Method for treating and recycling resources of hydrogen energy new material production wastewater

Abstract

The application discloses a hydrogen energy new material production wastewater treatment and resource regeneration method, which comprises the following steps: (1) adding an alkaline sodium salt solution into hydrogen energy new material production wastewater, fully stirring and reacting to regenerate production raw materials and intermediates and to precipitate, and filtering the filtrate into a crystallizer; (2) recycling the wastewater in a cooling device and the crystallizer by using an axial flow pump, and separating crystals and liquid in the crystallizer after cooling; (3) pumping the distillation tower kettle liquid into an evaporator; separating organic steam and ammonia gas from the top of the distillation tower, and obtaining organic condensate and high-purity ammonia gas after condensation; (4) respectively evaporating and dehydrating the sodium sulfate solution and the distillation tower kettle liquid, and separating evaporated clear liquid, evaporated thick liquid, crude salt products sodium sulfate and sodium chloride; and (5) preparing refined salt products sodium sulfate and sodium chloride by using an oxygen-rich gasification coupling catalytic combustion process. The application has high treatment efficiency, low operation cost, high utilization rate of intermediates, realizes ammonia and salt recovery, and thus additional value is generated.

Description

Technical Field

[0001] This invention relates to the field of wastewater treatment technology, specifically to a method for treating and regenerating wastewater from the production of hydrogen energy new materials. Background Technology

[0002] Hydrogen energy is a clean secondary energy source, and the research and development of new materials technologies is a key focus of the industry. However, wastewater from the production of hydrogen energy new materials is characterized by high ammonia nitrogen concentration (>3000 mg / L), high salt content (total sodium sulfate and sodium chloride >10%), and high organic matter concentration (>10000 mg / L, calculated as COD), making it a typical high-salt, high-ammonia-nitrogen, and high-organic-matter wastewater, which is extremely difficult to treat. To avoid the adverse environmental impacts of the development of the hydrogen energy industry, how to economically and efficiently treat wastewater from the production of hydrogen energy new materials is a pressing problem that needs to be solved in the field of wastewater treatment.

[0003] This type of wastewater is difficult to treat directly using biological processes. Currently, traditional treatment processes mainly include incineration (including direct incineration of waste liquid and incineration after evaporation and solidification) and advanced oxidation methods, which promote the decomposition of organic matter through strong oxidation. However, the problem with these methods is that:

[0004] First, the incineration temperature is higher than the melting point of salt, and the molten salt has a strong corrosive effect on refractory materials, resulting in a short furnace wall life and high equipment investment. In addition, the incineration produces a large volume of flue gas with a high concentration of acidic gases such as nitrogen oxides, and the flue gas treatment process is complex (quenching, desulfurization and denitrification, etc.), resulting in high operating costs.

[0005] Secondly, in order to achieve complete mineralization of organic pollutants, advanced oxidation methods (such as Fenton oxidation, electrocatalytic oxidation, wet oxidation, etc.) require a large amount of reagents, consume a lot of energy, and require high investment in some equipment.

[0006] In summary, although the above methods are universally applicable and effective, the high equipment investment and operating costs impose a significant economic burden on enterprises. To achieve green development and reduce costs while increasing efficiency, environmental governance should first consider recycling and creating high-value-added resources from waste, and then adopt targeted, efficient, and low-cost treatment technologies. This requires the cross-disciplinary integration of multiple fields, and therefore, the development of multi-technology coupled processes is a key focus of current environmental protection development. Summary of the Invention

[0007] The technical problem to be solved by the present invention is to provide a method for treating wastewater from the production of hydrogen energy new materials with high treatment efficiency and low operating cost, which can effectively remove pollutants from the water and recycle valuable resources in the water.

[0008] To address the aforementioned problems, the present invention provides the following technical solution: A method for treating and regenerating wastewater from the production of hydrogen energy new materials, comprising the following steps:

[0009] (1) Add alkaline sodium salt solution to the wastewater from the production of hydrogen energy new materials, stir and react thoroughly to regenerate and precipitate the raw materials and intermediates, and after solid-liquid separation, the slurry is recycled to the production workshop for reuse, and the filtrate enters the crystallizer.

[0010] (2) An axial flow pump is used to circulate the filtrate between the crystallizer and the cooler. The cooled wastewater crystallizes and separates solid and liquid in the crystallizer to recover Glauber's salt crystals and cooling residue.

