A treatment process for high-sulfate organic wastewater

Abstract

This invention relates to the field of wastewater treatment technology, specifically disclosing a treatment process for high-sulfate organic wastewater. The invention first uses electrodialysis to separate the high-sulfate organic wastewater into two streams under an electric field: sulfate ions are transferred from the high-sulfate organic wastewater to the purified water, resulting in a sulfate-rich concentrate; the high-sulfate organic wastewater then becomes a COD-rich desalination solution, which can be discharged in compliance with standards through conventional biological treatment. The sulfate-rich high-salt concentrate also includes some transferred COD and ammonia nitrogen, which are then treated biologically using halophilic bacteria tolerant to high salt concentrations to oxidize the COD and ammonia nitrogen. The ammonia nitrogen is oxidized to nitrate nitrogen, which is then connected to a sulfur autotrophic denitrification process to remove total nitrogen. The sulfur recovered from the biological treatment of the desalination solution serves as a packing material and electron donor for sulfur autotrophic bacteria, converting NO3- into nitrogen. ‑ -N is reduced to N2 without the need for an external carbon source, and at the same time, total nitrogen emissions meet the standards and sulfur resources are recycled, which has broad application prospects.

Description

Technical Field

[0001] This invention belongs to the field of wastewater treatment technology, and particularly relates to a treatment process for high-sulfate organic wastewater. Background Technology

[0002] High-sulfate organic wastewater exists in various industries such as chemical, pharmaceutical, papermaking, food processing, and mining. Traditional treatment methods include chemical methods, simple biochemical methods, two-stage anaerobic processes, and biological desulfurization technology. The presence of high sulfate makes it difficult to remove organic matter from the wastewater. Antibiotics, such as penicillin and clavulanic acid, are usually produced through bio-fermentation. The fermentation broth after fermentation is purified through extraction-back-extraction. The aqueous phase separated in the extraction step, after solvent recovery by distillation, becomes the degreasing aqueous phase (waste acid water). The degreasing aqueous phase contains a large amount of organic matter, and COD, ammonia nitrogen, and total nitrogen are high. Because sulfuric acid is used in the acidification process before extraction, SO4 in the degreasing aqueous phase is also high. 2- The content is also relatively high.

[0003] Currently, the mainstream treatment process for the degreasing aqueous phase is as follows: evaporation and concentration via mechanical vapor recompression (MVR), followed by spray drying in a spray drying tower, with the resulting solid treated as hazardous waste. The multi-stage MVR evaporation, spray drying, and hazardous waste disposal processes in these mainstream processes are extremely costly. Furthermore, high-COD wastewater typically undergoes methanogenesis in an anaerobic reactor to remove COD. However, the high sulfate content in the degreasing aqueous phase causes sulfate reduction to take precedence over methanogenesis, inhibiting COD removal. Therefore, conventional anaerobic-anoxic-aerobic biological treatment methods cannot be used for the degreasing aqueous phase. Thus, there is an urgent need to develop an improved process for effectively removing COD, ammonia nitrogen, and total nitrogen from the degreasing aqueous phase. Summary of the Invention

[0004] To address the aforementioned problems, this invention provides a treatment process for high-sulfate organic wastewater, combining electrodialysis with a fully biological treatment method, achieving green, energy-saving, and low-cost solutions. The sulfur autotrophic denitrification process of this invention does not require additional sulfur filler, is completely self-sufficient, and achieves resource recycling.

[0005] To achieve the above-mentioned objectives, the present invention adopts the following technical solution:

[0006] A process for treating high-sulfate organic wastewater includes the following steps:

[0007] S1. Electrodialysis is performed on high-sulfate organic wastewater to obtain a concentrated solution rich in sulfate and a desalinated solution rich in COD;

[0008] S2. The desalinated liquid is subjected to biochemical treatment to obtain sulfur and a first type of dischargeable water;

[0009] The concentrated solution was subjected to biochemical oxidation and nitrification reactions using halophilic bacteria to obtain a nitrated solution.

[0010] S3. The nitrified liquid is fed into anaerobic sludge to carry out sulfur autotrophic denitrification reaction to obtain a second effluent; the packing material for the sulfur autotrophic denitrification reaction is the sulfur.

