Green hydrogen dehydrating and drying system and treatment method thereof

Abstract

The invention relates to a green hydrogen dehydrating and drying system which comprises a plurality of drying modules, a cooler, a gas-liquid separator, a raw material hydrogen inlet, a product gas outlet, a heater and corresponding connecting pipelines, and the plurality of drying modules are communicated with one another; the raw material hydrogen inlet and the product gas outlet are respectively connected with the plurality of drying modules through connecting pipelines; the heater is connected with the drying module through a connecting pipeline and is used for heating dry regenerated hydrogen; the cooler is connected with the drying module through a connecting pipeline and is used for reducing the temperature of the high-temperature regenerated hydrogen; an inlet of the gas-liquid separator is connected with an outlet of the cooler through a connecting pipeline, and free water in the low-temperature regenerated hydrogen flows out. The green hydrogen dewatering and drying device and the treatment method thereof have the advantages that the problem that a matched dewatering and drying device cannot work at the load of 0-100% due to load change of a hydrogen production system in an existing treatment mode is solved.

Description

Technical Field

[0001] The present invention belongs to the technical field of hydrogen dehydration and drying, and particularly relates to a green hydrogen dehydration and drying system and a treatment method thereof. Background Art

[0002] Traditional electrolytic water hydrogen production devices use commercial power to produce hydrogen, and the power supply is stable. According to the existing technical level, the single-set load of electrolytic water hydrogen production devices is between 30% and 100%. The hydrogen produced by electrolytic water hydrogen production devices must be dried, and the processing load of the dehydration and drying devices supporting traditional electrolytic water hydrogen production devices using commercial power is between 20% and 100%.

[0003] Due to the demand for carbon neutrality, China has started to use a large amount of renewable electricity to produce green hydrogen. New energy photovoltaic and wind power have the characteristics of unstable power supply, and the power load range is 0 - 100%. Correspondingly, the hydrogen production capacity of electrolytic water hydrogen production equipment will also fluctuate between 0 and 100%. At this time, the existing hydrogen dehydration and drying devices in related technologies cannot be applied. Therefore, it is urgent to propose a green hydrogen dehydration and drying system and a treatment method thereof. Summary of the Invention

[0004] Object of the Invention

[0005] The object of the present invention is to provide a green hydrogen dehydration and drying system and a treatment method thereof to solve the problem that the supporting dehydration and drying device cannot work at 0 - 100% load due to the change of the load of the hydrogen production system in the existing treatment method.

[0006] To achieve the above object, the present invention provides the following technical solutions:

[0007] A green hydrogen dehydration and drying system includes a drying module, a cooler, a gas-liquid separator, a raw material hydrogen inlet, a product gas outlet, a heater, and corresponding connecting pipes. A plurality of drying modules are provided, and the plurality of drying modules are interconnected; the raw material hydrogen inlet and the product gas outlet are respectively connected to the plurality of drying modules through connecting pipes; the heater is connected to the drying module through a connecting pipe and is used to heat dry regeneration hydrogen;

[0008] The cooler is connected to the drying module through a connecting pipe and is used to reduce the temperature of high-temperature regeneration hydrogen;

[0009] The inlet of the gas-liquid separator is connected to the outlet of the cooler through a connecting pipe and is used to discharge the free water in the low-temperature regeneration hydrogen.

[0010] As a further description of the above solution, three drying modules are provided, namely drying module a, drying module b, and drying module c; when the green hydrogen dehydration and drying system is running, drying module a, drying module b, and drying module c have the following working connection states,

[0011] The first working connection state: the drying module c, the drying module a, and the drying module b are connected in series in sequence;

[0012] The second working connection state: the drying module b, the drying module c, and the drying module a are connected in series in sequence;

[0013] The third working connection state: the drying module a, the drying module b, and the drying module c are connected in series in sequence.

[0014] As a further description of the above solution, the drying module a includes a first drying tower, a switching valve aa, a switching valve ab, a switching valve ac, a switching valve ad, a switching valve ae, a switching valve af, and corresponding connecting pipes; the A interface of the first drying tower is respectively connected to the B port of the switching valve aa, the B port of the switching valve ab, and the B port of the switching valve ac through connecting pipes; the B interface of the first drying tower is respectively connected to the A port of the switching valve ad, the A port of the switching valve ae, and the A port of the switching valve af through connecting pipes;

[0015] The drying module b includes a second drying tower, a switching valve ba, a switching valve bb, a switching valve bc, a switching valve bd, a switching valve be, a switching valve bf, and corresponding connecting pipes; the A interface of the second drying tower is respectively connected to the B port of the switching valve ba, the B port of the switching valve bb, and the B port of the switching valve bc through connecting pipes; the B interface of the second drying tower is respectively connected to the A port of the switching valve bd, the A port of the switching valve be, and the A port of the switching valve bf through connecting pipes;

[0016] The drying module c includes a third drying tower, a switching valve ca, a switching valve cb, a switching valve cc, a switching valve cd, a switching valve ce, a switching valve cf, and corresponding connecting pipes; the A interface of the third drying tower is respectively connected to the B port of the switching valve ca, the B port of the switching valve cb, and the B port of the switching valve cc through connecting pipes; the B interface of the third drying tower is connected to the A port of the switching valve cd, the A port of the switching valve ce, and the A port of the switching valve through connecting pipes;

[0017] The raw material hydrogen inlet is connected to the A port of the switching valve aa, the A port of the switching valve ba, and the A port of the switching valve ca through connecting pipes; the product gas outlet is connected to the B port of the switching valve ad, the B port of the switching valve bd, and the B port of the switching valve cd through connecting pipes;

[0018] The inlet of the cooler is connected to the A ports of the switching valves ab, bb, and cb through connecting pipes respectively; the outlet of the cooler is connected to the inlet of the gas-liquid separator through a connecting pipe; the gas-phase outlet of the gas-liquid separator is connected to the A ports of the switching valves ac, bc, and cc through connecting pipes respectively; the inlet of the heater is connected to the B ports of the switching valves ae, be, and ce through connecting pipes respectively; the outlet of the heater is connected to the B ports of the switching valves af, bf, and cf through connecting pipes respectively.

[0019] As a further description of the above solution, the above green hydrogen dehydration and drying system further includes a free water outlet, a first dew point monitoring port, a second dew point monitoring port, and a third dew point monitoring port;

[0020] The free water outlet is connected to the liquid-phase outlet of the gas-liquid separator through a connecting pipe;

[0021] The first dew point monitoring port is communicated with the B interface of the first drying tower;

[0022] The second dew point monitoring port is communicated with the B interface of the second drying tower;

[0023] The third dew point monitoring port is communicated with the B interface of the third drying tower.

[0024] As a further description of the above solution, the first drying tower, the second drying tower, and the third drying tower are filled with adsorbents inside. The adsorbents are used to adsorb and dry the moisture in hydrogen, and the adsorbents are one or more combinations of molecular sieves, activated alumina, and silica gel;

[0025] The cooler uses cooling water or air as the cooling medium;

[0026] The heater uses resistance wires, steam, or heat-conducting oil as the heat medium.

[0027] A continuous hydrogen processing method using the above green hydrogen dehydration and drying system. Start any one of the multiple drying modules as the first drying module to enter the adsorption process. The first drying module adsorbs all the raw hydrogen entering from the raw hydrogen inlet. After adsorption, all the raw hydrogen becomes dry regeneration hydrogen; the dry regeneration hydrogen enters the second drying module in the regeneration process after passing through the heater. The regeneration hydrogen leaving this drying module enters the gas-liquid separator after being cooled by the cooler and becomes wet regeneration hydrogen; the wet regeneration hydrogen enters the third drying module in the auxiliary adsorption process. After auxiliary adsorption, the wet regeneration hydrogen is dried and flows out from the product gas outlet as the product gas;

[0028] After the regeneration of the second drying module is completed, the three drying modules enter the series adsorption process. The series sequence is the first drying module, the second drying module, and the third drying module in turn. The first drying module continues to adsorb the raw hydrogen gas entering from the raw hydrogen gas inlet. The raw hydrogen gas after adsorption is dried and flows through the second drying module and the third drying module in turn, and then flows out as the product gas from the product gas outlet. When the first drying module is saturated with adsorption, its adsorption of the raw hydrogen gas is stopped and it is regenerated. The third drying module enters the adsorption process, and the second drying module enters the auxiliary adsorption process.

