CN115818808A - Method for treating waste water generated in production of new hydrogen energy material and regenerating resources - Google Patents

Abstract

The invention relates to a method for treating waste water generated in the production of new hydrogen energy materials and regenerating resources, which comprises the following steps: (1) Adding an alkaline sodium salt solution into the wastewater generated in the production of the new hydrogen energy material, fully stirring and reacting to regenerate and separate out production raw materials and intermediates, and feeding the filtrate into a crystallizer; (2) Pumping by an axial flow pump to enable the wastewater to circulate in a cooler and a crystallizer, and crystallizing and carrying out solid-liquid separation on the cooled wastewater in the crystallizer; (3) pumping the rectifying tower bottom liquid into an evaporator; separating organic matter steam and ammonia gas from the top of the rectifying tower, and condensing to obtain organic condensate and high-purity ammonia gas; (4) Evaporating and dehydrating the sodium sulfate solution and the distillation tower bottom liquid respectively to separate an evaporated clear liquid, an evaporated concentrated liquid, and crude salt products, namely sodium sulfate and sodium chloride; (5) Refined salt products of sodium sulfate and sodium chloride are prepared by adopting an oxygen-enriched gasification coupled catalytic combustion process. The invention has high treatment efficiency, low operation cost and high utilization rate of the intermediate, and realizes the recovery of ammonia and salt, thereby generating additional value.

Description

A kind of hydrogen energy new material production wastewater treatment and resource regeneration method

technical field

The invention relates to the technical field of wastewater treatment, in particular to a method for wastewater treatment and resource regeneration in the production of new hydrogen energy materials.

Background technique

Hydrogen energy is a clean secondary energy source, among which, the R&D and manufacturing of new material technology is also the focus of industry development. However, the waste water from the production of new hydrogen energy materials has the characteristics of high ammonia nitrogen concentration (>3000mg/L), high salt content (the sum of sodium sulfate and sodium chloride>10%), and high organic matter concentration (>10000mg/L, calculated as COD) , which is a typical high-salt, high-ammonia-nitrogen, and high-organic matter wastewater, which is extremely difficult to treat. In order to avoid the adverse impact of the development of the hydrogen energy industry on the environment, how to economically and efficiently treat the wastewater produced by new hydrogen energy materials is an urgent problem in the field of wastewater treatment.

It is difficult to directly adopt biological treatment process for this kind of wastewater. Nowadays, the traditional treatment process mainly includes incineration method (including direct incineration of waste liquid, incineration after evaporation and solidification) and advanced oxidation method, which promotes the decomposition of organic matter through strong oxidation, but the problem is:

First of all, the incineration temperature is higher than the melting point of salt, and the molten salt has a strong corrosive effect on refractory materials, the life of the furnace wall is short, and the equipment investment is high; moreover, the amount of flue gas produced by incineration is large, and the concentration of acid gases such as nitrogen oxides is high. The gas treatment process is complex (quick cooling, desulfurization and denitrification, etc.), and the operating cost is high;

Secondly, in order to realize the complete mineralization of organic pollutants, advanced oxidation methods (such as Fenton, electrocatalytic oxidation, wet oxidation, etc.) require many chemicals, high energy consumption, and high investment in certain equipment.

In general, although the above methods are universal and effective, the high equipment investment and operating costs have caused a huge economic burden on the enterprise. In order to achieve green development and cost reduction and efficiency increase, the process of environmental protection governance should first consider recycling from waste and creating high value-added resources, and then adopt targeted high-efficiency and low-cost treatment technologies, which requires cross-integration of multiple disciplines , and therefore, the development of multi-technology coupling process is the focus of the current development in the field of environmental protection.