[0011] (3) Cooling residue is separated by distillation technology. The bottom liquid of the distillation column is pumped into the evaporation system. Organic vapor and ammonia are separated from the top of the distillation column. After condensation, organic condensate and high-purity ammonia are obtained. The organic condensate is recycled to the production workshop for reuse. Ammonia is absorbed by water to produce industrial ammonia water for reuse.

[0012] (4) The Glauber's salt crystals and the bottom liquid of the distillation column are respectively introduced into the evaporation system to remove water, and the clear evaporation liquid, the concentrated evaporation liquid, the crude salt products sodium sulfate and sodium chloride are separated. The clear evaporation liquid is reused as production water or discharged after biological treatment.

[0013] (5) The crude salt products sodium sulfate and sodium chloride are produced by oxygen-enriched oxidation coupled catalytic combustion. After the reaction is completed, refined salt products sodium sulfate and sodium chloride are obtained and reused as industrial salt.

[0014] Furthermore, in step (1), the salt content of the wastewater from the production of the new hydrogen energy materials is ≥10% (w / w), the COD is 10000~80000mg / L, and the ammonia nitrogen concentration is ≥3000mg / L.

[0015] Further, in step (1), the alkaline sodium salt solution is one or a combination of sodium hydroxide solution, sodium carbonate solution and sodium bicarbonate solution.

[0016] Further, in step (1), when the alkaline sodium salt solution is sodium hydroxide, the mass ratio to organic matter (calculated as COD) is 0.4 to 2.0; when the alkaline sodium salt solution is sodium carbonate, the mass ratio to organic matter (calculated as COD) is 0.6 to 2.7; when the alkaline sodium salt solution is sodium bicarbonate, the mass ratio to organic matter (calculated as COD) is 1.0 to 4.5; and the reaction time is 0.25 to 3.0 h.

[0017] Furthermore, in step (2), the temperature of the cooled wastewater in the cooler is controlled to be -5 to 10°C.

[0018] Furthermore, in step (3), the pressure at the top of the distillation column is ≤0.3MPaG; the organic condensate output is 0.5-3.0% (w / w) of the treated water volume; and the ammonia water is prepared by spray absorption or falling film absorption.

[0019] Furthermore, in step (4), the reuse rate of the evaporated clear liquid is 70-95% (w / w).

[0020] Further, in step (5), oxygen or a mixture of oxygen and inert gas is bubbled in, with the mass ratio of oxygen to organic matter (calculated as COD) being 1.0 to 4.0.

[0021] Furthermore, in step (5), the oxygen enrichment temperature is 400–750°C and the time is 1.0–4.0 h.

[0022] Furthermore, in step (5), the flue gas temperature of the catalytic combustion device is 260-400°C, the catalyst support is a porous material, and the effective component of the catalyst is one or a combination of transition metals and their oxides.

[0023] Beneficial effects: This invention has high processing efficiency, low operating cost, and high utilization rate of raw materials and intermediates; it can realize the recovery of ammonia and salt, thereby generating added value; the total amount of waste gas is small, the amount of nitrogen oxides generated is greatly reduced, and it is easy to treat.

[0024] Compared with the prior art, the positive and progressive effects of the present invention are as follows:

[0025] (1) The use of alkaline sodium salt solution to regenerate raw materials and intermediates improves the utilization rate of raw materials and is conducive to oxygen-enriched chemical coupling catalytic combustion reaction.

[0026] (2) The distillation separation technology further improves the utilization rate of raw materials and the purity of ammonia. The quality of ammonia water reaches the industrial ammonia water standard, with impurity content <0.1%. At the same time, it is conducive to improving the quality of evaporation liquid and realizing wastewater reuse.

[0027] (3) In the oxygen-enriched chemical coupled catalytic combustion reaction process, the oxygen-enriched atmosphere can significantly improve the quality of salt, reaching industrial-grade standards, and can be further utilized. Attached Figure Description

[0028] Figure 1 The process flow diagram of the method for treating wastewater and regenerating resources in the production of hydrogen energy new materials provided by the present invention. Detailed Implementation

[0029] The following will further explain the concept, specific structure, and technical effects of the present invention in conjunction with the accompanying drawings, so as to fully understand the purpose, features, and effects of the present invention.