[0029] Repeat the above steps, switch the first drying module, the second drying module, and the third drying module to perform adsorption, regeneration, auxiliary adsorption, and series adsorption operations, and cycle repeatedly to achieve continuous drying of the raw hydrogen gas.

[0030] As a further description of the above solution, there are three drying modules, namely drying module a, drying module b, and drying module c. When the green hydrogen dehydration drying system is running, it includes the following steps:

[0031] Step 1: Drying module c adsorbs, drying module a is regenerated, and drying module b performs auxiliary adsorption. The end sign of Step 1 is the end of the regeneration of drying module a.

[0032] Step 2: Drying module c, drying module a, and drying module b are connected in series for adsorption in turn. The end sign of Step 2 is that the dew point monitored by the third dew point monitoring port reaches the set threshold.

[0033] Step 3: Drying module b adsorbs, drying module c is regenerated, and drying module a performs auxiliary adsorption. The end sign of Step 3 is the end of the regeneration of drying module c.

[0034] Step 4: Drying module b, drying module c, and drying module a are connected in series for adsorption in turn. The end sign of Step 4 is that the dew point monitored by the second dew point monitoring port reaches the set threshold.

[0035] Step 5: Drying module a adsorbs, drying module b is regenerated, and drying module c performs auxiliary adsorption. The end sign of Step 5 is the end of the regeneration of drying module b.

[0036] Step 6: Drying module a, drying module b, and drying module c are connected in series for adsorption in turn. The end sign of Step 6 is that the dew point monitored by the first dew point monitoring port reaches the set threshold.

[0037] Step 7: Repeat Steps 1 to 6 to achieve continuous drying of hydrogen.

[0038] As a further description of the above solution, in Step 1, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module c, the heater, the drying module a, the cooler, the gas-liquid separator, and the drying module b to obtain the product gas, and the product gas flows out through the product gas outlet; in this step, after the hydrogen gas flows through the cooler, the water vapor in the hydrogen gas precipitates free water due to the temperature drop, and the free water flows out from the free water outlet;

[0039] In Step 2, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module c, the drying module a, and the drying module b to obtain the product gas, and the product gas flows out through the product gas outlet; the cooler, the gas-liquid separator, and the heater are set not to be connected to the gas flow path;

[0040] In Step 3, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module b, the heater, the drying module c, the cooler, the gas-liquid separator, and the drying module a to obtain the product gas, and the product gas flows out through the product gas outlet; in this step, after the hydrogen gas flows through the cooler, the water vapor in the hydrogen gas precipitates free water due to the temperature drop, and the free water flows out from the free water outlet;

[0041] In Step 4, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module b, the drying module c, and the drying module a to obtain the product gas, and the product gas flows out through the product gas outlet; the cooler, the gas-liquid separator, and the heater are set not to be connected to the gas flow path;

[0042] In Step 5, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module a, the heater, the drying module b, the cooler, the gas-liquid separator, and the drying module c to obtain the product gas, and the product gas flows out through the product gas outlet; in this step, after the hydrogen gas flows through the cooler, the water vapor in the hydrogen gas precipitates free water due to the temperature drop, and the free water flows out from the free water outlet;

[0043] In Step 6, the raw material hydrogen enters from the raw material hydrogen inlet, and successively flows through the drying module a, the drying module b, and the drying module c to obtain the product gas, and the product gas flows out through the product gas outlet; the cooler, the gas-liquid separator, and the heater are set not to be connected to the gas flow path;

[0044] As a further description of the above solution, the cooler, the gas-liquid separator, and the heater in Step 2 are replaced with those connected to the gas flow path; the cooler, the gas-liquid separator, and the heater in Step 4 are replaced with those connected to the gas flow path; the cooler, the gas-liquid separator, and the heater in Step 6 are replaced with those connected to the gas flow path.

[0045] As a further description of the above solution, the adsorption means that the raw material hydrogen gas passes through drying module a, drying module b, or drying module c, and the water in the raw material hydrogen gas is adsorbed by the adsorbent filled in the drying tower of one of the drying modules to obtain dry hydrogen gas; after the adsorbent is saturated with adsorption, regeneration is required. During regeneration, the water adsorbed by the adsorbent is desorbed, and after the regeneration is completed, the adsorbent regains the ability to adsorb water; the regeneration includes two stages: heating regeneration and cold blow regeneration, and the regeneration process first performs heating regeneration and then cold blow regeneration;

[0046] Heating regeneration stage:

[0047] The raw material hydrogen gas becomes dry regeneration hydrogen gas through the drying module in the adsorption process; the dry regeneration hydrogen gas enters the heater and is heated to 120 - 280 °C, then enters the drying module in the regeneration process to desorb the water adsorbed by the adsorbent in the drying tower. The dry regeneration hydrogen gas exits from the A interface of the drying module in the regeneration process to become high-temperature regeneration hydrogen gas;

[0048] The sign of the end of the heating regeneration is that the temperature of the high-temperature regeneration hydrogen gas reaches 120 - 280 °C;

[0049] Cold blow regeneration stage:

[0050] The raw material hydrogen gas becomes dry regeneration hydrogen gas through the drying module in the adsorption process and then enters the drying module in the regeneration process to blow cold the adsorbent in the drying tower. The dry regeneration hydrogen gas exits from the A interface of the drying module in the regeneration process to become high-temperature regeneration hydrogen gas;

[0051] The sign of the end of the cold blow is that the temperature of the high-temperature regeneration hydrogen gas reaches 4 - 45 °C;

[0052] The auxiliary adsorption means that the high-temperature regeneration hydrogen gas enters the cooler and is cooled to 4 - 40 °C to become low-temperature regeneration hydrogen gas. The low-temperature regeneration hydrogen gas enters the gas-liquid separator for gas-liquid separation to become wet regeneration hydrogen gas. The wet regeneration hydrogen gas flows out from the gas-phase outlet of the gas-liquid separator and enters the drying module in the auxiliary adsorption process. The water in the wet regeneration hydrogen gas is adsorbed by the adsorbent filled in the drying tower of the drying module in the auxiliary adsorption process to obtain dry product hydrogen gas, and the product hydrogen gas flows out through the product gas outlet; during the whole process of auxiliary adsorption, the adsorbent in the adsorption module will not be saturated with adsorption.

[0053] As a further description of the above solution, in step 2, step 4, and step 6, the set dew point threshold at the outlets of drying module a, drying module b, and drying module c is the same, all being -40 °C to -80 °C.

[0054] As a further description of the above solution, the heater in the above green hydrogen dehydration and drying system is cancelled, and built-in heaters are installed inside the first drying tower, the second drying tower and the third drying tower. At the same time, the switching valves ae, af, be, bf, ce and cf are cancelled; the switching valves ag, bg and cg are added;

[0055] The B interface of the first drying tower is connected to the B port of the switching valve ag through a connecting pipe; the B interface of the second drying tower is connected to the B port of the switching valve bg through a connecting pipe; the B interface of the third drying tower is connected to the B port of the switching valve cg through a connecting pipe; the A ports of the switching valves ag, bg and cg are connected through a connecting pipe.

[0056] As a further description of the above solution, the cooler, gas-liquid separator and heater in the above green hydrogen dehydration and drying system are cancelled. At the same time, the switching valves ab, ac, ae, af, bb, bc, be, bf, cb, cc, ce and cf are cancelled;

[0057] A first cooler, a first gas-liquid separator and a first heater are installed inside the drying module a; a second cooler, a second gas-liquid separator and a second heater are installed inside the drying module b; a third cooler, a third gas-liquid separator and a third heater are installed inside the drying module c; the switching valves ah, ai, bh, bi, ch and ci are added;

[0058] The A interface of the first drying tower is connected to the gas-phase outlet of the first gas-liquid separator through a connecting pipeline; the B interface of the first drying tower is connected to the outlet of the first heater through a connecting pipeline; the A interface of the second drying tower is connected to the gas-phase outlet of the second gas-liquid separator through a connecting pipeline; the B interface of the second drying tower is connected to the outlet of the second heater through a connecting pipeline; the A interface of the third drying tower is connected to the gas-phase outlet of the third gas-liquid separator through a connecting pipeline; the B interface of the third drying tower is connected to the outlet of the third heater through a connecting pipeline; the outlet of the first cooler is connected to the inlet of the first gas-liquid separator through a connecting pipeline; the inlet of the first cooler is connected to the B port of the switch valve ah through a connecting pipeline; the outlet of the second cooler is connected to the inlet of the second gas-liquid separator through a connecting pipeline; the inlet of the second cooler is connected to the B port of the switch valve bh through a connecting pipeline; the outlet of the third cooler is connected to the inlet of the third gas-liquid separator through a connecting pipeline; the inlet of the third cooler is connected to the B port of the switch valve ch through a connecting pipeline; the A ports of the switch valve ah, the switch valve bh, and the switch valve ch are connected through a connecting pipeline; the inlet of the first heater is connected to the A port of the switch valve ai through a connecting pipeline; the inlet of the second heater is connected to the A port of the switch valve bi through a connecting pipeline; the inlet of the first heater is connected to the A port of the switch valve ci through a connecting pipeline; the B ports of the switch valve ai, the switch valve bi, and the switch valve ci are connected through a connecting pipeline; the free water outlet is respectively connected to the liquid-phase outlets of the first gas-liquid separator, the second gas-liquid separator, and the third gas-liquid separator through connecting pipelines.

