Electrolyzed water cooling system for electrolytic hydrogen production

Abstract

The utility model provides an electrolyzed water cooling system for electrolytic hydrogen production, which comprises an adsorption type refrigerating system consisting of an adsorption bed, a condenser and an evaporator, in the evaporator, high-temperature electrolyzed water heats a liquid refrigerant, the liquid refrigerant absorbs heat and evaporates to generate a gaseous refrigerant, and the electrolyzed water releases heat for cooling. A gaseous refrigerant enters the adsorption bed to be adsorbed by the adsorbent, then saturated steam discharged in the synthetic ammonia production process is used for heat exchange with the adsorbent in the adsorption bed, the adsorbent is used for desorption, cooling of electrolyzed water is achieved through the adsorption refrigeration technology, and recycling of tail gas waste heat in the synthetic ammonia production process can be achieved. Compared with traditional compression refrigeration, the energy consumption during water electrolysis hydrogen production can be effectively reduced, and the hydrogen production cost is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to green ammonia production equipment technical field, concretely relates to a kind of electrolytic water cooling system for electrolytic hydrogen for cooling and cooling electrolytic water for electrolytic hydrogen in green ammonia production process. BACKGROUND

[0002] Green ammonia production process refers to the green electricity (photovoltaic, wind power, hydropower and tidal power) produced by renewable energy electrolytic water to produce green hydrogen, nitrogen is produced by air separation, and ammonia is produced by hydrogen and nitrogen synthesis reaction, which is green ammonia. Ammonia is used as fuel or as a carrier for storing and transporting hydrogen energy, which is one of the future trends of green energy development.

[0003] When nitrogen and hydrogen are synthesized into ammonia, they need to be carried out under high temperature and high pressure and catalyst conditions. A large amount of saturated steam is generated during the synthesis process, with a temperature of 250-350 ℃. Direct discharge of high-temperature saturated steam not only pollutes the environment but also causes a huge waste of energy. Currently, the saturated steam generated during the synthesis of ammonia is mainly recycled through heat exchange, such as heating recycled domestic water through plate heat exchangers or using the heated water for heating.

[0004] When green electricity is used to electrolyze water to produce green hydrogen, the most suitable temperature for electrolytic hydrogen production is 60-80℃. Within this temperature range, the water molecule activity and ion conductivity are good, and the hydrogen yield is high and the oxygen yield is low. However, heat is generated during the electrolysis process, causing the temperature of the electrolytic water to rise. Therefore, the temperature of the electrolytic water must be cooled to maintain it within the range of 60-80℃. Currently, the traditional compression refrigeration method is still used to cool the electrolytic water, which requires a large amount of electrical energy.

[0005] Adsorption refrigeration is a technology that uses the physical adsorption / desorption between adsorbent and refrigerant to achieve refrigeration. The entire adsorption refrigeration process includes four main steps: adsorption, desorption, condensation, and evaporation. First, the adsorbent in the adsorption bed is desorbed by passing high-temperature waste heat into the bed, producing gaseous refrigerant. The gaseous refrigerant enters the condenser and is condensed into liquid refrigerant. The liquid refrigerant enters the evaporator for storage. After desorption is complete, the pressure difference between the adsorption bed and the evaporator is used to exchange heat between the heat source in the evaporator and the liquid refrigerant. The liquid refrigerant absorbs heat and evaporates to produce gaseous refrigerant, which enters the adsorption bed under the action of pressure difference and is adsorbed by the adsorbent. The liquid refrigerant in the evaporator continuously evaporates to produce cold energy, and the adsorption bed continuously adsorbs the gaseous refrigerant evaporated from the evaporator, thereby cooling the heat source in the evaporator and achieving cooling of the heat source. SUMMARY

[0006] In summary, in order to overcome the prior art problems, the utility model provides an electrolytic water cooling system for electrolytic hydrogen production, which utilizes adsorption refrigeration technology to cool electrolytic water, uses high-temperature electrolytic water as a heat source to heat liquid refrigerant, and the liquid refrigerant in the evaporator absorbs heat to evaporate into gaseous refrigerant, and the electrolytic water is cooled by heat release, thereby realizing the cooling of electrolytic water during electrolytic hydrogen production, and compared with traditional compression refrigeration, the electrolytic hydrogen production can effectively reduce energy consumption and hydrogen production cost.

