A pretreatment process for pharmaceutical intermediate wastewater before biochemical treatment

Abstract

This invention discloses a pretreatment process for pharmaceutical intermediate wastewater before biochemical treatment, relating to the technical field of pretreatment of pharmaceutical intermediate wastewater before biochemical treatment. The treatment steps include: determining the required iron and carbon mass level for the wastewater's COD value; adjusting the wastewater's pH value; transporting the wastewater for micro-electrolysis and Fenton oxidation reactions; dynamically controlling the wastewater's pH value within a certain range during the reactions; adjusting the pH value of the effluent after the Fenton oxidation reaction; adding coagulants and flocculants for flocculation and sedimentation; and obtaining the effluent after filtration. This invention, by determining the iron and carbon mass level, can determine the dosage of relevant reagents in subsequent treatment steps and dynamically control the pH value of the iron-carbon micro-electrolysis and Fenton oxidation reactions within a range that yields good treatment results. This allows for a simpler and more efficient reduction of the organic matter concentration in pharmaceutical intermediate wastewater and, to a certain extent, improves its biodegradability.

Description

Technical Field

[0001] This invention relates to the technical field of pretreatment of pharmaceutical intermediate wastewater before biochemical treatment, and particularly to a pretreatment process for pharmaceutical intermediate wastewater before biochemical treatment. Background Technology

[0002] As more and more large pharmaceutical companies continue to optimize their industrial structure, the division of labor in their pharmaceutical processes has become increasingly refined, leading to the rapid development of my country's pharmaceutical intermediate industry. However, this has also resulted in the generation of a large amount of pharmaceutical intermediate wastewater, which typically comes from wastewater generated during the production of various drugs and from wastewater generated during the operation of production workshops and equipment. It is usually characterized by high salt content, high organic matter content, complex composition, high color, and large differences in composition. For some drugs, the pharmaceutical intermediate wastewater may also contain certain toxicity, which is not conducive to the growth of microorganisms and makes it difficult to carry out subsequent biochemical treatment, thus belonging to a type of difficult-to-treat industrial wastewater.

[0003] Iron-carbon microelectrolysis technology, also known as internal electrolysis technology, treats wastewater by introducing iron and carbon into the wastewater (electrolyte solution). The principle is that the potential difference between iron and carbon creates numerous micro-cells, which are then used to treat the wastewater. Iron acts as the anode in these micro-cells, releasing Fe2+. 2+ Carbon, acting as the cathode in this reaction, generates a large amount of highly active [H] and [O]. When the pH of the wastewater is slightly acidic, the large amount of active substances generated by the micro-electrolysis reaction can degrade most of the organic macromolecules in the wastewater through oxidation-reduction reactions due to chain breaking reactions. At the same time, the biodegradability of the wastewater will be greatly improved after iron-carbon micro-electrolysis treatment.

[0004] The Fenton reaction is an inorganic chemical reaction, typically involving ferrous ions (Fe²⁺). 2+ With hydrogen peroxide (H 2 O 2 Under acidic conditions, it can undergo the Fenton reaction, producing a large number of highly oxidizing hydroxyl radicals (·OH). These hydroxyl radicals (·OH) react with pollutants in various types of wastewater requiring treatment, primarily responsible for degrading various organic substances that remain in the wastewater due to difficulties in other reactions.

[0005] Dynamic acid-base regulation systems can measure the pH value of water samples and add acid or alkali solutions to maintain the pH value within a certain range, thereby maximizing the acid-base conditions required for the reaction process. The pH value during the reaction process is a major factor affecting the treatment effect of iron-carbon micro-electrolysis and Fenton oxidation reactions. Therefore, by controlling the reaction to always be carried out within a specific pH range through dynamic acid-base regulation systems, the best treatment effect can often be obtained. Summary of the Invention

[0006] In view of this, the present invention provides a treatment method that can efficiently reduce the concentration of organic matter and improve its biodegradability to a certain extent, so as to solve the problem of pharmaceutical intermediate wastewater with high organic matter concentration and poor biodegradability that cannot be effectively treated by traditional biological methods.

