Antibiotic wastewater pretreatment system

Abstract

The utility model relates to sewage treatment technical field, concretely is antibiotic sewage pretreatment system. The system includes the wastewater collection jar, the reaction kettle, the wastewater transfer tank, at least one iron carbon reactor, at least one flocculation reactor, the vertical flow sedimentation tank, the wastewater regulating jar and three effect evaporator connected in proper order, and the reaction kettle is connected with lime slurry and sulfuric acid feeding jar, and is equipped with cooling coil and stirring device, and realizes solid -liquid separation and liquid phase reflux through plate and frame filter press, and the flocculation reactor is connected with sodium hydroxide, PAC and PAM feeding jar, and the iron carbon reactor is equipped with iron carbon filler and aeration pipe, and the sludge storage tank of vertical flow sedimentation tank communicates with the reaction kettle, and the relevant feeding jar is equipped with metering pump, and the conveying pipeline is equipped with drive pump, and the liquid storage jar is equipped with liquid level meter, and the wastewater regulating jar and three effect evaporator are connected with biochemical system. The system can efficiently degrade antibiotic toxicity, improve sewage biochemical property, reduce the quantity of hazardous waste, adapt to different water quality, and create conditions for subsequent biochemical treatment.

Description

Technical Field

[0001] This utility model relates to the field of wastewater treatment technology, specifically to a pretreatment system for antibiotic wastewater. Background Technology

[0002] The production of antibiotics generates a large amount of characteristic wastewater, which exhibits significant complexity in quality: COD concentrations are generally as high as 10. 5 -2×10 5 The TP concentration in wastewater from the production of some phosphorus-containing antibiotics (such as fosfomycin) can reach 3000-4000 mg / L. Residual antibiotics (such as penicillin G and ceftriaxone) and their degradation intermediates (such as 6-aminopenicillanic acid) in the wastewater have strong biotoxicity and will inhibit the activity of nitrifying bacteria and aerobic heterotrophic bacteria in the subsequent biochemical system. As a result, the COD removal rate of traditional biochemical treatment is less than 50%, and the BOD / COD ratio is consistently lower than 0.2, which cannot meet the requirements of the "Water Pollutant Discharge Standard for Fermentation Pharmaceutical Industry" (GB21903-2008).

[0003] Currently, the pretreatment of antibiotic wastewater mainly employs single or simple combination processes, which have significant technical shortcomings: Physical treatment methods, such as activated carbon adsorption, can only remove some organic matter. The adsorbent saturation cycle is short (usually 7-10 days), regeneration requires high temperature (800-900℃), resulting in high operating costs and the inability to degrade antibiotic toxicity. Membrane filtration is susceptible to high TDS (90,000-100,000 mg / L), leading to membrane fouling. The flux decline rate exceeds 20% per month, and maintenance costs are high.

[0004] Chemical treatment methods: The traditional Fenton oxidation method requires the addition of large amounts of ferrous sulfate (500-800 mg / L) and hydrogen peroxide (300-500 mg / L), with the cost of the reagents exceeding 8 yuan / ton of water. Moreover, the iron-containing sludge produced has a water content of over 90%, increasing the amount of hazardous waste to be disposed of. The simple acid-base neutralization method can only adjust the pH and cannot remove antibiotic residues, nor does it improve biochemical properties.

[0005] Existing combined processes have the following drawbacks: Some systems use "neutralization + flocculation" pretreatment, but do not combine it with iron-carbon oxidation-reduction reaction, which fails to destroy the toxic structures of antibiotics such as the β-lactam ring and tetracycline skeleton, resulting in the subsequent biochemical system still being inhibited; moreover, most systems do not design sludge recycling and liquid phase reflux, and the phosphorus sludge (calcium phosphate) produced in the reactor is directly treated as hazardous waste with a water content of over 85% and a large volume. At the same time, the liquid phase after plate and frame filter press (containing unreacted phosphorus) is directly discharged, resulting in a TP removal rate of less than 60%, which still requires subsequent deep phosphorus removal.

