A cyclic hydrogen purification system and method

Abstract

The present invention discloses a cyclic hydrogen purification system and method, belonging to the technical field of hydrogen purification for electrolytic water hydrogen production. It includes a deoxidation mechanism, which is connected to the hydrogen outlet of the gas-liquid separator of the electrolytic water hydrogen production device; an adsorption and drying mechanism, which is connected to the deoxidation mechanism, and an adsorbent for adsorbing water vapor is filled in the adsorption and drying mechanism; a transportation mechanism, which is adapted to the adsorption and drying mechanism; wherein, the adsorption and drying mechanism includes: an adsorption unit; a regeneration unit; a cooling unit. The present invention purifies the raw hydrogen through the deoxidation mechanism and the adsorption and drying mechanism, and under the action of the adsorption and drying mechanism and the transportation mechanism, the adsorbent is completed online desorption regeneration and reused, solving the technical problem of complex control of the hydrogen purification system in the prior art, and achieving the technical effect of recycling the adsorbent.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen purification for hydrogen production by electrolyzing water, and particularly relates to a circulating hydrogen purification system and method. Background Art

[0002] Using surplus power from renewable energy such as wind power and photovoltaic power generation to electrolyze water on a large scale to produce green hydrogen, and then using green hydrogen to further synthesize green ammonia or methanol as fuel or chemical products or hydrogen storage media is one of the most feasible and effective technical paths to solve the current dilemma of renewable energy power consumption.

[0003] In the prior art, the hydrogen flowing out from hydrogen production by electrolyzing water needs to be further purified to remove a small amount of oxygen and a large amount of water vapor in the hydrogen, so as to obtain high-purity hydrogen suitable for industrial use. The current mainstream hydrogen purification method is catalytic deoxidation + three-tower adsorption drying. The adsorbent is filled in the adsorption tower in a fixed-bed manner, resulting in ineffective movement of the adsorbent. A large number of automatic valves need to be configured for repeated switching back and forth during the processes of adsorbing hydrogen and regenerating the adsorbent, and the control process is relatively complex and cumbersome. Summary of the Invention

[0004] The purpose of the present invention is to propose a circulating hydrogen purification system to solve the disadvantages of the complex and cumbersome hydrogen purification system in the prior art.

[0005] To achieve the above purpose, the present invention adopts the following technical solutions:

[0006] The first aspect of the present invention provides a circulating hydrogen purification system, including:

[0007] A deoxidation mechanism, one end of which is connected to the hydrogen outlet of the gas-liquid separator of the electrolytic water hydrogen production device, and is used to remove oxygen in the raw hydrogen;

[0008] An adsorption and drying mechanism, which is connected to the deoxidation mechanism, and an adsorbent for adsorbing water vapor is filled in the adsorption and drying mechanism, and the adsorption and drying mechanism is used for on-line desorption and regeneration of the adsorbent;

[0009] A transportation mechanism, which is adapted to the adsorption and drying mechanism, and is used to transport the adsorbent so that the adsorbent circulates in the adsorption and drying mechanism;

[0010] Wherein, the adsorption and drying mechanism includes:

[0011] An adsorption unit, which is connected to the deoxidation mechanism and is used for adsorbing and dehydrating the deoxidized hydrogen;

[0012] A regeneration unit, which is connected to the adsorption unit and is used for desorbing and regenerating the adsorbent;

[0013] A cooling unit, which is in communication with the regeneration unit and is used to cool and dry the adsorbent.

[0014] In some feasible embodiments, the deoxidization mechanism includes:

[0015] A deoxidizer, which is connected to the electrolytic water hydrogen production device. The deoxidizer is filled with a palladium catalyst. Oxygen and hydrogen in the raw hydrogen react to form water under the action of the palladium catalyst, removing the oxygen in the raw hydrogen. A first heater is also provided in the deoxidizer;

[0016] A first heat exchanger, which is arranged on the pipeline between the electrolytic water hydrogen production device and the deoxidizer, and the deoxidizer is in communication with the electrolytic water hydrogen production device through the first heat exchanger;

[0017] A cooler, which is in communication with the first heat exchanger and is used to cool the deoxidized hydrogen;

[0018] A gas-liquid separator, which is in communication with the cooler and is used to separate the deoxidized hydrogen and the liquid condensate.

[0019] In some feasible embodiments, the adsorption unit includes:

[0020] A first storage tank, which is in communication with the gas-liquid separator. The first storage tank is filled with an adsorbent. After the deoxidized hydrogen flows into the first storage tank, the adsorbent deeply adsorbs the water vapor in the deoxidized hydrogen to obtain product hydrogen;

[0021] A hydrogen main pipe, which is in communication with the first storage tank;

[0022] A filter, which is arranged on the hydrogen main pipe and is in communication with the first storage tank through the hydrogen main pipe.

[0023] In some feasible embodiments, the cooling unit includes:

[0024] A third storage tank, which is arranged at the bottom of the first storage tank and is used to store the regenerated adsorbent;

[0025] A hydrogen branch pipe, one end of which is in communication with the hydrogen main pipe and the other end is in communication with the third storage tank;

[0026] A fan, which is arranged on the hydrogen branch pipe and is used to blow-cool the adsorbent;

[0027] A flow regulating valve is provided on the hydrogen branch pipe to control the flow rate of the regenerated hydrogen.

[0028] In some feasible embodiments, the regeneration unit includes:

[0029] A second storage tank, which is located between the first storage tank and the third storage tank. The top end of the second storage tank is communicated with the bottom end of the first storage tank, and the bottom end of the second storage tank is communicated with the top end of the third storage tank. The second storage tank is used for storing the adsorbent with high humidity;

[0030] A second heat exchanger, one end of which is connected to the second storage tank, and the other end is communicated with the third storage tank and the cooler;

[0031] A second heater, which is arranged on the pipeline between the second heat exchanger and the second storage tank. The second heater is used for heating the regenerated hydrogen.

[0032] In some feasible embodiments, the first storage tank, the second storage tank and the third storage tank are vertically arranged in a tower shape from top to bottom. And, discharge pipes are arranged at the bottom ends of the first storage tank, the second storage tank and the third storage tank, and the first storage tank, the second storage tank and the third storage tank are communicated with each other through the discharge pipes;

[0033] Wherein, manual slide valves for discharging and electric rotary feeding valves for discharging are arranged on the discharge pipes.

[0034] In some feasible embodiments, level gauges are arranged in the first storage tank, the second storage tank and the third storage tank to monitor the material levels of the adsorbent in the first storage tank, the second storage tank and the third storage tank in real time;

[0035] Temperature sensors for monitoring the temperature of the adsorbent are also arranged in the first storage tank, the second storage tank and the third storage tank, and the temperature sensors are electrically connected to the flow regulating valve.

