Resourceful treatment process and system of desulfurization waste liquid in coking industry

Abstract

The application discloses a kind of resource processing technology and system of coking industry desulfurization waste liquid, belong to coking industry desulfurization waste liquid utilization and processing technical field.The system of the present application includes decoloring device, preheater, mixer, first reactor, second reactor, third reactor, fourth reactor, fifth reactor and conversion tower;Desulfurization waste liquid is decolorized, preheated, mixed with acid liquor, reacted multiple times, catalytically converted, cooled and separated, and ammonium thiosulfate and ammonium thiocyanate in the desulfurization waste liquid are all converted into ammonium sulfate and sulfur, then the resource recovery and processing of ammonium sulfate and water in the converted solution are realized by the characteristics of water deficiency and salt production in the sulfur-ammonium section of the coking system.The present application can realize the effective recovery and utilization of sulfur, nitrogen and water resources in the desulfurization waste liquid through the setting of multiple reactors and the effective regulation of experimental conditions;While reducing the difficulty of conversion waste gas treatment, the yield of sulfur is increased, and the continuity and economy of the waste liquid treatment process are improved.

Description

Technical Field

[0001] This invention relates to a resource-based treatment process and system for desulfurization wastewater in the coking industry, belonging to the field of utilization and treatment technology of desulfurization wastewater in the coking industry. Background Technology

[0002] Desulfurization wastewater is a pollutant listed in the "National Hazardous Waste List" generated during the desulfurization process of coke oven gas, and it is a highly hazardous pollutant. Currently, the treatment processes for desulfurization wastewater are mainly divided into three types: the first is the salt extraction method, represented by salt extraction; the second is the conversion method, represented by acid production; and the third is the pyrolysis method, represented by coking treatment at waste coal yards.

[0003] Salt extraction is a widely used method in the industry, with two main approaches: evaporation crystallization and stepwise crystallization. Evaporation crystallization extracts mixed ammonium salts from desulfurization wastewater through steam crystallization, then returns the condensate to the desulfurization system, thus treating the wastewater. However, due to the high toxicity of mixed ammonium salts and the lack of market demand, their disposal and utilization present a new and urgent environmental challenge. Stepwise crystallization utilizes ternary phase diagram theory to extract ammonium thiocyanate and ammonium sulfate from desulfurization wastewater. However, due to limited market capacity for ammonium thiocyanate, the obtained ammonium thiocyanate from desulfurization wastewater cannot be sold. Furthermore, this process faces challenges such as high investment costs, high operating expenses, and the generation of secondary pollution.

[0004] Because coking sulfur also faces difficulties in sales, some companies have adopted a process to treat both desulfurization wastewater and sulfur to produce sulfuric acid. This technology can effectively treat desulfurization wastewater while simultaneously producing sulfuric acid, which can be used as a raw material for the ammonium sulfate process. Its biggest advantage is that it can treat both desulfurization wastewater and sulfur sludge, two major pollutants. However, this process is complex, resulting in high investment, complicated operation, and high operating costs. Given the current sluggish sulfuric acid market, the widespread application of this technology will inevitably exacerbate the oversupply of sulfuric acid. Furthermore, the production of dilute sulfuric acid using this technology and the exhaust gases generated during incineration both introduce new environmental hazards.

[0005] Some enterprises discarded desulfurization wastewater at coal yards for coking treatment. The ammonium salts in the wastewater decomposed in the coke oven, and the final products—NH3, H2S, CO2, and N2—entered the subsequent coal purification system along with the raw coal gas. Only a small amount of H2S reacted chemically with the coke, thus achieving the purpose of treating the desulfurization wastewater. This method was once widely used by coking enterprises. Some enterprises attempted to optimize and improve the method by uniform spraying, mixing with a mixer, and injecting it into the coal charging tower. However, the final treatment method is essentially no different from directly dumping it at the coal yard. This method has problems such as affecting the moisture content of the coal entering the furnace, affecting coke quality, and creating a poor working environment. Especially with the full implementation of existing large coal yard enclosure projects, the drawbacks of this method for treating desulfurization wastewater have become more apparent, and enterprises have now abandoned this method.

[0006] Chinese patent CN112125319A discloses a technology for the full-component recovery of desulfurization wastewater. This technology converts desulfurization wastewater into ammonium bisulfate solution through catalytic conversion, and then incorporates it into the ammonium sulfate system to achieve the full-component recovery and utilization of desulfurization wastewater. However, this process has problems such as poor sulfur quality and ineffective treatment of conversion tail gas. Its process flow needs further optimization.