[0007] To solve the above technical problems, the utility model adopts the technical scheme that:

[0008] An electrolytic water cooling system for electrolytic hydrogen production, comprising:

[0009] An adsorption bed, which is provided with an adsorbent adsorption layer, has a desorption gas inlet for guiding saturated steam to flow in, a desorption tail gas outlet for guiding hot air to flow out, an adsorption gas inlet for guiding gaseous refrigerant to flow in, a desorption gas outlet for guiding gaseous refrigerant to flow out, a cooling medium inlet for guiding cooling medium to flow in, and a cooling medium outlet for guiding cooling medium to flow out, the desorption tail gas outlet is empty, the desorption gas outlet is communicated with a condensing gas inlet of a condenser, the adsorption gas inlet is communicated with an outlet of an evaporator through a pipeline, the cooling medium inlet of the adsorption bed is communicated with a cooling medium main pipe, and the cooling medium outlet of the adsorption bed is communicated with a cooling medium return pipe,

[0010] A condenser, which has a cooling medium inlet for guiding cooling medium to flow in, a cooling medium outlet for guiding cooling medium to flow out, a condensing gas inlet for guiding gaseous refrigerant to flow in, and a condensing liquid outlet for guiding liquid refrigerant to flow out, the cooling medium inlet of the condenser is communicated with the cooling medium main pipe, the cooling medium outlet of the condenser is communicated with a cooling return water pipe, and the condensing liquid outlet of the condenser is communicated with a condensing liquid inlet of the evaporator through a pipeline,

[0011] An evaporator, which has a condensing liquid inlet for guiding liquid refrigerant to flow in, an outlet for guiding gaseous refrigerant to flow out, a heating medium inlet for guiding high-temperature electrolytic water to flow in, and a heating medium outlet for guiding low-temperature electrolytic water to flow out, the outlet of the evaporator is communicated with the adsorption gas inlet of the adsorption bed, the heating medium inlet of the evaporator is communicated with an outlet of an electrolytic cell through a pipeline, and the heating medium outlet of the evaporator is communicated with a return water outlet of the electrolytic cell through a pipeline.

[0012] Further, the adsorbent is 13X zeolite, and the refrigerant is water.

[0013] Further, the desorption gas inlet of the adsorption bed is communicated with an exhaust outlet of an ammonia synthesis tower through a saturated steam pipeline.

[0014] Further, the desorption tail gas outlet of the adsorption bed is communicated with the air inlet of the air drafter through a tail gas main, and the air outlet of the air drafter is exhausted.

[0015] Further, a condensate control valve is arranged on the pipeline communicated with the condensate outlet of the condenser and the condensate inlet of the evaporator.

[0016] Further, a flow rate control valve is arranged on the pipeline communicated with the heating medium inlet of the evaporator and the water outlet of the electrolytic cell.

[0017] Further, the number of the adsorption beds is multiple, the multiple adsorption beds are arranged in parallel, the desorption air inlets of the multiple adsorption beds are respectively communicated with the saturated steam pipeline through pipelines, desorption air inlets are arranged on the pipelines, the desorption tail gas outlets of the multiple adsorption beds are respectively communicated with the tail gas main through pipelines, tail gas outlets are arranged on the pipelines, the desorption air outlets of the multiple adsorption beds are respectively communicated with the desorption gas main through pipelines, desorption air outlets are arranged on the pipelines, the desorption gas main is communicated with the condensing air inlet of the condenser, the adsorption air inlets of the multiple adsorption beds are respectively communicated with the adsorption air main through pipelines, adsorption air inlets are arranged on the pipelines, the adsorption air main is communicated with the air outlet of the evaporator, the cooling medium inlets of the multiple adsorption beds are respectively communicated with the cooling medium main through pipelines, cooling water inlets are arranged on the pipelines, the cooling medium outlets of the multiple adsorption beds are respectively communicated with the cooling medium return pipeline through pipelines, cooling water outlets are arranged on the pipelines.

[0018] The utility model discloses the beneficial effect is:

[0019] 1, the utility model discloses a utilization adsorption refrigeration technology is cooled to electrolytic water, and high temperature electrolytic water is heat source to liquid refrigerant heating, and liquid refrigerant absorbs heat and evaporates into gaseous refrigerant, and electrolytic water cooling, and the liquid refrigerant in evaporator continues to evaporate and generates cold, realizes the cooling of electrolytic water when electrolytic water is made hydrogen, compares with traditional compression refrigeration, can effectively reduce the energy consumption when electrolytic water is made hydrogen, reduces hydrogen production cost.