[0007] To achieve the above objectives, the present invention adopts the following technical solution:

[0008] A pretreatment process for pharmaceutical intermediate wastewater before biochemical treatment includes the following steps:

[0009] Step 1: Measure the COD concentration of pharmaceutical intermediate wastewater and allow it to enter the equalization tank directly or after dilution, then add acid to adjust the pH.

[0010] Step 2: Transport the pharmaceutical intermediate wastewater in the equalization tank to the iron-carbon tower. Set different iron-carbon mass water levels according to the COD concentration of the pharmaceutical intermediate wastewater for treatment. Aerate for 2 hours. During the aeration period, control it to carry out the iron-carbon micro-electrolysis reaction within an appropriate pH range.

[0011] Step 3: Transport the pharmaceutical intermediate wastewater after iron-carbon micro-electrolysis treatment to the Fenton oxidation tank, add hydrogen peroxide, and aerate for 2 hours. During the aeration period, control the pH value to carry out the Fenton oxidation reaction within an appropriate range.

[0012] Step 4: Adjust the pH of the pharmaceutical intermediate wastewater to 7±0.5 by adding alkali. Add different coagulants and flocculants according to the different types of pharmaceutical intermediate wastewater to carry out flocculation and sedimentation, and obtain the supernatant.

[0013] Preferably, the iron-carbon micro-electrolysis reaction is monitored and controlled using a dynamic acid-base adjustment system, and the pH value is dynamically balanced by titrating the acid-base solution to maintain the pH value at 2.9±0.3.

[0014] More preferably, the acid-base solution is a 5-10 mol / L sulfuric acid solution.

[0015] Preferably, the iron-carbon mass water level includes a high-multiplier iron-carbon mass water level, a low-multiplier iron-carbon mass water level, and a uniform iron-carbon mass water level.

[0016] Preferably, the high-compound iron-carbon mass water level is used to treat pharmaceutical intermediate wastewater with a mass of 3 times that of iron-carbon filler, and the high-compound iron-carbon mass water level is suitable for treating pharmaceutical intermediate wastewater with a COD concentration ≤ 4000 mg / L.

[0017] The low-component iron-carbon mass water level is used to treat pharmaceutical intermediate wastewater with a filler mass of 2 times that of iron-carbon filler. The low-component iron-carbon mass water level is suitable for the treatment of pharmaceutical intermediate wastewater with a COD concentration of 4000mg / L < COD concentration ≤ 8000mg / L.

[0018] The same iron and carbon mass water level is used to deal with pharmaceutical intermediate wastewater with the same iron and carbon filler mass. The same iron and carbon mass water level is suitable for the treatment of pharmaceutical intermediate wastewater with COD concentration of 8000mg / L < COD concentration ≤ 12000mg / L.

[0019] If the COD concentration of pharmaceutical intermediate wastewater is >12000mg / L, and the same iron and carbon mass water level cannot be used for treatment, the pharmaceutical intermediate wastewater should be diluted to an adjustable iron and carbon mass water level for treatment.

[0020] Preferably, the mass ratio of hydrogen peroxide to the wastewater after iron-carbon micro-electrolysis treatment in step 3 is determined based on the iron-carbon mass level.

[0021] When the iron-carbon mass water level is a high multiple of the iron-carbon mass water level, the mass ratio of hydrogen peroxide to wastewater after iron-carbon micro-electrolysis treatment is 3:250.

[0022] When the iron-carbon mass water level is at a low multiple of the iron-carbon mass water level, the mass ratio of hydrogen peroxide to the wastewater after iron-carbon micro-electrolysis treatment is 3:125.

[0023] When the iron and carbon mass water levels are the same, the mass ratio of hydrogen peroxide to the wastewater after iron and carbon micro-electrolysis treatment is 9:250.

[0024] More preferably, the mass concentration of the hydrogen peroxide is 30%.