[0007] In summary, current desulfurization wastewater treatment technologies in the industry suffer from problems such as high investment, high operating costs, serious secondary pollution, poor quality of by-products, and inefficient process flow. Summary of the Invention

[0008] To address the problems of high operating costs and severe secondary pollution in existing technologies, this invention aims to provide a resource-based treatment process and system for desulfurization wastewater in the coking industry, which can effectively recover and utilize resources such as sulfur, nitrogen, and water from the desulfurization wastewater.

[0009] The purpose of this invention is to convert all ammonium thiosulfate and ammonium thiocyanate in desulfurization wastewater into ammonium sulfate and sulfur. Then, leveraging the water-scarce salt production characteristic of the ammonium sulfate section in the coking system, the invention achieves resource recovery and treatment of ammonium sulfate and water in the post-conversion solution. This invention utilizes the oxidizing properties of ammonium sulfite, an intermediate product after ammonium thiosulfate conversion, and the reducing properties of hydrogen sulfide in the tail gas during ammonium thiocyanate conversion to achieve sulfur recovery. This reduces the difficulty of treating the conversion waste gas while increasing the sulfur yield. Furthermore, activated carbon and catalyst are separately packed in a fixed-bed reactor, improving the continuity and economy of the wastewater treatment process.

[0010] This invention provides a resource-based treatment process for desulfurization wastewater from the coking industry, comprising the following steps: (1) The desulfurization waste liquid is sent to the decolorization device for decolorization; In this invention, decolorization can be carried out in one of the following ways: ① Powdered activated carbon can be added to the desulfurization waste liquid, and then decolorization can be completed by stirring and filtering; ② Decolorization can be carried out by a fixed bed decolorization column, with the temperature controlled at 30-80℃.

[0011] (2) The decolorized waste liquid is sent to a preheating device; The preheating temperature is 120-130℃ and the pressure is 0.2-0.4MPa.

[0012] (3) The preheated waste liquid is sent to the mixer to be mixed with the acid liquid; The acid solution is a conversion solution, or sulfuric acid with a mass concentration of 2%-98%, and the pH after mixing is 2-4; (4) The mixed liquid is sent into the first reactor; the temperature is 120-140℃ and the pressure is 0.2-0.4MPa.

[0013] The first reactor is a static reactor. Its main purpose is to decompose ammonium thiosulfate and separate sulfur. The main reactions that occur are:

[0014] (5) The gas and liquid exiting the first reactor enter the second reactor through the outlet; the temperature is 120-140℃, and the pressure is 0.2-0.3MPa. The second reactor is a bubble reactor, the main purpose of which is to realize the reaction of ammonium sulfite in the waste liquid with hydrogen sulfide in the gas phase and the separation of sulfur. The main reactions that occur are:

[0015] (6) The gas and liquid from the second reactor enter the third reactor through the outlet; the temperature is controlled at 85-95℃ and the pressure is 0.01-0.1MPa.

[0016] The third reactor is a stirred reactor, designed to continue the reaction that occurred in the second reactor, ensuring the complete reaction of sulfites in the liquid phase. It also has an evaporation and concentration function to regulate the moisture entering the downstream reactor.

[0017] The gas at the top of the third reactor enters the scrubbing tower for washing and cooling, forming a gas-liquid two-phase system at a temperature of 35°C and a pressure of 5kPa-20kPa. The gas-liquid two-phase treatment methods are as follows: the liquid obtained after washing is collected and sent to the enterprise's biochemical system or added to the saturator during ammonium sulfate desaturation operation. The washed gas can be used in any one or more of the following processes: ① sent to the acid incinerator, ② sent to the carbonization chamber at the top of the coke oven, ③ sent to the negative pressure pipeline before the gas blower.

[0018] (7) The liquid at the bottom of the third reactor is pumped into the fourth reactor, which is a stirred reactor. Its main purpose is to convert ammonium thiocyanate. Acid is added to react and convert ammonium thiocyanate into ammonium sulfate. The main reactions that occur are as follows:

[0019] (8) Concentrated sulfuric acid is simultaneously added to the fourth reactor. The gas in the fourth reactor is sent back to the first reactor through the top gas outlet pipe, and the liquid in the fourth reactor is sent to the fifth reactor. The amount of concentrated sulfuric acid added is 20%-50% of the volumetric flow rate of the reactants in the fourth reactor (i.e., the liquid from the bottom of the third reactor). The temperature in the fourth reactor is 120℃-140℃, and the pressure is 0.3MPa-0.5MPa.