[0020] 2, the utility model discloses that the desorption air inlet of adsorption bed is communicated with the exhaust port of ammonia synthesis tower, and saturated steam is entered into adsorption bed in the production process of synthetic ammonia, and saturated steam exchanges heat with adsorbent in adsorption bed, and adsorbent desorption, realizes the recycling of tail gas waste heat in the production process of synthetic ammonia, saves the energy consumption of adsorbent desorption in adsorption bed simultaneously, energy saving and emission reduction, reduces cost.

[0021] 3、The number of the adsorption beds is multiple, and the multiple adsorption beds are arranged in parallel, and in use, the multiple adsorption beds arranged in parallel can be used alternately, thereby effectively realizing continuous production, and the continuous cooling of the high-temperature electrolytic water can be realized, the high-temperature electrolytic water can be kept at a proper electrolysis temperature, and the hydrogen yield during the production of green electricity hydrogen is improved. BRIEF DESCRIPTION OF DRAWINGS

[0022] Figure 1 It is a structural schematic diagram of the utility model. DETAILED DESCRIPTION

[0023] The utility model will be further explained in detail in connection with the drawings.

[0024] As Figure 1 The electrolytic water cooling system for electrolytic hydrogen production includes an ammonia synthesis tower 1, and the exhaust port of the ammonia synthesis tower 1 is connected with an adsorption bed group through a saturated steam pipeline; saturated steam generated in the ammonia synthesis reaction flows out from the exhaust port of the ammonia synthesis tower 1 and enters the adsorption bed group through the saturated steam pipeline.

[0025] The adsorption bed group is composed of multiple adsorption beds arranged in parallel, the adsorption bed is internally provided with an adsorbent adsorption layer, and the adsorption bed is provided with a desorption air inlet for guiding hot dry air to flow in, a desorption tail gas outlet for guiding hot air to flow out, a desorption gas outlet for guiding gaseous refrigerant to flow out, a cooling medium inlet for guiding cooling medium to flow in, a cooling medium outlet for guiding cooling medium to flow out and an adsorption air inlet for guiding gaseous refrigerant to flow in; the desorption air inlets of the multiple adsorption beds are respectively connected with the saturated steam pipeline 8 through pipelines, and desorption air inlets are provided on the pipelines; the desorption tail gas outlets of the multiple adsorption beds are respectively connected with a tail gas main pipe 50 through pipelines, and tail gas outlet valves are provided on the pipelines; the desorption gas outlets of the multiple adsorption beds are respectively connected with a desorption gas main pipe 4 through pipelines, and desorption gas outlet valves are provided on the pipelines; the desorption gas main pipe 4 is connected with the condensing air inlet of the condenser 5; the adsorption air inlets of the multiple adsorption beds are respectively connected with an adsorption air main pipe 49 through pipelines, and adsorption air inlets are provided on the pipelines; the adsorption air main pipe 49 is connected with the air outlet of the evaporator 46; the cooling medium inlets of the multiple adsorption beds are respectively connected with a cooling medium main pipe 3 through pipelines, and cooling water inlets are provided on the pipelines; the cooling medium outlets of the multiple adsorption beds are respectively connected with a cooling medium return pipe 48 through pipelines, and cooling water outlets are provided on the pipelines. In the embodiment, the adsorbent is 13X zeolite, and the refrigerant is water.

[0026] In this embodiment, three adsorption beds arranged in parallel form an adsorption bed group, namely a first adsorption bed 23, a second adsorption bed 24, and a third adsorption bed 25. The desorption inlet of the first adsorption bed 23 is connected to the saturated steam pipeline 8 through a first desorption inlet pipeline 11, and a first desorption inlet valve 26 is provided on the first desorption inlet pipeline 11. The desorption inlet of the second adsorption bed 24 is connected to the saturated steam pipeline 8 through a second desorption inlet pipeline 14, and a second desorption inlet valve 16 is provided on the second desorption inlet pipeline 14. The desorption inlet of the third adsorption bed 25 is connected to the saturated steam pipeline 8 through a third desorption inlet pipeline 21, and a third desorption inlet valve 22 is provided on the third desorption inlet pipeline 21. The desorption tail gas outlet of the first adsorption bed 23 is connected to the tail gas main pipe 50 through the first tail gas pipeline 32. The first tail gas pipeline 32 is equipped with a first tail gas outlet valve 31. The desorption tail gas outlet of the second adsorption bed 24 is connected to the tail gas main pipe 50 through the second tail gas pipeline 38. The second tail gas pipeline 38 is equipped with a second tail gas outlet valve 37. The desorption tail gas outlet of the third adsorption bed 25 is connected to the tail gas main pipe 50 through the third tail gas pipeline 42. The third tail gas pipeline 42 is equipped with a third tail gas outlet valve 41. The tail gas main pipe 50 is connected to the air inlet of the induced draft fan 51, and the air outlet of the induced draft fan 51 is vented.