[0025] Preferably, the Fenton oxidation reaction allows the pH value to change naturally between 2.6 and the threshold 4.0. The process is not controlled by adding acid or alkali solutions. If the pH value reaches the threshold 4.0 by increasing, an acidic solution is added to maintain the dynamic balance of the pH value, so that the pH value is maintained in the range of 3.7±0.3 to continue the Fenton reaction until the pH reaches the threshold and the above operation is repeated.

[0026] More preferably, the acidic solution is a 5-10 mol / L sulfuric acid solution.

[0027] Preferably, the different types of pharmaceutical intermediate wastewater include: wastewater generated from anti-inflammatory drug intermediates, wastewater generated from antitumor drug intermediates, waste liquid generated by pharmaceutical processing equipment during the production process and wastewater from various pharmaceutical intermediates, or a mixture of wastewater generated from multiple pharmaceutical intermediates.

[0028] Preferably, the coagulant is polyferric sulfate; and the flocculant is polyvinylamide.

[0029] Preferably, the dosage of the coagulant is 1500-2000 ppm relative to the concentration of wastewater generated from anti-inflammatory drug intermediates, 1800-2200 ppm relative to the concentration of wastewater generated from antitumor drug intermediates, 2000-2400 ppm relative to the concentration of the mixture of waste liquid generated from the treatment equipment during the drug production process and wastewater from various drug intermediates, and 2000-2400 ppm relative to the concentration of the mixture of wastewater generated from multiple drug intermediates.

[0030] Preferably, the dosage of the flocculant is 200-400 ppm relative to the concentration of wastewater generated from anti-inflammatory drug intermediates, 350 ppm relative to the concentration of wastewater generated from antitumor drug intermediates, 500-700 ppm relative to the concentration of the mixture of waste liquid generated from the treatment equipment during the drug production process and wastewater from various drug intermediates, and 650 ppm relative to the concentration of the mixture of wastewater generated from multiple drug intermediates.

[0031] As can be seen from the above technical solution, compared with the prior art, the present invention has the following beneficial effects:

[0032] 1. After selecting the appropriate iron and carbon water level for pharmaceutical intermediate wastewater, the dosage of subsequent treatment agents can be determined, making the treatment process easier to operate.

[0033] 2. By dynamically controlling the pH value during the iron-carbon micro-electrolysis and Fenton oxidation stages, the pH value is always kept within the optimal treatment range, which improves the treatment efficiency of organic matter in pharmaceutical intermediate wastewater to a certain extent. Detailed Implementation

[0034] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0035] Example 1

[0036] The acidic wastewater generated from anti-inflammatory drug intermediates is treated using the following steps:

[0037] (1) Wastewater conditioning treatment: After testing, it was found that the COD concentration of the acidic wastewater generated by the anti-inflammatory drug intermediate was 80,000 mg / L, which did not meet the standard for treatment at any iron and carbon mass water level. Therefore, it was necessary to condition the acidic wastewater generated by the anti-inflammatory drug intermediate. After conditioning treatment, the COD concentration of the water sample was 10,000 mg / L, which met the standard for treatment at the same iron and carbon mass water level.

[0038] (2) Acidification treatment: The acidic wastewater generated from the anti-inflammatory drug intermediate is introduced into the equalization tank and stirred. At the same time, a certain amount of sulfuric acid solution with a molar concentration of 5 mol / L is added to adjust the pH value of the acidic wastewater generated from the anti-inflammatory drug intermediate to 2.9±0.3.

[0039] (3) Iron-carbon micro-electrolysis treatment: The effluent flow rate of the regulating tank is set according to the same iron-carbon mass water level required to treat the acidic wastewater generated by the anti-inflammatory drug intermediate. The effluent is introduced into the iron-carbon reaction tank and fully aerated to ensure that the acidic wastewater generated by the anti-inflammatory drug intermediate comes into full contact with the iron-carbon packing. At the same time, the pH value of the water sample undergoing the iron-carbon micro-electrolysis reaction is measured and controlled by a dynamic acid-base balance system. The pH value is maintained at 2.9±0.3 by adding acid and base solutions. The iron-carbon micro-electrolysis reaction is carried out for 2 hours on the basis of maintaining dynamic balance of pH value throughout the process.

