquid inlet method can be switched between the cathode, anode, and anode and cathode liquid inlet modes, which can effectively ensure that in the event of a failure on one side, the other side can also perform electrolysis normally, thereby shortening the downtime;

[0057] By adding instant heaters 150 and temperature measuring elements 160 near the cathode and anode of the electrolytic cell 110 in the electrolytic module 1 100 and the electrolytic module 2 500, the electrolyte temperature of each channel can be controlled separately, and the problem of large electrolyte temperature hysteresis at the electrolytic cell 110 can be effectively solved, avoiding the problem of different electrolysis efficiencies of each channel due to the influence of temperature when other parameters are the same;

[0058] By setting an overflow port 230 on the cleaning device 210 and introducing the overflowing water into the anode circulation tank 510 and the cathode circulation tank 120 through corresponding pipelines, the liquid flows into the circulating liquid tank by the liquid level difference, so that the amount of water consumed during electrolysis is consistent with the amount of water replenished, and the alkali solution concentration in the entire circulation system is within a balanced range.

[0059] See also Figure 5 The condensation module 300 includes a heat exchanger 310, an air cooler 320, a gas-liquid separation tank 330, a cold water tank 340 and a condenser. The two groups of condensation modules 300 have the same structure. The heat source inlets of the heat exchangers 310 on the two groups of condensation modules 300 are respectively connected to the conveying air pipes on the tops of the two washers 210;

[0060] The heat source outlet of the heat exchanger 310 is connected to the low-level inlet of the gas-liquid separation tank 330 through a pipeline, and the bottoms of the gas-liquid separation tubes on the two groups of condensation modules 300 are respectively connected to the anode circulation tank 510 and the cathode circulation tank 120 through pipelines;

[0061] The cold source inlet of the heat exchanger 310 is connected to the condensation pump 2 350 through a pipeline, a flow meter 370, and a pressure transmitter 360. The condensation pump 2 350 is connected to the cold water tank 340 through a pipeline. The cold source outlet of the heat exchanger 310 is connected to the air cooler 320 through a pipeline. The air cooler 320 is connected to the cold water tank 340 through a pipeline.

[0062] As a second embodiment of the present invention, based on the above-mentioned first embodiment, the hydrogen and oxygen discharged from the scrubber 210 are subjected to heat exchange and cooling by the heat exchanger 310 for the hydrogen and oxygen produced by the electrolyzer 110, and then the gas-liquid separation is carried out efficiently and safely by the gas-liquid separation tank 330; at the same time, the cooling water after the heat exchange is cooled by the air cooler 320 to ensure that the cooling water in the entire cooling system can be maintained at a temperature within a specific range.

[0063] See also Figure 2 , the purge assembly 400 includes a pressure reducing valve 410, a pressure gauge 420, a float flowmeter 430 and a pressure transmitter 2 440, and an external nitrogen delivery pipe is connected to the pressure reducing valve 410;

[0064] The pressure reducing valve 410 is connected to the pressure gauge 420, the float flow meter 430 and the second pressure transmitter 440 through pipelines, and the second pressure transmitter 440 is connected to two sets of purge pipelines;

[0065] The two groups of purge pipelines are both installed with a solenoid valve 450 and a check valve 460 , and the ends of the two groups of purge pipelines are both provided with a purge port 470 , which are respectively connected to the exhaust pipes on the upper sides of the two gas-liquid separation tanks 330 .

[0066] As the third embodiment of the present invention, when it is necessary to purge the hydrogen and oxygen in the pipeline, the nitrogen is reduced in pressure by adjusting the pressure reducing valve 410 with a maximum output pressure of 0.3Mpa, and the float flowmeter 430 with a range of 0.25-2.5L / min is used to control the flow of nitrogen. Then, the nitrogen is separately controlled through the solenoid valve 450 of the purge pipeline to enter the corresponding purge port 470 to purge the hydrogen and oxygen in the pipeline. At the same time, the pressure transmitter 2 440 and the solenoid valve 450 form a chain control. The solenoid valve 450 can only be opened when the pressure transmitter 2 440 has a reading, so as to prevent the solenoid valve 450 from opening without pressure and causing air to enter the electrolytic cell 110.

[0067] The present invention also relates to a hydrogen production process based on AEM technology, comprising the following steps:

[0068] Before the anionic and anodic electrolytic cells 110 are filled with liquid, the alkali solution is heated by an 800W alkali-resistant instant heater 150 in each channel. The real-time temperature is detected by a temperature measuring element 160 in front of the liquid inlet of the electrolytic cell 110 to control the electrolysis temperature of each cell individually. Different channels can be heated to different temperatures according to needs, which is convenient for observing and testing electrolysis performance and has a significant experimental effect on membrane electrode performance analysis.

