System for producing hydrogen and co-producing solid salt by using non-pure water solution

Abstract

The utility model discloses a non-pure aqueous solution hydrogen production and solid salt co-production system, which belongs to the field of electrochemistry and comprises a non-pure aqueous solution hydrogen production subsystem and a salt crystallization separation subsystem which are connected with each other. A non-pure water solution mass transfer device is arranged in a salt crystallization separation cabin of the salt crystallization separation subsystem, a non-pure water solution inlet and a pure water vapor outlet are formed in the salt crystallization separation cabin, and the non-pure water solution inlet is connected with a first valve; a solid salt outlet is formed in the solid-liquid separator; a second valve is arranged between the salt crystal separation cabin and the solid-liquid separator; the non-pure water solution mass transfer device comprises a non-pure water solution mass transfer unit, and a waterproof breathable layer is attached to the surface of the non-pure water solution mass transfer unit. The device disclosed by the utility model can fundamentally solve the problems of failure of an ion exchange membrane, inactivation of a catalyst, generation of alkaline precipitate and toxic gas and the like caused by complex ion components, and achieves double-effect utilization of energy regeneration and resource utilization of non-pure water solution.

Description

Technical Field

[0001] The utility model relates to the field of electrochemistry, and more specifically to a non-pure aqueous solution hydrogen production and solid salt co-production system. Background Art

[0002] Hydrogen energy has the advantages of wide sources, storability, multiple uses, zero carbon and zero pollution, and high energy density. It is a key component of the future energy field. Directly using natural seawater, salt lake water, high-concentration industrial wastewater and other non-pure water for electrolysis to produce hydrogen is a green and efficient means. However, most of the existing non-pure water direct hydrogen production uses modified catalysts, but non-pure water solutions are rich in impure ions. Direct electrolysis will cause a series of problems such as chlorine evolution side reactions, catalyst deactivation, system poisoning, calcium and magnesium precipitation, and membrane clogging.

[0003] In addition, seawater, salt lake water, high-concentration industrial wastewater, etc. contain a large amount of salt components that can be recycled. If the water is consumed through the electrolysis process, the salt component is extracted after the feed liquid is concentrated, and high-value-added solid products are produced while hydrogen is produced, it will achieve the dual-effect utilization of resources and energy. Utility Model Content

[0004] The purpose of the utility model is to overcome the deficiencies of the prior art and provide a non-pure aqueous solution hydrogen production and solid salt co-production system, which fundamentally solves the problems of complex ion components causing ion exchange membrane failure, catalyst deactivation, alkaline precipitation and toxic gas generation. Pure water can be directly obtained from non-pure water for hydrogen production through electrolytes. While consuming water by electrolysis, these non-pure aqueous solutions can be brought to a saturated state, and the salt-containing components can be separated out to form a solid product with added value, thereby achieving the dual-effect utilization of non-pure aqueous solutions as energy and resources.

[0005] The purpose of the utility model is achieved through the following solutions:

[0006] A non-pure aqueous solution hydrogen production and solid salt co-production system, comprising a non-pure aqueous solution hydrogen production subsystem and a salt crystallization separation subsystem, wherein the non-pure aqueous solution hydrogen production subsystem is connected to the salt crystallization separation subsystem; the salt crystallization separation subsystem comprises a salt crystallization separation cabin; a non-pure aqueous solution mass transferor is arranged inside the salt crystallization separation cabin, a non-pure aqueous solution inlet and a pure water vapor outlet are arranged on the salt crystallization separation cabin, and the non-pure aqueous solution inlet is connected to a first valve; a solid salt discharge outlet is arranged on the solid-liquid separator, and a second valve is arranged between the salt crystallization separation cabin and the solid-liquid separator; the non-pure aqueous solution mass transferor comprises non-pure aqueous solution mass transfer units A1~An, and a waterproof and breathable layer is attached to the surface of the non-pure aqueous solution mass transfer units A1~An.

[0007] Furthermore, a heat-insulating layer is provided on the wall surface of the salt crystallization separation cabin.