[0059] Advantages and effects of the present invention:

[0060] 1. The present invention provides a green hydrogen dehydration and drying device and its treatment method. The entire raw material gas volume is used to regenerate the drying tower in the regeneration process, and the entire raw material gas volume can enable the drying tower in the regeneration process to complete regeneration in the shortest time. When the raw material gas is interrupted, that is, when the raw material gas volume is 0, and in the heating regeneration process, the heating regeneration process is interrupted. When waiting for the raw material gas supply to resume, the drying tower in the regeneration process cannot carry out heating regeneration, and the drying tower loses heat due to natural heat dissipation. The existing hydrogen drying system uses time as the sign to switch the drying tower, and the regeneration gas volume used is 10-20% of the raw material gas volume. The sum of the set regeneration times is consistent with the switching cycle. If the raw material hydrogen gas volume is lower than 10% of the design value or even interrupted, then regeneration cannot be completed within the set time. The present invention uses the entire raw material hydrogen gas volume for regeneration, and uses the dew point value at the outlet of the drying tower in the adsorption process as the switching sign. Even if the raw material gas volume is lower than 10% for a long time, or even the raw material gas volume is 0, the reserved time for series adsorption can be occupied to complete regeneration. The present invention can solve the problem that the supporting dehydration and drying device cannot operate at 0-100% load due to the load change of the hydrogen production system in the existing treatment method, and can perfectly match the high operation flexibility requirements of 99.999% green hydrogen production.

[0061] 2. The hydrogen purification system provided by the present invention has three drying modules. A first dew point monitoring port is added in drying module a, a second dew point monitoring port is added in drying module b, and a third dew point monitoring port is added in drying module c. The present invention creatively uses the dew point threshold of the dew point monitoring port as the switching standard for the working state of each drying module. The hydrogen purification device provided by the present invention greatly saves the ineffective working time in the traditional working method, fully exerts the adsorption performance of the drying module, and greatly improves the working efficiency of the hydrogen purification system.

[0062] 3. Before the drying module is switched, the present invention adopts a working method of sequentially connecting multiple drying modules in series for adsorption, which can perfectly avoid system failures caused by inaccurate switching cycles or internal leakage of valves in the traditional parallel treatment method. The hydrogen purification system provided by the present invention greatly improves the stability and reliability of the hydrogen purification system.

[0063] 4. The present invention saves the floor area, construction cost and operation cost of the device and reduces the management difficulty and cost, so it can be applied to industrial treatment and is suitable for large-scale promotion. BRIEF DESCRIPTION OF THE DRAWINGS

[0064] Figure 1 It is a schematic diagram of the green hydrogen dehydration and drying system according to Embodiment 1 of the present invention;

[0065] Figure 2 It is a schematic diagram of the green hydrogen dehydration and drying system according to Embodiment 2 of the present invention;

[0066] Figure 3 Schematic diagram of the green hydrogen dehydration and drying system according to Embodiment 3 of the present invention.

[0067] In the attached drawings, the list of components represented by each reference numeral is as follows:

[0068] 1 - Drying module a, 2 - Drying module b, 3 - Drying module c, 4 - Cooler, 5 - Gas - liquid separator, 6 - Heater, 21 - Raw gas inlet, 22 - Product gas outlet, 23 - Free water outlet, 11 - First drying tower, 12 - Second drying tower, 13 - Third drying tower, 4 - Cooler, 41 - First cooler, 42 - Second cooler, 43 - Third cooler, 5 - Gas - liquid separator, 51 - First gas - liquid separator, 52 - Second gas - liquid separator, 53 - Third gas - liquid separator, 6 - Heater, 61 - First heater, 62 - Second heater, 63 - Third heater, 241 - First dew point monitoring port, 242 - Second dew point monitoring port, 243 - Third dew point monitoring port, 311 - On - off valve, 312 - On - off valve, 313 - On - off valve, 314 - On - off valve, 315 - On - off valve, 316 - On - off valve, 321 On - off valve, 322 - On - off valve, 323 - On - off valve, 324 - On - off valve, 325 - On - off valve, 326 - On - off valve, 331 On - off valve, 332 - On - off valve, 333 - On - off valve, 334 - On - off valve, 335 - On - off valve, 336 - On - off valve, 3131 - On - off valve ah, 3132 - On - off valve ai, 3231 - On - off valve bh, 3232 - On - off valve bi, 3331 - On - off valve ch, 3332 - On - off valve ci, 3121 - On - off valve ag, 3221 - On - off valve bg, 3321 - On - off valve cg. Detailed implementation manners

[0069] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without making creative efforts belong to the scope of protection of the present invention.

[0070] A green hydrogen dehydration and drying system provided by the present invention includes a drying module, a cooler 4, a gas-liquid separator 5, a raw material hydrogen inlet 21, a product gas outlet 22, a heater 6 and corresponding connecting pipes. A plurality of drying modules are provided, and the plurality of drying modules are interconnected; the raw material hydrogen inlet 21 and the product gas outlet 22 are respectively connected to the plurality of drying modules through connecting pipes; the heater 6 is connected to the drying module through a connecting pipe for heating dry regeneration hydrogen; the cooler 4 is connected to the drying module through a connecting pipe for reducing the temperature of high-temperature regeneration hydrogen; the inlet of the gas-liquid separator 5 is connected to the outlet of the cooler 4 through a connecting pipe for discharging free water in the low-temperature regeneration hydrogen.

[0071] Three drying modules are provided in the present invention, namely drying module a1, drying module b2 and drying module c3; when the green hydrogen dehydration and drying system is operating, the drying module a1, drying module b2 and drying module c3 have the following working connection states: the first working connection state: the drying module c3, the drying module a1 and the drying module b2 are connected in series in sequence; the second working connection state: the drying module b2, the drying module c3 and the drying module a1 are connected in series in sequence; the third working connection state: the drying module a1, the drying module b2 and the drying module c3 are connected in series in sequence. Before the drying module is switched, the present invention adopts a working mode of sequentially adsorbing in series by a plurality of drying modules, which can perfectly avoid system failures caused by inaccurate switching cycles or internal leakage of valves in the traditional parallel processing mode. The hydrogen purification system provided by the present invention greatly improves the stability and reliability of the hydrogen purification system.