Contents of the invention

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

In order to solve the above problems, the present invention provides the following technical solutions: a method for treating waste water and resource regeneration of hydrogen energy new material production according to the present invention, comprising the following steps:

(1) Add alkaline sodium salt solution to the production wastewater of hydrogen energy new materials, fully stir the reaction to regenerate and precipitate the production raw materials and intermediates, and circulate the slurry to the production workshop for reuse after solid-liquid separation, and the filtrate enters the crystallizer;

(2) The filtrate is internally circulated between the crystallizer and the cooler by adopting axial flow pump suction, and the cooled waste water is crystallized and solid-liquid separated in the crystallizer, and then reclaimed to obtain mirabilite crystals and cooling raffinate;

(3) Rectification and separation technology is adopted for the cooling raffinate, and the liquid in the rectification tower is pumped into the evaporation system; organic vapor and ammonia gas are separated from the top of the rectification tower, and organic condensate and high-purity ammonia gas are obtained after condensation. Organic condensate Circulate to the production workshop for reuse, ammonia gas is absorbed by water to make industrial ammonia water for reuse;

(4) Glauber's salt crystals and rectification tower still liquid enter the evaporation system to remove water respectively, separate the evaporated clear liquid, evaporated concentrated liquid, and crude salt products sodium sulfate and sodium chloride, and reuse the evaporated clear liquid as water replenishment for production or use efflux after biological treatment;

(5) The crude salt products sodium sulfate and sodium chloride are catalyzed and combusted by oxygen-enriched oxidation. After the reaction, the refined salt products sodium sulfate and sodium chloride are produced, which can be reused as industrial salt.

Further, in step (1), the salt content of the hydrogen energy new material production wastewater is ≥10% (w/w), the COD is 10000-80000 mg/L, and the ammonia nitrogen concentration is ≥3000 mg/L.

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.

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

Further, in step (2), the temperature of the wastewater after cooling in the cooler is controlled at -5-10°C.

Further, in step (3), the pressure at the top of the rectifying tower is less than or equal to 0.3MPaG; the output of organic condensate is 0.5-3.0% (w/w) of the treated water; the ammonia water is prepared by spraying absorption or reducing Membrane absorption.

Furthermore, in step (4), the recycling ratio of the evaporated clear liquid is 70-95% (w/w).

Further, in step (5), oxygen or a mixture of oxygen and inert gas is blown in, and the mass ratio of oxygen to organic matter (calculated as COD) is 1.0-4.0.

Further, in step (5), the temperature of the oxygen-enriched oxidation is 400-750° C., and the time is 1.0-4.0 h.

Furthermore, in step (5), the flue gas temperature of the catalytic combustion device is 260-400°C, the catalyst carrier is a porous material, and the active component of the catalyst is one or more of transition metals and their oxides The combination.

Beneficial effects: the present invention has high treatment efficiency, low operating cost, high utilization rate of production raw materials and intermediates; it can realize recovery of ammonia and salt, thereby generating added value; the total amount of waste gas is small, the amount of nitrogen oxides is greatly reduced, and it is easy to handle .

Compared with the prior art, the positive progress effect of the present invention is:

(1) Alkaline sodium salt solution is used to realize the regeneration of production raw materials and intermediates, which improves the utilization rate of raw materials and is beneficial to the coupled catalytic combustion reaction of oxygen-enriched oxidation.

(2) The rectification separation technology further improves the utilization rate of raw materials and the purity of ammonia gas. The quality of ammonia water reaches the industrial ammonia water standard, and the impurity content is less than 0.1%. At the same time, it is beneficial to improve the quality of evaporated clear liquid and realize the reuse of wastewater.

(3) In the oxygen-enriched oxidation coupling catalytic combustion reaction process, the oxygen-enriched atmosphere can significantly improve the salt quality, reaching industrial-grade standards, and can be further utilized.

Description of drawings

Fig. 1 is a process flow chart of the method for treating waste water and regenerating resources from the production of new hydrogen energy materials provided by the present invention.

Detailed ways

The idea, specific structure and technical effects of the present invention will be further described below in conjunction with the accompanying drawings, so as to fully understand the purpose, features and effects of the present invention.

Example 1

The salt content of wastewater produced by a new hydrogen energy material is 23.1% (w/w), the COD is 21800mg/L, and the ammonia nitrogen concentration is 9400mg/L.