[0006] Furthermore, existing systems have poor adaptability to water quality fluctuations: when the TP concentration in antibiotic wastewater suddenly increases from 170 mg / L (crystallization mother liquor) to 3630 mg / L (extraction aqueous phase), stable treatment cannot be achieved by flexibly adjusting process parameters (lime slurry dosage, iron-carbon reaction pH), easily leading to problems such as substandard phosphorus removal or waste of reagents. Therefore, there is an urgent need to develop a highly efficient pretreatment system integrating "toxicity degradation - biochemical enhancement - resource recycling - hazardous waste reduction" to address the pain points of existing technologies. Utility Model Content

[0007] In view of the shortcomings of the prior art, the purpose of this utility model is to provide an antibiotic wastewater pretreatment system that, through a two-stage iron-carbon reaction, achieves a removal rate of antibiotic residues ≥90%, with a toxic structure destruction rate of β-lactam antibiotics exceeding 95%; the inhibition rate of Escherichia coli in the treated wastewater is reduced from 80% to below 10%, ensuring the microbial activity of the subsequent A / O biochemical system, and maintaining a COD removal rate of over 95%.

[0008] This utility model is achieved using the following technical solution: The antibiotic wastewater pretreatment system comprises, in sequence, a wastewater collection tank, a reaction vessel, a wastewater transfer tank, at least one iron-carbon reactor, at least one flocculation reactor, a vertical flow sedimentation tank, a wastewater regulating tank, and a triple-effect evaporator connected by pipelines. The reaction vessel's feed inlet is connected to a lime slurry feed tank and a sulfuric acid feed tank via pipelines. A cooling coil is installed on the outside of the reaction vessel, and a stirring device is installed inside. The solid phase outlet of the reaction vessel is connected to a plate and frame filter press via pipelines. The liquid phase outlet of the plate and frame filter press is returned to the reaction vessel via pipelines, and the solid phase outlet is connected to a hazardous waste tank via pipelines. The flocculation reactor's feed inlet is connected to a sodium hydroxide feed tank, a PAC feed tank, and a PAM feed tank via pipelines. A stirring device is installed inside the flocculation reactor. The solid phase outlet of the vertical flow sedimentation tank is connected to a sludge storage tank via pipelines, and the outlet of the sludge storage tank is connected to the reaction vessel via pipelines. The iron-carbon reactor contains iron-carbon packing material and aeration pipes, and the aeration pipes are connected to a Roots blower via pipelines.

[0009] Metering pumps are installed on the outlet pipelines of the lime slurry feeding tank, sulfuric acid feeding tank, sodium hydroxide feeding tank, PAC feeding tank, and PAM feeding tank; drive pumps are installed on the pipelines of the solid phase outlet of the reactor, the outlet of the wastewater transfer tank, the solid phase outlet of the vertical flow sedimentation tank, and the liquid phase outlet of the plate and frame filter press; level gauges are installed in the wastewater collection tank, the wastewater transfer tank, the wastewater regulating tank, and the sulfuric acid feeding tank; the outlets of the wastewater regulating tank and the triple-effect evaporator are respectively connected to the biochemical system through pipelines.

[0010] The iron-carbon reactor consists of two reactors, namely iron-carbon reactor #1 and iron-carbon reactor #2. The particle size of the iron-carbon packing material inside the two reactors is 5-10 mm, and the mass ratio of elemental iron to activated carbon in the iron-carbon packing material is 3:1-5:1.

[0011] There are two flocculation reactors, namely Flocculation Reactor No. 1 and Flocculation Reactor No. 2.

[0012] The medium in the cooling coil is circulating water, with an inlet water temperature of 15-20℃ and an outlet water temperature not exceeding 35℃.

[0013] The stirring speed of the stirring device in the reactor and flocculation reactor is 30-60 rpm; the stirring speed of the stirring device in the lime slurry feeding tank, sodium hydroxide feeding tank, PAC feeding tank and PAM feeding tank is 15-30 rpm.