[0020] (9) The gas at the top of the fifth reactor enters the second reactor, and the liquid in the fifth reactor enters the conversion tower; the fifth reactor is a static reactor, and the main reactions that occur are the same as those in the fourth reactor.

[0021] The temperature in the fifth reactor is 120℃-140℃, and the pressure is 0.2MPa-0.4MPa.

[0022] (10) The liquid in the conversion tower is filtered through a precision filter to remove particles ≥50μm and then sent to the ammonium sulfate section. The gas in the conversion tower is sent to the third reactor. The conversion tower is a packed tower with carbon-based catalyst as the packing material. The temperature of the conversion tower is 80℃-95℃ and the pressure is controlled at 0.02-0.04MPa.

[0023] (11) Sulfur will be deposited at the bottom of the first reactor, the second reactor, the fourth reactor and the fifth reactor during the reaction process. Liquid sulfur needs to be released from the bottom of the above reactors in a heat-preserving state periodically and sold or sent to the enterprise's acid production system; or the liquid sulfur can be cooled and molded to generate sulfur and sold or sent to the enterprise's acid production system.

[0024] The above-mentioned processing technology includes five reactors connected in sequence. The first, second, fourth and fifth reactors all generate sulfur; the gas from the fifth reactor is recycled to the second reactor; and the gas from the fourth reactor is recycled to the first reactor.

[0025] This invention provides a resource-based treatment system for desulfurization wastewater in the coking industry, comprising a decolorization device, a preheater, a mixer, a first reactor, a second reactor, a third reactor, a fourth reactor, a fifth reactor, and a conversion tower. The decolorization device is sequentially connected to the preheater and the mixer. The mixer has an inlet for conversion liquid or acid liquid, and its outlet is connected to the first reactor. The first, second, third, fourth, and fifth reactors and the conversion tower are connected in series. The first reactor is a static reactor, the second reactor is a bubbling reactor, the third and fourth reactors are stirred reactors, and the fifth reactor is a static reactor. The bottom of the first, second, fourth, and fifth reactors all have sulfur outlets. The gas outlet of the fifth reactor is connected to the second reactor. The gas outlet of the fourth reactor is connected to the first reactor. The gas outlet of the conversion tower is connected to the third reactor, and the gas outlet of the third reactor is connected to a scrubbing tower. The gas outlet of the scrubbing tower leads to the next process, and the liquid outlet of the scrubbing tower leads to a biochemical system or an ammonium sulfate system. The liquid outlet of the conversion tower is connected to a precision filter, and the solid phase outlet of the precision filter is connected to the ammonium sulfate section.

[0026] The beneficial effects of this invention are: (1) By setting up multiple reactors and effectively controlling experimental conditions, the present invention can realize the effective recovery and utilization of resources such as sulfur, nitrogen and water in desulfurization waste liquid.

[0027] (2) All ammonium thiosulfate and ammonium thiocyanate in the desulfurization waste liquid are converted into ammonium sulfate and sulfur. Then, taking advantage of the water shortage and salt production characteristics of the ammonium sulfate section in the coking system, the resource recovery and treatment of ammonium sulfate and water in the solution after conversion are realized.

[0028] (3) By taking advantage of the oxidizing properties of ammonium sulfite, an intermediate product after the conversion of ammonium thiosulfate, and the reducing properties of hydrogen sulfide in the tail gas of the conversion of ammonium thiocyanate, sulfur can be recovered. This reduces the difficulty of treating the conversion waste gas, increases the sulfur yield, and improves the continuity and economy of the waste liquid treatment process. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of the resource utilization treatment system for desulfurization wastewater in the coking industry according to the present invention.

[0030] In the diagram: 1 is the decolorization device, 2 is the preheater, 3 is the mixer, 4 is the first reactor, 5 is the second reactor, 6 is the third reactor, 7 is the fourth reactor, 8 is the fifth reactor, 9 is the conversion tower, 10 is the inlet of the conversion liquid or acid, 11 is the sulfur outlet, 12 is the washing tower, and 13 is the precision filter. Detailed Implementation

[0031] The present invention will be further illustrated by the following embodiments, but is not limited to the following embodiments.