[0008] Furthermore, it also includes a solid-liquid separator, and the solid-liquid separator and the salt crystallization separation cabin are connected through the second valve; when a batch of feed liquid reacts completely, the next batch of non-pure aqueous solution is added through the non-pure aqueous solution inlet and the first valve; the salt sedimentation area at the bottom of the salt crystallization separation cabin has a solid outlet channel, which is connected to the second valve, and enters the solid-liquid separator by opening the second valve. After the water in the solid particles is removed in the solid-liquid separator, the solid salt product is obtained and discharged from the solid salt outlet; the electrolyte of pure water is obtained from the salt crystallization separation cabin, and is returned to the electrolyte storage tank of the non-pure aqueous solution hydrogen production subsystem for storage, while replenishing pure water for the electrolysis system and preparing for the next electrolysis.

[0009] Furthermore, the structure of each of the non-pure aqueous solution mass transfer units A1 to An is a plate type or a hollow fiber type.

[0010] Furthermore, the non-pure aqueous solution includes any one of seawater, salt lake water, chemical water, river water, lake water, wastewater, swamp water and domestic sewage.

[0011] Furthermore, the waterproof and breathable layer includes any one of a porous TPU membrane, a PDMS membrane, and a PTFE membrane.

[0012] Furthermore, the waterproof and breathable layer includes a porous waterproof and breathable mass transfer layer prepared by using graphene, PVDF particles, PTFE particles and by spraying, screen printing, and electrostatic adsorption.

[0013] Furthermore, the thermal insulation layer includes a vacuum sandwich structure or a thermal insulation coating directly coated on the wall surface of the salt crystal separation cabin 17 .

[0014] The beneficial effects of the utility model include:

[0015] The utility model provides a non-pure aqueous solution hydrogen production and solid salt co-production system based on a newly discovered principle, which integrates an energy supply module, an electrolytic hydrogen production module, a salt crystallization separation module, a non-pure aqueous solution mass transfer module, a hydrogen collection module, an oxygen collection module and a cooling module.

[0016] The utility model constructs a non-pure water hydrogen production and solid salt co-production system, which has the following functions: 1) fundamentally solves the problem that the complex ion components make the ion exchange membrane ineffective, the catalyst deactivated, and alkaline precipitation and toxic gas generated, and can directly obtain pure water for hydrogen production from various non-pure waters such as sea water, river water, lake water, silt, swamp, salt lake water, industrial wastewater, etc. through electrolytes; 2) while consuming water by electrolysis, these non-pure aqueous solutions can be saturated, and the salt-containing components can be separated to form solid products with added value. The non-pure aqueous solution is used for energy and resources.

[0017] The utility model realizes the functions of direct electrolysis of non-pure water to produce hydrogen and co-produce solid salt, and at the same time utilizes the waste heat of the electrolysis hydrogen production system itself to increase the phase change mass transfer rate, reduce the system electrolyte temperature, accelerate the salt precipitation rate, and co-produce pure water. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0019] Figure 1 This is a structural diagram of a non-pure aqueous solution hydrogen production and solid salt co-production system according to an embodiment of the utility model;

[0020] Figure 2 The stability test results of using the utility model to produce hydrogen from salt lake water and simultaneously concentrate to form lithium salt;

[0021] Figure 3 The stability test results of using the utility model to produce hydrogen in chemical industry and simultaneously concentrate to form sodium salt;

[0022] In the figure, 1-power supply module; 2-electrolyzer; 3-hydrogen separator; 4-hydrogen purifier; 5-hydrogen regulating valve; 6-hydrogen check valve; 7-hydrogen cooler; 8-hydrogen storage tank; 9-oxygen separator; 10-oxygen purifier; 11-oxygen regulating valve; 12-oxygen check valve; 13-oxygen cooler; 14-oxygen storage tank; 15-cooling water tank; 16-cooling water pump; 17-salt crystallization separation cabin; 18-non-pure aqueous solution mass transfer device; 19-non-pure aqueous solution inlet; 20-first valve 1; 21-pure water vapor outlet; 22-second valve; 23-solid-liquid separator; 24-solid salt outlet; 25-electrolyte buffer tank; 26-pressure relief valve; 27-external electrolyte storage tank; 28-control valve; A1~An-non-pure aqueous solution mass transfer unit. DETAILED DESCRIPTION

[0023] All features disclosed in all embodiments in this specification, or steps in all methods or processes implicitly disclosed, except for mutually exclusive features and / or steps, can be combined and / or expanded or replaced in any manner.