A hydrogen energy new material production wastewater treatment and resource regeneration method of the present invention comprises the following steps:

(1) Add sodium hydroxide solution to the waste water produced by new hydrogen energy materials, the ratio of sodium hydroxide to organic matter (calculated as COD) is 2.0, and the reaction time is 1.0 h. Fully stir the reaction to regenerate and precipitate the production raw materials and intermediates. After solid-liquid separation, the quality of the slurry is 3.1% of the treated water, and its quality meets the production requirements. It is recycled to the production workshop for reuse, and the filtrate enters the crystallizer;

(2) Axial flow pump is used to circulate the waste water in the cooler and the crystallizer, and the cooled waste water is crystallized and separated from solid and liquid in the crystallizer; the temperature of the cooler and the crystallizer is 1±2°C to obtain Glauber’s salt The crystals are dissolved and prepared into sodium sulfate solution and enter the evaporation system; the cooled raffinate enters the rectification tower.

(3) Rectification and separation technology is adopted for the cooling raffinate, and the liquid in the rectification tower is pumped into the evaporation system; the organic vapor and ammonia gas are separated from the top of the rectification tower, and organic condensate and high-purity ammonia gas are obtained after condensation, and the organic solution is circulated To the production workshop for reuse, ammonia gas is absorbed by water to make industrial ammonia water for reuse; the pressure at the top of the rectification tower is 0.05MPaG; the output of organic condensate is 1.8% (w/w) of the treated water; ammonia gas preparation method For falling film absorption, the concentration of ammonia water is 21.1%, the content of organic impurities is 0.06%, and the recovery rate of ammonia reaches 78%.

(4) The sodium sulfate solution and the liquid in the rectification column are dehydrated by evaporation respectively, and the evaporated clear liquid, the evaporated concentrated liquid, and the crude salt products sodium sulfate and sodium chloride are separated; the evaporated clear liquid is reused as production water replenishment or biological treatment back row. The COD of the evaporated supernatant is 668mg/L, and the ammonia nitrogen is 23mg/L, meeting the production requirements. The evaporated clear liquid is reused to the production system, and the reuse ratio is 95% (w/w), and the remaining evaporated clear liquid is discharged after reaching the standard through biological treatment; the obtained crude sodium sulfate and sodium chloride are transported to the oxygen-enriched oxidation device.

(5) The crude salt products sodium sulfate and sodium chloride are processed by oxygen-enriched oxidation coupling catalytic combustion. After the reaction, refined salt products sodium sulfate and sodium chloride are produced, which can be reused as industrial salt.

The oxygen-enriched oxidation temperatures of crude sodium sulfate and sodium chloride are 700°C and 650°C respectively, and the reaction time is 1.5h.

The blown gas is air, wherein the mass ratio of oxygen to organic matter (calculated as COD) is 1.3. The refined sodium sulfate has a better whiteness, with a purity of 98.1%, and a water-insoluble content of 0.23%, reaching the industrial anhydrous sodium sulfate class III standard; the refined sodium chloride has a better whiteness, with a purity of 97.8%, and water The insoluble matter content is 0.19%, reaching the secondary standard of industrial sodium chloride. The temperature of the flue gas entering the catalytic combustion device is about 300-330°C, and the catalyst is a porous material impregnated with palladium and platinum; the flue gas at the outlet of the device can be discharged to the standard after simple treatment (cooling, alkali washing).

Example 2

Example 2 is the operation result of Example 1 under different operating parameters. The difference is that the alkaline sodium salt solution is sodium carbonate solution, the ratio of sodium carbonate to organic matter (calculated as COD) is 2.7, and the reaction time is 1.5h. After filtration, the quality of the slurry is 4.3% of the treated water. Its quality meets the production requirements and can be fully reused in the front-end production system. The filtrate enters the back-end processing unit, and the device can run well and stably.

Example 3

Example 3 is the operation result of Example 1 under different operating parameters. The difference is that the alkaline sodium salt solution is 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 quality of the slurry is 0.5% of the treated water, and its quality also meets the production requirements. It can be reused in the front-end production system, and the filtrate enters the back-end processing unit, and the device can run well and stably.

