Comprehensive recovery treatment system and method for waste liquid containing sulfur and various ammonium salts

Abstract

The invention relates to the technical field of environmental protection, and particularly provides a comprehensive recovery treatment system and method for waste liquid containing sulfur and various ammonium salts. The treatment system comprises a sulfur foam tank, a super centrifuge, a clear liquid tank, a concentrated acid tower, an oxidation tower, a conversion tower, a filtering system, an ammonium sulfate storage tank, a concentrated sulfur foam buffer tank, an incineration system, a purification system, a drying system, a conversion system, an absorption system and a tail absorption system. Slurry such as solid sulfur is subjected to high-temperature combustion in an incinerator to obtain flue gas containing sulfur dioxide, and then the flue gas enters a subsequent sulfuric acid production process system to prepare a finished product of industrial sulfuric acid, so that recycling of sulfur resources is realized. Ammonium thiosulfate and ammonium thiocyanate are completely converted into an ammonium sulfate product by the ammonium salt solution through oxidation, conversion and other processes, so that the recycling of nitrogen resources is realized.

Description

Technical Field

[0001] The invention relates to the technical field of environmental protection, and in particular to a comprehensive recovery and treatment system and method for waste liquid containing sulfur and multiple ammonium salts. Background Art

[0002] In the coking process of the coking industry, the coke oven gas contains toxic and harmful gases such as H2S and HCN, which will cause serious pollution to the environment. The industry generally adopts ammonia wet oxidation desulfurization process with HPF, PDS and other catalysts to remove H2S and HCN from coke oven gas. During the ammonia wet oxidation desulfurization and decyanation process, ammonium sulfate, ammonium thiosulfate, ammonium thiocyanate and other desulfurization waste liquids and sulfur foam will be continuously produced. Sulfur foam not only pollutes the environment, but also significantly reduces the desulfurization efficiency when the salt content in the desulfurization liquid reaches a certain value. In order to maintain the balance of the total salt content in the desulfurization liquid and thus maintain the desulfurization efficiency, the production unit must replace a certain amount of desulfurization liquid every day, which not only increases the production and processing costs, but also the improper treatment of the replaced desulfurization liquid (sulfur foam) will cause huge environmental pressure.

[0003] The traditional treatment process of sulfur foam is to filter the sulfur foam, incinerate the filtrate to produce sulfuric acid, evaporate and concentrate the clear liquid, and then send the concentrated slurry containing a large amount of ammonium sulfate, ammonium thiosulfate, ammonium thiocyanate and other ammonium salts into the incineration acid production system. Ammonium salts bring great difficulties to the acid production process, not only the exhaust nitrogen oxides exceed the standard, but also the product quality of industrial sulfuric acid decreases. The nitrogen element in the ammonium salt is not only not recovered, but also becomes a negative factor in the treatment process.

[0004] The main feature of the present invention is that the sulfur element and the nitrogen element in the sulfur foam can be converted into two products, industrial sulfuric acid and ammonium sulfate, respectively, which not only avoids the negative impact of the nitrogen element on the treatment process, but also converts the nitrogen element into a valuable ammonium sulfate product. The present invention realizes the full recycling of sulfur resources and nitrogen resources, kills two birds with one stone, and turns waste into treasure.

[0005] The process of treating sulfur foam containing various impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, ammonium thiocyanate, etc. is stable, and SO2 and NO in tail gas X The incineration system meets emission standards, has high thermal efficiency, consumes less fuel, and greatly reduces processing costs. It also has high recovery rates for sulfur and nitrogen, good product quality, and a green production process, with great environmental and economic benefits. Summary of the invention

[0006] In view of this, the present invention proposes a comprehensive recovery and treatment system and method for waste liquid containing sulfur and various ammonium salts, which separates solid sulfur and ammonium salt solution by filtration, and solid sulfur and other slurries are burned at high temperature in an incinerator to obtain flue gas containing sulfur dioxide, which then enters the subsequent sulfuric acid production process system to produce finished industrial sulfuric acid, thereby realizing the recovery and utilization of sulfur resources. The ammonium salt solution converts ammonium thiosulfate and ammonium thiocyanate into ammonium sulfate products through oxidation, conversion and other processes, thereby realizing the recovery and utilization of nitrogen resources.

