CN115124190A - Di-tert-butyl dicarbonate wastewater standard treatment device and method - Google Patents

Abstract

The invention discloses a standard-compliant treatment device for di-tert-butyl dicarbonate wastewater, comprising a comprehensive regulating tank, an iron-carbon electrochemical reaction tank, an iron-carbon sedimentation tank, an intermediate water tank, a hydrolysis and acidification tank, and a UASB dehydration tank, which are sequentially connected in series through pipelines. Oxygen tower, anoxic tank, A/O aerobic tank, secondary sedimentation tank and clear water tank, wherein, the high-salt wastewater and low-salt wastewater in the production process of di-tert-butyl dicarbonate enter the standard-compliant treatment device through a comprehensive adjustment tank , the domestic sewage enters the standard-compliant treatment device through the intermediate pool, and the treated non-water enters the clean water pool. The invention also provides a corresponding treatment method for reaching the standard. The treatment method of the present invention can make macromolecular pollutants in wastewater into small molecular pollutants, and refractory pollutants into easily degradable pollutants, so that the organic matter in the wastewater can be removed by anaerobic and hydrolysis methods as much as possible, so that Reduce the organic load and operating cost of the A/O aerobic system.

Description

A kind of device and method for treating waste water of di-tert-butyl dicarbonate up to standard

technical field

The invention relates to the technical field of sewage treatment, in particular to a standard treatment device and method for di-tert-butyl dicarbonate waste water.

Background technique

For the pharmaceutical and chemical industry producing di-tert-butyl dicarbonate, the wastewater mainly comes from the condensed wastewater of the double-effect or triple-effect forced circulation evaporator, the drainage of the circulating cooling system and some domestic wastewater. Therefore, industrial wastewater contains high-salt wastewater and low-salt wastewater. The chemical oxygen demand (COD) in wastewater is very high at 30000-50000mg/L, while the chemical oxygen demand (COD) in domestic sewage is higher than The low is 300-500mg/L. After the above wastewater is mixed, the COD concentration is 15000-20000mg/L, the B/C (BOD/COD) of the wastewater is very low, and it belongs to the wastewater with high organic concentration and difficult to biodegrade. In view of the above characteristics of wastewater, it is difficult to directly use biological methods to treat high-concentration refractory organic wastewater. Therefore, there is an urgent need to provide a standard treatment process for di-tert-butyl dicarbonate wastewater.

SUMMARY OF THE INVENTION

The technical problem to be solved by the present invention is to provide a standard treatment device and method for di-tert-butyl dicarbonate wastewater, which solves the technical problem that high-concentration di-tert-butyl dicarbonate wastewater is difficult to biochemically treat.

In order to solve the above-mentioned technical problems, the present invention provides the following technical solutions:

The invention provides a standard treatment device for di-tert-butyl dicarbonate wastewater, which comprises a comprehensive regulating tank, an iron-carbon electrochemical reaction tank, an iron-carbon sedimentation tank, an intermediate water tank, a hydrolysis and acidification tank, and a UASB dehydration tank, which are connected in series through pipelines. Oxygen tower, anoxic tank, A/O aerobic tank, secondary sedimentation tank and clear water tank, wherein the high-salt wastewater and low-salt wastewater in the production process of di-tert-butyl dicarbonate enter the standard-compliant treatment device through a comprehensive adjustment tank , the domestic sewage enters the standard-compliant treatment device through the intermediate pool, and the treated non-water enters the clear water pool.

Further, an aeration and stirring device is provided in the comprehensive adjustment tank and the intermediate tank.

Further, the outlet of the UASB anaerobic tower is provided with an anaerobic return line for the effluent to return to the hydrolysis and acidification tank; the outlet of the A/O aerobic tank is provided with a nitrification return line for the return of the effluent to the anoxic tank.

Further, a sludge return pipeline is set at the outlet of the secondary sedimentation tank, and the sludge deposited in the secondary sedimentation tank is returned to the hydrolysis and acidification tank, the anoxic tank and the A/O aerobic tank through the return pipeline.

Further, the up-to-standard treatment device also includes a sludge concentration tank, the sludge concentration tank is connected with the secondary sedimentation tank through a pipeline, and the remaining sludge in the secondary sedimentation tank is transported to the sludge concentration tank through the pipeline. .