[0032] Example 1: A resource-based treatment system for desulfurization wastewater in the coking industry is provided. like Figure 1 As shown, the resource utilization system for desulfurization wastewater in the coking industry provided by the present invention includes a decolorization device 1, a preheater 2, a mixer 3, a first reactor 4, a second reactor 5, a third reactor 6, a fourth reactor 7, a fifth reactor 8, and a conversion tower 9. The decolorization device 1 is connected in sequence to the preheater 2 and the mixer 3. The mixer 3 is provided with an inlet 10 for conversion liquid or acid liquid. The outlet of the mixer 3 is connected to the first reactor 4. The first reactor 4, the second reactor 5, the third reactor 6, the fourth reactor 7, the fifth reactor 8, and the conversion tower 9 are connected in series. The first reactor 4 is a static reactor, the second reactor 5 is a bubbling reactor, and ... Reactor 7 is a stirred reactor, and reactor 8 is a static reactor. The bottom of reactors 1, 2, 4 and 5 all have sulfur outlets 11. The gas outlet of reactor 8 is connected to reactor 2. The gas outlet of reactor 4 is connected to reactor 4. The gas outlet of conversion tower 9 is connected to reactor 3. The gas outlet of reactor 3 is connected to scrubbing tower 12. The gas outlet of scrubbing tower 12 leads to the next process, and the liquid outlet of scrubbing tower 12 leads to the biochemical system or ammonium sulfate system. The liquid outlet of conversion tower 9 is connected to precision filter 13. The solid phase outlet of precision filter (particulate matter below 50μm) is connected to the ammonium sulfate section.

[0033] Example 2: A resource-based treatment process for desulfurization wastewater in the coking industry is provided. A process for resource-based treatment of desulfurization wastewater using the resource-based treatment system for coking industry desulfurization wastewater described in Example 1 is provided, comprising the following steps: (1) The desulfurization waste liquid is sent to the decolorization device for decolorization. The activated carbon used for decolorization is packed in the decolorization column in the form of a fixed bed. The temperature of the decolorization process is controlled at 60℃.

[0034] (2) The decolorized waste liquid is pressurized to 0.4MPa by a pump and sent to a preheater to preheat the temperature of the waste liquid to 130℃.

[0035] (3) The preheated waste liquid is sent to a mixer and mixed with sulfuric acid with a mass concentration of 30%. The pH of the solution after mixing is 2. (4) The mixed liquid is sent to the first reactor to decompose ammonium thiosulfate and separate sulfur; the temperature is controlled at 130℃ and the pressure is 0.25MPa. (5) The gas and liquid from the first reactor enter the second reactor through the outlet to realize the reaction of ammonium sulfite in the waste liquid with hydrogen sulfide in the gas phase and the separation of sulfur; the temperature of the second reactor is 120℃ and the pressure is 0.2MPa. (6) The gas and liquid from the second reactor enter the third reactor through the outlet for further reaction and concentration. The concentration ratio is 20%, the temperature is controlled at 90℃, and the pressure is 0.01MPa. The gas at the top of the third reactor is cooled by washing. The temperature of the washing tower is 35℃ and the pressure is 5kPa. After washing, a two-phase gas and liquid are obtained. The liquid phase is collected and sent to the enterprise's biochemical system, and the gas phase is sent to the carbonization chamber at the top of the coke oven.

[0036] (7) The liquid at the bottom of the third reactor is pumped into the fourth reactor at a temperature of 130°C and a pressure of 0.3 MPa. 20% of the volumetric flow rate of the reactants in the fourth reactor (mass concentration of 97%) is simultaneously added to the fourth reactor. The gas in the fourth reactor is sent back to the first reactor through the top gas outlet pipe, and the liquid in the fourth reactor is sent into the fifth reactor. The temperature in the fifth reactor is 120°C and the pressure is 0.2 MPa.

[0037] (8) The gas at the top of the fifth reactor enters the second reactor, and the liquid in the fifth reactor enters the conversion tower. The conversion tower is a packed tower with carbon-based catalyst as the packing material. The temperature of the conversion tower is 85°C and the pressure is controlled at 0.02 MPa.

[0038] (9) The liquid in the conversion tower is filtered by a precision filter to remove particles ≥50μm and then sent to the ammonium sulfate section, while the gas in the conversion tower is sent to the third reactor.