[0014] The metering pump has a flow rate adjustment accuracy of ±1% and a maximum output pressure of not less than 0.6 MPa.

[0015] The vertical flow sedimentation tank has a central water inlet and peripheral water outlet structure, with a cone bottom angle of 60-90° and an effective water depth to diameter ratio of 1.2-1.5.

[0016] The airflow adjustment range of the Roots blower is 0.5-1.0 m³ / h. 3 / (m 2 h), wind pressure is 30-50 kPa.

[0017] Reactor Unit: Lime slurry (concentration 10-15%) is added to the reactor via a lime slurry feeding tank, reacting with phosphate ions in the wastewater to form calcium phosphate precipitate, while simultaneously neutralizing acidic wastewater (pH adjusted from 1-2 to 7-8); a sulfuric acid feeding tank is used for fine-tuning the pH (pH needs to be lowered to around 4 before the iron-carbon reaction); an external cooling coil controls the reaction temperature at 25-30℃ via circulating water to avoid reagent decomposition caused by the exothermic neutralization reaction; an internal stirring device ensures uniform reaction, with a reaction time of 30-60 minutes; a plate and frame filter press separates the solid and liquid phases after the reaction, sending the solid phase (phosphorus sludge) to a hazardous waste tank, while the liquid phase is returned to the reactor to improve the phosphorus removal rate (TP removal rate ≥98%).

[0018] Iron-carbon reaction unit: Iron-carbon reactors #1 and #2 are connected in series. The internal iron-carbon packing produces Fe through micro-electrolysis. 2+ [H] disrupts the toxic functional groups of antibiotics (β-lactam ring opening, amino oxidation); the Roots blower provides aeration, which on the one hand promotes Fe... 2+ Oxidized to Fe 3+(Enhancing flocculation effect), on the other hand, improving the contact efficiency between wastewater and packing material, with a residence time of 2-4 hours; sulfuric acid is added to the No. 2 iron-carbon reactor to maintain the pH at around 4, ensuring the continuous progress of the micro-electrolysis reaction.

[0019] Flocculation and sedimentation unit: In flocculation reactors #1 and #2, the pH is adjusted to 7-8 by the sodium hydroxide feeding tank, and 50-100 mg / LPAC (polyaluminum chloride, 10% concentration) is added by the PAC feeding tank to form primary flocs. 2-5 mg / LPAM (polyacrylamide, molecular weight 8-12 million) is added by the PAM feeding tank to promote floc aggregation. The two-stage flocculation ensures a suspended solids removal rate of ≥95%. The vertical flow sedimentation tank adopts a central water inlet design with a residence time of 1-2 hours. The flocs settle under gravity, and the sludge is sent to the sludge storage tank and then returned to the reactor to reduce the sludge moisture content (from 85% to below 60%), thus reducing the volume of hazardous waste.

[0020] Control and Biochemical Connection Unit: The wastewater regulating tank monitors the water volume through a level gauge and adjusts the pH (7-8) and temperature (25-30℃). Wastewater that meets the water quality standards is directly sent to the biochemical system; wastewater that does not meet the standards is sent to a triple-effect evaporator to reduce the water volume through evaporation and concentration (concentration ratio 3-5 times). The concentrated liquid is then sent to the biochemical system to reduce the biochemical treatment load; metering pumps ensure the accuracy of reagent dosing and drive pumps to realize wastewater transfer between units.

[0021] Compared with the prior art, the beneficial effects of this utility model are: (1) Through a two-stage iron-carbon reaction, the removal rate of antibiotic residues is ≥90%, of which the toxic structure destruction rate of β-lactam antibiotics is over 95%; the inhibition rate of Escherichia coli in the treated wastewater is reduced from 80% to below 10%, ensuring the microbial activity of the subsequent A / O biochemical system, and the COD removal rate is stable at over 95%. The iron-carbon reaction converts the recalcitrant organic matter in the wastewater into easily biodegradable small molecules, increasing the BOD / COD ratio from 0.1-0.15 to 0.3-0.35, meeting the influent requirements of the biochemical system; in Example 1, the treated wastewater directly enters the A / O system, with a total COD removal rate of 98% and an effluent COD ≤500mg / L.