[0069] At the same time, it is only necessary to heat the anode circulation tank 510 and the cathode circulation tank 120 to a moderate temperature (40-50°C), without heating to the actual electrolysis temperature, thereby improving the overall heating time. The instant heater 150 is arranged near the entrance of the electrolytic cell 110, and the water pipe along the way is short and the heat dissipation is reduced, so the final temperature entering the cell can be controlled within ±0.5°C of the user-set temperature;

[0070] The hydrogen and oxygen generated by the electrolysis of the cathode and cathode flow back to the anode circulation tank 510 and the cathode circulation tank 120 through corresponding pipelines, and after being cleaned by the liquid in the anode circulation tank 510 and the cathode circulation tank 120, the water vapor contained in the anode circulation tank 510 and the cathode circulation tank 120 is initially removed, and then the preliminarily treated hydrogen and oxygen are transported to the two cleaning devices 210 through pipelines;

[0071] The alkaline substances in hydrogen and oxygen are cleaned with pure water through two 2L cleaning tanks 210. In the initial state, pure water is added to the cleaning tank 210. The gas generated after electrolysis passes through the gas outlets of the anode circulation tank 510 and the cathode circulation tank 120 and then enters from the low water level of the cleaning tank 210. The alkaline solution is diluted in pure water, and the gas is discharged through the exhaust port above.

[0072] An online detector for alkali concentration is used on the circulating water outlet pipes of the anode circulating tank 510 and the cathode circulating tank 120. A concentration range can be set on the host computer. If the concentration range is exceeded, the user is prompted to replace the alkali solution or dilute it. This is simple and practical. At the same time, there is a self-overflow port leading to the circulating liquid tank on the side of the cleaning device 210. When the water level of the cleaning device 210 reaches the self-overflow port position, the liquid flows into the circulating liquid tank through the liquid level difference, so that the amount of water consumed during electrolysis is consistent with the amount of water added, and the alkali concentration in the entire circulation system is in a balanced range.

[0073] During the installation process, the height of the cleaning device 210 must be maintained at least above the horizontal height of the anode circulation tank 510 and the cathode circulation tank 120 to prevent the liquid from the overflow port of the cleaning device 210 from failing to reach the circulating liquid tank through the liquid level difference (liquid level sensors are installed inside the anode circulation tank 510 and the cathode circulation tank 120. When the liquid level is lower than the set value, new pure water will be injected into the cleaning device 210, and the consumed water will be replenished into the anode circulation tank 510 and the cathode circulation tank 120 through the overflow port 230 to ensure that the alkali concentration in the entire circulation system is within a balanced range);

[0074] A heat exchanger 310 (plate heat exchanger 310) with a maximum volume flow rate of 4m3 / h is used to heat and cool the hydrogen and oxygen generated by the electrolytic cell 110, and then the gas-liquid separation is carried out efficiently and safely through the gas-liquid separation tank 330; an air cooler 320 with a rated flow rate of 25L / min is used to cool the cooling water after the heat exchange, ensuring that the cooling water in the cooling system can be maintained at a temperature within a specific range; at the same time, an adjustable flow meter 370 is used at the inlet and outlet of the heat exchanger 310, and the heat exchange efficiency can be adjusted as needed;

[0075] After the electrolytic cell 110 is stopped, in order to prevent the internal water channel of the electrolytic cell 110 from being blocked due to the crystallization of the alkali solution at low temperature, the electrolytic cell 110 needs to be flushed with alkali solution. A 5.3L / min diaphragm pump is used to extract pure water from the cooling water tank and flush the electrolytic cell 110 and the subsequent pipelines from the water inlets of the cathode and anode at the same time, which can not only cool down but also clean the electrolytic cell with alkali solution.

[0076] When the electrolysis stops or there is a large gas leakage, the hydrogen and oxygen in the pipeline need to be purged to prevent leakage into the laboratory or factory air and cause safety accidents; before the nitrogen enters the test system, the pressure reducing valve 410 with a maximum output pressure of 0.3Mpa is adjusted, and the flow rate of the nitrogen is controlled by the float flowmeter 430 with a range of 0.25-2.5L / min to prevent the intake pressure and flow from being too large, which may cause damage to the instruments in the system. The air intake of the purge pipeline is controlled by the solenoid valve 450 separately for the pipeline that needs to be purged. At the same time, the pressure transmitter 440 and the solenoid valve 450 form a chain control. The solenoid valve 450 can only be opened when the pressure transmitter 440 has a reading, so as to prevent the solenoid valve 450 from opening without pressure and causing air to enter the electrolytic cell 110.