[0036] In some feasible embodiments, the transportation mechanism includes:

[0037] A conveyor, which is arranged below the discharge pipe at the bottom end of the third storage tank;

[0038] A bucket elevator, which is arranged at one end of the conveyor and is adapted to the conveyor;

[0039] A chute, which is located above the first storage tank and is adapted to the bucket elevator;

[0040] Wherein, a discharge valve adapted to the chute is further provided on the first storage tank.

[0041] The second aspect of the present invention provides a purification method for a cyclic hydrogen purification system, which adopts a cyclic hydrogen purification system described in any one of the first aspects. The purification method includes:

[0042] S1: Introduce raw material hydrogen, and perform deoxidation, dehydration, and adsorption on the raw material hydrogen to obtain product hydrogen;

[0043] S2: Replace the adsorbent in the first storage tank according to the saturation degree of the adsorbent in the first storage tank;

[0044] S3: Adjust the flow rate of the regeneration hydrogen through the flow regulating valve according to the temperature deviation value in the second storage tank.

[0045] In some feasible embodiments, adjusting the flow rate of the regeneration hydrogen according to the temperature deviation value in the second storage tank further includes:

[0046] S31: Obtain the temperature deviation value in the second storage tank;

[0047] Wherein, the temperature deviation value = actual temperature value - preset temperature value

[0048] S32: Adjust the flow rate of the regeneration hydrogen based on the temperature deviation value;

[0049] Adjusting the flow rate of the regeneration hydrogen based on the temperature deviation value includes:

[0050] Generate regeneration hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold;

[0051] Generating the first adjustment information for the regeneration hydrogen flow rate based on the temperature deviation value and the first temperature deviation threshold by comparing the temperature deviation value with the first temperature deviation threshold, and generating the regeneration hydrogen flow rate adjustment information when the temperature deviation value exceeds the first temperature deviation threshold.

[0052] Generating regeneration hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold includes:

[0053] S321: Generate the first regeneration hydrogen flow rate adjustment information based on the temperature deviation value and the second temperature deviation threshold;

[0054] Generating the second adjustment information for the regeneration hydrogen flow rate based on the temperature deviation value and the second temperature deviation threshold by comparing the temperature deviation value with the second temperature deviation threshold, and generating the first regeneration hydrogen flow rate adjustment information when the temperature deviation value exceeds the first temperature deviation threshold and is less than the second temperature deviation value.

[0055] The first regenerated hydrogen flow rate adjustment information includes:

[0056] Adjust the flow rate of the regenerated hydrogen based on the temperature deviation value and the second temperature deviation threshold. The specific method is:

[0057] ;

[0058] Wherein, is the flow rate of the regenerated hydrogen obtained at the current time point, is the flow rate of the regenerated hydrogen at the previous time point, is the set second temperature deviation threshold;

[0059] S322. Generate the second regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the third temperature deviation threshold;

[0060] The generation of the second regenerated hydrogen flow rate adjustment information is performed by comparing the temperature deviation value with the third temperature deviation threshold, and generating the second regenerated hydrogen flow rate adjustment information when the temperature deviation value exceeds the second temperature deviation threshold and is less than the third temperature deviation threshold.

[0061] The generation of the second regenerated hydrogen flow rate adjustment information includes:

[0062] Adjust the flow rate of the regenerated hydrogen based on the temperature deviation value. The specific method is:

[0063] ;

[0064] Wherein, is the flow rate of the regenerated hydrogen; is the proportionality coefficient; is the integral coefficient, is the differential coefficient, is the temperature deviation value, is the sampling time.

[0065] The integral coefficient is calculated as:

[0066] ;

[0067] Wherein, is the final integral value, is the amplitude, are the minimum integral value and the maximum integral value respectively.

[0068] The adjustment of the flow rate of the regenerated hydrogen based on the temperature deviation value further includes:

[0069] S323. Generate the third regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the third temperature deviation threshold;

[0070] The third regeneration hydrogen flow rate adjustment information generated based on the temperature deviation value and the third temperature deviation threshold is obtained by comparing the temperature deviation value with the third temperature deviation threshold, and the third regeneration hydrogen flow rate adjustment information is generated when the temperature deviation value exceeds the third temperature deviation threshold.

[0071] The method for adjusting the regeneration hydrogen flow rate based on the temperature deviation value and the third temperature deviation threshold is as follows:

[0072] ;

[0073] Wherein, is the proportional term, is the integral term, is the differential term, are respectively the set minimum flow rate threshold and maximum flow rate threshold.

[0074] The beneficial effects of the present invention are as follows:

[0075] In the present invention, the raw material hydrogen is purified through the deoxidation mechanism and the adsorption drying mechanism, and under the action of the adsorption drying mechanism and the transportation mechanism, the adsorbent completes on-line desorption regeneration and is reused, solving the technical problem of complex control of the hydrogen purification system in the prior art, and achieving the technical effect of recycling the adsorbent. Description of the Drawings

[0076] Figure 1 is the overall structural schematic diagram of a cyclic hydrogen purification system provided in an embodiment of the present invention;

[0077] The marks in the figure are shown as follows:

[0078] 1. Deoxidation mechanism; 11. Deoxidizer; 111. First heater; 12. First heat exchanger; 13. Cooler; 14. Gas-water separator;

[0079] 2. Adsorption drying mechanism; 21. Adsorption unit; 211. First storage tank; 212. Hydrogen main pipe; 213. Filter; 22. Regeneration unit; 221. Second storage tank; 222. Second heat exchanger; 223. Second heater; 23. Cooling unit; 231. Third storage tank; 232. Hydrogen branch pipe; 233. Fan; 234. Flow regulating valve; 24. Discharge pipe; 241. Manual blanking plug valve; 242. Electric rotary feeding valve for blanking;

[0080] 3. Transportation mechanism; 31. Conveyor; 32. Bucket elevator; 33. Chute; 34. Discharge valve. Detailed Embodiments

[0081] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. It is obvious that the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0082] It should be noted that all directional indications (such as up, down, left, right, front, back...) in the embodiments of the present invention are only used to explain the relative position relationship and movement conditions between components in a specific posture (as shown in the accompanying drawings). If the specific posture changes, the directional indications will also change accordingly.

[0083] In the present invention, unless otherwise clearly defined and limited, the terms "connection", "fixation", etc. should be understood in a broad sense. For example, "fixation" can be a fixed connection, a detachable connection, or integrated; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two components or the interaction relationship between two components, unless otherwise clearly limited. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific situations.