[0022] (2) Liquid phase reflux in the plate and frame filter press increases the TP removal rate from 60% in the traditional process to over 98%; after the sludge is returned to the reactor, the moisture content drops from 85% to below 60%, the volume of hazardous waste is reduced by 40%, and the hazardous waste disposal cost per ton of wastewater is reduced by 35%. By precisely controlling the dosage of reagents through metering pumps, both high-phosphorus and low-phosphorus wastewater can be treated to meet the standards, and reagent waste is reduced by 15%; the triple-effect evaporator is linked with the biochemical system, and high-concentration wastewater is concentrated and regenerated, saving 25% of aeration energy consumption compared to direct biochemical treatment. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the structure of the antibiotic wastewater pretreatment system of this utility model; In the diagram: 1. Wastewater collection tank; 2. Reactor; 3. Wastewater transfer tank; 4. Iron-carbon reactor #1; 5. Iron-carbon reactor #2; 6. Flocculation reactor #1; 7. Flocculation reactor #2; 8. Vertical flow sedimentation tank; 9. Wastewater regulating tank; 10. Triple-effect evaporator; 11. Lime slurry feeding tank; 12. Sulfuric acid feeding tank; 13. Plate and frame filter press; 14. Hazardous waste pool; 15. Sodium hydroxide feeding tank; 16. PAC feeding tank; 17. PAM feeding tank; 18. Sludge storage tank; 19. Biochemical system; 20. Metering pump; 21. Drive pump; 22. Level gauge; 23. Iron-carbon packing; 24. Aeration pipe; 25. Roots blower; 26. Cooling coil; 27. Stirring device. Detailed Implementation

[0024] To make the objectives and technical solutions of this utility model clearer, the present utility model will be further described in detail below with reference to the accompanying drawings.

[0025] Example 1 like Figure 1 As shown, the antibiotic wastewater pretreatment system includes a wastewater collection tank 1, a reaction vessel 2, a wastewater transfer tank 3, at least one iron-carbon reactor, at least one flocculation reactor, a vertical flow sedimentation tank 8, a wastewater regulating tank 9, and a triple-effect evaporator 10, all connected sequentially by pipelines. The feed inlet of the reaction vessel 2 is connected via pipelines to a lime slurry feed tank 11 and a sulfuric acid feed tank 12. The reaction vessel 2 has a cooling coil 26 on its outer side and a stirring device 27 inside. The solid phase outlet of the reaction vessel 2 is connected via a pipeline to a plate and frame filter press 13. The liquid phase outlet of the plate and frame filter press 13... The outlet flows back to the reactor 2 via a pipeline, and the solid phase outlet is connected to the hazardous waste pool 14 via a pipeline; the feed port of the flocculation reactor is connected to the sodium hydroxide feed tank 15, the PAC feed tank 16, and the PAM feed tank 17 via pipelines respectively, and the flocculation reactor is equipped with a stirring device 27; the solid phase outlet of the vertical flow sedimentation tank 8 is connected to the sludge storage tank 18 via a pipeline, and the outlet of the sludge storage tank 18 is connected to the reactor 2 via a pipeline; the iron-carbon reactor is equipped with iron-carbon packing 23 and aeration pipe 24, and the aeration pipe 24 is connected to the Roots blower 25 via a pipeline.

[0026] Metering pumps 20 are installed on the outlet pipelines of lime slurry feeding tank 11, sulfuric acid feeding tank 12, sodium hydroxide feeding tank 15, PAC feeding tank 16, and PAM feeding tank 17; drive pumps 21 are installed on the pipelines of the solid phase outlet of the reactor 2, the outlet of the wastewater transfer tank 3, the solid phase outlet of the vertical flow sedimentation tank 8, and the liquid phase outlet of the plate and frame filter press 13; level gauges 22 are installed in the wastewater collection tank 1, the wastewater transfer tank 3, the wastewater regulating tank 9, and the sulfuric acid feeding tank 12; the outlets of the wastewater regulating tank 9 and the triple-effect evaporator 10 are respectively connected to the biochemical system 19 through pipelines.