[0007] The technical solution of the present invention is achieved as follows: the present invention provides a comprehensive recovery and treatment system for waste liquid containing sulfur and multiple ammonium salts, comprising a sulfur foam tank and a super centrifuge, wherein the discharge port of the sulfur foam tank is connected with the feed port of the super centrifuge, the solid discharge port of the super centrifuge, the concentrated sulfur foam buffer tank, the incineration system, the purification system, the drying system, the conversion system, the absorption system and the tail suction system are connected in sequence; the liquid discharge port of the super centrifuge, the clear liquid tank, the concentration tower, the oxidation tower, the conversion tower, the filtration system and the ammonium sulfate storage tank are connected in sequence.

[0008] In some embodiments, the filter residue outlet of the filtration system is connected to the concentrated sulfur foam buffer tank.

[0009] In some embodiments, the clear liquid outlet of the concentration column is connected to the clear liquid tank.

[0010] In a second aspect, the present invention further provides a processing method based on the above processing system, comprising the following steps:

[0011] S1, the waste liquid to be treated enters the super centrifuge for solid-liquid separation, the solid phase enters the concentrated sulfur foam buffer tank, and the liquid phase enters the clear liquid tank;

[0012] S2. Part of the clear liquid in the clear liquid tank is returned to the coking desulfurization, and the remaining part enters the concentration tower for concentration treatment. The clear liquid concentrated in the concentration tower is returned to the clear liquid tank, and the concentrated slurry enters the oxidation tower for oxidation treatment. The oxidized liquid after oxidation treatment enters the conversion tower, and the conversion liquid is generated under the catalytic action of the catalyst in the conversion tower. The conversion liquid enters the filtration system, and the filter residue enters the concentrated sulfur foam buffer tank. The filtrate is an ammonium sulfate solution;

[0013] S3. The slurry in the foam buffer tank directly enters the incineration system for incineration treatment, and the flue gas from the incineration ultrasound enters the purification system. The purified flue gas enters the drying system for dehydration and drying. The dried flue gas enters the conversion system. The converted flue gas enters the absorption system with concentrated sulfuric acid as the absorbent. The flue gas absorbed by the absorption system is treated by the tail suction system and discharged.

[0014] In some embodiments, the rotation speed for solid-liquid separation is 1000-2000 rpm, and the centrifugation time is 15-25 min.

[0015] In some embodiments, the supernatant liquid returned to the coking desulfurization accounts for 60-70 wt % of the total supernatant liquid.

[0016] In some embodiments, the oxidation treatment conditions include: adding excess air into the oxidation tower, the air excess coefficient is 30-50%, the pressure is 0.4-0.6 MPa, and the temperature is 100-150°C.

[0017] In some embodiments, the catalytic temperature in the conversion tower is 50-80° C., the pressure is 0.02-0.06 MPa, and the catalyst is a composite carbon-based catalyst.

[0018] In some embodiments, the temperature in the incineration system is 1000-1100° C., and the incineration system is under negative pressure.

[0019] In some embodiments, the purification system includes a high-efficiency humidification tower, a packing cooling tower and a two-stage electric demister connected in sequence, and the flue gas temperature after purification by the purification system is ≤40°C and the acid mist content is ≤5mg / m 3 .

[0020] In some embodiments, the conversion system uses a double conversion process, catalyzed by a vanadium catalyst, and the conversion temperature is 400-600°C.

[0021] In some embodiments, the vanadium catalyst includes a diatomaceous earth support and a vanadium pentoxide catalyst.

[0022] In some embodiments, the drying system uses 93% concentrated sulfuric acid for drying and dehydration, and the moisture content of the flue gas after drying is ≤0.1g / Nm 3 .

[0023] In some embodiments, 98% concentrated sulfuric acid is used as the absorbent in the absorption system, and the absorption temperature is 50-90°C.