Example 4

Example 4 is the operation result of Example 1 under different operating parameters. The difference is that the pressure at the top of the rectification tower is 0.3MPaG, and the output of organic condensate is 0.5% (w/w) of the treated water. At this time, the concentration of the obtained ammonia water was 20.4%, the organic impurity content was 0.04%, and the ammonia recovery rate was 57%.

Example 5

The difference between embodiment 5 and embodiment 1 lies in the fluctuation of the water quality of the treatment object, and its water quality index is: salt content 18.5%, COD is 78000mg/L, ammonia nitrogen is 3140mg/L. During the treatment process, the mass ratio of oxygen to organic matter (COD) in the oxygen-enriched oxidation process is 4.0, the oxygen-enriched oxidation temperatures of sodium sulfate and sodium chloride are 750°C and 670°C, respectively, and the rest of the process conditions remain the same. The obtained slurry can also be reused to the front-end production system; the recovered ammonia concentration is 20.7%, and the organic impurity content is 0.09%; the output of organic condensate is 3.0% (w/w) of the treated water; the clear liquid is evaporated The COD of the product is 2370mg/L, the ammonia nitrogen is 9mg/L, and the recycling rate is 81%. The whiteness of the refined sodium sulfate and sodium chloride is better, both reaching the industrial standard.

Example 6

The salt content of the waste water produced by a new hydrogen energy material is 10.7%, the COD is 57000mg/L, and the ammonia nitrogen is 10800mg/L.

(1) Add sodium hydroxide and sodium carbonate mixed solution therein, the ratio of sodium hydroxide to organic matter (in COD) is 0.4, the ratio of sodium carbonate to organic matter (in COD) is 0.7, and the stirring reaction time is 0.3h. After filtration, the quality of the slurry is 3.2% of the treated water, and its quality meets the production requirements. It is reused to the front-end production system, and the filtrate enters the crystallizer.

(2) The temperature of the cooler and the crystallizer is controlled at 6±2°C to obtain Glauber’s salt crystals, which are dissolved and prepared into a sodium sulfate solution and then enter the evaporator; the cooled raffinate enters the rectification tower.

(3) The pressure at the top of the rectifying tower is controlled to be 0.05 MPaG, and the output of the organic condensate is 2.0% (w/w) of the treated water; the still liquid of the rectifying tower is pumped into the evaporator. Ammonia is prepared by falling film absorption, the concentration of ammonia water is 21.6%, the content of organic impurities is 0.08%, and the recovery rate of ammonia reaches 83%.

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

(5) The oxygen-enriched oxidation temperatures of crude sodium sulfate and sodium chloride are 480°C and 620°C respectively, the reaction time is 4.0h, and the gas blown in is a mixture of pure oxygen and air, wherein oxygen and organic matter (in COD Count) mass ratio is 2.5. The refined sodium sulfate has a better whiteness, with a purity of 97.8%, and a water-insoluble content of 0.21%, reaching the industrial anhydrous sodium sulfate class III standard; the refined sodium chloride has a better whiteness, with a purity of 97.4%. The insoluble matter content is 0.18%, reaching the secondary standard of industrial sodium chloride. The temperature of the flue gas entering the catalytic combustion device is 260-310 ° C, and the catalyst is a combination of nickel, cobalt oxide, manganese oxide and copper oxide compound; the flue gas at the outlet of the device can reach the standard emission after simple treatment (cooling, alkali washing).

Example 7

Example 7 is the operation result of Example 6 under different operating parameters. The difference is that the temperature of the cooler and crystallizer is controlled at -2±2°C, so that more mirabilite crystals can be obtained, and the refined sodium sulfate product can also meet the industrial anhydrous sodium sulfate Class III standard.

Example 8

Example 8 is the operation result of Example 6 under different operating parameters. The difference is that the alkaline sodium salt solution is a mixed solution of sodium hydroxide and sodium bicarbonate, the ratio of sodium hydroxide to organic matter (in COD) is 0.4, and the ratio of sodium bicarbonate to organic matter (in COD) is 1.2. After filtration, the quality of the slurry is 1.3% of the treated water, which meets the production requirements and can be fully reused in the front-end production system. The filtrate enters the back-end processing unit, and the device can run well and stably.