[0077] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A hydrogen production device based on AEM technology, comprising: An electrolysis module 1 (100), an electrolysis module 2 (500), a cleaning component (200), a condensation module (300) and a purge component (400), characterized in that the electrolysis module 1 (100) and the electrolysis module 2 (500) form a complete bipolar liquid-inlet electrolysis system, the electrolysis module 1 (100) is connected to a group of cleaning components (200) through a pipeline, and the electrolysis module 2 (500) is connected to another group of cleaning components (200) through a pipeline; One group of the cleaning components (200) is connected to one group of condensing modules (300) via a pipeline, and another group of the cleaning components (200) is connected to another group of condensing modules (300) via a pipeline; The ends of the purge assembly (400) are respectively connected to the exhaust pipes of the two condensation modules (300).

2. A hydrogen production equipment based on AEM technology as claimed in claim 1, characterized in that: The electrolysis module 1 (100) comprises an electrolytic cell (110), a cathode circulation tank (120), a condensation pump 1 (130) and an instant heater (150), wherein the cathode circulation tank (120) is connected to the condensation pump 1 (130) via a pipeline; The condensation pump (130) is connected to the pressure transmitter (140) through a pipeline, the pressure transmitter (140) is connected to the instant heater (150) through a pipeline, the instant heater (150) is close to the electrolytic cell (110), and a temperature measuring element (160) is installed on the pipeline between the instant heater (150) and the electrolytic cell (110), and the cathode liquid inlet of the electrolytic cell (110) is connected to the temperature measuring element (160) through a pipeline; The temperature measuring element (160) is connected to the internal temperature control component signal of the instant heater (150) via a wireless signal, the cathode exhaust port of the electrolytic cell (110) is connected to the air inlet of the cathode circulation tank (120) via a pipeline, and the instant heater (150) is an 800W heater that is resistant to alkali corrosion.

3. A hydrogen production equipment based on AEM technology as claimed in claim 2, characterized in that: The electrolysis module 2 (500) includes an anode circulation tank (510), and the anode circulation tank (510) is connected to the anode liquid inlet of the electrolytic cell (110) through a pipeline, a condensation pump 1 (130), a pressure transmitter 1 (140), an instant heater (150) and a temperature measuring element (160), and the anode exhaust port of the electrolytic cell (110) is connected to the air inlet of the anode circulation tank (510) through a pipeline.

4. A hydrogen production equipment based on AEM technology as claimed in claim 3, characterized in that: The cleaning assembly (200) comprises a cleaning device (210) and a pure water delivery pipe (220), and the two groups of cleaning components (200) have the same structure, the upper side of the side of the cleaning device (210) is connected to the pure water delivery pipe (220), the pure water delivery pipe (220) is connected to an external pure water supply device, and the tops of the two groups of cleaning devices (210) are equipped with delivery air pipes; An overflow port (230) is provided on the side of the cleaning device (210), and the overflow ports (230) on the two groups of cleaning devices (210) are respectively connected to the upper sides of the sides of the cathode circulation tank (120) and the anode circulation tank (510) through pipelines, and the height of the overflow port (230) is greater than the height of the cathode circulation tank (120) and the anode circulation tank (510).

5. A hydrogen production equipment based on AEM technology as claimed in claim 4, characterized in that: The condensation module (300) comprises a heat exchanger (310), an air cooler (320), a gas-liquid separation tank (330), a cold water tank (340) and a condenser. The two groups of condensation modules (300) have the same structure. The heat source inlets of the heat exchangers (310) on the two groups of condensation modules (300) are respectively connected to the air delivery pipes on the tops of the two washers (210); The heat source outlet of the heat exchanger (310) is connected to the low-level inlet of the gas-liquid separation tank (330) through a pipeline, and the bottoms of the gas-liquid separation tubes on the two groups of condensation modules (300) are respectively connected to the anode circulation tank (510) and the cathode circulation tank (120) through pipelines; The cold source inlet of the heat exchanger (310) is connected to the second condensation pump (350) through a pipeline, a flow meter (370), and a third pressure transmitter (360); the second condensation pump (350) is connected to the cold water tank (340) through a pipeline; the cold source outlet of the heat exchanger (310) is connected to the air cooler (320) through a pipeline; and the air cooler (320) is connected to the cold water tank (340) through a pipeline.

6. A hydrogen production equipment based on AEM technology as claimed in claim 5, characterized in that: The purge assembly (400) includes a pressure reducing valve (410), a pressure gauge (420), a float flowmeter (430) and a second pressure transmitter (440), and an external nitrogen delivery pipe is connected to the pressure reducing valve (410); The pressure reducing valve (410) is connected to a pressure gauge (420), a float flowmeter (430) and a second pressure transmitter (440) through pipelines, and the second pressure transmitter (440) is connected to two sets of purge pipelines; The two groups of purge pipelines are both installed with a solenoid valve (450) and a check valve (460), and the ends of the two groups of purge pipelines are both provided with a purge port (470), and the two purge ports (470) are respectively connected to the exhaust pipes on the upper sides of the two gas-liquid separation tanks (330).