[0039] (10) Sulfur will be deposited at the bottom of the first reactor, the second reactor, the fourth reactor and the fifth reactor during the reaction process. Liquid sulfur is released from the bottom of the above reactors every 4 hours under heat preservation. After being cooled and molded, the sulfur is sold.

[0040] Example 3: A resource-based treatment process for desulfurization wastewater from the coking industry is provided. A process for resource-based treatment of desulfurization wastewater using the resource-based treatment system for coking industry desulfurization wastewater described in Example 1 is provided, comprising the following steps: (1) The desulfurization waste liquid is sent into the decolorization device, powdered activated carbon is added to the desulfurization waste liquid, and then the decolorization is completed by stirring and filtering. The decolorization temperature is 80℃.

[0041] (2) The decolorized waste liquid is filtered, and the filtrate is sent to the preheating device. The preheating temperature is controlled at 130℃ and the pressure is controlled at 0.4MPa.

[0042] (3) The preheated waste liquid is sent to a mixer to mix with the acid solution. The acid solution is 98% concentrated sulfuric acid, and the pH of the mixed solution is 3.

[0043] (4) The mixed liquid is sent to the first reactor. The temperature of the first reactor is 130°C and the pressure is 0.3MPa. Sulfur will be deposited at the bottom of the first reactor. Liquid sulfur is released from the bottom every 4 hours under the heat preservation condition and sent to the sulfur warehouse after cooling.

[0044] (5) The gas and liquid from the first reactor enter the second reactor in series through the outlet. The temperature of the second reactor is 125℃ and the pressure is 0.2MPa. Sulfur will be deposited at the bottom of the second reactor. Liquid sulfur is released from the bottom every 4 hours under heat preservation conditions and sent to the sulfur storage after cooling.

[0045] (6) The gas and liquid from the second reactor are connected in series through the outlet to the third reactor. The temperature of the third reactor is 90℃ and the pressure is 0.05MPa. The gas at the top of the third reactor is cooled by washing. The temperature is 35℃ and the pressure is 10KPa. The gas and liquid phases are treated as follows: the cooled liquid is collected and sent to the enterprise's biochemical system, and the cooled gas is sent to the acid incinerator for combustion.

[0046] (7) The liquid at the bottom of the third reactor is pumped into the fourth reactor. The pressure of the fourth reactor is 0.4 MPa. A certain amount of concentrated sulfuric acid is added to the fourth reactor at the same time. The amount of sulfuric acid added is 35% of the volume flow rate of the waste liquid. The gas in the fourth reactor is sent back to the first reactor through the top gas outlet pipe. Sulfur will be deposited at the bottom of the fourth reactor. Liquid sulfur is released from the bottom every 4 hours under the heat preservation condition and sent to the sulfur storage after cooling.

[0047] (8) The liquid in the fourth reactor is sent to the fifth reactor. The temperature of the fifth reactor is 140°C and the pressure is 0.3MPa. The gas at the top of the fifth reactor enters the second reactor. Sulfur will be deposited at the bottom of the fifth reactor. Liquid sulfur is released from the bottom every 4 hours under heat preservation conditions and sent to the sulfur storage after cooling.

[0048] (9) The liquid in the fifth reactor enters the conversion tower, which is a packed tower with a carbon-based catalyst as the packing material. The temperature of the conversion tower is 80°C and the pressure is 0.025 MPa. The gas in the conversion tower is sent to the third reactor.

[0049] (10) The liquid in the conversion tower is filtered by a precision filter and then sent to the ammonium sulfate section.