[0027] There are two iron-carbon reactors, namely iron-carbon reactor 4 (No. 1) and iron-carbon reactor 5 (No. 2). The iron-carbon packing material 23 inside the two iron-carbon reactors has a particle size of 5-10 mm, and the mass ratio of elemental iron to activated carbon in the iron-carbon packing material is 3:1-5:1.

[0028] There are two flocculation reactors, namely Flocculation Reactor No. 1 (6) and Flocculation Reactor No. 2 (7).

[0029] The medium in the cooling coil 26 is circulating water, with an inlet water temperature of 15-20℃ and an outlet water temperature not exceeding 35℃.

[0030] The stirring device 27 in the reaction vessel 2 and the flocculation reactor rotates at 60 rpm; the stirring device 27 in the lime slurry feeding tank 11, sodium hydroxide feeding tank 15, PAC feeding tank 16 and PAM feeding tank 17 rotates at 30 rpm.

[0031] The flow rate regulation accuracy of metering pump 20 is ±1%, and the maximum output pressure is not less than 0.6MPa.

[0032] The vertical flow sedimentation tank 8 has a central water inlet and peripheral water outlet structure. The cone bottom angle of the tank body is 60°, and the ratio of the effective water depth to the diameter of the tank is 1.2.

[0033] Example 2: Pretreatment of high-phosphorus antibiotic wastewater (extraction aqueous phase) Influent water quality: The aqueous phase after extraction from penicillin G production, pH=1, COD=109000mg / L, NH3-N=38mg / L, TDS=92700mg / L, TP=3630mg / L, TN=2900mg / L, penicillin G residue=85mg / L, BOD / COD=0.12.

[0034] Treatment process: Neutralization and phosphorus removal → two-stage iron and carbon → two-stage flocculation → sedimentation → conditioning → biochemical / evaporation.

[0035] Detailed operation steps: Wastewater collection and neutralization: Wastewater is collected through wastewater collection tank 1 and sent to reactor 2 by drive pump 21; metering pump 20 of lime slurry feeding tank 11 is turned on, 12% lime slurry (dosage 800mg / L) is added, and stirring device 27 (speed 40rpm) is turned on at the same time. 20℃ circulating water is introduced through cooling coil 26 to control the reaction temperature at 28℃ and react for 45min; sample test pH=7.5, TP drops to 520mg / L.

[0036] Plate and frame filter press and reflux: After the reaction, the mixture is sent to the plate and frame filter press 13 by the drive pump 21 at a pressure of 0.4 MPa and a filtration time of 30 min; the solid phase (phosphorus mud, water content 82%) is sent to the hazardous waste tank 14, and the liquid phase (TP=320 mg / L) is sent to the reaction vessel 2 by the reflux pump. 5% sulfuric acid (dosage 50 mg / L) is added, and the reaction continues for 30 min until the TP drops to 48 mg / L.

[0037] Two-stage iron-carbon reaction: Wastewater is fed into wastewater transfer tank 3, and then pumped into iron-carbon reactor 4 by drive pump 21; Roots blower 25 is turned on with an air volume of 0.8 m³ / h. 3 / (m 2 h), iron-carbon packing material (iron-carbon ratio 4:1, particle size 8mm) reacts with wastewater for 3h, and the pH of the sample is 5.2; the wastewater enters the No. 2 iron-carbon reactor 5, 5% sulfuric acid (dosage 30mg / L) is added, the pH is adjusted to 4.0, and the reaction continues for 2h; the penicillin G residue is 4.1mg / L, COD is 76890mg / L, and BOD / COD is 0.31.