7. A hydrogen production process based on AEM technology as claimed in any one of claims 1 to 6, characterized in that: The steps include: a. Before the anion and anode double-sided electrolytic cells (110) are filled with liquid, the alkali solution is heated in each channel by an instant heater (150) with a power of 800W and resistant to alkali solution corrosion. The real-time temperature is detected by a temperature measuring element (160) in front of the liquid inlet of the electrolytic cell (110) to individually control the electrolysis temperature of each cell. Different channels can be heated to different temperatures according to needs, which is convenient for observing and testing electrolysis performance, and has a significant experimental effect on membrane electrode performance analysis; At the same time, the anode circulation tank (510) and the cathode circulation tank (120) only need to be heated to a moderate temperature (40-50°C), and do not need to be heated to the actual electrolysis temperature, thereby improving the overall heating time. The instant heater (150) is arranged near the entrance of the electrolytic cell (110), and the water pipe along the way is short and the heat dissipation is reduced, so the final temperature entering the cell can be controlled within ±0.5°C of the user-set temperature; b. The hydrogen and oxygen generated by the electrolysis of the cathode and cathode flow back to the anode circulation tank (510) and the cathode circulation tank (120) through corresponding pipelines, and after being cleaned by the liquid in the anode circulation tank (510) and the cathode circulation tank (120), the water vapor contained in the anode circulation tank (510) and the cathode circulation tank (120) is initially removed, and then the hydrogen and oxygen after the initial treatment are transported to the two cleaning devices (210) through pipelines; Alkaline substances in hydrogen and oxygen are cleaned with pure water through two 2L cleaning tanks (210). In the initial state, pure water is added to the cleaning tank (210). The gas generated after electrolysis passes through the gas outlets of the anode circulation tank (510) and the cathode circulation tank (120) and then enters from the low water level of the cleaning tank (210). The alkali solution is diluted in pure water, and the gas is discharged through the exhaust port above. An online detector for alkali solution concentration is used on the circulating water outlet pipes of the anode circulating tank (510) and the cathode circulating tank (120). A concentration range can be set on the host computer. If the concentration is beyond the range, the user is prompted to replace the alkali solution or dilute it. This is simple and practical. At the same time, there is a self-overflow port leading to the circulating liquid tank on the side of the cleaning device (210). When the water level of the cleaning device (210) reaches the self-overflow port position, the liquid flows into the circulating liquid tank through the liquid level difference, so that the amount of water consumed during electrolysis is consistent with the amount of water added, and the alkali solution concentration in the entire circulation system is within a balanced range. During installation, the height of the cleaning device (210) must be maintained at least above the horizontal heights of the anode circulation tank (510) and the cathode circulation tank (120) to prevent the liquid from overflowing from the cleaning device (210) from failing to reach the circulation tank due to the liquid level difference. c. A heat exchanger (310) with a maximum volume flow rate of 4m3 / h is used to heat exchange and cool down the hydrogen and oxygen generated by the electrolytic cell (110), and then the gas-liquid separation is carried out efficiently and safely through the gas-liquid separation tank (330); an air cooler (320) with a rated flow rate of 25L / min is used to cool down the cooling water after the heat exchange, so as to ensure that the cooling water in the cooling system can be maintained at a temperature within a specific range; at the same time, an adjustable flow meter (370) is used at the inlet and outlet of the heat exchanger (310), so that the heat exchange efficiency can be adjusted as needed; d. After the electrolytic cell (110) is stopped, in order to prevent the internal water path of the electrolytic cell (110) from being blocked due to crystallization of the alkali solution at low temperature, the electrolytic cell (110) needs to be flushed with alkali solution. Pure water from the cooling water tank is pumped out using a 5.3 L / min diaphragm pump, and the electrolytic cell (110) and the subsequent pipelines are flushed from the water inlets of the cathode and anode at the same time, which can both cool down and clean the electrolytic cell with alkali solution. e. When the electrolysis stops or there is a large gas leak, the hydrogen and oxygen in the pipeline need to be purged to prevent leakage into the laboratory or factory air and cause safety accidents; Before the nitrogen enters the test system, the pressure reducing valve (410) with a maximum output pressure of 0.3Mpa is adjusted, and the flow rate of the nitrogen is controlled by a float flowmeter (430) with a range of 0.25-2.5L / min to prevent the intake pressure and flow from being too large, which may damage the instruments in the system. The intake of the purge pipeline is controlled by the solenoid valve (450) to control the pipeline that needs to be purged. At the same time, the pressure transmitter 2 (440) and the solenoid valve (450) form a chain control. The solenoid valve (450) can only be opened when the pressure transmitter 2 (440) has a reading, so as to prevent the solenoid valve (450) from being opened without pressure, causing air to enter the electrolytic cell (110).

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