[0072] The drying module a1 of the present invention includes a first drying tower 11, a switching valve aa311, a switching valve ab312, a switching valve ac313, a switching valve ad314, a switching valve ae315, a switching valve af316 and corresponding connecting pipes; wherein the A interface of the first drying tower 11 is connected to the B port of the switching valve aa311, the B port of the switching valve ab312 and the B port of the switching valve ac313 through connecting pipes; the B interface of the first drying tower 11 is connected to the A port of the switching valve ad314, the A port of the switching valve ae315 and the A port of the switching valve af316 through connecting pipes; wherein the drying module b2 includes a second drying tower 12, a switching valve ba321, a switching valve bb322, a switching valve bc323, a switching valve bd324, a switching valve be325, a switching valve bf326 and corresponding connecting pipes; the A interface of the second drying tower 12 is connected to the B port of the switching valve ba321, the B port of the switching valve bb322 and the B port of the switching valve bc323 through connecting pipes; the B interface of the second drying tower 12 is connected to the A port of the switching valve bd324, the A port of the switching valve be325 and the A port of the switching valve bf326 through connecting pipes; wherein the drying module c3 includes a third drying tower 13, a switching valve ca331, a switching valve cb332, a switching valve cc333, a switching valve cd334, a switching valve ce335, a switching valve cf336 and corresponding connecting pipes; the A interface of the third drying tower 13 is connected to the B port of the switching valve ca331, the B port of the switching valve cb332 and the B port of the switching valve cc333 through connecting pipes; the B interface of the third drying tower 13 is connected to the A port of the switching valve cd334, the A port of the switching valve ce335 and the A port of the switching valve cf336 through connecting pipes; wherein the raw material hydrogen inlet 21 is connected to the A port of the switching valve aa311, the A port of the switching valve ba321 and the A port of the switching valve ca331 through connecting pipes; wherein the product gas outlet 22 is connected to the B port of the switching valve ad314, the B port of the switching valve bd324 and the B port of the switching valve cd334 through connecting pipes; wherein the cooler 4 inlet is connected to the A port of the switching valve ab312, the A port of the switching valve bb322 and the A port of the switching valve cb332 through connecting pipes; wherein the cooler 4 outlet is connected to the inlet of the gas-liquid separator 5 through a connecting pipe; the gas phase outlet of the gas-liquid separator 5 is connected to the A port of the switching valve ac313, the A port of the switching valve bc323 and the A port of the switching valve cc333 through connecting pipes; wherein the heater 6 inlet is connected to the B port of the switching valve ae315, the B port of the switching valve be325 and the B port of the switching valve ce335 through connecting pipes; wherein the heater 6 outlet is connected to the B port of the switching valve af316, the B port of the switching valve bf326 and the B port of the switching valve cf336 through connecting pipes.

[0073] The green hydrogen dehydration drying system of the present invention further includes a free water outlet 23, a first dew point monitoring port 241, a second dew point monitoring port 242 and a third dew point monitoring port 243, wherein the free water outlet 23 is connected to the liquid phase outlet of the gas-liquid separator 5 through a connecting pipe; wherein the first dew point monitoring port 241 is connected to the B interface of the first drying tower 11; wherein the second dew point monitoring port 242 is connected to the B interface of the second drying tower 12; wherein the third dew point monitoring port 243 is connected to the B interface of the third drying tower 13. The present invention innovatively adopts the dew point threshold of the dew point monitoring port as the switching standard for the working state of each drying module. The hydrogen purification device provided by the present invention greatly saves the invalid working time in the traditional working mode, gives full play to the adsorption performance of the drying module, and greatly improves the working efficiency of the hydrogen purification system.

[0074] The first drying tower 11, the second drying tower 12 and the third drying tower 13 of the present invention are filled with adsorbents, wherein the adsorbents are used to adsorb and dry moisture in hydrogen, wherein the adsorbents are one or more combinations of molecular sieves, activated alumina and silica gel; wherein the cooler 4 uses cooling water or air as the cooling medium; wherein the heater 6 uses resistance wire, steam or thermal oil as the heat medium.

[0075] A method for continuously treating hydrogen using the above-mentioned green hydrogen dehydration drying system, starting any one of the multiple drying modules as the first drying module to enter the adsorption process, the first drying module adsorbs all the raw hydrogen entering the raw hydrogen inlet 21, and all the raw hydrogen after adsorption becomes dry regenerated hydrogen; the dry regenerated hydrogen enters the second drying module in the regeneration process after passing through the heater 6, and the regenerated hydrogen leaving the drying module enters the gas-liquid separator 5 after being cooled by the cooler 4 to become wet regenerated hydrogen; the wet regenerated hydrogen enters the third drying module in the auxiliary adsorption process, and the wet regenerated hydrogen after auxiliary adsorption is dried and flows out from the product gas outlet 22 as product gas;

[0076] When the regeneration of the second drying module is completed, the three drying modules enter the series adsorption process, and the series connection order is the first drying module, the second drying module and the third drying module in sequence; the first drying module continues to adsorb the raw hydrogen entering the raw hydrogen inlet 21, and the raw hydrogen after adsorption is dried, and flows through the second drying module and the third drying module in sequence and then flows out from the product gas outlet 22 as product gas; when the first drying module is saturated with adsorption, it stops adsorbing the raw hydrogen and regenerates it; the third drying module enters the adsorption process, and the second drying module enters the auxiliary adsorption process;

[0077] Repeat the above steps, switch the first drying module, the second drying module, and the third drying module to perform operations of adsorption, regeneration, auxiliary adsorption, and series adsorption, and repeat in a cycle to achieve continuous drying of the raw material hydrogen gas. In the present invention, all of the raw material gas volume is used to regenerate the drying tower in the regeneration process, and all of the raw material gas volume can enable the drying tower in the regeneration process to complete regeneration in the shortest time; when the raw material gas is interrupted, that is, when the raw material gas volume is 0, and in the heating regeneration process, the heating regeneration process is interrupted. When waiting for the raw material gas supply to resume, the drying tower in the regeneration process cannot perform heating regeneration, and the drying tower loses heat due to natural heat dissipation. The existing hydrogen drying system uses time as the sign to switch the drying tower, the amount of regeneration gas used is 10-20% of the raw material gas volume, and the sum of the set regeneration times is consistent with the switching cycle. If the raw material hydrogen gas volume is less than 10% of the design value or even interrupted, then regeneration cannot be completed within the set time. The present invention uses all of the raw material hydrogen gas volume for regeneration, and uses the dew point value at the outlet of the drying tower in the adsorption process as the switching sign. Even if the raw material gas volume is less than 10% for a long time, or even the raw material gas volume is 0, the time reserved for series adsorption can be used to complete regeneration. The present invention can solve the problem in the existing treatment method that the supporting dehydration drying device cannot operate at 0-100% load due to the load change of the hydrogen production system, and can perfectly match the high operation flexibility requirements of 99.999% green hydrogen production.

[0078] The drying module of the present invention is provided with three, namely drying module a1, drying module b2, and drying module c3. When the green hydrogen dehydration drying system is operating, it includes the following steps:

[0079] Step 1: Drying module c3 adsorbs, drying module a1 regenerates, and drying module b2 performs auxiliary adsorption. The end sign of Step 1 is the end of the regeneration of drying module a1;

[0080] Step 2: Drying module c3, drying module a1, and drying module b2 are successively connected in series for adsorption. The end sign of Step 2 is that the dew point at the outlet of drying module c3 monitored by the third dew point monitoring port 243 reaches the set threshold;

[0081] Step 3: Drying module b2 adsorbs, drying module c3 regenerates, and drying module a1 performs auxiliary adsorption. The end sign of Step 3 is the end of the regeneration of drying module c3;

[0082] Step 4: Drying module b2, drying module c3, and drying module a1 are successively connected in series for adsorption. The end sign of Step 4 is that the dew point at the outlet of drying module b2 monitored by the second dew point monitoring port 242 reaches the set threshold;

[0083] Step 5: Drying module a1 adsorbs, drying module b2 regenerates, and drying module c3 performs auxiliary adsorption. The end sign of Step 5 is the end of the regeneration of drying module b2;

[0084] Step 6: Drying module a1, drying module b2 and drying module c3 are adsorbed in series in sequence. The sign of the end of step 6 is that the outlet dew point of drying module a1 monitored by the first dew point monitoring port 241 reaches the set threshold;

[0085] Step 7: Repeat steps 1 to 6 to achieve continuous hydrogen drying.

[0086] The present invention innovatively uses the dew point threshold of the dew point monitoring port as the switching standard for the working state of each drying module. The hydrogen purification device provided by the present invention greatly saves the ineffective working time in the traditional working mode, gives full play to the adsorption performance of the drying module, and greatly improves the working efficiency of the hydrogen purification system. The present invention adopts a working mode of adsorbing multiple drying modules in series in sequence before switching the drying module, which can perfectly avoid system failures caused by inaccurate switching cycles or valve internal leakage in the traditional parallel processing mode. The hydrogen purification system provided by the present invention greatly improves the stability and reliability of the hydrogen purification system.