[0084] In addition, if there are descriptions involving "first", "second", etc. in the embodiments of the present invention, the descriptions of "first", "second", etc. are only for descriptive purposes and cannot be understood as indicating or implying their relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first" and "second" may explicitly or implicitly include at least one of such features. In addition, the meaning of "and / or" appearing throughout the text includes three parallel solutions. Taking "A and / or B" as an example, it includes solution A, solution B, or a solution that satisfies both A and B at the same time. In addition, the technical solutions between various embodiments can be combined with each other, but it must be based on the fact that those of ordinary skill in the art can implement them. When the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such a combination of technical solutions does not exist and is not within the protection scope required by the present invention.

[0085] Refer to Figure 1 As shown, in order to solve the disadvantages of the complex and cumbersome hydrogen purification process in the prior art, on the one hand, the present invention provides a cyclic hydrogen purification system in an embodiment. The cyclic hydrogen purification system is connected to an electrolytic water hydrogen production device and includes a deoxidation mechanism 1, an adsorption and drying mechanism 2 connected to the deoxidation mechanism 1, and a transportation mechanism 3 connected to the adsorption and drying mechanism 2.

[0086] It should be understood that the cyclic hydrogen purification system in this application needs to operate under positive pressure, and all components of the deoxidation mechanism 1, the adsorption and drying mechanism 2, and the transportation mechanism 3 are designed to be sealed to prevent hydrogen leakage. Corresponding explosion-proof measures are provided for each mechanism and pipeline, which can effectively prevent and reduce the harm caused by explosion and improve the overall safety of the system.

[0087] Specifically, the deoxidation mechanism 1 is connected to the hydrogen outlet of the gas-liquid separator of the electrolytic water hydrogen production device. The deoxidation mechanism 1 can remove the oxygen contained in the raw hydrogen flowing out of the electrolytic water hydrogen production device to obtain deoxidized hydrogen. The raw hydrogen refers to the hydrogen produced by the electrolytic water hydrogen production device, which is doped with impurity oxygen and water vapor. The deoxidized hydrogen refers to the hydrogen obtained after the raw hydrogen is deoxidized, which does not contain impurity oxygen but contains water vapor.

[0088] In this embodiment, the deoxidation mechanism 1 includes a deoxidizer 11, a first heat exchanger 12 connected to the deoxidizer 11, a cooler 13 connected to the first heat exchanger 12, and a gas-water separator 14 connected to the cooler 13.

[0089] Specifically, the deoxidizer 11 is connected to the electrolytic water hydrogen production device. The deoxidizer 11 is filled with a palladium catalyst. After the raw hydrogen enters the deoxidizer 11, a reaction occurs under the action of the palladium catalyst, causing the oxygen and hydrogen in the raw hydrogen to react to form water, thereby removing the impurity oxygen in the raw hydrogen. In this embodiment, since the palladium catalyst has higher activity at high temperatures, to improve the reaction efficiency of oxygen and hydrogen in the raw hydrogen in the deoxidizer 11, a first heater 111 is provided in the deoxidizer 11. The first heater 111 uses an electric heater to convert electrical energy into heat energy, thereby heating the raw hydrogen and the palladium catalyst, and then improving the reaction efficiency of oxygen and hydrogen. It includes, but is not limited to, a resistive electric heater, and can also be an inductive electric heater. Compared with other types of heaters, the electric heater has a high heat conversion efficiency and no open flame hazard, improving the safety of the production process.

[0090] The first heat exchanger 12 is arranged on the pipeline between the electrolytic water hydrogen production device and the deoxidizer 11, and the deoxidizer 11 is connected to the electrolytic water hydrogen production device through the first heat exchanger 12, so that the raw material hydrogen first passes through the first heat exchanger 12 and then enters the deoxidizer 11. Among them, the first heat exchanger 12 includes a first air inlet, a first air outlet, a second air inlet and a second air outlet. The first air inlet is connected to the hydrogen outlet of the electrolytic water hydrogen production device, the first air outlet is connected to the air inlet end of the deoxidizer 11, and the deoxidizer 11 is connected to the electrolytic water hydrogen production device through the first heat exchanger 12, that is, the raw material hydrogen flows out from the hydrogen outlet of the electrolytic water hydrogen production device, enters the first heat exchanger 12 through the first air inlet, and then flows into the deoxidizer 11 through the first air outlet.

[0091] The first heat exchanger 12 can be, but is not limited to, a shell-and-tube heat exchanger, and can also be a plate heat exchanger or a finned heat exchanger and other heat exchangers with heat exchange functions. In this embodiment, the first heat exchanger 12 adopts a shell-and-tube heat exchanger, which is composed of a shell, a tube bundle, a tube sheet, a head and other parts. By the hot fluid flowing in the tube of the shell-and-tube heat exchanger, the heat in the tube is conducted through the tube wall to the cold fluid outside the tube wall, and the cold fluid flows in the shell and absorbs the heat transferred from the hot fluid in the tube, so as to achieve the purpose of heat exchange.

[0092] The second air inlet is connected to the air outlet end of the deoxidizer 11, so that a closed loop is formed between the deoxidizer 11 and the first heat exchanger 12. The deoxidized hydrogen generated after the raw material hydrogen reacts in the deoxidizer 11 flows back into the first heat exchanger 12 through the second air inlet. By using the heat carried by the deoxidized hydrogen, the raw material hydrogen flowing into the heat exchanger from the electrolytic water hydrogen production device subsequently exchanges heat with the deoxidized hydrogen, thereby performing primary heating on the raw material hydrogen before it enters the deoxidizer 11, further increasing the temperature of the raw material hydrogen, and making its reaction with the palladium catalyst more sufficient after it enters the deoxidizer 11.

[0093] The cooler 13 is connected to the second air outlet in the first heat exchanger 12 and is used to cool the deoxidized hydrogen. Since the raw material hydrogen is heated in the deoxidizer 11 during the process of being transformed into deoxidized hydrogen, the temperature of the deoxidized hydrogen flowing out of the deoxidizer 11 is relatively high. After performing primary cooling on the deoxidized hydrogen by exchanging heat with the raw material hydrogen in the first heat exchanger 12, it then flows into the cooler 13 for secondary cooling, so that the water vapor in the deoxidized hydrogen condenses into liquid condensate water.

[0094] In some preferred embodiments, the cooler 13 is a water-cooled industrial chiller, which includes structures such as a cooler 13, a water pump, and a cooling tower. It has high cooling efficiency and low maintenance cost to provide stable and efficient heat dissipation for the deoxygenated hydrogen. More preferably, the cooler 13 adopts the countercurrent principle, making the flow direction of the coolant in the cooler 13 opposite to the flow direction of the hydrogen to optimize the cooling effect.