The present invention also provides a standard treatment method for di-tert-butyl dicarbonate wastewater, comprising the following steps:

S1. the waste water produced in the production process of di-tert-butyl dicarbonate is passed into the comprehensive regulating tank, and the water quality, water quantity and pH of the waste water are adjusted;

S2. The effluent from the comprehensive regulation tank enters the iron-carbon electrochemical reaction tank, and performs micro-electrolysis reaction to oxidize and decompose the macromolecular organic matter in the wastewater into small molecular organic matter;

S3. The effluent from the iron-carbon electrochemical reaction tank enters the iron-carbon sedimentation tank to separate the mud and water and clarify the effluent;

S4. The effluent from the iron-carbon sedimentation tank enters the intermediate tank, where it is mixed with domestic sewage, and the wastewater is homogenized at the same time;

S5. The effluent from the intermediate tank enters the hydrolysis and acidification tank, and through the hydrolysis and acidification of anaerobic microorganisms, the B/C ratio of the wastewater is improved;

S6. The effluent from the hydrolysis and acidification tank enters the UASB anaerobic tower for anaerobic biochemical reaction to further improve the B/C ratio of the wastewater; part of the effluent from the UASB anaerobic tower is returned to the hydrolysis and acidification tank through the anaerobic reflux pipeline;

S7. The effluent from the UASB anaerobic tower enters the anoxic tank, removes the organic matter in the wastewater by anaerobic and hydrolysis, and improves the B/C ratio of the wastewater;

S8. The effluent of the anoxic tank enters the A/O aerobic tank, and performs aerobic biochemical reaction to degrade the remaining small molecular organic matter; the nitrification solution after aerobic treatment is returned to the anoxic tank, and the mixed solution of the nitrification solution is refluxed;

S9. The effluent from the A/O aerobic tank enters the secondary sedimentation tank for mud-water separation, the upper layer of clean water flows into the clean-water tank for discharge up to the standard, and the lower layer of sludge is partially returned to the hydrolysis acidification tank, anoxic tank and A/O aerobic tank, and some pumps into the sludge thickening tank;

S10. The sludge in the sludge thickening tank is subjected to pressure filtration, the supernatant is returned to the adjustment tank for further treatment, and the formed sludge cake is transported out for disposal.

Further, in step S1, the waste water generated in the production process of di-tert-butyl dicarbonate includes high-salt waste water and low-salt waste water, and after mixing the high-salt waste water and low-salt waste water in a comprehensive adjustment tank, the COD of the waste water is controlled. The value is about 20000mg/L, and the pH is 6-7.

Further, in step S2, the pH in the iron-carbon electrochemical reaction tank is controlled to be below 4-5, and after the micro-electrolysis reaction, the COD of the wastewater is reduced to below 16000 mg/L.

Further, in step S4, the pH of the wastewater in the intermediate pool is adjusted to 6.5-7.0 with alkali;

Further, in step S5, the pH of the wastewater in the hydrolysis acidification tank is 6.0-7.0;

Further, in step S6, the operating temperature of the UASB anaerobic tower is 35-38 °C, the hydraulic retention time is 2d, and the pH of the control wastewater is 6.5-7.5; 50% of the effluent from the UASB anaerobic tower is returned to the hydrolysis and acidification tank, and 50% The effluent enters the anoxic pool.

Further, in step S7, the hydraulic retention time of the anoxic tank is 1 d.

Further, in step S8, the dissolved oxygen content in the A/O aerobic tank is controlled to be more than 2 mg/L, the temperature is 10-30 °C, and the sedimentation ratio after the sludge is settled for 30 min is 50-70%; A/O aerobic The reflux ratio of the nitrification solution from the pool to the anoxic pool is 1:1.

Further, in step S9, the sludge in the lower layer of the secondary sedimentation tank is returned to the hydrolysis acidification tank, the anoxic tank and the A/O aerobic tank at a weekly rate of 20%, and the excess sludge is pumped into the sludge thickening tank.

Further, after the treatment, the COD removal rate in the wastewater reaches more than 98%.

Compared with the prior art, the beneficial effects of the present invention are:

1. The standard treatment method of di-tert-butyl dicarbonate wastewater of the present invention utilizes the front pretreatment measures such as chemical oxidation decomposition of iron-carbon electrochemical reaction, hydrolysis acidification biochemical pretreatment, UASB anaerobic reaction degradation, etc., to realize the removal of macromolecular organic matter. It is gradually decomposed into small molecular organic substances, so that macromolecular pollutants in wastewater become small molecular pollutants, and refractory pollutants become easily degradable pollutants, so that organic substances in wastewater can be removed as much as possible by anaerobic and hydrolysis methods. Reduce the organic load and operating cost of the A/O aerobic system.

2. The method for up-to-standard treatment of di-tert-butyl dicarbonate wastewater of the present invention realizes that the COD of wastewater is reduced from 15,000-20,000 mg/L of influent to below 500 mg/L of effluent, and solves the problem of up-to-standard treatment of low B/C ratio and high concentration organic wastewater A low-cost and high-efficiency biological treatment method for di-tert-butyl dicarbonate wastewater is realized.

Description of drawings

Fig. 1 is the process flow diagram of the standard treatment method of di-tert-butyl dicarbonate waste water of the present invention.

Detailed ways

The present invention will be further described below with reference to the accompanying drawings and specific embodiments, so that those skilled in the art can better understand the present invention and implement it, but the embodiments are not intended to limit the present invention.

Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terms used in the description of the present invention are for the purpose of describing specific embodiments only, and are not intended to limit the present invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.