[0011] Compared to existing technologies, this invention first concentrates high-sulfate organic wastewater through electrodialysis: sulfate, a portion of COD, ammonia nitrogen, and total nitrogen migrate simultaneously to the clean water side, forming a concentrated solution rich in sulfate; the salinity and COD of the high-sulfate organic wastewater are significantly reduced, yielding a desalinated solution rich in COD, which can meet standards with conventional biological treatment. For the concentrated solution rich in sulfate, this invention employs a halophilic bacteria process to achieve ammonia nitrogen oxidation under "high salt without dilution" conditions, reducing NH4+. + -N is converted to NO3 - -N; the effluent has a high concentration of nitrate nitrogen and is rich in sulfate. This invention further utilizes sulfur particles recovered from the desalination solution in the biological treatment unit as filler and electron donors. A biofilm forms on the sulfur surface, and autotrophic bacteria thrive on S... 0 NO3 as an electron donor - -N is reduced to N2 without the need for an external carbon source, significantly reducing operating costs and avoiding the risk of secondary pollution, ultimately achieving total nitrogen emission standards while completing the closed-loop utilization of sulfur resources.

[0012] Preferably, in step S1, the SO4 in the high-sulfate organic wastewater 2- The content is 10~30 g / L, the COD content is 50~80 g / L, the total nitrogen content is 2~8 g / L, the ammonia nitrogen content is 1~5 g / L, and the total phosphorus content is 0.1~1 g / L.

[0013] More preferably, the high-sulfate organic wastewater is the degreased aqueous phase generated during the extraction of drugs using the extraction method in the fermentation pharmaceutical production process.

[0014] More preferably, the drug is an antibiotic. Even more preferably, the antibiotic includes penicillin or clavulanic acid.

[0015] Preferably, the pretreatment prior to the electrodialysis includes: filtering the high-sulfate organic wastewater through a 0.4-0.5 μm filter membrane and adjusting the pH to 3.5-4.5.

[0016] Preferably, in step S1, the electrodialysis is performed using a constant voltage current, with a voltage of 45~55 V and a current density of 160~200 mA / cm². 2 .

[0017] More preferably, in step S1, the electrodialysis is performed using a constant voltage current of 50 V.

[0018] Preferably, in step S1, the electrodialysis membrane is an acid-resistant homogeneous membrane, and the electrode solution includes Na2SO4 with a mass concentration of 2% to 4%; the concentration factor of the sulfate in the electrodialysis is greater than 1.3.

[0019] More preferably, in step S1, the polar liquid is 3% Na2SO4.

[0020] Preferably, in step S1, the electrodialysis is stopped when the conductivity of the desalination solution drops to 2-4 mS / cm, the total dissolved solids (TDS) drops to 1-3 g / L, or the current drops to 8%-12% of the initial value.

[0021] More preferably, in step S1, the electrodialysis is stopped when the conductivity of the desalination solution drops to 3 mS / cm, the TDS drops to 2 g / L, or the current drops to 10% of the initial value.

[0022] Preferably, in step S1, the concentrated liquid contains SO4 2- The content is 15~35 g / L, the COD content is 5~12 g / L, the total nitrogen content is 0.5~3 g / L, the ammonia nitrogen content is 0.5~2 g / L, and the total phosphorus content is 0.1~2 g / L.

[0023] Preferably, in step S1, the SO4 in the desalination solution... 2- The content is 0.5~1.5 g / L, the COD content is 45~75 g / L, the total nitrogen content is 1.5~2.5 g / L, the ammonia nitrogen content is 0.5~1.5 g / L, and the total phosphorus content is 0.1~5 g / L.

[0024] Preferably, in step S2, the specific steps of the biochemical treatment include: subjecting the desalinated liquid to anaerobic reaction, anoxic reaction and aerobic reaction in sequence.

[0025] More preferably, in step S2, the anaerobic reaction is equipped with SO4 2- A desulfurization device for reducing sulfur to sulfur, wherein the method for preparing sulfur includes the following steps:

[0026] (1) Rinse the desulfurization unit to obtain sulfur slurry;

[0027] (2) The sulfur slurry is precipitated, concentrated, and dehydrated to obtain sulfur paste;

[0028] (3) The sulfur paste is granulated, cooled, dehydrated, and sieved;

[0029] The sulfur has a particle size of 5-8 mm.

[0030] More preferably, the desulfurization device is a desulfurization tower, and the sulfur has a particle size of 6-7 mm.