[0040] (4) Fenton oxidation reaction: The effluent from the iron-carbon reaction tank is fed into the Fenton oxidation tank. A certain amount of hydrogen peroxide solution with a mass concentration of 30% is added according to the mass ratio of hydrogen peroxide to effluent from the iron-carbon reaction tank corresponding to the same iron-carbon mass water level. Then, the tank is aerated for 2 hours. During the aeration period, the pH value of the acidic wastewater generated by the anti-inflammatory drug intermediate is monitored throughout the process through a dynamic acid-base balance system. During the monitoring process, the pH value is allowed to change naturally from the pH control range of 2.9±0.3 to the threshold of 4.0 in the iron-carbon micro-electrolysis pH range. If the pH value of the acidic wastewater generated by the anti-inflammatory drug intermediate naturally increases to the threshold of 4.0, a certain amount of sulfuric acid solution with a molar concentration of 5mol / L is added to maintain the pH value of the water sample at 3.7±0.3, so as to achieve dynamic balance of pH value of the water sample during the Fenton oxidation process and obtain the water sample after Fenton oxidation treatment.

[0041] (5) Flocculation treatment: Add an alkaline agent to the acidic wastewater generated by the anti-inflammatory drug intermediate. After the pH is controlled to be neutral or weakly alkaline, add flocculant and coagulant. The amount of polyferric sulfate added is 1800 ppm relative to the concentration of the acidic wastewater generated by the anti-inflammatory drug intermediate, and the amount of polyvinylamide (cationic) added is 250 ppm relative to the concentration of the acidic wastewater generated by the anti-inflammatory drug intermediate. After flocculation for 30 min, filter to remove floating floc residues and precipitates from the water sample.

[0042] (6) Results analysis: After the above steps, the COD concentration of the acidic wastewater generated by the anti-inflammatory drug intermediate was reduced from the initial 10000 mg / L to 5400 mg / L. The final treatment efficiency was about 46% through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation.

[0043] Example 2

[0044] The alkaline wastewater generated from anti-inflammatory drug intermediates is treated using the following steps:

[0045] After testing, it was found that the COD concentration of the alkaline wastewater generated by the anti-inflammatory drug intermediate was 230,000 mg / L, which did not meet the standard for treatment at any iron and carbon mass water level. It was necessary to adjust the alkaline wastewater generated by the anti-inflammatory drug intermediate. After adjustment, the COD concentration of the water sample was 10,000 mg / L, which met the standard for treatment at the same iron and carbon mass water level. Therefore, according to the amount of water discharged from the adjustment tank required at the same iron and carbon mass water level and the amount of hydrogen peroxide required for the Fenton oxidation reaction, the operation steps (2) to (4) in Example 1 were repeated.

[0046] Flocculation treatment: An alkaline agent is added to the alkaline wastewater generated from the anti-inflammatory drug intermediate. After the pH is controlled to be neutral or weakly alkaline, flocculants and coagulants are added. The dosage of polyferric sulfate is 1700 ppm relative to the concentration of alkaline wastewater generated from the anti-inflammatory drug intermediate, and the dosage of polyvinylamide (cationic) is 300 ppm relative to the concentration of alkaline wastewater generated from the anti-inflammatory drug intermediate. After flocculation for 30 minutes, the sample is filtered to remove floating floc residues and precipitates.

[0047] Results analysis: After the above steps, the COD concentration of the alkaline wastewater generated from anti-inflammatory drug intermediates decreased from the initial 10000 mg / L to 5530 mg / L. The final treatment efficiency through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation was approximately 44.7%.