[0024] The specific implementation process of the utility model is as follows:

[0025] The utility model provides a non-pure aqueous solution hydrogen production and solid salt co-production system, which integrates an energy supply module, an electrolytic hydrogen production module, a salt crystallization separation module, a non-pure aqueous solution mass transfer module, a hydrogen collection module, an oxygen collection module, and a cooling module.

[0026] First, follow the Figure 1 The non-pure aqueous solution hydrogen production and solid salt co-production system of the utility model is constructed as shown. Among them, the energy supply module is used for power supply. Figure 1 As shown, the power supply module 1 is used to provide power to the electrolysis hydrogen production module.

[0027] Before the reaction starts, the electrolyte is pumped into the external electrolyte storage tank 27, and the electrolyte enters the electrolytic cell 2, the hydrogen separator 3, the oxygen separator 9, the electrolyte buffer tank 25, and the non-pure aqueous solution mass transfer device 18. A control valve 28 and a pump are provided between the external electrolyte storage tank 27 and the electrolyte buffer tank 25, and the electrolyte buffer tank 25 is provided with a pressure relief valve 26.

[0028] When hydrogen production begins, the electrolyte in the electrolytic cell 2 undergoes a redox reaction to generate hydrogen and oxygen. If the electrolytic cell 2 is an alkaline electrolytic cell or an AEM (anion exchange membrane) electrolytic cell, the electrolyte first undergoes a reduction hydrogen evolution reaction at the cathode to generate OH - The electrolyte enters the anode through the diaphragm or anion exchange membrane and undergoes an oxidation reaction to produce oxygen. If the electrolyzer is a PEM (proton exchange membrane) electrolyzer, the electrolyte now undergoes an oxidation oxygen evolution reaction at the anode to produce H + It enters the cathode through the proton exchange membrane and undergoes a reduction reaction to produce hydrogen.

[0029] The generated hydrogen and oxygen enter the hydrogen separator 3 and the oxygen separator 9 respectively. This process separates the generated hydrogen / oxygen from the mixed electrolyte or water.

[0030] The separated hydrogen and oxygen enter the hydrogen purifier 4 and the oxygen purifier 10 respectively. This process further cleans the electrolyte and water in the gas that have not been separated completely.

[0031] The cleaned hydrogen enters the hydrogen cooler 7 to dry and cool the hydrogen under the control of the hydrogen regulating valve 5 and the hydrogen check valve 6, and is then stored in the hydrogen storage tank 8. The cleaned oxygen enters the oxygen cooler 13 to dry and cool the oxygen under the control of the oxygen regulating valve 11 and the oxygen check valve 12, and is then stored in the hydrogen storage tank 14.

[0032] It should be noted that the oxygen purifier 10, the oxygen cooler 13, the oxygen regulating valve 11, the oxygen check valve 12, and the oxygen storage tank 14 are not essential items and can be flexibly determined according to the back-end requirements.