[0027] The desorption outlet of the first adsorption bed 23 is connected to the desorption gas main pipe 4 through the first desorption gas outlet pipeline 10. A first desorption gas outlet valve 6 is installed on the first desorption gas outlet pipeline 10. The desorption outlet of the second adsorption bed 24 is connected to the desorption gas main pipe 4 through the second desorption gas outlet pipeline 13. A second desorption gas outlet valve 15 is installed on the second desorption gas outlet pipeline 13. The desorption outlet of the third adsorption bed 25 is connected to the desorption gas main pipe 4 through the third desorption gas outlet pipeline 20. A third desorption gas outlet valve 19 is installed on the third desorption gas outlet pipeline 20. The desorption gas main pipe 4 is connected to the condenser inlet of the condenser 5.

[0028] The adsorption inlet of the first adsorption bed 23 is connected to the adsorption inlet main pipe 49 through the first adsorption inlet pipe 30. A first adsorption inlet valve 33 is provided on the first adsorption inlet pipe 30. The adsorption inlet of the second adsorption bed 24 is connected to the adsorption inlet main pipe 49 through the second adsorption inlet pipe 36. A second adsorption inlet valve 44 is provided on the second adsorption inlet pipe 36. The adsorption inlet of the third adsorption bed 25 is connected to the adsorption inlet main pipe 49 through the third adsorption inlet pipe 40. A third adsorption inlet valve 45 is provided on the third adsorption inlet pipe 40. The adsorption inlet main pipe 49 is connected to the outlet of the evaporator 46.

[0029] The cooling medium inlet of the first adsorption bed 23 is connected to the cooling medium main pipe 3 through the first cooling medium inlet pipe 9, and the first cooling water inlet valve 2 is arranged on the first cooling medium inlet pipe 9. The cooling medium inlet of the second adsorption bed 24 is connected to the cooling medium main pipe 3 through the second cooling medium inlet pipe 12, and the second cooling water inlet valve 7 is arranged on the second cooling medium inlet pipe 12. The cooling medium inlet of the third adsorption bed 25 is connected to the cooling medium main pipe 3 through the third cooling medium inlet pipe 17, and the third cooling water inlet valve 18 is arranged on the third cooling medium inlet pipe 17. In the embodiment, low-temperature cooling water is used as the cooling medium, and the cooling medium main pipe 3 is connected to the cooling tower water outlet. The cooling medium outlet of the first adsorption bed 23 is connected to the cooling medium return pipe 48 through the first cooling medium outlet pipe 28, and the first cooling water return valve 29 is arranged on the first cooling medium outlet pipe 28. The cooling medium outlet of the second adsorption bed 24 is connected to the cooling medium return pipe 48 through the second cooling medium outlet pipe 35, and the second cooling water return valve 34 is arranged on the second cooling medium outlet pipe 35. The cooling medium outlet of the third adsorption bed 25 is connected to the cooling medium return pipe 48 through the third cooling medium outlet pipe 39, and the third cooling water return valve 43 is arranged on the third cooling medium outlet pipe 39. The cooling medium return pipe 48 is connected to the cooling tower water return outlet.

[0030] The condenser 5 has a cooling medium inlet for guiding the flow of cooling medium, a cooling medium outlet for guiding the flow of cooling medium, a condensing gas inlet for guiding the flow of gaseous refrigerant, and a condensing liquid outlet for guiding the flow of liquid refrigerant. The cooling medium inlet of the condenser 5 is connected to the cooling medium main pipe 3, the cooling medium outlet of the condenser 5 is connected to the cooling water return pipe, and the condensing liquid outlet of the condenser 5 is connected to the condensing liquid inlet of the evaporator 46 through a pipe, and the condensing liquid control valve 27 is arranged on the pipe.