[0048] Example 3

[0049] Wastewater generated from intermediates of anti-tumor drugs is treated using the following steps:

[0050] After testing, it was found that the COD concentration of the wastewater generated by the intermediate of antitumor drugs was 100,000 mg / L, which did not meet the standard for treatment at any iron and carbon mass water level. It was necessary to adjust the wastewater generated by the intermediate of antitumor drugs. After adjustment, the COD concentration of the water sample was 10,000 mg / L, which met the standard for treatment at the same iron and carbon mass water level. Therefore, according to the amount of water discharged from the adjustment tank required at the same iron and carbon mass water level and the amount of hydrogen peroxide required for the Fenton oxidation reaction, the operation steps (2) to (4) in Example 1 were repeated.

[0051] Flocculation treatment: An alkaline agent is added to the wastewater generated from the intermediates of antitumor drugs. After the pH is controlled to be neutral or weakly alkaline, flocculants and coagulants are added. The dosage of polyferric sulfate is 2000 ppm relative to the concentration of the wastewater generated from the intermediates of antitumor drugs, and the dosage of polyvinylamide (cationic) is 350 ppm relative to the concentration of the wastewater generated from the intermediates of antitumor drugs. After flocculation for 30 minutes, the sample is filtered to remove floating floc residues and precipitates.

[0052] Results analysis: After treatment using the above steps, the COD concentration of wastewater generated from antitumor drug intermediates decreased from the initial 10000 mg / L to 5590 mg / L. The final treatment efficiency through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation was approximately 44.1%. Its biodegradability (B / C) ratio improved from 0.1534 to 0.27124.

[0053] Example 4

[0054] The following steps are used to treat the mixture of waste liquid generated from pharmaceutical production equipment and wastewater from various pharmaceutical intermediates:

[0055] The mixed water sample contains dichloromethane, tetrahydrofuran, toluene, nitrobenzene, chlorobenzene, n-hexane, petroleum ether, acetone, and pump area waste liquid, etc., and the specific concentration of each component is unknown. After measurement, it was found that the COD concentration of the mixed water sample was 5200 mg / L, which meets the standard of low-multiplied iron and carbon mass water level. Therefore, no adjustment treatment is required for the mixed water sample. So, according to the water output of the adjustment tank required for low-multiplied iron and carbon mass water level and the amount of hydrogen peroxide required for Fenton oxidation reaction, the operation steps (2) to (4) in Example 1 are repeated.

[0056] Flocculation treatment: An alkaline agent is added to the mixture of waste liquid generated by the pharmaceutical production equipment and wastewater from various pharmaceutical intermediates. After the pH is controlled to be neutral or weakly alkaline, flocculants and coagulants are added. The dosage of polyferric sulfate is 2200 ppm relative to the concentration of the mixed water sample, and the dosage of polyvinylamide (cationic) is 550 ppm relative to the concentration of the mixed water sample. After flocculation for 30 minutes, the mixture is filtered to remove floating floc residues and precipitates from the water sample.

[0057] Results analysis: After the above steps, the COD concentration of the mixture of waste liquid generated by the equipment during the production process and wastewater from various pharmaceutical intermediates decreased from the initial 5200 mg / L to 3500 mg / L. The final treatment efficiency through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation was approximately 32.7%, and the biodegradability B / C ratio increased from 0.1649 to 0.2548.

[0058] Example 5

[0059] The following steps were used to treat a mixed water sample containing wastewater from various pharmaceutical intermediates:

[0060] After testing, it was found that the COD concentration of the mixed water sample of wastewater generated by various pharmaceutical intermediates was 8400 mg / L, which met the standard for treatment at the same iron and carbon mass water level. Therefore, it was not necessary to dilute the mixed water sample of wastewater generated by various pharmaceutical intermediates. Thus, according to the amount of water discharged from the equalization tank required at the same iron and carbon mass water level and the amount of hydrogen peroxide required for the Fenton oxidation reaction, the operation steps (2) to (4) in Example 1 were repeated.