[0033] The electrolyte entering the non-pure aqueous solution mass transfer device 18 is divided into non-pure aqueous solution mass transfer units A1~An. A waterproof and breathable layer is attached to the surface of the non-pure aqueous solution mass transfer units A1~An. The membrane layer only allows water vapor to pass through, and does not allow liquid water to penetrate and pollute each other. When the electrolyte passes through the non-pure aqueous solution mass transfer device 18, under the action of the interface vapor pressure difference between the non-pure aqueous solution and the electrolyte, the non-pure aqueous solution undergoes gasification on the surface of the waterproof and breathable layer to produce water vapor. The water vapor enters the electrolyte side through the waterproof and breathable layer, and induces the water vapor phase change to liquefy under the action of the interface pressure difference to replenish water for the electrolyte. Therefore, the non-pure aqueous solution in the salt crystallization separation cabin 17 can continuously replenish pure water to the electrolyte in the non-pure aqueous solution mass transfer device 18 for electrolytic hydrogen production. After the non-pure aqueous solution in the salt crystallization separation cabin 17 is continuously consumed, the solution concentration continues to increase until it reaches a saturated state, and solid particles are precipitated and settle to the bottom of the salt crystallization separation cabin 17. In addition, the salt crystallization separation cabin 17 can be provided with an insulation layer on the wall to optimize the system. Since the hydrogen production system generates a large amount of heat, the high-temperature electrolyte enters the salt crystallization separation cabin 17 to exchange heat with the low-temperature non-pure water solution, so that the non-pure water solution is heated up, and the insulation effect of the salt crystallization separation cabin 17 further prevents heat from being lost to the outside; the vapor pressure difference between the non-pure water solution and the electrolyte increases after the temperature is increased, further increasing the phase change mass transfer rate of the non-pure water solution to the electrolyte, so that more pure water is continuously added to the electrolyte for electrolytic hydrogen production; at the same time, due to the increase in temperature in the salt crystallization separation cabin 17, the water is continuously evaporated outward and discharged through the pure water vapor outlet 21, and pure water vapor can be further obtained, and pure water can be co-produced after condensation and liquefaction. The above process accelerates the consumption of water and will also accelerate the precipitation of crystallized salt. The salt crystallization separation cabin 17 is provided with a non-pure water solution inlet 19 and a first valve 20. When a batch of feed liquid reacts completely, the next batch of non-pure water solution is added. The salt precipitation area at the bottom of the salt crystallization separation cabin has a second valve 22 for leading out the solid (with a small amount of water) channel, which enters the solid-liquid separator 23, removes a small amount of water from the solid particles, and obtains a solid salt product and is discharged from the solid salt outlet 24. The electrolyte of pure water is obtained from the salt crystallization separation cabin 17 and returned to the external electrolyte storage tank 27 for storage, which replenishes pure water for the electrolysis system and prepares for the next electrolysis.

[0034] During the whole reaction process, the total amount of electrolyte is regulated by the liquid level controller. When the liquid levels in the hydrogen separator 3 and the oxygen separator 9 are reduced to a specific value, the electrolyte is continuously replenished into the system from the external electrolyte storage tank 27 through control.

[0035] In the whole system, there is also an internal circulation cooling system, which consists of a cooling water tank 15 and a cooling water pump 16, and provides cooling water for the hydrogen separator 3, the hydrogen purifier 4, the hydrogen cooler 7, the oxygen separator 9, the oxygen purifier 10, and the oxygen cooler 13.

[0036] After the reaction is completed, the electrolyte is discharged through the pressure relief valve 26.

[0037] The salt crystallization separation cabin of the utility model can be made of corrosion-resistant materials such as 316L stainless steel, and has a baffle for solid salt crystal sedimentation and a stirring blade for helping the solid salt flow and discharge at the bottom. Its structure can be various structures such as cylindrical and square. The wall surface (inner wall or outer wall) can be further optimized to add a thermal insulation layer, which can be composed of a vacuum interlayer or a thermal insulation coating. The salt crystallization separation cabin has a hole for the electrolyte pipeline to enter / exit, and is sealed to prevent the leakage of non-pure water. At the same time, a channel for the non-pure water solution to enter and a channel for the solid salt to be discharged are provided. In addition, the salt crystallization separation cabin also has an outlet for pure water vapor, which can be further connected to a condenser to condense and liquefy the water vapor for recycling.

[0038] The non-pure aqueous solution mass transfer unit used in the utility model can be any mass transfer device that can achieve two-phase liquid isolation but allow gas to pass, such as a commercially mature flat-plate membrane distillation reactor, a hollow fiber membrane distillation reactor, or any self-made device with two-phase independent mass transfer space isolated by a waterproof and breathable layer.

[0039] The waterproof and breathable layer in the non-pure aqueous solution mass transfer device used in the utility model can be a porous TPU film, PDMS, PTFE film or a porous waterproof and breathable mass transfer layer prepared by spraying, screen printing, and electrostatic adsorption of graphene, PVDF particles, and PTFE particles. The waterproof and breathable layer has a hydrophobic effect, allowing only water vapor to pass through, and not allowing liquid water to penetrate and pollute each other.