[0095] The gas-liquid separator 14 is connected to the cooler 13. The gas-liquid separator 14 is used to separate the deoxygenated hydrogen and the liquid condensate. Among them, the gas-liquid separator 14 can be, but is not limited to, a gravity sedimentation type gas-liquid separator 14, and can also be a cyclone type gas-liquid separator 14 or a primary filter type gas-liquid separator 14. In this embodiment, a gravity sedimentation type gas-liquid separator 14 is adopted. After the mixture of deoxygenated hydrogen and condensate enters the separator, due to the density difference between the gas and the liquid, under the action of gravity, the liquid sinks downward due to its larger density and accumulates at the bottom of the separator to form a liquid layer; the gas flows upward due to its smaller density and is discharged from the separator through the gas outlet, thus realizing the separation of the deoxygenated hydrogen and the liquid condensate.

[0096] In this embodiment, the adsorption drying mechanism 2 is connected to the deoxygenation mechanism 1. The adsorption drying mechanism 2 is used to adsorb the water vapor in the deoxygenated hydrogen. Since there is still some water vapor mixed in the deoxygenated hydrogen after the deoxygenated hydrogen removes the condensed liquid water through the gas-liquid separator 14, after the deoxygenated hydrogen flows into the adsorption drying mechanism 2, the water vapor in the deoxygenated hydrogen is adsorbed, thereby obtaining product hydrogen. It should be understood that the product hydrogen refers to clean hydrogen with a purity of 99.8% or more.

[0097] Specifically, the adsorption drying mechanism 2 includes an adsorption unit 21, which is connected to the gas-water separator 14 in the deoxidation mechanism 1 and is used to adsorb water vapor in the deoxidized hydrogen gas. It includes a first storage tank 211 and a filter 213 connected to the first storage tank 211. One end of the first storage tank 211 is connected to the gas-water separator 14. The first storage tank 211 is filled with adsorbents such as activated carbon and molecular sieve for adsorbing water vapor. After the deoxidized hydrogen gas flows into the first storage tank 211, the water vapor in the deoxidized hydrogen gas is deeply adsorbed by the adsorbent, and thus the product hydrogen gas is obtained. The other end of the first storage tank 211 is connected to a hydrogen main pipe 212. The filter 213 is arranged on the hydrogen main pipe 212, and the filter 213 is connected to the first storage tank 211 through the hydrogen main pipe 212. The filter 213 is used to remove impurity dust in the product hydrogen gas. For example, the filter 213 adopts a common cartridge filter 213. When the hydrogen gas containing dust enters the filter 213, it will first contact the filter element. Since the particle size of the dust particles is larger than the size of the pores of the filter element, when the hydrogen gas passes through the filter element, the dust particles will be intercepted on the outer surface of the filter element, thereby realizing the filtration and purification of the dust in the hydrogen gas. The product hydrogen gas purified by the filter 213 is sent to a hydrogen storage tank for storage.

[0098] In this embodiment, since the adsorbent will gradually become saturated after long-term use and the water absorption efficiency will gradually decrease, the adsorption drying mechanism 2 is also used to desorb and regenerate the adsorbent online to achieve the purpose of recycling.

[0099] The adsorption drying mechanism 2 further includes a regeneration unit 22 and a cooling unit 23 connected to the regeneration unit 22. Specifically, the regeneration unit 22 is connected to the first storage tank 211 in the adsorption unit 21, and the regeneration unit 22 is used to desorb and regenerate the adsorbent at high temperature. One end of the cooling unit 23 is connected to the hydrogen main pipe 212 in the adsorption unit 21, and the other end is connected to the regeneration unit 22. By introducing a part of the product hydrogen gas in the hydrogen main pipe 212 as the regeneration hydrogen gas into the cooling unit 23, the adsorbent located in the cooling unit 23 is cooled, and the regeneration hydrogen gas flows into the regeneration unit 22. It should be understood that the regeneration hydrogen gas refers to 10 - 50% of the product hydrogen gas that is filtered by the filter 213 and branched out through the hydrogen main pipe 212.

[0100] More specifically, the cooling unit 23 is connected to the regeneration unit 22 and is used to cool and dry the adsorbent. The cooling unit 23 includes a third storage tank 231, a hydrogen branch pipe 232 connected to the third storage tank 231, and a blower 233 provided on the hydrogen branch pipe 232. The third storage tank 231 is arranged at the bottom end of the first storage tank 211 and is used to store the regenerated adsorbent. One end of the hydrogen branch pipe 232 is connected to the hydrogen main pipe 212, and the other end is connected to the third storage tank 231, so as to introduce the product hydrogen in the hydrogen main pipe 212 into the third storage tank 231 as the regeneration hydrogen through the hydrogen branch pipe 232. Since the regenerated adsorbent is in a high-temperature and high-heat state, in order to make the adsorbent reach an available temperature, the blower 233 is provided on the hydrogen branch pipe 232. The blower 233 is a booster blower 233. On the one hand, it can dynamically adjust the rotation speed according to the pressure requirement of hydrogen, thereby overcoming the resistance of the entire regeneration hydrogen flow through each device and pipeline, making the pressure of the regeneration hydrogen balanced with the pressure of the raw material hydrogen, effectively improving the efficiency and safety of hydrogen transportation. On the other hand, it can blow and cool the high-temperature and high-heat adsorbent in the second storage tank 221 and recover the waste heat, reducing the temperature of the adsorbent to meet the adsorption working temperature requirement.

[0101] In some preferred embodiments, a flow regulating valve 234 is further provided on the hydrogen branch pipe 232, and the flow regulating valve 234 is used to control the flow rate of the regeneration hydrogen entering the hydrogen branch pipe 232.

[0102] In this embodiment, the regeneration unit 22 includes a second storage tank 221, a second heat exchanger 222 connected to the second storage tank 221, and a second heater 223. Specifically, the second storage tank 221 is located between the first storage tank 211 and the third storage tank 231. The second storage tank 221 is used to store the high-humidity adsorbent. The first storage tank 211, the second storage tank 221, and the third storage tank 231 are vertically arranged in a tower shape from top to bottom. Moreover, discharge pipes 24 are provided at the bottom ends of the first storage tank 211, the second storage tank 221, and the third storage tank 231. The first storage tank 211, the second storage tank 221, and the third storage tank 231 are connected through the discharge pipes 24, that is, the top end of the second storage tank 221 is connected to the bottom end of the first storage tank 211, and the bottom end of the second storage tank 221 is connected to the top end of the third storage tank 231, so that the adsorbent in the first storage tank 211 can flow into the second storage tank 221 and the third storage tank 231 in sequence.