[0061] Flocculation treatment: An alkaline agent was added to a mixed water sample containing wastewater from various pharmaceutical intermediates. After the pH was controlled to be neutral or weakly alkaline, flocculants and coagulants were added. The dosage of polyferric sulfate was 2300 ppm relative to the concentration of the mixed water sample containing wastewater from various pharmaceutical intermediates, and the dosage of polyvinylamide (cationic) was 650 ppm relative to the concentration of the mixed water sample containing wastewater from various pharmaceutical intermediates. After flocculation for 30 minutes, the sample was filtered to remove floating floc residues and sediments.

[0062] Results analysis: After the above steps, the COD concentration of the mixed wastewater sample from various pharmaceutical intermediates decreased from the initial 8400 mg / L to 4690 mg / L. The final treatment efficiency through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation was approximately 44.2%, and the biodegradability (B / C) ratio increased from 0.1954 to 0.3545.

[0063] Comparative experimental cases

[0064] The following steps were used to treat a mixed water sample containing wastewater from various pharmaceutical intermediates:

[0065] (1) Wastewater conditioning and treatment: After testing, it was found that the COD concentration of the mixed water sample of wastewater generated by various pharmaceutical intermediates was 8400 mg / L, which met the standard for treatment at the same iron and carbon mass water level. Therefore, it is not necessary to dilute the mixed water sample of wastewater generated by various pharmaceutical intermediates.

[0066] (2) Acidification treatment: The mixed water sample of wastewater from various pharmaceutical intermediates is introduced into the equalization tank and stirred. At the same time, a certain amount of sulfuric acid solution with a molar concentration of 5 mol / L is added to adjust the pH value of the mixed water sample of wastewater from various pharmaceutical intermediates to 2.9±0.3.

[0067] (3) Iron-carbon micro-electrolysis treatment: The effluent flow rate of the regulating tank is set according to the same iron-carbon mass water level required for treating the mixed water sample of wastewater generated from multiple pharmaceutical intermediates. The effluent is introduced into the iron-carbon reaction tank and fully aerated to ensure that the mixed water sample of wastewater generated from multiple pharmaceutical intermediates is fully in contact with the iron-carbon packing. The pH value is not controlled during the reaction. The reaction time is 2 hours.

[0068] (4) Fenton oxidation reaction: The effluent from the iron-carbon reaction tank is fed into the Fenton oxidation tank. A certain amount of hydrogen peroxide solution with a mass concentration of 30% is added according to the mass ratio of hydrogen peroxide to the effluent from the iron-carbon reaction tank corresponding to the same iron-carbon mass water level. Then, the tank is aerated for 2 hours. During the aeration period, the pH value is not controlled. After treatment, the water sample after Fenton oxidation treatment is obtained.

[0069] (5) Flocculation treatment: Alkali agent is added to the mixed water sample of wastewater generated from multiple pharmaceutical intermediates. After the pH is controlled to be neutral or weakly alkaline, flocculant and coagulant are added. The dosage of polyferric sulfate is 2300 ppm relative to the concentration of the mixed water sample of wastewater generated from multiple pharmaceutical intermediates, and the dosage of polyvinylamide (cationic) is 650 ppm relative to the concentration of the mixed water sample of wastewater generated from multiple pharmaceutical intermediates. After flocculation for 30 min, the sample is filtered to remove floating floc residues and sediments.

[0070] Results analysis: After the above steps, the COD concentration of the mixed wastewater sample from various pharmaceutical intermediates decreased from the initial 8400 mg / L to 5637 mg / L. The final treatment efficiency through the combined reaction of iron-carbon micro-electrolysis and Fenton oxidation was approximately 32.9%, and the biodegradability (B / C) ratio increased from 0.1954 to 0.2534.

[0071] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on its differences from other embodiments. Similar or identical parts between embodiments can be referred to interchangeably. For the apparatus disclosed in the embodiments, since they correspond to the methods disclosed in the embodiments, the description is relatively simple; relevant parts can be referred to the method section.