[0040] The electrolyte used in the utility model depends on the different electrolytic cells. If an alkaline electrolytic cell or an AEM electrolytic cell is used, an alkaline electrolyte such as a 20wt% to 40wt% KOH solution or a 20 to 30wt% NaOH solution can be used. If a PEM electrolytic cell is used, an acidic liquid electrolyte such as an H2SO4 solution, an H3PO4 solution, an HClO4 solution, etc. can be used.

[0041] The non-pure aqueous solution mentioned in the utility model includes all non-pure water resources such as seawater, salt lake water, chemical water, river water, lake water, wastewater, swamp water, domestic sewage, etc. Seawater can be used to produce hydrogen and extract sodium salt at the same time, and salt lake water can be used to produce hydrogen and extract lithium salt at the same time.

[0042] The technical process in the utility model can be fully automatically controlled by PID control and the like, thereby realizing full process automation of the electrolytic hydrogen production process.

[0043] The system of the utility model has the following advantages:

[0044] 1) It can realize the direct electrolysis of non-pure aqueous solutions to produce hydrogen, and the energy consumption of electrolysis is equivalent to that of industrial electrolysis of pure water, without the need for additional desalination / purification energy consumption, and the electrolysis effect is consistent with the electrolysis performance of commercial electrolyzers. Specifically, while producing hydrogen by electrolysis, the electrolyte enters the salt crystallization separation cabin to exchange heat with the non-pure aqueous solution, taking away the heat generated by the electrolysis. At the same time, the water in the salt crystallization separation cabin is continuously consumed, and the solution gradually becomes a saturated solution, and finally a solid salt with added value can be obtained. Non-pure aqueous solutions can be directly used to produce hydrogen and co-produce solid salt with added value, such as using salt lake water to produce hydrogen and extracting lithium salts, and using seawater to produce hydrogen and extracting sodium salts. In addition, by optimizing the salt crystallization separation cabin, applying an insulation layer on the surface or setting up a vacuum sandwich structure for overall insulation, the waste heat generated by the electrolysis process can be collected to increase the system's phase change mass transfer rate and accelerate the salt crystallization process, thereby accelerating the migration of water from the non-pure aqueous solution to the electrolyte, accelerating the water replenishment rate and the salt extraction rate. At the same time, the non-pure aqueous solution can generate water vapor when it is heated up, and pure water resources can be obtained after condensation and liquefaction for utilization.

[0045] 2) It can realize a dynamic and continuous process of hydrogen production using any aqueous solution without time and space differences, can realize energy conversion and stable storage of unstable renewable energy, and provide technical means for the construction of future energy systems. At the same time, it can co-produce pure water resources and solid salts in the hydrogen production process, realizing the resource and energy utilization of non-pure aqueous solutions.

[0046] 3) By utilizing the heat exchange between the non-pure aqueous solution and the electrolyte, on the one hand, the non-pure aqueous solution is heated up, the phase change mass transfer rate of the system is increased, and the replenishment rate of pure water is increased; on the other hand, the non-pure aqueous solution is directly used to cool the electrolyte, which can save the investment in additional equipment to cool the electrolyte, and has good benefits in the large-scale hydrogen production process; at the same time, after the accelerated migration of water, the concentration rate of the feed liquid is accelerated, which increases the salt precipitation rate.

[0047] 4) Commercial electrolyzers and electrolytes can be directly used, which greatly improves the conductivity and electrochemical performance of the electrolysis system and avoids the direct production of H from non-pure aqueous solutions. + and OH - The problem of low transmission efficiency at the anode and cathode is caused by low concentration.

[0048] 5) It enhances the imagination of traditional non-pure aqueous solution electrolysis hydrogen production. It can realize direct hydrogen production without the need for non-pure aqueous solution desalination / purification process, and can also co-produce solid salt and pure water with added value. There is no need to build a large-scale desalination plant or a dedicated solid recovery plant, which greatly reduces the cost of construction, operation, manpower, maintenance and other aspects.