[0031] The evaporator 46 has a condensing liquid inlet for guiding the flow of liquid refrigerant, a gas outlet for guiding the flow of gaseous refrigerant, a heating medium inlet for guiding the flow of high-temperature electrolysis water, and a heating medium outlet for guiding the flow of low-temperature electrolysis water. The gas outlet of the evaporator 46 is connected to the adsorption gas inlet of the adsorption bed, the heating medium inlet of the evaporator 46 is connected to the electrolysis cell water outlet through a pipe, and the flow rate control valve 47 is arranged on the pipe. The heating medium outlet of the evaporator 46 is connected to the electrolysis cell water return outlet through a pipe.

[0032] When in use, the induced draft fan 51, the first desorption inlet valve 26, the second desorption inlet valve 16, the third desorption inlet valve 22, the first desorption outlet valve 6, the second desorption outlet valve 15, the third desorption outlet valve 19, the first tail gas outlet valve 31, the second tail gas outlet valve 37 and the third tail gas outlet valve 41 are opened. Under the action of the induced draft fan 51, the saturated steam discharged from the outlet of the ammonia synthesis tower 1 enters the saturated steam pipeline 8, and then enters the first adsorption bed 23, the second adsorption bed 24 and the third adsorption bed 25 through the first desorption inlet pipeline 11, the second desorption inlet pipeline 14 and the third desorption inlet pipeline 21 respectively along the saturated steam pipeline 8. The high-temperature saturated steam exchanges heat with the 13x zeolite in the first adsorption bed 23, the 13x zeolite in the second adsorption bed 24 and the 13x zeolite in the third adsorption bed 25, the 13x zeolite absorbs heat and desorbs, and the saturated steam releases heat and cools down. The cooled saturated steam enters the tail gas main pipeline 50 along the first tail gas pipeline 32, the second tail gas pipeline 38 and the third tail gas pipeline 42 under the action of the induced draft fan 51, and then is discharged under the action of the induced draft fan 51. The gaseous refrigerant desorbed from the 13x zeolite in the three adsorption beds enters the desorption gas main pipeline 4 along the first desorption outlet pipeline 10, the second desorption outlet pipeline 13 and the third desorption outlet pipeline 20 respectively, and then enters the condenser 5 from the condensing inlet under the action of the desorption gas main pipeline 4. In this embodiment, the refrigerant is water, so the gaseous refrigerant is water vapor. The water vapor enters the condenser 5 from the condensing inlet, and the cooling water in the cooling medium main pipeline 3 enters the condenser 5 from the cooling medium inlet. In the condenser 5, the water vapor is condensed into condensed water by the cooling water. The condensed water has a relatively high temperature, and the cooling water entering the condenser 5 is heated. The heated cooling water enters the cooling tower through the cooling medium return pipeline 48. When the steam pressure in the first adsorption bed 23, the second adsorption bed 24 and the third adsorption bed 25 decreases to a set value, the first desorption inlet valve 26, the second desorption inlet valve 16, the third desorption inlet valve 22, the first desorption outlet valve 6, the second desorption outlet valve 15, the third desorption outlet valve 19, the first tail gas outlet valve 31, the second tail gas outlet valve 37 and the third tail gas outlet valve 41 are closed, and the desorption of the three adsorption beds is completed.

[0033] After the desorption is completed, the first cooling water inlet valve 2, the first cooling water outlet valve 29, the first adsorption gas inlet valve 33 and the condensate control valve 27 are opened, the flow rate control valve 47 is opened, the high-temperature electrolytic water enters the evaporator 46 from the heating medium inlet of the evaporator 46, the liquid refrigerant flowing out of the condenser 5 enters the evaporator along the pipeline, in the evaporator 46, the liquid refrigerant absorbs the heat in the high-temperature electrolytic water, the liquid refrigerant evaporates into gaseous refrigerant by absorbing heat, and the high-temperature electrolytic water is cooled. In this embodiment, the refrigerant is water, so the liquid refrigerant flowing out of the condenser 5 is water, and in the evaporator 46, the water absorbs the heat in the high-temperature electrolytic water, and the water evaporates into water vapor. By adjusting the flow rate control valve 47, the water inlet amount of the high-temperature electrolytic water can be controlled, so that the cooled electrolytic water is maintained within the range of 60-80°C, and the cooled electrolytic water flows back to the electrolytic cell from the heating medium outlet of the evaporator 46 to participate in electrolysis to produce hydrogen. Under the action of the pressure difference between the first adsorption bed 23 and the evaporator 46, the gaseous refrigerant, i.e. water vapor, evaporated by the evaporator 46 enters the first adsorption bed 23 through the adsorption gas inlet of the first adsorption bed 23 along the adsorption gas inlet pipeline 30 and the adsorption gas inlet main pipeline 49, and the water vapor is adsorbed by the 13X zeolite in the first adsorption bed 23. The cooling water in the cooling medium main pipeline 3 enters the first adsorption bed 23 through the first cooling medium inlet pipeline 9 and the cooling medium inlet of the first adsorption bed 23, and then flows out of the cooling medium outlet of the first adsorption bed 23, enters the cooling tower along the cooling medium return pipeline 48, and cools the adsorbent in the first adsorption bed 23, thereby facilitating the adsorption of the adsorbent to the refrigerant.