[0024] Compared with the prior art, the present invention has the following beneficial effects:

[0025] The present invention can convert sulfur foam containing various impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, ammonium thiocyanate, etc. into industrial sulfuric acid products and nitrogen into ammonium sulfate products after the above-mentioned process treatment, thereby achieving the most ideal desulfurization and denitrification effects. The efficient recycling of sulfur and nitrogen resources is achieved. The greatest feature of the present invention is that it effectively solves the problem of environmentally friendly treatment of sulfur foam. The process flow for treating sulfur foam containing various impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, ammonium thiocyanate, etc. is stable, and SO2 and NO in the tail gas are reduced. X The incineration system meets emission standards, has high thermal efficiency, consumes less fuel, greatly reduces processing costs, and has a high recovery rate of sulfur and nitrogen elements and good product quality.

[0026] The production process is green, environmentally friendly, efficient, energy-saving, safe and stable. It has good environmental and economic benefits and is worthy of vigorous promotion and application in practice. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0028] Figure 1 The figure is a flow chart of the method of the present invention. DETAILED DESCRIPTION

[0029] The following will be combined with the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0030] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the art to which the embodiments of the present invention belong. If the definitions set forth in this section are contrary to or otherwise inconsistent with the definitions set forth in the patents, patent applications, published patent applications, and other publications incorporated herein by reference, the definitions listed in this section take precedence over the definitions incorporated herein by reference.

[0031] Unless otherwise specified, the methods used in the following examples are all conventional methods. Unless otherwise specified, the materials, reagents and instruments used are all conventional materials, reagents and instruments in the art, and can be obtained by those skilled in the art through commercial channels.

[0032] When an amount, concentration or other value or parameter is expressed as a range, a preferred range or a range defined by a series of upper preferred values ​​and lower preferred values, this should be understood as specifically disclosing all ranges formed by any pairing of any range upper limit or preferred value with any range lower limit or preferred value, regardless of whether the range is disclosed separately. For example, when a range of "1 to 5" is disclosed, the described range should be interpreted as including the range "1 to 4", "1 to 3", "1 to 2", "1 to 2 and 4 to 5", "1 to 3 and 5", etc. When a numerical range is described herein, unless otherwise stated, the range is intended to include its end values ​​and all integers and fractions within the range. In the present specification and claims, range definitions can be combined and / or interchanged, and if not otherwise stated, these ranges include all subranges contained therein.

[0033] Example 1

[0034] like Figure 1 As shown, this embodiment provides a method for treating waste liquid containing impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate in the coking industry, and the specific steps are as follows:

[0035] S1. The waste liquid (sulfur foam) containing impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate is transported to a super centrifuge (2) through a pipeline using a centrifugal pump to obtain a clear liquid and a concentrated sulfur foam. 60% of the clear liquid is returned to the coking desulfurization section, and the remaining 40% of the clear liquid enters a concentration tower (4).

[0036] S2, sending the clear liquid in S1 to a concentration tower (4), where the clear liquid is evaporated and concentrated in the concentration tower (4) to obtain an ammonium salt concentrate with a relatively high concentration, which is then sent to an oxidation tower (5), and the evaporated condensate is returned to the clear liquid tank (3).

[0037] S3, the ammonium salt concentrated solution in S2 is sent to an oxidation tower (5), and excess air is added into the oxidation tower (5), the air excess coefficient is 30%, the pressure in the tower is 0.4-0.6 MPa, and the temperature is between 100-150° C. The concentrated solution is fully oxidized under these operating conditions, and the ammonium thiosulfate in the oxidation solution is completely oxidized to ammonium sulfate.

[0038] S4, the oxidation liquid in S3 is sent to the conversion tower (6), and a composite carbon-based catalyst is added to the conversion tower (6), the temperature is controlled between 50-80°C, and the pressure is controlled between 0.02-0.06MPa. Under these operating conditions, the oxidation liquid is fully converted, and the ammonium thiocyanate in the conversion liquid is completely converted into ammonium sulfate. At this time, the conversion liquid mainly contains suspended sulfur and ammonium sulfate. After the efficient oxidation and catalytic conversion process, the ammonium thiosulfate and ammonium thiocyanate are completely converted into ammonium sulfate, thereby realizing the full recovery of nitrogen resources and avoiding environmental pollution.