[0031] In the anaerobic reaction stage of the biochemical treatment process, this invention removes SO4 from the COD-rich desalination liquid using a desulfurization tower. 2- Restore to S 0 Using recovered sulfur particles as filler and electron donors, autotrophic bacteria feed on S... 0 NO3 as an electron donor - -N is reduced to N2 without the need for an external carbon source, which can achieve both compliance with total nitrogen emission standards and closed-loop utilization of sulfur resources.

[0032] Preferably, in step S2, the first dischargeable water has a COD content of less than 500 mg / L, a total nitrogen content of less than 15 mg / L, an ammonia nitrogen content of less than 10 mg / L, and a total phosphorus content of less than 5 mg / L.

[0033] Preferably, in step S2, the nitration reaction is followed by vertical sedimentation.

[0034] Preferably, in step S2, the COD content in the nitrification liquid is 0.1~1.5 g / L, the total nitrogen content is 1~2 g / L, the ammonia nitrogen content is 1~5 mg / L, and the total phosphorus content is 1~5 mg / L.

[0035] Preferably, in step S3, the sulfur autotrophic denitrification reaction is carried out in an upflow anaerobic sludge blanket reactor (UASB), and the reaction conditions include: no aeration, dissolved oxygen (DO) < 0.2 mg / L, and hydraulic retention time of 6-10 h; the volume of sulfur accounts for approximately 75%-85% of the capacity of the upflow anaerobic sludge blanket reactor, and the porosity is 0.4-0.6.

[0036] Further preferably, the conditions for the sulfur autotrophic denitrification reaction include: no aeration, dissolved oxygen (DO) < 0.1 mg / L, hydraulic retention time of 8 hours; the amount of sulfur used accounts for 80% to 82% of the capacity of the upflow anaerobic sludge bed reactor, and the porosity is 0.45.

[0037] The high upward flow rate of this invention helps to flush away trace amounts of sulfides and biofilm that may be generated during the reaction, preventing filter bed clogging and facilitating the formation of an active biofilm of suitable thickness. This invention does not involve aeration during sulfur autotrophic denitrification, strictly controlling the dissolved oxygen concentration in the reactor to ensure the system is in an optimal anoxic state, promoting the dominant growth and metabolism of sulfur autotrophic denitrifying bacteria.

[0038] Preferably, in step S2, the COD content of the second effluent is 450~550 mg / L, the total nitrogen content is 10~15 mg / L, the ammonia nitrogen content is 1~5 mg / L, and the total phosphorus content is 0.1~2 mg / L.

[0039] This invention separates high-sulfate organic wastewater into a sulfate-rich concentrate and a COD-rich desalination solution via electrodialysis under an electric field. Under the electric field of electrodialysis, sulfate ions gradually transfer from the high-sulfate organic wastewater to the purified water. The high-sulfate organic wastewater ultimately becomes the desalination solution, which enters an anaerobic + A / O reactor and can be discharged after conventional biological treatment. The sulfate concentration in the purified water gradually increases, eventually becoming a high-salt concentrate rich in sulfate, along with some transferred COD, ammonia nitrogen, and total nitrogen. The high-salt concentrate is treated biologically by halophilic bacteria tolerant to high salt concentrations, oxidizing COD and ammonia nitrogen. The ammonia nitrogen is oxidized to total nitrogen, which is then removed by a sulfur autotrophic denitrification process. This invention uses recovered sulfur granules as packing material and electron donors for autotrophic bacteria, converting NO3... - -N is reduced to N2 without the need for an external carbon source, thus achieving both total nitrogen emission standards and sulfur resource recycling. Attached Figure Description

[0040] Figure 1 This is a flowchart of the aqueous phase treatment process for clavulanic acid defatting in an embodiment of the present invention. Detailed Implementation

[0041] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be described in detail below with reference to embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention.

[0042] The preparation process of sulfur used in the specific embodiments of the present invention includes the following steps:

[0043] (1) Sulfur acquisition: Sulfur slurry is obtained by periodically flushing the biological desulfurization tower in the biochemical treatment unit.

[0044] (2) Separation and dehydration: After the sulfur slurry is precipitated and concentrated, it is dehydrated into sulfur paste by a filter press.

[0045] (3) Granulation: The sulfur paste is granulated by a granulator (such as a drum granulator) and then screened.

[0046] In this specific embodiment of the invention, the halophilic bacteria used are laboratory-acclimated sludge, wherein the sludge is a mixture of sludge from the secondary sedimentation tank of a wastewater treatment plant and sludge from a salt field. This invention does not limit the sludge acclimation method; conventional practices in the field are sufficient.

[0047] To better illustrate the present invention, further examples are provided below.