[0034] When the first adsorption bed 23 is saturated, the first cooling water inlet valve 2, the first cooling water outlet valve 29, the first adsorption gas inlet valve 33 are closed, the second cooling water inlet valve 7, the second cooling water outlet valve 34, the second adsorption gas inlet valve 44, the first desorption gas inlet valve 26, the first desorption gas outlet valve 6 and the first tail gas outlet valve 31 are opened. Under the action of the pressure difference between the second adsorption bed 24 and the evaporator 46, the water vapor generated by the evaporator 46 enters the second adsorption bed 24 along the adsorption gas inlet pipeline 36 and the adsorption gas inlet main pipeline 49, and the gaseous refrigerant is adsorbed by the 13X zeolite in the second adsorption bed 24, so that the liquid refrigerant entering the evaporator 46 continues to evaporate by absorbing heat, and the high-temperature electrolytic water continues to cool. The cooling water in the cooling medium main pipeline 3 enters the second adsorption bed 24 through the second cooling medium inlet pipeline 12, and then flows out of the cooling medium outlet of the second adsorption bed 24, enters the cooling tower along the cooling medium return pipeline 48, and cools the adsorbent in the second adsorption bed 24. At the same time, the saturated steam in the saturated steam pipeline 8 enters the first adsorption bed 23 through the first desorption gas inlet pipeline 11, and the 13X zeolite in the first adsorption bed 23 is subjected to heat exchange by the saturated steam, and the 13X zeolite is desorbed after absorbing heat.

[0035] Similarly, when the second adsorption bed 24 is saturated, the second cooling water inlet valve 7, the second cooling water outlet valve 34, and the second adsorption gas inlet valve 44 are closed, and the third cooling water inlet valve 18, the third cooling water outlet valve 43, the third adsorption gas inlet valve 45, the second desorption gas inlet valve 16, the second desorption gas outlet valve 15, and the second tail gas outlet valve 37 are opened. Under the pressure difference between the third adsorption bed 25 and the evaporator 46, the gaseous refrigerant generated by the evaporator 46 enters the third adsorption bed 25 through the adsorption gas inlet manifold 49 and the third adsorption gas inlet pipeline 40, and the gaseous refrigerant is adsorbed by the 13X zeolite in the third adsorption bed 25. The gaseous refrigerant flowing out of the evaporator 46 is adsorbed by the third adsorption bed 25, so that the liquid refrigerant entering the evaporator 46 is continuously evaporated by heat absorption, and the high-temperature electrolysis water is continuously cooled. The cooling water in the cooling medium manifold 3 enters the third adsorption bed 25 through the third cooling medium inlet pipe 17, and then flows out of the third adsorption bed 25 through the cooling medium outlet of the third adsorption bed 25, and enters the cooling tower for cooling through the cooling medium return pipe 48. At the same time, the saturated steam in the saturated steam pipeline 8 enters the second adsorption bed 24 through the second desorption gas inlet pipeline 14, and the saturated steam exchanges heat with the 13X zeolite in the second adsorption bed 24, and the 13X zeolite is desorbed after heat absorption.

[0036] When the third adsorption bed 25 is saturated, the third cooling water inlet valve 18, the third cooling water outlet valve 43, and the third adsorption gas inlet valve 45 are closed, and the first cooling water inlet valve 2, the first cooling water outlet valve 29, the first adsorption gas inlet valve 33, the third desorption gas inlet valve 22, the third desorption gas outlet valve 19, and the third tail gas outlet valve 41 are opened. Under the pressure difference between the first adsorption bed 23 and the evaporator 46, the gaseous refrigerant generated by the evaporator 46 re-enters the first adsorption bed 23 and is adsorbed by the 13X zeolite in the first adsorption bed 23.