[0039] S5, the conversion liquid in S4 is pumped into the filtration system (7) through the pipeline for filtration, the filtrate is an ammonium sulfate solution, and the filter residue is solid sulfur. The ammonium sulfate solution is sent to the ammonium sulfate storage tank (8) as a product for storage, and the filter residue is sent to the concentrated sulfur foam buffer tank (9).

[0040] S6, the concentrated sulfur foam in S1 is sent to the concentrated sulfur foam buffer tank (9) for temporary buffering, and the sulfur slurry coming out of the concentrated sulfur foam buffer tank (9) is directly sent to the incineration system (10), and at the same time, excessive air is added to the inlet for high-temperature incineration. The temperature in the incinerator is 1000-1100° C., and the pressure is controlled at a slightly negative pressure state. Under such operating conditions, the sulfur is completely burned to become SO2, and the high-temperature flue gas containing SO2 enters the purification system (11).

[0041] S7, the high-temperature flue gas containing SO2 in S6 is sent to the purification system (11), and the purification system (11) adopts a closed acid washing process of "high-efficiency humidification tower-packed cooling tower-two-stage electric demister". After the high-temperature flue gas is washed by the purification system (11), the temperature is ≤40°C and the acid mist content is ≤5mg / m 3 , particle content ≤10mg / m 3 Impurities, acid mist and other harmful substances in the flue gas are removed, and the purified qualified flue gas enters the drying system (12) for dehydration and drying.

[0042] S8: Send the qualified flue gas in S7 to the drying system (12) for dehydration. The drying system (12) uses 93% concentrated sulfuric acid for dehydration. The moisture content in the flue gas after drying is ≤0.1g / Nm 3 , the dried flue gas enters the conversion system (13).

[0043] S9, the qualified flue gas in S8 is sent to the conversion system (13), and the conversion adopts a double conversion process, with vanadium pentoxide and diatomaceous earth as the main components of vanadium coal catalyst, which greatly reduces the reaction temperature. The reaction temperature is controlled between 400-600 ° C, the first total conversion rate is ≥95%, and the second total conversion rate is ≥99.8%. Under this operating condition, most of SO2 is converted into SO3, and the flue gas containing SO3 after conversion enters the absorption system (14).

[0044] S10, sending the flue gas containing SO3 after conversion in S9 to the absorption system (14), the absorption system (14) uses 98% concentrated sulfuric acid as the absorbent, the absorption temperature is controlled between 50-90°C, SO3 is combined with H2O to obtain industrial sulfuric acid product, under this operating condition, the absorption rate of SO3 is ≥99.95%, and the flue gas from the absorption system (14) is sent to the tail suction system (15). This process converts all the waste sulfur into industrial sulfuric acid, realizes the full recovery of sulfur resources, and avoids environmental pollution.

[0045] S11, sending the flue gas from the absorption system (14) in S10 to the tail suction system (15) for desulfurization. The desulfurizer is hydrogen peroxide, and the dilute sulfuric acid obtained after the reaction is used as water for the absorption system (14). The tail gas after desulfurization meets the emission standards, thus solving the problem of sulfur dioxide polluting the environment.

[0046] In this embodiment, sulfur foam containing various impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate is treated by the above process, and the sulfur element is converted into an industrial sulfuric acid product, and the nitrogen element is converted into an ammonium sulfate product, thereby achieving the most ideal desulfurization and denitrification effect. The efficient recycling of sulfur and nitrogen resources is achieved. The greatest feature of the present invention is that it effectively solves the problem of environmentally friendly treatment of sulfur foam. The process flow for treating sulfur foam containing various impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate is stable, and SO2 and NO in the tail gas are reduced. X The incineration system meets emission standards, has high thermal efficiency, consumes less fuel, greatly reduces processing costs, and has a high recovery rate of sulfur and nitrogen elements and good product quality.

[0047] Example 2

[0048] This embodiment provides a method for treating waste liquid containing impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate in the coking industry. The specific steps are as follows:

[0049] S1. The waste liquid (sulfur foam) containing impurities such as sulfur, ammonium sulfate, ammonium thiosulfate, and ammonium thiocyanate is transported to a super centrifuge (2) through a pipeline using a centrifugal pump to obtain a clear liquid and a concentrated sulfur foam. 70% of the clear liquid is returned to the coking desulfurization section, and the remaining 30% of the clear liquid enters a concentration tower (4).