[0103] In some preferred embodiments, the first storage tank 211, the second storage tank 221, and the third storage tank 231 are all in the shape of a conical hopper. The conical hopper structure is a geometric structure similar to a cone or a pyramid, with a circular or polygonal (such as square) bottom and a flared top, presenting a gradually narrowing shape from the top to the bottom. This enables the adsorbent to naturally converge towards the bottom discharge ports of the first storage tank 211, the second storage tank 221, and the third storage tank 231 under its own gravity, and reduces the possibility of the adsorbent piling up during flow.

[0104] One end of the second heat exchanger 222 is connected to the second storage tank 221, and the other end is connected to the third storage tank 231. Among them, the structure of the second heat exchanger 222 is the same as that of the first heat exchanger 12. The second heat exchanger 222 includes a third inlet, a third outlet, a fourth inlet, and a fourth outlet. The third inlet is connected to the outlet end of the third storage tank 231, and the third outlet end is connected to the inlet end of the second storage tank 221. After the regenerated hydrogen flows out of the third storage tank 231, it enters the second heat exchanger 222 through the third inlet and enters the second storage tank 221 through the third outlet.

[0105] Since the desorption of the high-humidity adsorbent needs to be carried out in a relatively high-temperature environment, to increase the temperature of the regenerated hydrogen entering the second storage tank 221, the second heater 223 is arranged on the pipeline between the second heat exchanger 222 and the second storage tank 221. The second heat exchanger 222 is composed of a heating element, a heat insulation layer, a shell, a temperature control system, etc. For example, the heating element is a resistance wire. When the power is connected, the current passes through the resistance wire, and the electrical energy is converted into heat energy on the resistance wire, causing the temperature of the resistance wire to rise. Then, the heat is transferred to the object or medium in contact with it through heat conduction, thereby realizing the heating of the object or medium. When the regenerated hydrogen flows out through the third outlet in the second heat exchanger 222, the second heater 223 heats the regenerated hydrogen, so that after the high-temperature regenerated hydrogen enters the second storage tank 221, it can desorb the high-humidity adsorbent in the second storage tank 221 at a high temperature, thereby regenerating the adsorbent. The fourth inlet is connected to the outlet end of the second storage tank 221, and the fourth outlet is connected to the inlet end of the cooler 13, so that a loop is formed between the second storage tank 221 and the second heat exchanger 222. Thus, the regenerated hydrogen flowing out of the second storage tank 221 flows back into the second heat exchanger 222 again and then into the cooler 13 to cool the regenerated hydrogen.

[0106] In this embodiment, when the regenerated hydrogen continuously flows into the second heat exchanger 222, since the regenerated hydrogen flowing into the second storage tank 221 is heated by the second heater 223, its heat is much higher than the heat of the regenerated hydrogen flowing from the third storage tank 231 into the second heat exchanger 222. Therefore, the regenerated hydrogen flowing back into the second heat exchanger 222 from the second storage tank 221 exchanges heat with the regenerated hydrogen flowing into the second heat exchanger 222 from the third storage tank 231 in the second heat exchanger 222. When the regenerated hydrogen flows into the second storage tank 221, the regenerated hydrogen is preheated at the first stage through the heat exchange of the second heat exchanger 222, and the second heater 223 performs the second-stage heating on the regenerated hydrogen, so that the regenerated hydrogen flowing into the second storage tank 221 reaches the temperature required for the desorption and regeneration of the adsorbent.

[0107] When the regenerated hydrogen flows back into the second heat exchanger 222 from the second storage tank 221, the heated regenerated hydrogen can exchange heat with the regenerated hydrogen flowing into the second heat exchanger 222 from the third air inlet through the second heat exchanger 222, so that the regenerated hydrogen is cooled at the first stage. Since the water generated after the adsorbent in the second storage tank 221 is desorbed enters the regenerated hydrogen in the form of water vapor, at this time, both the regenerated hydrogen and the deoxygenated hydrogen are hydrogen containing water. Therefore, the regenerated hydrogen flows into the cooler 13 through the fourth air outlet, converges with the deoxygenated hydrogen, and undergoes the same cooling, dehydration, and adsorption processes as the deoxygenated hydrogen to regenerate the product hydrogen, thus realizing the recycling of the regenerated hydrogen and reducing the use cost.

[0108] In this embodiment, a manual slide valve 241 and an electric rotary feeder valve 242 are arranged on the discharge pipe 24, and the electric rotary feeder valve 242 is located below the manual slide valve 241. For example, the manual slide valve 241 is composed of components such as a valve body, a valve plate, an operating rod, and a sealing ring. By controlling the operating rod, the opening and closing of the discharge pipe 24 can be realized to control the flow of the adsorbent in the discharge pipe 24. The electric rotary feeder valve 242 is composed of components such as a valve body, a valve wheel, a frequency conversion motor, a speed reducer, and a sealing ring. The valve wheel and the valve body form a closed channel. The frequency conversion motor drives the speed reducer to drive the valve wheel to rotate, realizing precise control and adjustment of the material to adjust the flow rate of the adsorbent flowing through the discharge pipe 24. Moreover, the rotary feeder valve needs to have a gas locking function to prevent the air flow from intermixing between the front and rear of the valve, thereby affecting the purity of the product hydrogen.

[0109] In some preferred embodiments, level gauges are provided in the first storage tank 211, the second storage tank 221, and the third storage tank 231 to monitor the amount of adsorbent filled therein in real time. To facilitate real-time monitoring of the temperature of the adsorbent in the first storage tank 211, the second storage tank 221, and the third storage tank 231, temperature sensors are further provided in the first storage tank 211, the second storage tank 221, and the third storage tank 231, and the temperature sensors are in telecommunication connection with the flow regulating valve 234. For example, the temperature sensor is a thermocouple temperature sensor, which measures temperature using the thermoelectric effect, has a fast response speed and high accuracy. When the temperature monitored by the temperature sensor changes, the opening degree of the flow regulating valve 234 can be controlled by an external controller, thereby adjusting the flow rate of the regenerative hydrogen.

[0110] In this embodiment, to achieve the purpose of reusing the adsorbent after desorption, the adsorbent after desorption is refilled into the first storage tank 211 for use. The transport mechanism 3 is adapted to the adsorption drying mechanism 2. One end thereof is located at the bottom end of the third storage tank 231, and the other end is located at the top end of the first storage tank 211. The adsorbent in the third storage tank 231 is transported to the first storage tank 211 through the transport mechanism 3, so that the adsorbent circulates in the adsorption drying mechanism 2.