Example 9

The salt content of the waste water produced by a new hydrogen energy material is 21.4%, the COD is 13900mg/L, and the ammonia nitrogen is 8700mg/L.

(1) Add sodium hydroxide solution therein, 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 quality of the slurry is 0.7% of the treated water, and its quality meets the production requirements. It is reused to the front-end production system, and the filtrate enters the crystallizer.

(2) The temperature of the cooler and the crystallizer is controlled at 0±2°C to obtain Glauber’s salt crystals, which are dissolved and prepared into a sodium sulfate solution and then enter the evaporator; the cooled raffinate enters the rectification tower.

(3) The pressure at the top of the rectifying tower is controlled to be 0.1 MPaG, and the output of the organic condensate is 0.7% (w/w) of the treated water; the still liquid of the rectifying tower is pumped into the evaporator. Ammonia gas is prepared by spraying and absorbing. The concentration of ammonia water is 15.7%, the content of organic impurities is 0.04%, and the recovery rate of ammonia reaches 71%.

(4) The sodium sulfate solution and the rectifying column still liquid were dehydrated by evaporation respectively, and the COD of the evaporated clear liquid was 320 mg/L, and the ammonia nitrogen was 24 mg/L, which met the production requirements. 95% of the evaporated liquid is recycled to the production system; the obtained crude sodium sulfate and sodium chloride are sent to the oxygen-enriched oxidation unit.

(5) The oxygen-enriched oxidation temperature of crude sodium sulfate and sodium chloride is 430°C and 650°C respectively, the reaction time is 2.0h, the gas blown in is air, and the mass ratio of oxygen to organic matter (calculated as COD) is 1.1 . The refined sodium sulfate has a better whiteness, with a purity of 98.2%, and a water-insoluble content of 0.09%, reaching the industrial anhydrous sodium sulfate Class III standard; the refined sodium chloride has a better whiteness, with a purity of 98.1%, and water The insoluble matter content is 0.11%, reaching the secondary standard of industrial sodium chloride. The temperature of the flue gas entering the catalytic combustion device is 320-400 °C, and the catalyst is a combination of nickel, cobalt oxide, manganese oxide and copper oxide compound; the flue gas at the outlet of the device can reach the standard emission after simple treatment (cooling, alkali washing).

Comparative example 1

This comparative example is the operating result of Example 1 under different operating parameters. The difference is that after adding the sodium hydroxide solution, the stirring reaction time is 0.1h.

After the stirring reaction, the organic flocs are viscous, the solid-liquid separation efficiency is significantly reduced, and the flocs are easy to adhere to the surface of the filter membrane/filter cloth, making it difficult to collect the slurry. At the same time, flaky organic flocs appeared during the cooling crystallization process, a large amount of organic matter was entrained in the Glauber's salt crystals, and the recovery rate of the evaporated liquid was low (COD reached 6000mg/L).

Comparative example 2

This comparative example is the operating result of Example 1 under different operating parameters. The difference is that the ratio of sodium hydroxide to organic matter (in terms of COD) is 0.2.

Under this condition, the output of the organic condensate at the top of the rectifying tower is 0.9% (w/w) of the treated water; was 94.2%.

Comparative example 3

This comparative example is the operating result of Example 1 under different operating parameters. The difference is that the mass ratio of oxygen to organic matter (COD) in the oxygen-enriched oxidation device is 0.8.

The whiteness of refined sodium sulfate is not good, it is light gray, and the water-insoluble content is 0.37%; the whiteness of refined sodium chloride is poor, it is gray, and the water-insoluble content is 0.52%.

Comparative example 4

This comparative example is the operating result of Example 6 under different operating parameters. The difference is that the pressure at the top of the distillation column is 0.35MPaG.

Under this condition, the output of organic condensate is 1.8% (w/w) of the treated water, and the condensate contains a large amount of ammonia, resulting in a low amount of ammonia gas entering the absorption device, and the ammonia recovery rate is <40%.