[0037] According to the above working sequence, when the first adsorption bed 23 is saturated, the second adsorption bed 24 and the third adsorption bed 25 are desorbed, and when the second adsorption bed 24 is saturated, the third adsorption bed 25 is adsorbed, and the first adsorption bed 23 and the second adsorption bed 24 are desorbed. In this way, the three adsorption beds work alternately, so that the condensed water entering the evaporator 46 is continuously evaporated by heat absorption, and the high-temperature electrolysis water is continuously cooled, providing continuous 60-80℃ electrolysis water for electrolysis of hydrogen, thereby stabilizing the electrolysis water temperature in the electrolysis cell and effectively improving the hydrogen production efficiency and hydrogen yield of green energy electrolysis of hydrogen.

[0038] It should be noted that the above-described embodiments are illustrative of the technical scheme of the present application and are not limiting, and equivalent replacements or other modifications made by those skilled in the art based on the prior art should be included within the scope of the rights required by the present application as long as they do not exceed the ideas and scope of the technical scheme of the present application.

Claims

1. An electrolytic water cooling system for electrolytic hydrogen production, characterized by, The application relates to a refrigeration system, which comprises: an adsorption bed with an adsorbent adsorption layer, a desorption gas inlet for saturated steam, a desorption tail gas outlet, an adsorption gas inlet for gaseous refrigerant, a desorption gas outlet, a cooling medium inlet and a cooling medium outlet, the desorption tail gas outlet is connected with a condenser, the adsorption gas inlet is connected with an evaporator, the cooling medium inlet is connected with a cooling medium main pipe, and the cooling medium outlet is connected with a cooling medium return pipe, a condenser with a cooling medium inlet, a cooling medium outlet, a condensation gas inlet and a condensation liquid outlet, the cooling medium inlet is connected with the cooling medium main pipe, the cooling medium outlet is connected with the cooling water return pipe, and the condensation liquid outlet is connected with the evaporator, an evaporator with a condensation liquid inlet, a gas outlet, a heating medium inlet and a heating medium outlet, the gas outlet is connected with the adsorption gas inlet, the heating medium inlet is connected with an electrolytic cell, and the heating medium outlet is connected with the electrolytic cell.

2. The water cooling system for electrolysis of water for hydrogen production according to claim 1, characterized in that: The adsorbent is 13X zeolite, and the refrigerant is water.

3. The water electrolysis cooling system for hydrogen production by electrolysis according to claim 1, characterized in that: The desorption gas inlet of the adsorption bed is connected with an ammonia synthesis tower through a saturated steam pipe.

4. The water cooling system for electrolysis of water for hydrogen production according to claim 3, characterized in that: The desorption tail gas outlet of the adsorption bed is connected with an air fan through a tail gas main pipe.

5. The water cooling system for electrolysis of water for hydrogen production according to claim 1, characterized in that: The condensation liquid outlet of the condenser is provided with a condensation liquid control valve.

6. The water cooling system for electrolysis of water for hydrogen production according to claim 1, characterized in that: The heating medium inlet of the evaporator is provided with a flow rate control valve.

7. The water cooling system for electrolysis of water for hydrogen production according to any one of claims 1-6, characterized in that: The adsorption bed is provided in plurality, and the plurality of adsorption beds are connected in parallel, the desorption gas inlets of the plurality of adsorption beds are respectively connected with a saturated steam pipe through pipes, the pipes are provided with desorption gas inlets, the desorption tail gas outlets of the plurality of adsorption beds are respectively connected with a tail gas main pipe through pipes, the pipes are provided with tail gas outlets, the desorption gas outlets of the plurality of adsorption beds are respectively connected with a desorption gas main pipe through pipes, the pipes are provided with desorption gas outlets, the desorption gas main pipe is connected with the condenser, the adsorption gas inlets of the plurality of adsorption beds are respectively connected with an adsorption gas main pipe through pipes, the pipes are provided with adsorption gas inlets, the adsorption gas main pipe is connected with the evaporator, the cooling medium inlets of the plurality of adsorption beds are respectively connected with a cooling medium main pipe through pipes, the pipes are provided with cooling water inlets, and the cooling medium outlets of the plurality of adsorption beds are respectively connected with a cooling medium return pipe through pipes, the pipes are provided with cooling water outlets.

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