[0030] Example 1

[0031] The wastewater from the production of a certain hydrogen energy new material has a salt content of 23.1% (w / w), a COD of 21800 mg / L, and an ammonia nitrogen concentration of 9400 mg / L.

[0032] The present invention provides a method for treating and regenerating wastewater from the production of hydrogen energy novel materials, comprising the following steps:

[0033] (1) Add sodium hydroxide solution to the wastewater from the production of hydrogen energy new materials. The ratio of sodium hydroxide to organic matter (calculated as COD) is 2.0, and the reaction time is 1.0 h. Stir the reaction thoroughly to regenerate and precipitate the raw materials and intermediates. After solid-liquid separation, the slurry mass is 3.1% of the treated water volume. Its quality meets the production requirements and is recycled to the production workshop for reuse. The filtrate enters the crystallizer.

[0034] (2) The wastewater is circulated in the cooler and crystallizer by axial flow pump. The cooled wastewater crystallizes and separates solid and liquid in the crystallizer. The temperature of the cooler and crystallizer is 1±2℃. Glauber's salt crystals are obtained, dissolved and prepared into sodium sulfate solution and then enter the evaporation system. The cooling residue enters the distillation tower.

[0035] (3) The cooling residue is separated by distillation technology. The bottom liquid of the distillation column is pumped into the evaporation system. Organic vapor and ammonia are separated from the top of the distillation column. After condensation, organic condensate and high-purity ammonia are obtained. The organic solution is recycled to the production workshop for reuse. The ammonia is absorbed by water to produce industrial ammonia water for reuse. The pressure at the top of the distillation column is 0.05 MPaG. The amount of organic condensate produced is 1.8% (w / w) of the treated water volume. The ammonia is prepared by falling film absorption. The concentration of the ammonia water is 21.1%, the content of organic impurities is 0.06%, and the ammonia recovery rate reaches 78%.

[0036] (4) The sodium sulfate solution and the bottom liquid of the distillation column are dehydrated by evaporation to separate the clear evaporator, the concentrated evaporator, and the crude salt products sodium sulfate and sodium chloride. The clear evaporator is reused as production makeup water or discharged after biological treatment. The COD of the clear evaporator is 668 mg / L and the ammonia nitrogen is 23 mg / L, which meets the production requirements. The clear evaporator is reused in the production system at a rate of 95% (w / w), and the remaining clear evaporator is discharged after biological treatment to meet the standards. The obtained crude sodium sulfate and sodium chloride are transported to the oxygen-enriched oxidation unit.

[0037] (5) The crude salt products sodium sulfate and sodium chloride are treated by oxygen-enriched oxidation coupled catalytic combustion. After the reaction is completed, refined salt products sodium sulfate and sodium chloride are obtained and reused as industrial salt.

[0038] The oxygen-enriched oxidation temperatures for crude sodium sulfate and sodium chloride were 700℃ and 650℃, respectively, and the reaction time was 1.5h.

[0039] The introduced gas is air, with an oxygen to organic matter (COD) mass ratio of 1.3. The refined sodium sulfate has good whiteness, a purity of 98.1%, and a water-insoluble content of 0.23%, meeting the Class III standard for industrial anhydrous sodium sulfate. The refined sodium chloride has good whiteness, a purity of 97.8%, and a water-insoluble content of 0.19%, meeting the Class II standard for industrial sodium chloride. The flue gas entering the catalytic combustion unit has a temperature of approximately 300–330°C, and the catalyst is a palladium- and platinum-impregnated porous material. The flue gas exiting the unit can meet emission standards after simple treatment (cooling and alkaline washing).

[0040] Example 2

[0041] Example 2 presents the operational results of Example 1 under different operating parameters. The difference lies in that the alkaline sodium salt solution is a sodium carbonate solution, the ratio of sodium carbonate to organic matter (calculated as COD) is 2.7, and the reaction time is 1.5 hours. After filtration, the slurry mass is 4.3% of the treated water volume, and its quality meets production requirements. It can be entirely reused in the front-end production system, while the filtrate enters the back-end treatment unit. The device operates well and stably.

[0042] Example 3

[0043] Example 3 presents the operational results of Example 1 under different operating parameters. The difference lies in that the alkaline sodium salt solution is a sodium bicarbonate solution, the ratio of sodium bicarbonate to organic matter (calculated as COD) is 4.3, and the reaction time is 3.0 h. After filtration, the slurry mass is 0.5% of the treated water volume, and its quality still meets production requirements, allowing it to be reused in the front-end production system. The filtrate enters the back-end treatment unit, and the device operates well and stably.