[0087] In step 1 of the present invention, raw hydrogen enters from the raw hydrogen inlet 21, flows through the drying module c3, the heater 6, the drying module a1, the cooler 4, the gas-liquid separator 5 and the drying module b2 in sequence to obtain product gas, and the product gas flows out through the product gas outlet 22; after the treated raw hydrogen flows through the cooler 4, the saturated water vapor is cooled and free water is precipitated, and the free water flows out from the free water outlet 23;

[0088] In step 2, the raw hydrogen enters from the raw hydrogen inlet 21, flows through the drying module c3, the drying module a1 and the drying module b2 in sequence to obtain the product gas, and then the product gas flows out through the product gas outlet 22; the cooler 4, the gas-liquid separator 5 and the heater 6 are set not to be connected to the air flow path;

[0089] In step 3, the raw hydrogen enters from the raw hydrogen inlet 21, flows through the drying module b2, the heater 6, the drying module c3, the cooler 4, the gas-liquid separator 5 and the drying module a1 in sequence to obtain the product gas, and the product gas flows out through the product gas outlet 22; after the treated raw hydrogen flows through the cooler 4, the saturated water vapor is cooled and free water is precipitated, and the free water flows out from the free water outlet 23;

[0090] In step 4, the raw hydrogen enters from the raw hydrogen inlet 21, flows through the drying module b2, the drying module c3 and the drying module a1 in sequence to obtain the product gas, and then the product gas flows out through the product gas outlet 22; the cooler 4, the gas-liquid separator 5 and the heater 6 are set not to be connected to the air flow path;

[0091] In step 5, the raw material hydrogen gas enters from the raw material hydrogen gas inlet 21, flows through the drying module a1, the heater 6, the drying module b2, the cooler 4, the gas-liquid separator 5, and the drying module c3 in sequence, and then the product gas is obtained. The product gas flows out through the product gas outlet 22; after the processed raw material hydrogen gas flows through the cooler 4, the saturated water vapor precipitates free water due to the temperature reduction, and the free water flows out from the free water outlet 23;

[0092] In step 6, the raw material hydrogen gas enters from the raw material hydrogen gas inlet 21, flows through the drying module a1, the drying module b2, and the drying module c3 in sequence, and then the product gas is obtained, and then the product gas flows out through the product gas outlet 22; the cooler 4, the gas-liquid separator 5, and the heater 6 are set not to be connected to the gas flow path.

[0093] In the present invention, the cooler 4, the gas-liquid separator 5, and the heater 6 in step 2 are replaced to be connected to the gas flow path; the cooler 4, the gas-liquid separator 5, and the heater 6 in step 4 are replaced to be connected to the gas flow path; the cooler 4, the gas-liquid separator 5, and the heater 6 in step 6 are replaced to be connected to the gas flow path.

[0094] The adsorption in the present invention means that the raw material hydrogen gas passes through the drying module a1 or the drying module b2 or the drying module c3, and the moisture in the raw material hydrogen gas is adsorbed by the adsorbent filled in the drying tower in one of the drying modules to obtain a state of dry hydrogen gas; after the adsorbent is saturated with adsorption, regeneration is required. During regeneration, the adsorbed moisture by the adsorbent is desorbed, and after the regeneration is completed, the adsorbent regains the adsorption capacity for moisture; the regeneration includes two stages of heating regeneration and cold blow regeneration, and the regeneration process first performs heating regeneration and then cold blow regeneration;

[0095] Heating regeneration stage:

[0096] The raw material hydrogen gas becomes dry regeneration hydrogen gas through the drying module in the adsorption process; the dry regeneration hydrogen gas enters the heater 6 and is heated to 120 - 280 °C, then enters the drying module in the regeneration process, and desorbs the moisture adsorbed by the adsorbent in the corresponding drying tower of the drying module. The dry regeneration hydrogen gas flows out from the A interface of the drying module in the regeneration process and becomes high-temperature regeneration hydrogen gas;

[0097] The sign of the end of heating regeneration is that the temperature of the high-temperature regeneration hydrogen gas flowing out from the A interface of the corresponding drying tower in the drying module in the heating regeneration process reaches 120 - 280 °C;

[0098] Cold blow regeneration stage:

[0099] The raw material hydrogen gas becomes dry regenerated hydrogen gas after passing through the drying module in the adsorption process and then enters the heater 6. At this time, the heater is not heated, and the dry regenerated hydrogen gas maintaining its own temperature enters the drying module in the regeneration process to blow and cool the adsorbent in the corresponding drying tower in this drying module. The dry regenerated hydrogen gas flows out from the A interface of the drying module in the regeneration process and becomes high-temperature regenerated hydrogen gas;

[0100] The sign of the end of the cold blow is that the temperature of the high-temperature regenerated hydrogen gas flowing out from the A interface of the corresponding drying tower in the drying module in the cold blow regeneration process reaches 4 - 45°C;

[0101] The auxiliary adsorption means that the high-temperature regenerated hydrogen gas enters the cooler 4 and is cooled to 4 - 40°C to become low-temperature regenerated hydrogen gas. The low-temperature regenerated hydrogen gas enters the gas-liquid separator 5 for gas-liquid separation and then becomes wet regenerated hydrogen gas. The wet regenerated hydrogen gas flows out from the gas-phase outlet of the gas-liquid separator 5 and enters the drying module in the auxiliary adsorption process. The moisture in the wet regenerated hydrogen gas is adsorbed by the adsorbent filled in the drying tower in the drying module in the auxiliary adsorption process to obtain dry product hydrogen gas, and the product hydrogen gas flows out through the product gas outlet 22; During the whole process of auxiliary adsorption, the adsorbent in the adsorption module will not be saturated with adsorption.

[0102] In step 2, step 4 and step 6 of the present invention, the dew point setting thresholds at the outlets of the drying module a1, the drying module b2 and the drying module c3 are the same, all being -40°C to -80°C.

[0103] The green hydrogen dehydration and drying system of the present invention cancels the heater 6, and built-in heaters are provided inside the first drying tower 11, the second drying tower 12 and the third drying tower 13. At the same time, the switching valves ae315, the switching valves af316, the switching valves be325, the switching valves bf326, the switching valves ce335 and the switching valves cf336 are cancelled; The switching valves ag3121, the switching valves bg3221 and the switching valves cg3321 are added;

[0104] The B interface of the first drying tower 11 is connected to the B port of the switching valve ag3121 through a connecting pipeline; The B interface of the second drying tower 12 is connected to the B port of the switching valve bg3221 through a connecting pipeline; The B interface of the third drying tower 13 is connected to the B port of the switching valve cg3321 through a connecting pipeline; The A ports of the switching valve ag3121, the switching valve bg3221 and the switching valve cg3321 are connected through a connecting pipeline.

[0105] The green hydrogen dehydration and drying system of the present invention cancels the cooler 4, the gas-liquid separator 5, and the heater 6, and at the same time cancels the switching valves ab312, switching valve ac(313), switching valve ae315, switching valve af316, switching valve bb322, switching valve bc(323), switching valve be325, switching valve bf326, switching valve cb332, switching valve cc(333), switching valve ce335, and switching valve cf336;

[0106] Inside the drying module a1, a first cooler 41, a first gas-liquid separator 51, and a first heater 61 are provided; inside the drying module b2, a second cooler 42, a second gas-liquid separator 52, and a second heater 62 are provided; inside the drying module c3, a third cooler 43, a third gas-liquid separator 53, and a third heater 63 are provided; the switching valves ah3131, switching valve ai3132, switching valve bh3231, switching valve bi3232, switching valve ch3331, and switching valve ci3332 are added;

[0107] The A interface of the first drying tower 11 is connected to the gas-phase outlet of the first gas-liquid separator 51 through a connecting pipeline; the B interface of the first drying tower 11 is connected to the outlet of the first heater 61 through a connecting pipeline; the A interface of the second drying tower 12 is connected to the gas-phase outlet of the second gas-liquid separator 52 through a connecting pipeline; the B interface of the second drying tower 12 is connected to the outlet of the second heater 62 through a connecting pipeline; the A interface of the third drying tower 13 is connected to the gas-phase outlet of the third gas-liquid separator 53 through a connecting pipeline; the B interface of the third drying tower 13 is connected to the outlet of the third heater 63 through a connecting pipeline; the outlet of the first cooler 41 is connected to the inlet of the first gas-liquid separator 51 through a connecting pipeline; the inlet of the first cooler 41 is connected to the B port of the switch valve ah3131 through a connecting pipeline; the outlet of the second cooler 42 is connected to the inlet of the second gas-liquid separator 52 through a connecting pipeline; the inlet of the second cooler 42 is connected to the B port of the switch valve bh3231 through a connecting pipeline; the outlet of the third cooler 43 is connected to the inlet of the third gas-liquid separator 53 through a connecting pipeline; the inlet of the third cooler 43 is connected to the B port of the switch valve ch3331 through a connecting pipeline; the A ports of the switch valve ah3131, the switch valve bh3231, and the switch valve ch3331 are connected through a connecting pipeline; the inlet of the first heater 61 is connected to the A port of the switch valve ai3132 through a connecting pipeline; the inlet of the second heater 62 is connected to the A port of the switch valve bi3232 through a connecting pipeline; the inlet of the third heater 63 is connected to the A port of the switch valve ci3332 through a connecting pipeline; the B ports of the switch valve ai3132, the switch valve bi3232, and the switch valve ci3332 are connected through a connecting pipeline; the free water outlet 23 is respectively connected to the liquid-phase outlets of the first gas-liquid separator 51, the second gas-liquid separator 52, and the third gas-liquid separator 53 through connecting pipelines.