[0050] S2, sending the clear liquid in S1 to a concentration tower (4), where the clear liquid is evaporated and concentrated in the concentration tower (4) to obtain an ammonium salt concentrate with a relatively high concentration, which is then sent to an oxidation tower (5), and the evaporated condensate is returned to the clear liquid tank (3).

[0051] S3, the ammonium salt concentrated solution in S2 is sent to an oxidation tower (5), and excess air is added into the oxidation tower (5), the air excess coefficient is 50%, the pressure in the tower is 0.4-0.6 MPa, and the temperature is between 100-150° C. The concentrated solution is fully oxidized under these operating conditions, and the ammonium thiosulfate in the oxidation solution is completely oxidized to ammonium sulfate.

[0052] S4, the oxidation liquid in S3 is sent to the conversion tower (6), and a composite carbon-based catalyst is added to the conversion tower (6), the temperature is controlled between 50-80°C, and the pressure is controlled between 0.02-0.06MPa. Under these operating conditions, the oxidation liquid is fully converted, and the ammonium thiocyanate in the conversion liquid is completely converted into ammonium sulfate. At this time, the conversion liquid mainly contains suspended sulfur and ammonium sulfate. After the efficient oxidation and catalytic conversion process, the ammonium thiosulfate and ammonium thiocyanate are completely converted into ammonium sulfate, thereby realizing the full recovery of nitrogen resources and avoiding environmental pollution.

[0053] S5, the conversion liquid in S4 is pumped into the filtration system (7) through the pipeline for filtration, the filtrate is an ammonium sulfate solution, and the filter residue is solid sulfur. The ammonium sulfate solution is sent to the ammonium sulfate storage tank (8) as a product for storage, and the filter residue is sent to the concentrated sulfur foam buffer tank (9).

[0054] S6, the concentrated sulfur foam in S1 is sent to the concentrated sulfur foam buffer tank (9) for temporary buffering, and the sulfur slurry coming out of the concentrated sulfur foam buffer tank (9) is directly sent to the incineration system (10), and at the same time, excessive air is added to the inlet for high-temperature incineration. The temperature in the incinerator is 1000-1100° C., and the pressure is controlled at a slightly negative pressure state. Under such operating conditions, the sulfur is completely burned to become SO2, and the high-temperature flue gas containing SO2 enters the purification system (11).

[0055] S7, the high-temperature flue gas containing SO2 in S6 is sent to the purification system (11), and the purification system (11) adopts a closed acid washing process of "high-efficiency humidification tower-packed cooling tower-two-stage electric demister". After the high-temperature flue gas is washed by the purification system (11), the temperature is ≤40°C and the acid mist content is ≤5mg / m 3 , particle content ≤10mg / m 3 Impurities, acid mist and other harmful substances in the flue gas are removed, and the purified qualified flue gas enters the drying system (12) for dehydration and drying.

[0056] S8: Send the qualified flue gas in S7 to the drying system (12) for dehydration. The drying system (12) uses 93% concentrated sulfuric acid for dehydration. The moisture content in the flue gas after drying is ≤0.1g / Nm 3 , the dried flue gas enters the conversion system (13).

[0057] S9, the qualified flue gas in S8 is sent to the conversion system (13), and the conversion adopts a double conversion process, with vanadium pentoxide and diatomaceous earth as the main components of vanadium coal catalyst, which greatly reduces the reaction temperature. The reaction temperature is controlled between 400-600 ° C, the first total conversion rate is ≥95%, and the second total conversion rate is ≥99.8%. Under this operating condition, most of SO2 is converted into SO3, and the flue gas containing SO3 after conversion enters the absorption system (14).

[0058] S10, sending the flue gas containing SO3 after conversion in S9 to the absorption system (14), the absorption system (14) uses 98% concentrated sulfuric acid as the absorbent, the absorption temperature is controlled between 50-90°C, SO3 is combined with H2O to obtain industrial sulfuric acid product, under this operating condition, the absorption rate of SO3 is ≥99.95%, and the flue gas from the absorption system (14) is sent to the tail suction system (15). This process converts all the waste sulfur into industrial sulfuric acid, realizes the full recovery of sulfur resources, and avoids environmental pollution.