[0048] Example 1

[0049] This embodiment provides a clavulanic acid degreasing aqueous phase treatment process (see...). Figure 1 ), including the following steps:

[0050] S1. Electrodialysis section: 14.8 kg of clavulanic acid-degreased aqueous phase (containing COD of 62758 mg / L, total nitrogen of 5281 mg / L, ammonia nitrogen of 2617 mg / L, total phosphorus of 550 mg / L, and sulfate of 18200 mg / L) was used as the solution to be treated. It was first filtered through a 0.45 μm filter membrane and the pH was adjusted to 3.8. Then, electrodialysis was carried out at a constant voltage of 50 V. When the conductivity of the purified water (RO water, initial mass of 11 kg) side dropped to 3 mS / cm, electrodialysis was stopped, and a concentrated solution rich in sulfate and a desalinated solution rich in COD were obtained.

[0051] RO water is water purified using reverse osmosis technology. The electrodialysis membrane is an acid-resistant homogeneous membrane with 60 membrane pairs (total membrane area 7.2 m²). 2 The total voltage was 50 V, with a single-pair voltage of approximately 0.83 V. The electrode solution used was 3% Na₂SO₄, with independent circulation and a flow rate of 6 cm / s. During electrodialysis, the volumes of the desalinated and concentrated solutions were measured, and conductivity, TDS, COD, and pH were also measured.

[0052] S2. Halophilic Bacteria Section: The pH of the COD-rich desalinated solution is adjusted to approximately 7 and then fed into the biological treatment unit (including sequentially connected anaerobic, anoxic, and aerobic zones). The effluent meets industrial wastewater discharge standards (COD content below 500 mg / L, total nitrogen content below 15 mg / L, ammonia nitrogen content below 10 mg / L, and total phosphorus content below 5 mg / L). The anaerobic zone is equipped with SO42-... 2- The final product is converted into sulfur in a desulfurization tower. This invention does not limit the biochemical treatment unit; conventional methods in the field can be used.

[0053] The sulfate-rich concentrate is fed into a halophilic bacteria biological treatment unit (comprising sequentially connected anoxic and aerobic zones), operating as an A / O system. The electrodialysis concentrate sequentially passes through section A (anoxic), section O (aerobic), vertical flow sedimentation, and effluent, yielding a concentrated solution where ammonia nitrogen has been converted to nitrate nitrogen, including NO3-. - -N content ≥1000 mg / L.

[0054] S3. Sulfur Autotrophic Denitrification Section: A sulfur autotrophic denitrification UASB reactor was constructed. The reactor body was cylindrical, with a total height of 2.0 meters and a diameter of 25 centimeters. The reactor was filled with 80 liters of sulfur granules, with a packing height of 1.6 meters. The particle size of the sulfur granules ranged from 5 to 8 millimeters, and the porosity of the filter layer formed by the accumulation was approximately 0.45. The concentrated liquid obtained in step S2 was used as the feed water and introduced into the UASB reactor, with bottom entry and top exit, continuous feed water flow, no aeration, dissolved oxygen (DO) < 0.1 mg / L; the hydraulic retention time was 8 hours, yielding wastewater that met the discharge standards.

[0055] Example 2

[0056] This embodiment provides a clavulanic acid degreasing aqueous phase treatment process, including the following steps:

[0057] S1. Electrodialysis section: 89 kg of clavulanic acid defatted aqueous phase (containing COD of 75825 mg / L, total nitrogen of 5485 mg / L, ammonia nitrogen of 1842 mg / L, total phosphorus of 351 mg / L, and sulfate of 18625 mg / L) was used as the solution to be treated. It was first filtered through a 0.45 μm filter membrane and the pH was adjusted to 3.8. Then, electrodialysis was carried out at a constant voltage of 50 V. When the current dropped to 10% of the initial value, electrodialysis was stopped, and a concentrated solution rich in sulfate and a desalinated solution rich in COD were obtained.

[0058] RO water is water purified using reverse osmosis technology. The electrodialysis membrane is an acid-resistant homogeneous membrane with 60 membrane pairs (total membrane area 7.2 m²). 2 The total voltage was 50 V, with a single-pair voltage of approximately 0.83 V. The electrode solution used was 3% Na₂SO₄, with independent circulation and a flow rate of 6 cm / s. During electrodialysis, the volumes of the desalinated and concentrated solutions were measured, and conductivity, TDS, COD, and pH were also measured.