[0108] In the embodiments of the present invention, all embodiments are implemented according to Figure 1 the structural schematic diagram shown, and all embodiments are implemented according to the following method:

[0109] The raw material hydrogen flows through the drying module a, the drying module b, and the drying module c in the order of the steps.

[0110] Step 1: The drying module c adsorbs, the drying module a regenerates, the drying module b assists in adsorption. After the regeneration of the drying module a is completed, enter Step 2;

[0111] Step 2: The drying module c, the drying module a, and the drying module b are connected in series for adsorption in sequence. When it is detected that the dew point at the outlet of the drying module c is greater than the set value of -70°C, enter Step 3;

[0112] Step 3: The drying module b adsorbs, the drying module c regenerates, and the drying module a assists in adsorption. After the regeneration of the drying module c is completed, proceed to Step 4;

[0113] Step 4: The drying modules b, c, and a are successively connected in series for adsorption; when the dew point at the outlet of the drying module b is detected to be greater than the set value of -70 °C, proceed to Step 5;

[0114] Step 6: The drying module a adsorbs, the drying module b regenerates, and the drying module c assists in adsorption. After the regeneration of the drying module b is completed, proceed to Step 6;

[0115] Step 6: The drying modules a, b, and c are successively connected in series for adsorption. When the dew point at the outlet of the drying module a is detected to be greater than the set value of -70 °C, Step 6 ends;

[0116] After 6 steps, a cycle of circulation is completed.

[0117] In all embodiments, the atmospheric dew point of the raw material hydrogen inlet is -22 °C, and the raw material gas pressure is 1.6 MPa; the adsorbent loading of the first drying tower, the second drying tower, and the third drying tower is 140 kg of 5A molecular sieve; the inlet temperature of the regeneration gas of the drying tower for heating regeneration is 200 °C, the end temperature of heating regeneration is 200 °C, and the end temperature of cold blow is 40 °C. The atmospheric dew point of the product hydrogen is -75 °C, and the pressure is 1.5 MPa;

[0118] Example 1

[0119] In this example, the flow rate of the raw material hydrogen is 1000 Nm 3 / h, and the working load is 100%.

[0120] In Steps 1, 3, and 5, in each step, 1400 Nm of the raw material hydrogen is dried 3 , and the drying module in the adsorption process adsorbs for 1.4 h; the drying module in the regeneration process is heated and regenerated for 1 h and cold blown for 0.4 h; the drying module in the auxiliary adsorption process assists in adsorption for 1.4 h.

[0121] In Steps 2, 4, and 6, in each step, 10600 Nm of the raw material hydrogen is dried 3 , and the three drying modules are successively connected in series for adsorption for 10.6 h according to the sequence of different steps.

[0122] In this example, the flow rate of the product hydrogen is 991 Nm 3 / h, the total amount of the dried raw material hydrogen is 36000 Nm 3 , and it takes 36 h; there is no hydrogen consumption during the regeneration process in this example, and the load of the dried raw material hydrogen is 100%.

[0123] Example 2

[0124] In this embodiment, the flow rate of the raw material hydrogen gas fluctuates between 0 and 1000 Nm 3 / h, and the working load is 0 to 100%, as shown in Table 1:

[0125] Duration h 1 8 2 12 2 10 Flow rate <![CDATA[Nm 3 / h]]> 300 0 500 1000 300 0 Gas volume <![CDATA[Nm 3 > 300 0 1000 12000 600 0 Load ％ 30 0 50 100 30 0 Duration h 1 12 1 10 1 8 Flow rate <![CDATA[Nm 3 / h]]> 300 1000 900 0 900 1000 Gas volume <![CDATA[Nm 3 > 300 12000 900 0 900 8000 Load ％ 30 100 90 0 90 100

[0126] Table 1

[0127] In step 1, 1700 Nm of the raw material hydrogen gas is dried 3 ; the drying module c adsorbs for 1 h for the first time, pauses for 8 h, and adsorbs for 2.4 h for the second time; the drying module a is heated and regenerated for 1 h for the first time, pauses for 8 h, and is heated and regenerated for 2 h for the second time, and is cold-blown and regenerated for 0.4 h; the drying module b performs auxiliary adsorption for 1 h for the first time, pauses for 8 h, and performs auxiliary adsorption for 2.4 h for the second time;

[0128] In step 2, 10300 Nm of the raw material hydrogen gas is dried 3 ; the drying modules are serially adsorbed for 10.3 h;

[0129] In step 3, 1400 Nm of the raw material hydrogen gas is dried 3 ; the drying module b adsorbs for about 1.63 h; the drying module c is heated and regenerated for 1 hour and cold-blown and regenerated for about 0.63 h; the drying module a performs auxiliary adsorption for about 1.63 h;

[0130] In step 4, 10600 Nm of the raw material hydrogen gas is dried 3 ; the drying modules are serially adsorbed for 22.47 h;

[0131] In step 5, 1400 Nm of the raw material hydrogen gas is dried 3 ; the drying module a adsorbs for 1.4 h; the drying module b is heated and regenerated for 1 hour and cold-blown and regenerated for 0.4 h; the drying module c performs auxiliary adsorption for 1.4 h;

[0132] In step 6, 10600 Nm of the raw material hydrogen gas is dried 3 , and the drying modules are serially adsorbed for 20.8 h.

[0133] In this embodiment, the flow rate of the product hydrogen gas is shown in Table 2, and the total amount of the dried raw material hydrogen gas is 36000 Nm 3 , and it takes 68 h; there is no hydrogen consumption during the regeneration process in this embodiment, and the working load is 0 to 100%.

[0134] Duration h 1 8 2 12 2 10 Flow rate <![CDATA[Nm 3 / h]]> 297.375 0 495.625 991.25 297.375 0 Gas volume <![CDATA[Nm 3 > 297.375 0 991.25 11895 594.75 0 Load ％ 29.7375 0 49.5625 99.125 29.7375 0 Duration h 1 12 1 10 1 8 Flow rate <![CDATA[Nm 3 / h]]> 297.375 991.25 892.125 0 892.125 991.25 Gas volume <![CDATA[Nm 3 > 297.375 11895 892.125 0 892.125 7930 Load ％ 29.7375 99.125 89.2125 0 89.2125 99.125

[0135] Table 2

[0136] The core idea of the present invention is to use the total raw gas volume to regenerate the drying tower in the regeneration process. The total raw gas volume can enable the drying tower in the regeneration process to complete regeneration in the shortest time. When the raw gas is interrupted, i.e., the raw gas volume is 0, and during the heating regeneration process, the drying tower in the regeneration process only loses heat due to natural heat dissipation. After the gas supply is restored, the regenerated raw gas and the time occupied by series adsorption are used to complete regeneration. At the same time, the present invention saves the floor area, construction cost and operation cost of the device and reduces the management difficulty and cost. Therefore, it can be applied to industrial treatment and is suitable for large-scale promotion.

[0137] The above are only several embodiments of the present application and do not impose any form of limitation on the present application. Although the present application is disclosed as above with preferred embodiments, it is not intended to limit the present application. Any person skilled in the art, without departing from the scope of the technical solution of the present application, making some changes or modifications using the technical content disclosed above is equivalent to equivalent implementation cases and all fall within the scope of the technical solution.