Claims

1. A resource-based treatment process for desulfurization wastewater from the coking industry, characterized in that... Includes the following steps: (1) The desulfurization waste liquid is sent to the decolorization device for decolorization; (2) The decolorized waste liquid is sent to a preheating device; the preheating temperature is 120-130℃ and the pressure is 0.2-0.4MPa; (3) The preheated waste liquid is sent to the mixer to be mixed with the acid liquid; (4) The mixed liquid is fed into the first reactor; the temperature is 120-140℃ and the pressure is 0.2-0.4MPa; the first reactor is a static reactor in which ammonium thiosulfate is decomposed and sulfur is separated. (5) The gas and liquid from the first reactor enter the second reactor through the outlet; the temperature is 120-140℃ and the pressure is 0.2-0.3MPa; the second reactor is a bubble reactor, which realizes the reaction of ammonium sulfite in the waste liquid with hydrogen sulfide in the gas phase and the separation of sulfur; (6) The gas and liquid from the second reactor enter the third reactor through the outlet; the temperature is controlled at 85-95℃ and the pressure is 0.01-0.1MPa; (7) The liquid at the bottom of the third reactor is pumped into the fourth reactor, where acid is added to convert ammonium thiocyanate into ammonium sulfate; (8) Concentrated sulfuric acid is simultaneously added to the fourth reactor. The gas in the fourth reactor is sent back to the first reactor through the top gas outlet pipe, and the liquid in the fourth reactor is sent to the fifth reactor. (9) The gas at the top of the fifth reactor enters the second reactor, and the liquid in the fifth reactor enters the conversion tower; (10) The liquid in the conversion tower is sent to the ammonium sulfate section after the particles ≥50μm are filtered out by a precision filter, and the gas in the conversion tower is sent to the third reactor. (11) Sulfur will be deposited at the bottom of the first reactor, the second reactor, the fourth reactor and the fifth reactor during the reaction process. Liquid sulfur needs to be released from the bottom of the above reactors periodically under heat preservation conditions and sold or sent to the enterprise's acid production system; or the liquid sulfur can be cooled and molded to generate sulfur and sold or sent to the enterprise's acid production system.

2. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, The decolorization is carried out using one of the following methods: ① adding powdered activated carbon to the desulfurization waste liquid and then completing the decolorization by stirring and filtering; ② decolorizing through a fixed-bed decolorization column with the temperature controlled at 30-80℃.

3. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, In step (3), the acid solution is sulfuric acid with a mass concentration of 2%-98%, and the pH after mixing is 2-4.

4. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, The third reactor is a stirred reactor, in which the reaction in the second reactor continues to occur, ensuring the complete reaction of sulfites in the liquid phase. It also has an evaporation and concentration function to regulate the moisture entering the downstream reactor.

5. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 4, characterized in that, The gas at the top of the third reactor enters the scrubbing tower for washing and cooling, forming a gas-liquid two-phase system at a temperature of 35°C and a pressure of 5kPa-20kPa. The gas-liquid two-phase treatment methods are as follows: the liquid obtained by cooling is collected and sent to the enterprise's biochemical system or added to the saturator during the ammonium sulfate desaturation operation. The cooled gas is used for any of the following processes: ① sent to the acid incinerator, ② sent to the carbonization chamber at the top of the coke oven, ③ sent to the negative pressure pipeline before the gas blower.

6. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, The fourth reactor is a stirred reactor, with a temperature of 120℃-140℃ and a pressure of 0.3MPa-0.5MPa. In step (8), the amount of concentrated sulfuric acid added is 20%-50% of the volumetric flow rate of the reactants in the fourth reactor.

7. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, The fifth reactor is a static reactor, with a temperature of 120℃-140℃ and a pressure of 0.2MPa-0.4MPa.

8. The resource-based treatment process for desulfurization wastewater in the coking industry according to claim 1, characterized in that, The conversion tower is a packed tower, with carbon-based catalyst as the packing material. The temperature of the conversion tower is 80℃-95℃, and the pressure is controlled at 0.02-0.04MPa.

9. A resource recovery system for desulfurization wastewater from the coking industry, used in the resource recovery process for desulfurization wastewater from the coking industry as described in any one of claims 1 to 8, characterized in that, The reactor comprises a decolorization unit, a preheater, a mixer, a first reactor, a second reactor, a third reactor, a fourth reactor, a fifth reactor, and a conversion tower. The decolorization unit is sequentially connected to the preheater and the mixer. The mixer has an acid inlet, and its outlet is connected to the first reactor. The first, second, third, fourth, and fifth reactors and the conversion tower are connected in series. The first reactor is a static reactor, the second reactor is a bubble-type reactor, the third and fourth reactors are stirred reactors, and the fifth reactor is a static reactor. The bottom of the first, second, fourth, and fifth reactors all have sulfur outlets. The gas outlet of the fifth reactor is connected to the second reactor. The gas outlet of the fourth reactor is connected to the first reactor. The gas outlet of the conversion tower is connected to the third reactor, and the gas outlet of the third reactor is connected to a scrubbing tower. The gas outlet of the scrubbing tower leads to the next process, and the liquid outlet of the scrubbing tower leads to a biochemical system or an ammonium sulfate system. The liquid outlet of the conversion tower is connected to a precision filter, and the solid phase outlet of the precision filter is connected to the ammonium sulfate section.

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