[0049] 6) In the utility model, the water added to the electrolyte in the mass transfer device is impurity-free water, thus breaking through the bottleneck of direct non-pure aqueous solution hydrogen production being restricted by factors such as solution composition over time, climate, and human activities. At the same time, the system can be used for electrolytic hydrogen production in any non-pure water environment such as seawater, salt lake water, underground mine water, chemical water, river water, lake water, sludge, swamp, and river, greatly broadening the source range of hydrogen energy, and generating solid salt with added value for further recycling. In addition, the utility model breaks through the direct non-pure aqueous solution hydrogen production where chloride ions are oxidized to produce Cl2 or ClO - The bottleneck of corrosion and toxic substances is a green, non-toxic and environmentally friendly process system. This solution system does not contain impurity ions such as calcium ions and magnesium ions. There will be no calcium and magnesium precipitation during long-term operation, which reduces the cost of subsequent cleaning and maintenance.

[0050] 7) Internal self-circulation of electrolytes can be achieved without the need to add additional electrolytes and pure water.

[0051] 8) The excess heat generated by the electrolysis system is fully utilized to enhance its own mass transfer and co-produce solid salt and pure water, thus achieving efficient use of energy.

[0052] All devices, components and units in the utility model can use existing commercial mature objects, which greatly ensures the stability and feasibility of the system. Moreover, due to the maturity of the system, large-scale preparation can be easily and quickly realized.

[0053] The implementation effect verification of this utility model:

[0054] 1. Using LiCl as simulated salt lake water, 1L solution was concentrated from 0.07M to 2.92M, and after adding K2CO3 solution, high economic value Li2CO3 product and H2 were produced. The electrolysis system was at 400mA / cm 2 Under the current density, it can run stably for 200h. Figure 2 shown.

[0055] 2. Using chemical wastewater as feed liquid, the electrolysis system is at 250mA / cm 2 Under the current density, stable operation for 100h, such as Figure 3 As shown, while achieving hydrogen production, sodium sulfate and sodium chloride crystalline solids are produced.

[0056] It should be noted that within the scope of protection defined in the claims of the present utility model, the following embodiments can be combined and / or expanded or replaced in any logical way from the above specific implementation methods, such as disclosed technical principles, disclosed technical features or implicitly disclosed technical features.

[0057] Example 1

[0058] A non-pure aqueous solution hydrogen production and solid salt co-production system, comprising a non-pure aqueous solution hydrogen production subsystem and a salt crystallization separation subsystem, wherein the non-pure aqueous solution hydrogen production subsystem is connected to the salt crystallization separation subsystem; the salt crystallization separation subsystem comprises a salt crystallization separation cabin 17; a non-pure aqueous solution mass transferor 18 is arranged inside the salt crystallization separation cabin 17, a non-pure aqueous solution inlet 19 and a pure water vapor outlet 21 are arranged on the salt crystallization separation cabin 17, and the non-pure aqueous solution inlet 19 is connected to a first valve 20; a solid salt discharge outlet 24 is arranged on the solid-liquid separator 23, and a second valve 22 is arranged between the salt crystallization separation cabin 17 and the solid-liquid separator 23; the non-pure aqueous solution mass transferor 18 comprises non-pure aqueous solution mass transfer units A1~An, and a waterproof and breathable layer is attached to the surface of the non-pure aqueous solution mass transfer units A1~An.

[0059] Example 2

[0060] On the basis of Example 1, a heat-insulating layer is provided on the wall surface of the salt crystallization separation cabin 17 .

[0061] Example 3

[0062] On the basis of Example 1, it also includes a solid-liquid separator 23, and the solid-liquid separator 23 and the salt crystallization separation cabin 17 are connected through the second valve 22; when a batch of liquid feed is completely reacted, the next batch of non-pure aqueous solution is added through the non-pure aqueous solution inlet 19 and the first valve 20; the salt precipitation area at the bottom of the salt crystallization separation cabin 17 has a solid outlet channel, which is connected to the second valve 22, and enters the solid-liquid separator 23 by opening the second valve 22. After the water in the solid particles is removed in the solid-liquid separator 23, the solid salt product is obtained and discharged from the solid salt outlet 24; the electrolyte of pure water is obtained from the salt crystallization separation cabin 17, and is returned to the electrolyte storage tank of the non-pure aqueous solution hydrogen production subsystem for storage, while replenishing pure water for the electrolysis system and preparing for the next electrolysis.

[0063] Example 4

[0064] On the basis of Example 1, the structure of each mass transfer unit in the non-pure aqueous solution mass transfer units A1 to An is a plate type or a hollow fiber type.