Claims

1. A green hydrogen dehydration and drying system, characterized in that, It includes a drying module, a cooler (4), a gas-liquid separator (5), a raw material hydrogen inlet (21), a product gas outlet (22), a heater (6) and corresponding connecting pipes; multiple drying modules are provided, and the multiple drying modules are interconnected; the raw material hydrogen inlet (21) and the product gas outlet (22) are respectively connected to the multiple drying modules through connecting pipes; the heater (6) is connected to the drying module through a connecting pipe and is used to heat the dry regeneration hydrogen; The cooler (4) is connected to the drying module through a connecting pipe and is used to reduce the temperature of the high-temperature regeneration hydrogen; The inlet of the gas-liquid separator (5) is connected to the outlet of the cooler (4) through a connecting pipe and is used to drain the free water in the low-temperature regeneration hydrogen.

2. The green hydrogen dehydration and drying system according to claim 1, wherein Three drying modules are provided, namely drying module a (1), drying module b (2) and drying module c (3); when the green hydrogen dehydration drying system is running, drying module a (1), drying module b (2) and drying module c (3) have the following working connection states, The first working connection state: drying module c (3), drying module a (1) and drying module b (2) are connected in series in sequence; The second working connection state: drying module b (2), drying module c (3) and drying module a (1) are connected in series in sequence; The third working connection state: drying module a (1), drying module b (2) and drying module c (3) are connected in series in sequence.

3. The green hydrogen dehydration and drying system according to claim 2, characterized in that, The drying module a (1) includes a first drying tower (11), a switching valve aa (311), a switching valve ab (312), a switching valve ac (313), a switching valve ad (314), a switching valve ae (315), a switching valve af (316) and corresponding connecting pipes; the A interface of the first drying tower (11) is respectively connected to the B port of the switching valve aa (311), the B port of the switching valve ab (312) and the B port of the switching valve ac (313) through connecting pipes; the B interface of the first drying tower (11) is respectively connected to the A port of the switching valve ad (314), the A port of the switching valve ae (315) and the A port of the switching valve af (316) through connecting pipes; The drying module b (2) includes a second drying tower (12), a switching valve ba (321), a switching valve bb (322), a switching valve bc (323), a switching valve bd (324), a switching valve be (325), a switching valve bf (326) and corresponding connecting pipes; the A interface of the second drying tower (12) is respectively connected to the B port of the switching valve ba (321), the B port of the switching valve bb (322) and the B port of the switching valve bc (323) through connecting pipes; the B interface of the second drying tower (12) is respectively connected to the A port of the switching valve bd (324), the A port of the switching valve be (325) and the A port of the switching valve bf (326) through connecting pipes; The drying module c (3) includes a third drying tower (13), a switching valve ca (331), a switching valve cb (332), a switching valve cc (333), a switching valve cd (334), a switching valve ce (335), a switching valve cf (336) and corresponding connecting pipes; the A interface of the third drying tower (13) is connected to the B port of the switching valve ca (331), the B port of the switching valve cb (332) and the B port of the switching valve cc (333) through connecting pipes; the B interface of the third drying tower (13) is connected to the A port of the switching valve cd (334), the A port of the switching valve ce (335) and the A port of the switching valve cf (336) through connecting pipes; The raw material hydrogen inlet (21) is connected to the A port of the switching valve aa (311), the A port of the switching valve ba (321) and the A port of the switching valve ca (331) through connecting pipes; the product gas outlet (22) is connected to the B port of the switching valve ad (314), the B port of the switching valve bd (324) and the B port of the switching valve cd (334) through connecting pipes; The inlet of the cooler (4) is respectively connected to the A port of the switching valve ab (312), the A port of the switching valve bb (322) and the A port of the switching valve cb (332) through connecting pipes; the outlet of the cooler (4) is connected to the inlet of the gas-liquid separator (5) through a connecting pipe; the gas-phase outlet of the gas-liquid separator (5) is respectively connected to the A port of the switching valve ac (313), the A port of the switching valve bc (323) and the A port of the switching valve cc (333) through connecting pipes; the inlet of the heater (6) is respectively connected to the B port of the switching valve ae (315), the B port of the switching valve be (325) and the B port of the switching valve ce (335) through connecting pipes; the outlet of the heater (6) is connected to the B port of the switching valve af (316), the B port of the switching valve bf (326) and the B port of the switching valve cf (336) through connecting pipes.

4. The green hydrogen dehydration and drying system according to claim 1, wherein It also includes a free water outlet (23), a first dew point monitoring port (241), a second dew point monitoring port (242) and a third dew point monitoring port (243); The free water outlet (23) is connected to the liquid-phase outlet of the gas-liquid separator (5) through a connecting pipe; The first dew point monitoring port (241) is communicated with the B interface of the first drying tower (11); The second dew point monitoring port (242) is communicated with the B interface of the second drying tower (12); The third dew point monitoring port (243) is communicated with the B interface of the third drying tower (13).

5. The green hydrogen dehydration and drying system according to claim 3, wherein, The first drying tower (11), the second drying tower (12) and the third drying tower (13) are filled with an adsorbent inside, and the adsorbent is used to adsorb and dry the moisture in hydrogen, and the adsorbent is one or a combination of molecular sieve, activated alumina and silica gel; The cooler (4) uses cooling water or air as a cooling medium; The heater (6) uses a resistance wire, steam or heat-conducting oil as a heat medium.

6. A method for continuously processing hydrogen using the green hydrogen dehydration and drying system according to any one of claims 1-5, characterized in that any one of the plurality of drying modules is started as the first drying module to enter the adsorption process. The first drying module adsorbs all the raw hydrogen entering from the raw hydrogen inlet (21). After adsorption, all the raw hydrogen becomes dry regeneration hydrogen. The dry regeneration hydrogen enters the second drying module in the regeneration process after passing through the heater (6). The regeneration hydrogen exiting this drying module enters the gas-liquid separator (5) after being cooled by the cooler (4) and becomes wet regeneration hydrogen. The wet regeneration hydrogen enters the third drying module in the auxiliary adsorption process. After auxiliary adsorption, the wet regeneration hydrogen is dried and flows out as product gas from the product gas outlet (22). When the regeneration of the second drying module is completed, the three drying modules enter the series adsorption process. The series sequence is the first drying module, the second drying module, and the third drying module in sequence. The first drying module continues to adsorb the raw hydrogen entering from the raw hydrogen inlet (21). After adsorption, the raw hydrogen is dried and flows through the second drying module and the third drying module in sequence and then flows out as product gas from the product gas outlet (22). When the first drying module is saturated with adsorption, its adsorption of raw hydrogen is stopped and it is regenerated. The third drying module enters the adsorption process, and the second drying module enters the auxiliary adsorption process. Repeat the above steps, switch the first drying module, the second drying module, and the third drying module to perform operations of adsorption, regeneration, auxiliary adsorption, and series adsorption, and cycle repeatedly to achieve continuous drying of raw hydrogen.

7. The continuous hydrogen treatment method according to claim 6, characterized in that, There are three drying modules, namely drying module a (1), drying module b (2), and drying module c (3). When the green hydrogen dehydration and drying system is operating, it includes the following steps: Step 1: Drying module c (3) adsorbs, drying module a (1) is regenerated, and drying module b (2) performs auxiliary adsorption. The end mark of Step 1 is the completion of the regeneration of drying module a (1). Step 2: Drying module c (3), drying module a (1), and drying module b (2) perform series adsorption in sequence. The end mark of Step 2 is that the dew point monitored by the third dew point monitoring port (243) reaches the set threshold. Step 3: Drying module b (2) adsorbs, drying module c (3) is regenerated, and drying module a (1) performs auxiliary adsorption. The end mark of Step 3 is the completion of the regeneration of drying module c (3). Step 4: Drying module b (2), drying module c (3), and drying module a (1) perform series adsorption in sequence. The end mark of Step 4 is that the dew point monitored by the second dew point monitoring port (242) reaches the set threshold. Step 5: Drying module a (1) adsorbs, drying module b (2) is regenerated, and drying module c (3) performs auxiliary adsorption. The end mark of Step 5 is the completion of the regeneration of drying module b (2). Step 6: Drying module a (1), drying module b (2), and drying module c (3) perform series adsorption in sequence. The end mark of Step 6 is that the dew point monitored by the first dew point monitoring port (241) reaches the set threshold. Step 7: Repeat Steps 1 to 6 to achieve continuous drying of hydrogen.