[0038] Two-stage flocculation and sedimentation: Wastewater enters flocculation reactor 6 (No. 1), metering pump 20 of sodium hydroxide feed tank 15 is turned on, 10% sodium hydroxide (dosage 40 mg / L) is added, and pH is adjusted to 7.2; metering pump 20 of PAC feed tank 16 is turned on, 80 mg / L PAC (10% concentration) is added, and stirring (35 rpm) is performed for 15 min; wastewater enters flocculation reactor 7 (No. 2), metering pump 20 of PAM feed tank 17 is turned on, 3 mg / L PAM (molecular weight 10 million) is added, and stirring (25 rpm) is performed for 10 min; wastewater is sent to vertical flow sedimentation tank 8 (cone bottom angle 75°, effective water depth 3 m), and retained for 1.5 h, with a suspended solids removal rate of 96%; sludge is sent to sludge storage tank 18, and then sent to reactor 2 by drive pump 21.

[0039] Conditioning and Biochemical Integration: After sedimentation, the wastewater enters the wastewater conditioning tank 9. The water quality is tested and found to be: pH=7.3, COD=13200mg / L, TP=45mg / L, NH3-N=30mg / L, BOD / COD=0.33. The wastewater is then directly fed into the biochemical system 19 (A / O process) by the drive pump 21. After subsequent biochemical treatment, the effluent COD is 480mg / L, which meets the requirements of GB21903-2008.

[0040] Example 3: Pretreatment of low-phosphorus antibiotic wastewater (centrifuged mother liquor + wash water) Influent water quality: derived from a mixture of crystallization centrifugation mother liquor and wash water from ceftriaxone production, pH=4.5, COD=215000mg / L, NH3-N=390mg / L, TDS=95100mg / L, TP=170mg / L, TN=2500mg / L, ceftriaxone residue=120mg / L, BOD / COD=0.10.

[0041] Processing steps: acid adjustment → two-stage iron-carbon → two-stage flocculation → precipitation → evaporation → biochemical treatment.

[0042] Detailed operation steps: Wastewater collection and acid adjustment: Wastewater is collected through wastewater collection tank 1 and sent to reaction vessel 2 by drive pump 21; turn on metering pump 20 of sulfuric acid feed tank 12, add 5% sulfuric acid (dosage 60mg / L), turn on stirring device 27 (speed 35rpm), control reaction temperature at 25℃ (cooling coil is filled with 18℃ circulating water), react for 20min, pH=4.0 (no need to add lime slurry to avoid the formation of calcium acetate viscous precipitate).

[0043] Two-stage iron-carbon reaction: Wastewater is fed into wastewater transfer tank 3, and then pumped into iron-carbon reactor 4 by drive pump 21; Roots blower 25 has an air volume of 0.6 m³ / h. 3 / (m 2 h), the iron-carbon packing material (iron-carbon ratio 3:1, particle size 6mm) reacted for 3.5h, pH=5.5; the wastewater entered the No.2 iron-carbon reactor 5, 5% sulfuric acid was added (dosage 25mg / L), the pH was adjusted to 4.2, and the reaction was carried out for 2.5h; the ceftriaxone residue was detected to be 5.8mg / L, COD=151230mg / L, and BOD / COD=0.29.

[0044] Two-stage flocculation and sedimentation: Wastewater enters flocculation reactor 6 (1#), 10% sodium hydroxide (50 mg / L) is added, and the pH is adjusted to 7.5; 100 mg / L PAC (10% concentration) is added, and the mixture is stirred (40 rpm) for 15 min; the mixture enters flocculation reactor 7 (2#), 4 mg / L PAC is added, and the mixture is stirred (30 rpm) for 10 min; the mixture is then sent to vertical flow sedimentation tank 8 (cone bottom angle 80°, effective water depth 3.5 m), where it is retained for 2 h, achieving a suspended solids removal rate of 97%. The sludge is sent to sludge storage tank 18 and returned to reactor 2.