[0059] S2. Halophilic Bacteria Section: The pH of the COD-rich desalinated solution is adjusted to approximately 7 and then fed into the biological treatment unit (including sequentially connected anaerobic, anoxic, and aerobic zones). The effluent meets industrial wastewater discharge standards (COD content below 500 mg / L, total nitrogen content below 15 mg / L, ammonia nitrogen content below 10 mg / L, and total phosphorus content below 5 mg / L). The anaerobic zone is equipped with SO42-... 2- The final product is converted into sulfur in a desulfurization tower. This invention does not limit the biochemical treatment unit; conventional methods in the field can be used.

[0060] The sulfate-rich concentrate is fed into a halophilic bacteria biological treatment unit (comprising sequentially connected anoxic and aerobic zones), operating as an A / O system. The electrodialysis concentrate sequentially passes through section A (anoxic), section O (aerobic), vertical flow sedimentation, and effluent, yielding a concentrated solution where ammonia nitrogen has been converted to nitrate nitrogen, including NO3-. - -N content ≥1000 mg / L.

[0061] S3. Sulfur Autotrophic Denitrification Section: A sulfur autotrophic denitrification UASB reactor was constructed. The reactor body was cylindrical, with a total height of 2.0 meters and a diameter of 25 centimeters. The reactor was filled with 80 liters of sulfur granules, with a packing height of 1.6 meters. The particle size of the sulfur granules ranged from 5 to 8 millimeters, and the porosity of the filter layer formed by the accumulation was approximately 0.45. The concentrated liquid obtained in step S2 was used as the feed water and introduced into the UASB reactor, with bottom entry and top exit, continuous feed water flow, no aeration, dissolved oxygen (DO) < 0.1 mg / L; the hydraulic retention time was 8 hours, yielding wastewater that met the discharge standards.

[0062] Detection Example 1

[0063] 1. Processing effect of the electrodialysis stage

[0064] The water quality indicators of the degreased aqueous phase of clavulanic acid were tested before and after electrodialysis treatment according to the methods described in Examples 1 and 2. The results are shown in Table 1.

[0065] Table 1. Changes in water quality indicators before and after electrodialysis treatment

[0066]

[0067] As shown in Table 1, after electrodialysis treatment of the clavulanic acid degreasing aqueous phase according to the methods described in Examples 1 and 2, the sulfate concentration in the degreasing aqueous phase was significantly reduced, falling below 1000 mg / L, and no longer inhibiting the anaerobic methanogenesis process. In particular, in Example 1, the sulfate concentration decreased to 776 mg / L, with 96% of the total sulfate in the degreasing aqueous phase being transferred to the clear water end as a concentrated solution, while the COD transferred thereafter was only 12%.

[0068] 2. Effect of halophilic bacteria segment processing

[0069] The water quality indicators of the effluent concentrate from the electrodialysis section were tested before and after treatment with halophilic bacteria according to the methods described in Examples 1 and 2. The results are shown in Table 2.

[0070] Table 2 Changes in water quality indicators before and after halophilic bacteria treatment

[0071]

[0072] As shown in Table 2, after the electrodialysis section effluent concentrate was treated with halophilic bacteria according to the methods described in Examples 1 and 2, the concentrations of COD, total nitrogen, ammonia nitrogen, and total phosphorus in the water were significantly reduced. This indicates that halophilic bacteria can tolerate high sulfate concentrations and significantly reduce COD, ammonia nitrogen, total nitrogen, and total phosphorus under these conditions, thus achieving the oxidation of ammonia nitrogen to total nitrogen and biological phosphorus removal.

[0073] 3. Treatment effect of the sulfur autotrophic denitrification stage process

[0074] The water quality indicators of the halophilic bacteria section before and after treatment were tested according to the methods described in Examples 1 and 2. The results are shown in Table 3.

[0075] Table 3 Changes in water quality indicators before and after different treatment processes

[0076]

[0077] As shown in Table 3, after treating the effluent from the halophilic bacteria stage according to the methods described in Examples 1 and 2, the concentrations of COD, total nitrogen, ammonia nitrogen, and total phosphorus in the water were further reduced, indicating that the sulfur autotrophic denitrification process of the present invention can effectively reduce the nitrates produced in the effluent from the halophilic bacteria stage. The final total nitrogen concentration in the effluent all met the current wastewater discharge standards (TN < 15 mg / L), demonstrating that the present invention, by combining electrodialysis-halophilic bacteria process-sulfur autotrophic denitrification process, can achieve efficient treatment of the clavulanic acid degreasing aqueous phase.