[0044] Example 4

[0045] Example 4 presents the operational results of Example 1 under different operating parameters. The difference lies in that the pressure at the top of the distillation column is 0.3 MPaG, and the amount of organic condensate collected is 0.5% (w / w) of the treated water volume. At this time, the concentration of the ammonia water obtained is 20.4%, the organic impurity content is 0.04%, and the ammonia recovery rate is 57%.

[0046] Example 5

[0047] The difference between Example 5 and Example 1 lies in the fluctuation of the water quality of the treated object. The water quality indicators are: salt content 18.5%, COD 78000 mg / L, and ammonia nitrogen 3140 mg / L. During the treatment process, the oxygen to organic matter (based on COD) mass ratio in the oxygen-enriched process is 4.0, and the oxygen-enriched temperatures for sodium sulfate and sodium chloride are 750℃ and 670℃, respectively, with other process conditions remaining consistent. The obtained slurry can also be reused in the front-end production system; the recovered ammonia concentration is 20.7%, and the organic impurity content is 0.09%; the amount of organic condensate extracted is 3.0% (w / w) of the treated water volume; the COD of the evaporated clear liquid is 2370 mg / L, and the ammonia nitrogen is 9 mg / L, with a reuse rate of 81%; the refined sodium sulfate and sodium chloride have good whiteness, both meeting industrial-grade standards.

[0048] Example 6

[0049] The wastewater from the production of a certain hydrogen energy new material has a salt content of 10.7%, a COD of 57,000 mg / L, and an ammonia nitrogen content of 10,800 mg / L.

[0050] (1) Add a mixed solution of sodium hydroxide and sodium carbonate, with a sodium hydroxide to organic matter (COD) ratio of 0.4 and a sodium carbonate to organic matter (COD) ratio of 0.7, and stir for 0.3 hours. After filtration, the slurry mass is 3.2% of the treated water volume, and its quality meets the production requirements. It is recycled to the front-end production system, and the filtrate enters the crystallizer.

[0051] (2) The temperature of the cooler and crystallizer is controlled at 6±2℃ to obtain Glauber's salt crystals, which are then dissolved and prepared into sodium sulfate solution before entering the evaporator; the cooling residue enters the distillation column.

[0052] (3) The pressure at the top of the distillation column is controlled at 0.05 MPaG, and the organic condensate is collected at 2.0% (w / w) of the treated water volume; the bottom liquid of the distillation column is pumped into the evaporator. Ammonia is prepared by falling film absorption, and the concentration of the ammonia water obtained is 21.6%, the content of organic impurities is 0.08%, and the ammonia recovery rate reaches 83%.

[0053] (4) The sodium sulfate solution and the bottom liquid of the distillation column were dehydrated by evaporation. The COD of the clear liquid was 1955 mg / L and the ammonia nitrogen was 88 mg / L, which met the production requirements. 74% of the clear liquid was recycled to the production system; the crude sodium sulfate and sodium chloride obtained were transported to the oxygen-enriched oxidation unit.

[0054] (5) The oxygen-enriched oxidation temperatures of crude sodium sulfate and sodium chloride are 480℃ and 620℃, respectively, with a reaction time of 4.0h. The gas blown in is a mixture of pure oxygen and air, with a mass ratio of oxygen to organic matter (calculated as COD) of 2.5. The refined sodium sulfate has better whiteness, a purity of 97.8%, and a water-insoluble content of 0.21%, meeting the Class III standard for industrial anhydrous sodium sulfate; the refined sodium chloride has better whiteness, a purity of 97.4%, and a water-insoluble content of 0.18%, meeting the Class II standard for industrial sodium chloride. The flue gas temperature entering the catalytic combustion device is 260~310℃, and the catalyst is a combination of nickel, cobalt oxide, manganese oxide, and copper oxide complex; the flue gas at the device outlet can meet the emission standards after simple treatment (cooling and alkaline washing).

[0055] Example 7

[0056] Example 7 presents the operational results of Example 6 under different operating parameters. The difference lies in that the temperature of the cooler and crystallizer is controlled at -2±2℃, which yields more sodium sulfate crystals, and the refined sodium sulfate product also meets the Class III standard for industrial anhydrous sodium sulfate.