[0045] Evaporation and biochemical integration: After sedimentation, the wastewater enters the wastewater equalization tank 9, where COD is measured to be 68,000 mg / L and BOD / COD ratio is 0.32. It is then pumped by the drive pump 21 into the triple-effect evaporator 10 at an evaporation temperature of 60℃, a vacuum of -0.08 MPa, and a concentration ratio of 4:1. The concentrated liquid (COD=272,000 mg / L) is sent to the biochemical system 19 (UASB+A / O process), and the condensate (COD=850 mg / L) is directly discharged after meeting the standards. After subsequent biochemical treatment, the effluent COD of the concentrated liquid is 520 mg / L.

Claims

1. A pretreatment system for antibiotic-containing wastewater, characterized in that, The system includes a wastewater collection tank (1), a reaction vessel (2), a wastewater transfer tank (3), at least one iron-carbon reactor, at least one flocculation reactor, a vertical flow sedimentation tank (8), a wastewater regulating tank (9), and a triple-effect evaporator (10), all connected in sequence by pipelines. The feed inlet of the reaction vessel (2) is connected to a lime slurry feed tank (11) and a sulfuric acid feed tank (12) via pipelines. The reaction vessel (2) is equipped with a cooling coil (26) on its outside and a stirring device (27) inside. The solid phase outlet of the reaction vessel (2) is connected to a plate and frame filter press (13) via pipelines, and the liquid phase outlet of the plate and frame filter press (13) is returned via pipelines. The solid phase outlet is connected to the hazardous waste tank (14) via a pipeline. The feed port of the flocculation reactor is connected to the sodium hydroxide feed tank (15), PAC feed tank (16) and PAM feed tank (17) via pipelines. The flocculation reactor is equipped with a stirring device (27). The solid phase outlet of the vertical flow sedimentation tank (8) is connected to the sludge storage tank (18) via a pipeline. The outlet of the sludge storage tank (18) is connected to the reactor (2) via a pipeline. The iron-carbon reactor is equipped with iron-carbon packing (23) and aeration pipe (24). The aeration pipe (24) is connected to the Roots blower (25) via a pipeline.

2. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, Metering pumps (20) are installed on the outlet pipelines of the lime slurry feeding tank (11), sulfuric acid feeding tank (12), sodium hydroxide feeding tank (15), PAC feeding tank (16) and PAM feeding tank (17); driving pumps (21) are installed on the pipelines of the solid phase outlet of the reactor (2), the outlet of the wastewater transfer tank (3), the solid phase outlet of the vertical flow sedimentation tank (8) and the liquid phase outlet of the plate and frame filter press (13); level gauges (22) are installed in the wastewater collection tank (1), the wastewater transfer tank (3), the wastewater regulating tank (9) and the sulfuric acid feeding tank (12); the outlets of the wastewater regulating tank (9) and the triple-effect evaporator (10) are respectively connected to the biochemical system (19) through pipelines.

3. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, The iron-carbon reactor consists of two reactors, namely, iron-carbon reactor #1 (4) and iron-carbon reactor #2 (5), and the iron-carbon packing material (23) inside the two iron-carbon reactors has a particle size of 5-10 mm, and the mass ratio of elemental iron to activated carbon in the iron-carbon packing material is 3:1-5:

1.

4. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, There are two flocculation reactors, namely Flocculation Reactor No. 1 (6) and Flocculation Reactor No. 2 (7).

5. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, The medium of the cooling coil (26) is circulating water, with an inlet water temperature of 15-20℃ and an outlet water temperature not exceeding 35℃.

6. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, The stirring device (27) in the reactor (2) and flocculation reactor has a rotation speed of 30-60 rpm; the stirring device (27) in the lime slurry feeding tank (11), sodium hydroxide feeding tank (15), PAC feeding tank (16) and PAM feeding tank (17) has a rotation speed of 15-30 rpm.

7. The antibiotic wastewater pretreatment system according to claim 1, characterized in that, The vertical flow sedimentation tank (8) has a central water inlet and peripheral water outlet structure. The cone bottom angle of the tank body is 60-90°, and the ratio of the effective water depth to the diameter in the tank is 1.2-1.5.

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