[0065] Example 5

[0066] Based on Example 1, the non-pure aqueous solution includes any one of seawater, salt lake water, chemical water, river water, lake water, wastewater, swamp water and domestic sewage.

[0067] Example 6

[0068] Based on Example 1, the waterproof and breathable layer includes any one of a porous TPU membrane, a PDMS membrane, and a PTFE membrane.

[0069] Example 7

[0070] On the basis of Example 1, the waterproof and breathable layer includes a porous waterproof and breathable mass transfer layer prepared by using graphene, PVDF particles, and PTFE particles through spraying, screen printing, and electrostatic adsorption.

[0071] Example 8

[0072] On the basis of Example 2, the thermal insulation layer includes a vacuum sandwich structure or a thermal insulation coating directly coated on the wall surface of the salt crystal separation cabin 17 .

[0073] In addition to the above examples, those skilled in the art may obtain other embodiments based on the above disclosure or by using the knowledge or technology in the relevant field to make changes. The features of each embodiment may be interchangeable or replaced. The changes and modifications made by those skilled in the art do not depart from the spirit and scope of the present invention and should be within the scope of protection of the claims attached to the present invention.

Claims

1. A non-pure aqueous solution hydrogen production and solid salt co-production system, It is characterized in that The invention comprises a non-pure aqueous solution hydrogen production subsystem and a salt crystallization separation subsystem, wherein the non-pure aqueous solution hydrogen production subsystem is connected to the salt crystallization separation subsystem; the salt crystallization separation subsystem comprises a salt crystallization separation cabin (17); a non-pure aqueous solution mass transfer device (18) is arranged inside the salt crystallization separation cabin (17); a non-pure aqueous solution inlet (19) and a pure water vapor outlet (21) are arranged on the salt crystallization separation cabin (17); the non-pure aqueous solution inlet (19) is connected to a first valve (20); a solid salt discharge outlet (24) is arranged on the solid-liquid separator (23); a second valve (22) is arranged between the salt crystallization separation cabin (17) and the solid-liquid separator (23); the non-pure aqueous solution mass transfer device (18) comprises non-pure aqueous solution mass transfer units A1-An, and a waterproof and breathable layer is attached to the surface of the non-pure aqueous solution mass transfer units A1-An.

2. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that A heat-insulating layer is provided on the wall surface of the salt crystallization separation chamber (17).

3. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that The invention also comprises a solid-liquid separator (23), wherein the solid-liquid separator (23) and the salt crystallization separation chamber (17) are connected via the second valve (22); when a batch of liquid feed is completely reacted, the next batch of non-pure aqueous solution is added via the non-pure aqueous solution inlet (19) and the first valve (20); the salt precipitation area at the bottom of the salt crystallization separation chamber (17) has a solid outlet channel, wherein the channel is connected to the second valve (22), and the solid feed enters the solid-liquid separator (23) by opening the second valve (22), and after the water in the solid particles is removed in the solid-liquid separator (23), a solid salt product is obtained and discharged from the solid salt outlet (24); the electrolyte of pure water is obtained from the salt crystallization separation chamber (17), and is returned to the electrolyte storage tank of the non-pure aqueous solution hydrogen production subsystem for storage, so as to replenish the electrolysis system with pure water and prepare for the next electrolysis.

4. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that The structure of each of the non-pure aqueous solution mass transfer units A1 to An is a plate type or a hollow fiber type.

5. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that The non-pure aqueous solution includes any one of sea water, salt lake water, chemical water, river water, lake water, waste water, swamp water and domestic sewage.

6. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that The waterproof and breathable layer includes any one of a porous TPU film, a PDMS film, and a PTFE film.

7. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 1, It is characterized in that The waterproof and breathable layer comprises a porous waterproof and breathable mass transfer layer which is prepared by using graphene, PVDF particles, and PTFE particles through spraying, screen printing, and electrostatic adsorption.

8. The non-pure aqueous solution hydrogen production and solid salt co-production system according to claim 2, It is characterized in that The thermal insulation layer comprises a vacuum sandwich structure or a thermal insulation coating directly coated on the wall surface of the salt crystal separation cabin (17).

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