[0057] Example 8

[0058] Example 8 presents the operational results of Example 6 under different operating parameters. The difference lies in that the alkaline sodium salt solution is a mixed solution of sodium hydroxide and sodium bicarbonate, with a sodium hydroxide to organic matter (COD) ratio of 0.4 and a sodium bicarbonate to organic matter (COD) ratio of 1.2. After filtration, the slurry mass is 1.3% of the treated water volume, meeting production requirements and can be entirely reused in the front-end production system. The filtrate enters the back-end treatment unit, and the device operates well and stably.

[0059] Example 9

[0060] The wastewater from the production of a certain hydrogen energy new material has a salt content of 21.4%, a COD of 13900 mg / L, and an ammonia nitrogen content of 8700 mg / L.

[0061] (1) Add sodium hydroxide solution to it, the ratio of sodium hydroxide to organic matter (calculated as COD) is 0.8, and the stirring reaction time is 1.2h. After filtration, the slurry mass is 0.7% of the treated water volume, and its quality meets the production requirements. It is recycled to the front-end production system, and the filtrate enters the crystallizer.

[0062] (2) The temperature of the cooler and crystallizer is controlled at 0±2℃ to obtain Glauber's salt crystals, which are then dissolved and prepared into sodium sulfate solution before entering the evaporator; the cooling residue enters the distillation column.

[0063] (3) The pressure at the top of the distillation column is controlled at 0.1 MPaG, and the amount of organic condensate collected is 0.7% (w / w) of the treated water volume; the bottom liquid of the distillation column is pumped into the evaporator. Ammonia is prepared by spray absorption, and the concentration of the ammonia water obtained is 15.7%, the content of organic impurities is 0.04%, and the ammonia recovery rate reaches 71%.

[0064] (4) The sodium sulfate solution and the bottom liquid of the distillation column were dehydrated by evaporation. The COD of the clear evaporation liquid was 320 mg / L and the ammonia nitrogen was 24 mg / L, which met the production requirements. 95% of the clear evaporation liquid was recycled to the production system; the crude sodium sulfate and sodium chloride obtained were transported to the oxygen-enriched oxidation unit.

[0065] (5) The oxygen-enriched oxidation temperatures of crude sodium sulfate and sodium chloride are 430℃ and 650℃, respectively, with a reaction time of 2.0h. The introduced gas is air, in which the mass ratio of oxygen to organic matter (calculated as COD) is 1.1. The refined sodium sulfate has better whiteness, a purity of 98.2%, and a water-insoluble content of 0.09%, meeting the Class III standard for industrial anhydrous sodium sulfate; the refined sodium chloride has better whiteness, a purity of 98.1%, and a water-insoluble content of 0.11%, meeting the Class II standard for industrial sodium chloride. The flue gas temperature entering the catalytic combustion device is 320-400℃, and the catalyst is a combination of nickel, cobalt oxide, manganese oxide, and copper oxide complex; the flue gas at the device outlet can meet the emission standards after simple treatment (cooling and alkaline washing).

[0066] Comparative Example 1

[0067] This comparative example shows the results of Example 1 under different operating parameters. The difference is that after adding sodium hydroxide solution, the stirring reaction time was 0.1 h.

[0068] After stirring and reacting, the organic flocs become viscous, significantly reducing the solid-liquid separation efficiency. Furthermore, the flocs easily adhere to the surface of the filter membrane / filter cloth, making slurry collection difficult. Simultaneously, flaky organic flocs appear during cooling and crystallization, and the Glauber's salt crystals contain a large amount of organic matter, resulting in a low evaporation liquor reuse rate (COD reaches 6000 mg / L).

[0069] Comparative Example 2

[0070] This comparative example shows the operating results of Example 1 under different operating parameters. The difference is that the ratio of sodium hydroxide to organic matter (calculated as COD) is 0.2.

[0071] Under these conditions, the amount of organic condensate collected from the top of the distillation column is 0.9% (w / w) of the treated water volume; and the purified sodium chloride has poor whiteness, is light pink, and has a low purity of only 94.2%.

[0072] Comparative Example 3

[0073] This comparative example shows the operating results of Example 1 under different operating parameters. The difference is that the mass ratio of oxygen to organic matter (calculated as COD) in the oxygen-enriched device is 0.8.

[0074] The refined sodium sulfate has poor whiteness, appearing pale gray, and contains 0.37% water-insoluble matter; the refined sodium chloride has poor whiteness, appearing gray, and contains 0.52% water-insoluble matter.