8. The continuous hydrogen treatment method according to claim 7, characterized in that, In Step 1, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module c (3), heater (6), drying module a (1), cooler (4), gas-liquid separator (5), and drying module b (2) in sequence to obtain the product gas, which flows out through the product gas outlet (22); in this step, after the hydrogen flows through the cooler (4), the water vapor in the hydrogen precipitates free water due to the temperature drop, and the free water flows out through the free water outlet (23); In Step 2, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module c (3), drying module a (1), and drying module b (2) in sequence to obtain the product gas, which flows out through the product gas outlet (22); the cooler (4), gas-liquid separator (5), and heater (6) are set not to be connected to the gas flow path; In Step 3, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module b (2), heater (6), drying module c (3), cooler (4), gas-liquid separator (5), and drying module a (1) in sequence to obtain the product gas, which flows out through the product gas outlet (22); in this step, after the hydrogen flows through the cooler (4), the water vapor in the hydrogen precipitates free water due to the temperature drop, and the free water flows out through the free water outlet (23); In Step 4, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module b (2), drying module c (3), and drying module a (1) in sequence to obtain the product gas, which flows out through the product gas outlet (22); the cooler (4), gas-liquid separator (5), and heater (6) are set not to be connected to the gas flow path; In Step 5, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module a (1), heater (6), drying module b (2), cooler (4), gas-liquid separator (5), and drying module c (3) in sequence to obtain the product gas, which flows out through the product gas outlet (22); in this step, after the hydrogen flows through the cooler (4), the water vapor in the hydrogen precipitates free water due to the temperature drop, and the free water flows out through the free water outlet (23); In Step 6, the raw hydrogen enters from the raw hydrogen inlet (21) and flows through the drying module a (1), drying module b (2), and drying module c (3) in sequence to obtain the product gas, which flows out through the product gas outlet (22); the cooler (4), gas-liquid separator (5), and heater (6) are set not to be connected to the gas flow path.

9. The continuous hydrogen treatment method according to claim 8, characterized in that, The cooler (4), gas-liquid separator (5), and heater (6) in Step 2 are replaced by being connected to the gas flow path; the cooler (4), gas-liquid separator (5), and heater (6) in Step 4 are replaced by being connected to the gas flow path; the cooler (4), gas-liquid separator (5), and heater (6) in Step 6 are replaced by being connected to the gas flow path.

10. The continuous hydrogen treatment method according to claim 8, characterized in that, The adsorption refers to the state in which the raw material hydrogen gas passes through drying module a (1), drying module b (2), or drying module c (3), and the water in the raw material hydrogen gas is adsorbed by the adsorbent filled in the drying tower of one of the drying modules to obtain dried hydrogen gas; after the adsorbent is saturated with adsorption, regeneration is required. During regeneration, the water adsorbed by the adsorbent is desorbed, and after the regeneration is completed, the adsorbent regains the ability to adsorb water; the regeneration includes two stages: heating regeneration and cold blow regeneration, and the regeneration process first performs heating regeneration and then cold blow regeneration; Heating regeneration stage: The raw material hydrogen gas becomes dry regeneration hydrogen gas through the drying module in the adsorption process; the dry regeneration hydrogen gas enters the heater (6) and is heated to 120 - 280 °C, then enters the drying module in the regeneration process to desorb the water adsorbed by the adsorbent in the drying tower. The dry regeneration hydrogen gas exits from the A interface of the drying module in the regeneration process to become high-temperature regeneration hydrogen gas; The sign that the heating regeneration is completed is that the temperature of the high-temperature regeneration hydrogen gas reaches 120 - 280 °C; Cold blow regeneration stage: The raw material hydrogen gas becomes dry regeneration hydrogen gas through the drying module in the adsorption process and then enters the drying module in the regeneration process to blow cold the adsorbent in the drying tower. The dry regeneration hydrogen gas exits from the A interface of the drying module in the regeneration process to become high-temperature regeneration hydrogen gas; The sign that the cold blow is completed is that the temperature of the high-temperature regeneration hydrogen gas reaches 4 - 45 °C; The auxiliary adsorption refers to the state in which the high-temperature regeneration hydrogen gas enters the cooler (4) and is cooled to 4 - 40 °C to become low-temperature regeneration hydrogen gas. The low-temperature regeneration hydrogen gas enters the gas-liquid separator (5) for gas-liquid separation and then becomes wet regeneration hydrogen gas. The wet regeneration hydrogen gas flows out from the gas-phase outlet of the gas-liquid separator (5) and enters the drying module in the auxiliary adsorption process. The water in the wet regeneration hydrogen gas is adsorbed by the adsorbent filled in the drying tower of the drying module in the auxiliary adsorption process to obtain dried product hydrogen gas, and the product hydrogen gas flows out through the product gas outlet (22); during the entire process of auxiliary adsorption, the adsorbent in the adsorption module will not be saturated with adsorption.

11. The continuous hydrogen treatment method according to claim 8, characterized in that, In step 2, step 4, and step 6, the set dew point threshold at the outlets of drying module a (1), drying module b (2), and drying module c (3) is the same, all being -40 °C to -80 °C.

12. The continuous hydrogen treatment method according to claim 8, characterized in that, Cancel the heater (6), and install built-in heaters inside the first drying tower (11), the second drying tower (12), and the third drying tower (13). At the same time, cancel the switch valves ae (315), af (316), be (325), bf (326), ce (335), and cf (336); add switch valves ag (3121), bg (3221), and cg (3321); The B interface of the first drying tower (11) is connected to the B port of the switching valve ag (3121) through a connecting pipeline; the B interface of the second drying tower (12) is connected to the B port of the switching valve bg (3221) through a connecting pipeline; the B interface of the third drying tower (13) is connected to the B port of the switching valve cg (3321) through a connecting pipeline; the A ports of the switching valve ag (3121), the switching valve bg (3221) and the switching valve cg (3321) are connected through a connecting pipeline.

13. The continuous hydrogen treatment method according to claim 8, characterized in that The cooler (4), the gas-liquid separator (5) and the heater (6) are cancelled, and at the same time, the switching valves ab (312), ac (313), ae (315), af (316), bb (322), bc (323), be (325), bf (326), cb (332), cc (333), ce (335) and cf (336) are cancelled; A first cooler (41), a first gas-liquid separator (51) and a first heater (61) are arranged inside the drying module a (1); a second cooler (42), a second gas-liquid separator (52) and a second heater (62) are arranged inside the drying module b (2); a third cooler (43), a third gas-liquid separator (53) and a third heater (63) are arranged inside the drying module c (3); the switching valves ah (3131), ai (3132), bh (3231), bi (3232), ch (3331) and ci (3332) are added; The A interface of the first drying tower (11) is connected to the gas-phase outlet of the first gas-liquid separator (51) through a connecting pipeline; the B interface of the first drying tower (11) is connected to the outlet of the first heater (61) through a connecting pipeline; the A interface of the second drying tower (12) is connected to the gas-phase outlet of the second gas-liquid separator (52) through a connecting pipeline; the B interface of the second drying tower (12) is connected to the outlet of the second heater (62) through a connecting pipeline; the A interface of the third drying tower (13) is connected to the gas-phase outlet of the third gas-liquid separator (53) through a connecting pipeline; the B interface of the third drying tower (13) is connected to the outlet of the third heater (63) through a connecting pipeline; the outlet of the first cooler (41) is connected to the inlet of the first gas-liquid separator (51) through a connecting pipeline; the inlet of the first cooler (41) is connected to the B port of the switching valve ah (3131) through a connecting pipeline; the outlet of the second cooler (42) is connected to the inlet of the second gas-liquid separator (52) through a connecting pipeline; the inlet of the second cooler (42) is connected to the B port of the switching valve bh (3231) through a connecting pipeline; the outlet of the third cooler (43) is connected to the inlet of the third gas-liquid separator (53) through a connecting pipeline; the inlet of the third cooler (43) is connected to the B port of the switching valve ch (3331) through a connecting pipeline; the A ports of the switching valve ah (3131), the switching valve bh (3231), and the switching valve ch (3331) are connected through a connecting pipeline; the inlet of the first heater (61) is connected to the A port of the switching valve ai (3132) through a connecting pipeline; the inlet of the second heater (62) is connected to the A port of the switching valve bi (3232) through a connecting pipeline; the inlet of the third heater (63) is connected to the A port of the switching valve ci (3332) through a connecting pipeline; the B ports of the switching valve ai (3132), the switching valve bi (3232), and the switching valve ci (3332) are connected through a connecting pipeline; the free water outlet (23) is respectively connected to the liquid-phase outlets of the first gas-liquid separator (51), the second gas-liquid separator (52), and the third gas-liquid separator (53) through connecting pipelines.

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