[0072] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A pretreatment process for pharmaceutical intermediate wastewater before biochemical treatment, characterized in that, Includes the following steps: Step 1: Measure the COD concentration of pharmaceutical intermediate wastewater and allow it to enter the equalization tank directly or after dilution, then add acid to adjust the pH. Step 2: Transport the pharmaceutical intermediate wastewater in the equalization tank to the iron-carbon tower. Set different iron-carbon mass water levels according to the COD concentration of the pharmaceutical intermediate wastewater for treatment, and control it to carry out iron-carbon micro-electrolysis reaction within an appropriate pH range. Step 3: The pharmaceutical intermediate wastewater after iron-carbon micro-electrolysis treatment is transported to the Fenton oxidation tank, hydrogen peroxide is added, and the Fenton oxidation reaction is carried out within an appropriate pH range. Step 4: Adjust the pH of the pharmaceutical intermediate wastewater to 7±0.5 by adding alkali. Add different coagulants and flocculants according to the different types of pharmaceutical intermediate wastewater to carry out flocculation and sedimentation to obtain the supernatant. The iron-carbon mass water level includes high-multiplier iron-carbon mass water level, low-multiplier iron-carbon mass water level, and the same iron-carbon mass water level. The iron-carbon micro-electrolysis reaction is monitored and controlled using a dynamic acid-base adjustment system, and the pH value is dynamically balanced by titrating the acid and base solutions to maintain the pH value at 2.9±0.

3. The high-compound iron-carbon mass water level is used to treat pharmaceutical intermediate wastewater with a mass of 3 times that of iron-carbon filler. The high-compound iron-carbon mass water level is suitable for treating pharmaceutical intermediate wastewater with a COD concentration ≤ 4000 mg / L. The low-component iron-carbon mass water level is used to treat pharmaceutical intermediate wastewater with a filler mass of 2 times that of iron-carbon filler. The low-component iron-carbon mass water level is suitable for the treatment of pharmaceutical intermediate wastewater with a COD concentration of 4000mg / L < COD concentration ≤ 8000mg / L. The same iron and carbon mass water level is used to deal with pharmaceutical intermediate wastewater with the same iron and carbon filler mass. The same iron and carbon mass water level is suitable for the treatment of pharmaceutical intermediate wastewater with COD concentration of 8000mg / L < COD concentration ≤ 12000mg / L. If the COD concentration of pharmaceutical intermediate wastewater is >12000mg / L and the same iron and carbon mass water level cannot be used to treat it, the pharmaceutical intermediate wastewater should be diluted to an adjustable iron and carbon mass water level for treatment. The Fenton oxidation reaction allows the pH value to change naturally from 2.6 to the threshold 4.

0. The process is not controlled by adding acid or alkali solutions. If the pH value reaches the threshold 4.0 by increasing, an acidic solution is added to maintain the dynamic balance of the pH value, so that the pH value is maintained in the range of 3.7±0.3 to continue the Fenton reaction until the pH reaches the threshold. The operation of adding an acidic solution to maintain the dynamic balance of the pH value is repeated. The mass ratio of hydrogen peroxide to the wastewater after iron-carbon micro-electrolysis treatment in step 3 is determined based on the iron-carbon mass level. When the iron-carbon mass water level is a high multiple of the iron-carbon mass water level, the mass ratio of hydrogen peroxide to wastewater after iron-carbon micro-electrolysis treatment is 3:

250. When the iron-carbon mass water level is at a low multiple of the iron-carbon mass water level, the mass ratio of hydrogen peroxide to the wastewater after iron-carbon micro-electrolysis treatment is 3:

125. When the iron and carbon mass water levels are the same, the mass ratio of hydrogen peroxide to the wastewater after iron and carbon micro-electrolysis treatment is 9:

250.

2. The process as claimed in claim 1, wherein the process is characterized by, The different types of pharmaceutical intermediate wastewater include: wastewater generated from anti-inflammatory drug intermediates, wastewater generated from anti-tumor drug intermediates, waste liquid generated by pharmaceutical processing equipment during the production process and wastewater from various pharmaceutical intermediates, or a mixture of wastewater generated from multiple pharmaceutical intermediates.