The preferred specific embodiments of the present invention have been described in detail above. It should be understood that those skilled in the art can make many modifications and changes according to 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 experiments on the basis of the prior art shall be within the scope of protection defined by the claims.

Claims (10)

1. A hydrogen energy new material production wastewater treatment and resource regeneration method, characterized in that it comprises the following steps: (1) Add alkaline sodium salt solution to the production wastewater of hydrogen energy new materials, fully stir the reaction to regenerate and precipitate the production raw materials and intermediates, and circulate the slurry to the production workshop for reuse after solid-liquid separation, and the filtrate enters the crystallizer; (2) The filtrate is internally circulated between the crystallizer and the cooler by adopting axial flow pump suction, and the cooled waste water is crystallized and solid-liquid separated in the crystallizer, and then reclaimed to obtain mirabilite crystals and cooling raffinate; (3) Rectification and separation technology is adopted for the cooling raffinate, and the liquid in the rectification tower is pumped into the evaporation system; organic vapor and ammonia gas are separated from the top of the rectification tower, and organic condensate and high-purity ammonia gas are obtained after condensation. Organic condensate Circulate to the production workshop for reuse, ammonia gas is absorbed by water to make industrial ammonia water for reuse; (4) Glauber's salt crystals and rectification tower still liquid enter the evaporation system to remove water respectively, separate the evaporated clear liquid, evaporated concentrated liquid, and crude salt products sodium sulfate and sodium chloride, and reuse the evaporated clear liquid as water replenishment for production or use efflux after biological treatment; (5) The crude salt products sodium sulfate and sodium chloride are catalyzed and combusted by oxygen-enriched oxidation. After the reaction, the refined salt products sodium sulfate and sodium chloride are produced, which can be reused as industrial salt. 2. The method according to claim 1, characterized in that: in step (1), the salt content of the hydrogen energy new material production wastewater is ≥ 10% (w/ w), COD is 10000~80000mg/L, ammonia nitrogen concentration is ≥3000mg/L. 3. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 1, characterized in that: in step (1), the alkaline sodium salt solution is sodium hydroxide solution, sodium carbonate solution and One or a combination of sodium bicarbonate solution. 4. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 2, characterized in that: in step (1), when the alkaline sodium salt solution is sodium hydroxide, it is mixed with organic matter (in the form of COD) mass ratio is 0.4 to 2.0; when the alkaline sodium salt solution is sodium carbonate, the mass ratio to organic matter (in COD) is 0.6 to 2.7; when the alkaline sodium salt solution is sodium bicarbonate, to organic matter (in COD) The mass ratio is 1.0-4.5; the reaction time is 0.25-3.0h. 5. The method for treating waste water and resource regeneration in the production of new hydrogen energy materials according to claim 1, characterized in that in step (2), the temperature of the waste water after cooling in the cooler is controlled to be -5-10°C. 6. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 1, characterized in that: in step (3), the pressure at the top of the rectification tower is ≤0.3MPaG; the output of organic condensate is 0.5-3.0% (w/w) of the treated water; ammonia water is prepared by spray absorption or falling film absorption. 7. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 1, characterized in that: in step (4), the reuse ratio of the evaporated clear liquid is 70-95% (w/ w). 8. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 1, characterized in that: in step (5), oxygen or a mixture of oxygen and inert gas is blown in, oxygen and organic matter (in the form of COD meter) mass ratio of 1.0 to 4.0. 9. The hydrogen energy new material production wastewater treatment and resource regeneration method according to claim 8, characterized in that: in step (5), the temperature of the oxygen-enriched oxidation is 400-750°C, and the time is 1.0- 4.0h. 10. The method for wastewater treatment and resource regeneration of new hydrogen energy materials production according to claim 9, characterized in that: in step (5), the flue gas temperature of the catalytic combustion device is 260-400°C, and the catalyst carrier It is a porous material, and the active ingredient of the catalyst is one or a combination of transition metals and their oxides.

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