[0059] S11, sending the flue gas from the absorption system (14) in S10 to the tail suction system (15) for desulfurization. The desulfurizer is hydrogen peroxide, and the dilute sulfuric acid obtained after the reaction is used as water for the absorption system (14). The tail gas after desulfurization meets the emission standards, thus solving the problem of sulfur dioxide polluting the environment.

[0060] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A comprehensive recovery and treatment system for waste liquid containing sulfur and various ammonium salts, characterized in that: It includes a sulfur foam tank and a super centrifuge. The discharge port of the sulfur foam tank is connected with the feed port of the super centrifuge. The solid discharge port of the super centrifuge, the concentrated sulfur foam buffer tank, the incineration system, the purification system, the drying system, the conversion system, the absorption system and the tail suction system are connected in sequence; the liquid discharge port of the super centrifuge, the clear liquid tank, the concentration tower, the oxidation tower, the conversion tower, the filtration system and the ammonium sulfate storage tank are connected in sequence.

2. The comprehensive recovery and treatment system for sulfur-containing and multiple ammonium salt waste liquids according to claim 1, characterized in that: The filter residue outlet of the filtration system is connected to the concentrated sulfur foam buffer tank.

3. The comprehensive recovery and treatment system for sulfur-containing and multiple ammonium salt waste liquids according to claim 1, characterized in that: The clear liquid outlet of the concentration tower is communicated with the clear liquid tank.

4. The method for treating the comprehensive recovery and treatment system of the sulfur-containing and multiple ammonium salt waste liquid according to any one of claims 1 to 3, characterized in that: The steps include: S1, the waste liquid to be treated enters the super centrifuge for solid-liquid separation, the solid phase enters the concentrated sulfur foam buffer tank, and the liquid phase enters the clear liquid tank; S2. Part of the clear liquid in the clear liquid tank is returned to the coking desulfurization, and the remaining part enters the concentration tower for concentration treatment. The clear liquid concentrated in the concentration tower is returned to the clear liquid tank, and the concentrated slurry enters the oxidation tower for oxidation treatment. The oxidized liquid after oxidation treatment enters the conversion tower, and the conversion liquid is generated under the catalytic action of the catalyst in the conversion tower. The conversion liquid enters the filtration system, and the filter residue enters the concentrated sulfur foam buffer tank. The filtrate is an ammonium sulfate solution; S3. The slurry in the foam buffer tank directly enters the incineration system for incineration treatment. The flue gas generated by incineration enters the purification system. The purified flue gas enters the drying system for dehydration and drying. The dried flue gas enters the conversion system. The converted flue gas enters the absorption system with concentrated sulfuric acid as the absorbent. The flue gas absorbed by the absorption system is treated by the tail suction system and discharged.

5. The processing method according to claim 4, characterized in that: The clear liquid returned to the coking desulfurization accounts for 60-70wt% of the total clear liquid.

6. The processing method according to claim 4, characterized in that: The conditions for the oxidation treatment include: adding excess air into the oxidation tower, the air excess coefficient is 30-50%, the pressure is 0.4-0.6MPa, and the temperature is 100-150°C.

7. The processing method according to claim 4, characterized in that: The catalytic temperature in the conversion tower is 50-80°C, the pressure is 0.02-0.06MPa, and the catalyst is a composite carbon-based catalyst.

8. The processing method according to claim 4, characterized in that: The temperature inside the incineration system is 1000-1100°C and there is negative pressure inside the incineration system.

9. The processing method according to claim 4, characterized in that: The purification system includes a high-efficiency humidification tower, a packing cooling tower and a two-stage electric demister connected in sequence. The flue gas temperature after purification by the purification system is ≤40℃ and the acid mist content is ≤5mg / m 3 .

10. The processing method according to claim 4, characterized in that: The conversion system adopts a double conversion process, catalyzed by vanadium catalyst, and the conversion temperature is 400-600℃.

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