[0111] Specifically, the transportation mechanism 3 includes a conveyor 31, a bucket elevator 32 adapted to the conveyor 31, a chute 33 connected to the bucket elevator 32, and a discharge valve 34 adapted to the chute 33. Specifically, the conveyor 31 is arranged below the discharge pipe 24 at the bottom end of the third storage box 231. Preferably, the conveyor 31 adopts a closed belt conveyor 31, which is composed of components such as a conveyor belt, idlers, a driver, and a closed housing. When the adsorbent in the third storage box 231 falls onto the conveyor 31, the adsorbent is transported by the belt of the conveyor to perform a primary transfer, and the closed housing prevents the adsorbent dust from splashing and scattering during the transfer, improving safety. The bucket elevator 32 is arranged at one end of the conveyor 31 and is adapted to the conveyor 31. For example, the bucket elevator 32 includes structures such as a chain, a hopper, and a driver. After the conveyor 31 transports the adsorbent to the bucket elevator 32, the adsorbent falls into the hopper. When the hopper is loaded with the adsorbent, the hopper is lifted to a height adapted to the first storage box 211 by the chain. And when the hopper is lifted to the set position, it automatically flips and discharges the adsorbent to perform a secondary transfer. The chute 33 is located above the first storage box 211 and is adapted to the bucket elevator 32, that is, the chute 33 is inclined. One end of it is adapted to the bucket elevator 32, and the other end is connected to the top end of the first storage box 211. That is, the end of the chute 33 close to the bucket elevator 32 is higher than the end connected to the first storage box 211, so that the adsorbent can naturally slide down by gravity to perform a third transfer of the adsorbent and make the adsorbent re-enter the first storage box 211 for recycling.

[0112] In some preferred embodiments, to prevent a large amount of air flow from surging when the adsorbent falls into the first storage box 211, the discharge valve 34 is arranged on the first storage box 211 and is adapted to the chute 33. That is, at the connection between the chute 33 and the first storage box 211, the discharge valve 34 is a double-layer heavy hammer flap valve. Its working principle is to use the self-gravity of the material to open the flap for discharging. When the material stops falling, the flap returns to the closed state under the action of the heavy hammer, achieving the purpose of preventing air flow from surging and reducing the scattering and flying of the adsorbent.

[0113] Referring to Figure 1 , the present application also provides a cyclic hydrogen purification method in a second aspect. The purification method is based on a cyclic hydrogen purification system described in the above solution. The purification method includes:

[0114] S1: Introduce raw hydrogen, perform deoxidation, dehydration, and adsorption on the raw hydrogen to obtain product hydrogen;

[0115] In this step, the raw material hydrogen flows into the deoxidizer 11 after being heated at the first stage by the first heat exchanger 12, and is heated at the second stage under the action of the first heater 111, so that the temperature of the raw material hydrogen reaches the requirement of the reaction temperature with the palladium catalyst. In the deoxidizer 11, the raw material hydrogen undergoes a chemical reaction under the action of the catalyst and high temperature to generate water, thereby removing the impurity oxygen in the raw material hydrogen and generating deoxidized hydrogen. The deoxidized hydrogen flows back into the first heat exchanger 12 again to exchange heat with the raw material hydrogen flowing out of the hydrogen outlet of the gas-liquid separator of the electrolyzed water hydrogen production device. After the first-stage cooling of the deoxidized hydrogen, it flows into the cooler 13 for the second-stage cooling. At this time, the water vapor in the deoxidized hydrogen becomes condensed water after cooling and flows into the gas-water separator 14 to separate and remove the condensed water. The raw material hydrogen after water removal enters the first storage tank 211 in the adsorption unit 21, and is deeply adsorbed and dehydrated by the adsorbent to obtain product hydrogen. During the process of the product hydrogen passing through the hydrogen main pipe 212, the product hydrogen is filtered by the filter 213 to obtain relatively pure hydrogen and sent to the hydrogen storage tank for storage.

[0116] S2: Replace the adsorbent in the first storage tank 211 according to the saturation degree of the adsorbent in the first storage tank 211;

[0117] The saturation degree of the adsorbent in the first storage tank 211 can be judged by the input amount of the raw material hydrogen. When the input amount of the deoxidized hydrogen in the first storage tank 211 exceeds the set input amount threshold, it means that the adsorbent has reached the saturation state and the adsorbent in the first storage tank 211 needs to be replaced;

[0118] Among them, the method of replacing the adsorbent in the first storage tank 211 is that the water-absorbed adsorbent in the first storage tank 211 flows into the second storage tank 221 for desorption and regeneration through the feeding electric rotary feeder valve 242. The desorbed and regenerated adsorbent in the second storage tank 221 flows into the third storage tank 231 for cooling. The adsorbent after cooling in the third storage tank 231 is fed into the conveyor 31, and the adsorbent that has completed desorption and cooling in the third storage tank is refilled into the first storage tank 211 through the transportation mechanism 3.

[0119] S3. Adjust the flow rate of the regeneration hydrogen according to the temperature deviation value in the second storage tank 221 through the flow regulating valve 234;

[0120] It can be understood that if the flow rate of the regenerated hydrogen introduced into the second storage tank 221 is too large, the adsorbent after adsorption treatment in the second storage tank 221 can be fully dried, but it will increase energy consumption and production costs. If the flow rate of the regenerated hydrogen is too small, the adsorbent after adsorption treatment in the second storage tank 221 cannot be fully dried. Therefore, to accurately control the flow rate of the regenerated hydrogen introduced into the second storage tank, adjusting the flow rate of the regenerated hydrogen according to the temperature deviation value in the second storage tank 221 includes:

[0121] S31. Obtain the temperature deviation value in the second storage tank 221;

[0122] Among them, the temperature deviation value = actual temperature value - preset temperature value;

[0123] The actual temperature value can be obtained by a temperature sensor provided in the second storage tank 221, and the preset temperature value can be obtained based on a database, historical data or experimental analysis.

[0124] S32. Adjust the flow rate of the regenerated hydrogen based on the temperature deviation value;

[0125] Adjusting the flow rate of the regenerated hydrogen based on the temperature deviation value includes:

[0126] Generate regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold;

[0127] The first temperature deviation threshold can be set based on a database, historical data or experimental analysis.

[0128] In some embodiments, generating the first regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold can be achieved by comparing the temperature deviation value with the first temperature deviation threshold. When the temperature deviation value exceeds the first temperature deviation threshold, regenerated hydrogen flow rate adjustment information is generated. For example, when the temperature deviation value exceeds the first temperature deviation threshold, the flow rate of the regenerated hydrogen is increased to reduce the temperature deviation and make the temperature deviation stable within the first temperature deviation threshold, so that the adsorbent can be fully dried while reducing energy consumption.