[0075] Comparative Example 4

[0076] This comparative example shows the operating results of Example 6 under different operating parameters. The difference is that the pressure at the top of the distillation column is 0.35 MPaG.

[0077] Under these conditions, the amount of organic condensate extracted is 1.8% (w / w) of the treated water volume. The condensate contains a large amount of ammonia, resulting in a low amount of ammonia entering the absorption unit and an ammonia recovery rate of <40%.

[0078] The preferred embodiments of the present invention have been described in detail above. It should be understood that those skilled in the art can make numerous modifications and variations based on the concept of the present invention without creative effort. Therefore, all technical solutions that can be obtained by those skilled in the art based on the concept of the present invention through logical analysis, reasoning, or limited experimentation on the basis of existing technology should be within the scope of protection defined by the claims.

Claims

1. A method for treating and regenerating wastewater from the production of hydrogen energy new materials, characterized in that... Includes the following steps: (1) Add alkaline sodium salt solution to the wastewater from the production of hydrogen energy new materials, stir and react thoroughly to regenerate and precipitate the raw materials and intermediates, and after solid-liquid separation, the slurry is recycled to the production workshop for reuse, and the filtrate enters the crystallizer. (2) An axial flow pump is used to circulate the filtrate between the crystallizer and the cooler. The cooled wastewater crystallizes and separates solid and liquid in the crystallizer to recover Glauber's salt crystals and cooling residue. (3) Cooling residue is separated by distillation technology. The bottom liquid of the distillation column is pumped into the evaporation system. Organic vapor and ammonia are separated from the top of the distillation column. After condensation, organic condensate and high-purity ammonia are obtained. The organic condensate is recycled to the production workshop for reuse. Ammonia is absorbed by water to produce industrial ammonia water for reuse. (4) The Glauber's salt crystals and the bottom liquid of the distillation column are respectively introduced into the evaporation system to remove water, and the clear evaporation liquid, the concentrated evaporation liquid, the crude salt products sodium sulfate and sodium chloride are separated. The clear evaporation liquid is reused as production water or discharged after biological treatment. (5) The crude salt products sodium sulfate and sodium chloride are produced by oxygen-enriched oxidation coupled catalytic combustion. After the reaction is completed, refined salt products sodium sulfate and sodium chloride are obtained and reused as industrial salt.

2. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (1), the salt content of the wastewater from the production of the new hydrogen energy materials is ≥10% (w / w), the COD is 10000~80000mg / L, and the ammonia nitrogen concentration is ≥3000mg / L.

3. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (1), the alkaline sodium salt solution is one or a combination of sodium hydroxide solution, sodium carbonate solution and sodium bicarbonate solution.

4. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 2, characterized in that: In step (1), when the alkaline sodium salt solution is sodium hydroxide, the mass ratio of sodium hydroxide to organic matter (calculated as COD) is 0.4 to 2.0; when the alkaline sodium salt solution is sodium carbonate, the mass ratio of sodium carbonate to organic matter (calculated as COD) is 0.6 to 2.7; when the alkaline sodium salt solution is sodium bicarbonate, the mass ratio of sodium carbonate to organic matter (calculated as COD) is 1.0 to 4.5; and the reaction time is 0.25 to 3.0 h.

5. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (2), the temperature of the cooled wastewater in the cooler is controlled to be -5 to 10°C.

6. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (3), the pressure at the top of the distillation column is ≤0.3MPaG; the organic condensate output is 0.5 to 3.0% (w / w) of the treated water volume; and the ammonia water is prepared by spray absorption or falling film absorption.

7. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (4), the recycling rate of the evaporated liquid is 70-95% (w / w).

8. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 1, characterized in that: In step (5), oxygen or a mixture of oxygen and inert gas is bubbled in, with the mass ratio of oxygen to organic matter (calculated as COD) being 1.0 to 4.

0.

9. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 8, characterized in that: In step (5), the oxygen enrichment temperature is 400-750℃ and the time is 1.0-4.0h.

10. The method for treating and regenerating wastewater from hydrogen energy new material production according to claim 9, characterized in that: In step (5), the flue gas temperature of the catalytic combustion device is 260-400°C, the catalyst support is a porous material, and the effective component of the catalyst is one or a combination of transition metals and their oxides.

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