[0078] 4. Cost Comparison

[0079] The energy consumption and operating cost of the combined process of the present invention (the complete process of Example 1) were compared with those of the traditional MVR evaporation, spray drying and hazardous waste disposal combined process. The results are shown in Table 4.

[0080] Table 4 Energy consumption and operating costs of different processes

[0081]

[0082] As shown in Table 4, the combined process of this invention works synergistically with each other, achieving an 80% reduction in energy consumption and an 86% reduction in operating costs compared to the traditional MVR evaporation process, demonstrating good environmental benefits and social responsibility value.

[0083] 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 or improvements made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A treatment process for high-sulfate organic wastewater, characterized in that, Includes the following steps: S1. The high-sulfate organic wastewater is filtered through a 0.4~0.5μm filter membrane and the pH is adjusted to 3.5~4.5; then electrodialysis is performed, wherein the sulfate concentration factor of the electrodialysis is greater than 1.3, to obtain a sulfate-rich concentrated solution and a COD-rich desalinated solution. The high-sulfate organic wastewater is the degreased aqueous phase generated during the extraction of drugs using the extraction method in the fermentation pharmaceutical production process; the high-sulfate organic wastewater contains SO4 2- The content is 10~30 g / L, COD content is 50~80 g / L, total nitrogen content is 2~8 g / L, ammonia nitrogen content is 1~5 g / L, and total phosphorus content is 0.1~1 g / L; SO4 in the concentrated liquid 2- The content is 15~35 g / L, the COD content is 5~12 g / L, the total nitrogen content is 0.5~3 g / L, the ammonia nitrogen content is 0.5~2 g / L, and the total phosphorus content is 0.1~2 g / L; SO4 in the desalination solution 2- The content is 0.5~1.5 g / L, the COD content is 45~75 g / L, the total nitrogen content is 1.5~5 g / L, the ammonia nitrogen content is 0.5~1.5 g / L, and the total phosphorus content is 0.1~5 g / L; S2. The desalinated liquid is subjected to biochemical treatment to obtain sulfur and a first type of dischargeable water; The concentrated solution was subjected to biochemical oxidation and nitrification reactions using halophilic bacteria to remove COD and obtain nitrified solution. S3. The nitrified liquid is fed into anaerobic sludge to carry out sulfur autotrophic denitrification reaction to obtain a second effluent; the packing material for the sulfur autotrophic denitrification reaction is the sulfur.

2. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, In step S1, the electrodialysis is performed using a constant voltage current, with a voltage of 45-55 V and a current density of 160-200 mA / cm². 2 The electrodialysis membrane is an acid-resistant homogeneous membrane, and the electrode solution includes Na2SO4 with a mass concentration of 2% to 4%.

3. The treatment process for high-sulfate organic wastewater according to claim 2, characterized in that, In step S1, the electrodialysis is stopped when the conductivity of the desalination solution drops to 2-4 mS / cm, the total dissolved solids drop to 1-3 g / L, or the current drops to 8%-12% of the initial value.

4. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, In step S2, the specific steps of the biochemical treatment include: subjecting the desalinated liquid to anaerobic reaction, hypoxic reaction and aerobic reaction in sequence.

5. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, In step S2, the biochemical treatment includes a desulfurization device, and the method for preparing sulfur includes the following steps: (1) Rinse the desulfurization unit to obtain sulfur slurry; (2) The sulfur slurry is precipitated, concentrated, and dehydrated to obtain sulfur paste; (3) The sulfur paste is granulated and sieved; The sulfur has a particle size of 5-8 mm.

6. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, In step S2, the COD content in the nitrification liquid is 0.1~1.5 g / L, the total nitrogen content is 1~2 g / L, the ammonia nitrogen content is 1~5 mg / L, and the total phosphorus content is 1~5 mg / L.

7. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, In step S3, the sulfur autotrophic denitrification reaction is carried out in an upflow anaerobic sludge bed reactor. The reaction conditions include: no aeration, dissolved oxygen (DO) < 0.2 mg / L, and hydraulic retention time of 6-10 h. The volume of sulfur accounts for 75%-85% of the capacity of the upflow anaerobic sludge bed reactor, and the porosity is 0.4-0.

6.

8. The treatment process for high-sulfate organic wastewater according to claim 1, characterized in that, The drug in question is an antibiotic.

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