[0129] Generating regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold includes:

[0130] S321. Generate the first regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the second temperature deviation threshold;

[0131] The second temperature deviation threshold can also be set based on a database, historical data or experimental analysis;

[0132] In some embodiments, generating the second regulation information for the regenerated hydrogen flow based on the temperature deviation value and the second temperature deviation threshold may be achieved by comparing the temperature deviation value with the second temperature deviation threshold. When the temperature deviation value exceeds the first temperature deviation threshold and is less than the second temperature deviation value, the first regulation information for the regenerated hydrogen flow is generated;

[0133] The first regulation information for the regenerated hydrogen flow includes:

[0134] Adjusting the flow rate of the regenerated hydrogen based on the temperature deviation value and the second temperature deviation threshold, the specific method is:

[0135] ;

[0136] Wherein, is the regenerated hydrogen flow rate obtained at the current time point, is the regenerated hydrogen flow rate at the previous time point, is the set second temperature deviation threshold;

[0137] The reason for the above is that when the temperature deviation value slightly exceeds the first temperature deviation threshold, by setting the first regulation information for the regenerated hydrogen flow to maintain a stable flow rate, frequent adjustment can be reduced, energy consumption can be lowered, and the service life of the equipment can be extended.

[0138] S322. Generating the second regulation information for the regenerated hydrogen flow based on the temperature deviation value and the third temperature deviation threshold;

[0139] In some embodiments, generating the second regulation information for the regenerated hydrogen flow based on the temperature deviation value and the third temperature deviation threshold may be achieved by comparing the temperature deviation value with the third temperature deviation threshold. When the temperature deviation value exceeds the second temperature deviation threshold and is less than the third temperature deviation threshold, the second regulation information for the regenerated hydrogen flow is generated;

[0140] Generating the second regulation information for the regenerated hydrogen flow includes:

[0141] Adjusting the flow rate of the regenerated hydrogen based on the temperature deviation value, the specific method is:

[0142] ;

[0143] Wherein, is the flow rate of the regenerated hydrogen; is the proportionality coefficient; is the integral coefficient, is the differential coefficient, is the temperature deviation value, is the sampling time;

[0144] In some embodiments, the integral coefficient is calculated as:

[0145] ;

[0146] Wherein, is the final integral coefficient, is the amplitude, are the minimum integral coefficient and the maximum integral coefficient respectively;

[0147] By setting the minimum and maximum values of the integral coefficient, it is avoided that the integral coefficient is distorted due to the change of the temperature deviation value, so as to avoid calculation errors during the process of adjusting the flow rate of the regenerated hydrogen, and the integral coefficient is limited.

[0148] In some embodiments, the method for adjusting the flow rate of the regenerated hydrogen based on the temperature deviation value further includes:

[0149] S323. Generating third regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the third temperature deviation threshold;

[0150] The third temperature deviation threshold can be set based on a database, historical data or experimental analysis;

[0151] In some embodiments, the generating of the third regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the third temperature deviation threshold can be performed by comparing the temperature deviation value with the third temperature deviation threshold, and generating the third regenerated hydrogen flow rate adjustment information when the temperature deviation value exceeds the third temperature deviation threshold;

[0152] The method for adjusting the flow rate of the regenerated hydrogen based on the temperature deviation value and the third temperature deviation threshold is:

[0153] ;

[0154] Wherein, is the proportionality coefficient, is the integral coefficient, is the differential coefficient, are the set minimum flow threshold and maximum flow threshold respectively;

[0155] When the temperature deviation value exceeds the third temperature deviation threshold, if the flow rate of the regenerated hydrogen is adjusted greatly, it may cause the flow rate of the regenerated hydrogen to be too large, resulting in the flow rate of the regenerated hydrogen exceeding the safe range and causing system failure. By setting the minimum and maximum thresholds of the regeneration flow rate, the flow rate of the regenerated hydrogen is controlled to be within the safe range, thereby improving the safety during the operation of the system.

[0156] The above are only the preferred specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution and inventive concept of the present invention, makes equivalent substitutions or changes, and should be covered within the protection scope of the present invention.

Claims

1. A cyclic hydrogen purification method, characterized in that, Based on a cyclic hydrogen purification system, the purification system includes: A deoxidation mechanism (1); the deoxidation mechanism (1) includes a cooler (13); An adsorption and drying mechanism (2), the adsorption and drying mechanism (2) is connected to the deoxidation mechanism (1); The adsorption and drying mechanism (2) includes: An adsorption unit (21), the adsorption unit (21) is connected to the deoxidation mechanism (1) and is used for adsorbing and dehydrating deoxidized hydrogen; A regeneration unit (22), the regeneration unit (22) is connected to the adsorption unit (21) and is used for desorbing and regenerating the adsorbent. The regeneration unit (22) includes a second heat exchanger (222), the second heat exchanger (222) includes a fourth air outlet, and the regenerated hydrogen flows into the cooler (13) through the fourth air outlet; A cooling unit (23), the cooling unit (23) is connected to the regeneration unit (22) and is used for cooling and drying the adsorbent; The adsorption unit (21) includes: A first storage box (211), the first storage box (211) is filled with an adsorbent; The regeneration unit (22) includes: A second storage box (221), the second storage box (221) is used for storing the adsorbent; The cooling unit (23) includes: A third storage box (231), the third storage box (231) is used for storing the regenerated adsorbent; A flow regulating valve (234) for controlling the flow rate of the regenerated hydrogen; The cyclic hydrogen purification method includes: S1: Introduce raw hydrogen, deoxidize, dehydrate and adsorb the raw hydrogen to obtain product hydrogen; S2: Replace the adsorbent in the first storage box (211) according to the saturation degree of the adsorbent in the first storage box (211); S3: Adjust the flow rate of the regenerated hydrogen through the flow regulating valve (234) according to the temperature deviation value in the second storage box (221); Adjusting the flow rate of the regenerated hydrogen according to the temperature deviation value in the second storage box (221) includes: S31. Obtain the temperature deviation value in the second storage box (221); Wherein, the temperature deviation value = actual temperature value - preset temperature value; S32. Adjust the flow rate of the regenerated hydrogen based on the temperature deviation value; Generating the regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold includes: S321. Generate the first regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the second temperature deviation threshold; S322. Generate the second regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the third temperature deviation threshold; Generating the regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the first temperature deviation threshold is by comparing the temperature deviation value with the first temperature deviation threshold, and generating the regenerated hydrogen flow rate adjustment information when the temperature deviation value exceeds the first temperature deviation threshold; Generating the first regenerated hydrogen flow rate adjustment information based on the temperature deviation value and the second temperature deviation threshold is by comparing the temperature deviation value with the second temperature deviation threshold, and generating the first regenerated hydrogen flow rate adjustment information when the temperature deviation value exceeds the first temperature deviation threshold and is less than the second temperature deviation threshold; The generation of the second regenerated hydrogen flow regulation information based on the temperature deviation value and the third temperature deviation threshold generates the second regenerated hydrogen flow regulation information by comparing the temperature deviation value with the third temperature deviation threshold. When the temperature deviation value exceeds the second temperature deviation threshold and is less than the third temperature deviation threshold, the second regenerated hydrogen flow regulation information is generated; The regulation of the regenerated hydrogen flow based on the temperature deviation value further includes: Generating the third regenerated hydrogen flow regulation information based on the temperature deviation value and the third temperature deviation threshold; The generation of the third regenerated hydrogen flow regulation information based on the temperature deviation value and the third temperature deviation threshold generates the third regenerated hydrogen flow regulation information by comparing the temperature deviation value with the third temperature deviation threshold. When the temperature deviation value exceeds the third temperature deviation threshold, the third regenerated hydrogen flow regulation information is generated.

2. A cyclic hydrogen purification method according to claim 1, wherein The first regenerated hydrogen flow regulation information includes: Regulating the flow of the regenerated hydrogen based on the temperature deviation value and the second temperature deviation threshold. The specific method is: ； Wherein, is the flow rate of the recycled hydrogen obtained at the current time point, is the flow rate of the recycled hydrogen at the previous time point, is the set second temperature deviation threshold; The generation of the second regenerated hydrogen flow regulation information includes: Regulating the flow of the regenerated hydrogen based on the temperature deviation value. The specific method is: ； Among them, is the flow rate of the recycled hydrogen; is the proportionality coefficient; is the integral coefficient, is the differential coefficient, is the temperature deviation value, is the sampling time; Among them, the calculation method of the integral coefficient is: ； Among them, is the final integral coefficient, is the amplitude, are the minimum integral coefficient and the maximum integral coefficient respectively; The method of regulating the regenerated hydrogen flow based on the temperature deviation value and the third temperature deviation threshold is: ； Among them, is the proportional term, is the integral term, is the derivative term, are respectively the set minimum and maximum flow thresholds.

3. A cyclic hydrogen purification method according to claim 1, characterized in that The deoxidation mechanism (1) is connected to the hydrogen outlet of the gas-liquid separator of the electrolytic water hydrogen production device and is used to remove oxygen in the raw material hydrogen; The adsorption drying mechanism (2) is filled with an adsorbent for adsorbing water vapor; Among them, the adsorption drying mechanism (2) further includes: An adsorption unit (21), the adsorption unit (21) is connected to the deoxidation mechanism (1) and is used for adsorbing and dehydrating the deoxidized hydrogen; The purification system further includes: A transportation mechanism (3), the transportation mechanism (3) is adapted to the adsorption drying mechanism (2) and is used for transporting the adsorbent to make the adsorbent circulate in the adsorption drying mechanism (2).

4. A cyclic hydrogen purification method according to claim 3, characterized in that, The deoxidation mechanism (1) includes: A deoxidizer (11), the deoxidizer (11) is connected to the electrolytic water hydrogen production device, the deoxidizer (11) is filled with a palladium catalyst, and oxygen in the raw material hydrogen reacts with hydrogen under the action of the palladium catalyst to generate water, removing oxygen in the raw material hydrogen. A first heater (111) is also provided in the deoxidizer (11); A first heat exchanger (12), the first heat exchanger (12) is arranged on the pipeline between the electrolytic water hydrogen production device and the deoxidizer (11), and the deoxidizer (11) is connected to the electrolytic water hydrogen production device through the first heat exchanger (12); A gas-water separator (14), the gas-water separator (14) is connected to the cooler (13), and the gas-water separator (14) is used for separating the deoxidized hydrogen and the liquid condensate.

5. A cyclic hydrogen purification method according to claim 4, characterized in that, The adsorption unit (21) further includes: A hydrogen main pipe (212), the hydrogen main pipe (212) is connected to the first storage tank (211); Filter (213), which is arranged on the hydrogen main pipe (212), and the filter (213) is connected to the first storage tank (211) through the hydrogen main pipe (212).

6. A cyclic hydrogen purification method according to claim 5, characterized in that, The cooling unit (23) further includes: Hydrogen branch pipe (232), one end of the hydrogen branch pipe (232) is connected to the hydrogen main pipe (212), and the other end is connected to the third storage tank (231), and the flow regulating valve (234) is arranged on the hydrogen branch pipe (232); Fan (233), which is arranged on the hydrogen branch pipe (232) and is used to blow and cool the adsorbent.

7. A cyclic hydrogen purification method according to claim 1, characterized in that, The second storage tank (221) is located between the first storage tank (211) and the third storage tank (231), and the top end of the second storage tank (221) is connected to the bottom end of the first storage tank (211), and the bottom end of the second storage tank (221) is connected to the top end of the third storage tank (231); The regeneration unit (22) further includes: Second heater (223), which is arranged on the pipeline between the second heat exchanger (222) and the second storage tank (221), and the second heater (223) is used to heat the regeneration hydrogen.

8. A cyclic hydrogen purification method according to claim 5, characterized in that, The first storage tank (211), the second storage tank (221) and the third storage tank (231) are vertically arranged in a tower shape from top to bottom, and discharge pipes (24) are arranged at the bottom ends of the first storage tank (211), the second storage tank (221) and the third storage tank (231), and the first storage tank (211), the second storage tank (221) and the third storage tank (231) are connected through the discharge pipes (24); Wherein, manual blanking plug valves (241) and electric rotary feeding valves (242) for blanking are arranged on the discharge pipes (24).

9. A cyclic hydrogen purification method according to claim 5, characterized in that, Level gauges are arranged in the first storage tank (211), the second storage tank (221) and the third storage tank (231) to monitor the level of the adsorbent in the first storage tank (211), the second storage tank (221) and the third storage tank (231) in real time; Temperature sensors for monitoring the temperature of the adsorbent are also arranged in the first storage tank (211), the second storage tank (221) and the third storage tank (231), and the temperature sensors are electrically connected to the flow regulating valve (234).

10. A cyclic hydrogen purification method according to claim 8, characterized in that, The transportation mechanism (3) includes: Conveyor (31), which is arranged below the discharge pipe (24) at the bottom end of the third storage tank (231); Bucket elevator (32), which is arranged at one end of the conveyor (31) and is adapted to the conveyor (31); Chute (33), which is located above the first storage tank (211) and is adapted to the bucket elevator (32); Among them, a discharge valve (34) adapted to the chute (33) is further provided on the first storage box (211).

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