The experimental methods used in the following examples are conventional methods unless otherwise specified, and the materials, reagents, etc. used can be obtained from commercial sources unless otherwise specified.

As mentioned in the background art, in the wastewater from the production of di-tert-butyl dicarbonate, the chemical oxygen demand (COD) is very high, reaching 30,000-50,000 mg/L, while the chemical oxygen demand (COD) of domestic sewage is relatively low, ranging from 300-500 mg. /L. After the above wastewater is mixed, the COD concentration is 15000-20000mg/L, and the B/C is very low, which belongs to the wastewater with high concentration of organic matter and difficult to biodegrade. This high-concentration refractory organic wastewater is difficult to be directly treated by biological methods.

In view of the above technical problems, the present invention provides a standard treatment system and a corresponding treatment method for di-tert-butyl dicarbonate wastewater, which solves the technical problem that high-concentration di-tert-butyl dicarbonate wastewater is difficult to biochemically treat.

Specifically, referring to Fig. 1, the standard treatment system for di-tert-butyl dicarbonate wastewater of the present invention comprises a comprehensive adjustment tank, an iron-carbon electrochemical reaction tank, an iron-carbon sedimentation tank, an intermediate water tank, and a hydrolysis acidification tank connected in sequence through pipelines , UASB anaerobic tower, anoxic tank, A/O aerobic tank, secondary sedimentation tank and clear water tank. Among them, an anaerobic return line is set at the outlet of the UASB anaerobic tower, which is used to return the effluent to the hydrolysis and acidification tank. A nitrification return line is set at the outlet of the A/O aerobic tank, which is used to return the effluent to the anoxic tank. A sludge return pipeline is set at the outlet of the secondary sedimentation tank to return the sludge to the hydrolysis acidification tank, anoxic tank and A/O aerobic tank.

In the above-mentioned up-to-standard treatment system, both the comprehensive regulating tank and the intermediate tank are equipped with COD online monitor, hydraulic stirring device/aeration stirring device, and the mixed wastewater is fully stirred and mixed to adjust the water quality, and the COD content of the wastewater is checked. Real-time monitoring to avoid excessive fluctuation of COD content in wastewater.

The above-mentioned up-to-standard treatment system further includes a sludge thickening tank, which is communicated with the secondary sedimentation tank through a pipeline, and the remaining sludge in the secondary sedimentation tank is transported to the sludge thickening tank through the pipeline. The sludge in the sludge thickening tank is further processed by pressure filtration to form a mud cake and sent to the outside for disposal.

The standard treatment method for di-tert-butyl dicarbonate wastewater provided by the invention comprises the following steps:

S1. Collect high-salt wastewater and low-salt wastewater generated in the production process of di-tert-butyl dicarbonate, and pump it into a comprehensive adjustment tank through workshop pipelines to adjust and homogenize water quality. There is a hydraulic mixer or aeration mixer in the comprehensive regulating tank, which can make the high-salt wastewater and the low-salt wastewater fully and evenly mix, and avoid the fluctuation of the COD concentration of the wastewater being too high or too low. In addition, a COD online monitor is also set up in the comprehensive regulation tank to monitor the COD of wastewater. Preferably, after the high-salt wastewater and the low-salt wastewater are mixed in the comprehensive regulating tank, the COD value of the wastewater is controlled to be about 20,000 mg/L, and the pH is 6-7.

S2. The effluent from the comprehensive adjustment tank enters the iron-carbon electrochemical reaction tank for micro-electrolysis reaction.

The principle of the iron-carbon micro-electrolysis reaction is that when iron filings and carbon particles are immersed in weakly acidic wastewater, numerous micro-galvanic cells will be formed in the wastewater due to the electrode potential difference between iron and carbon. These tiny batteries use low-potential iron as the anode and high-potential carbon as the cathode, and electrochemical reactions take place in an aqueous solution containing an acidic electrolyte. Due to the electrode potential difference of ^1.2V between ^Fe and C, countless micro-battery systems will be formed, and an electric field will be formed in the action space. A flocculant with high adsorption and flocculation activity. The cathode reacts with H ⁺ under aerobic conditions to form hydroxyl radicals [OH]. Under acidic conditions, hydroxyl radicals [OH] can undergo redox reactions with many components in wastewater, resulting in chain scission and degradation of organic macromolecules, and the cracking of macromolecular organic substances into small molecular organic substances that are easy to biochemically treat, thereby Improve the biodegradability of wastewater.

In the iron-carbon electrochemical reaction cell, in order to maintain the progress of the electrochemical reaction, the pH needs to be controlled to an acidic condition. When the pH of the wastewater is reduced to below 4-5, the COD removal rate of 20% can be achieved, and the COD of the wastewater can be reduced from 20000mg/L to 16000mg/L.

S3. The effluent from the iron-carbon electrochemical reaction tank enters the iron-carbon sedimentation tank for precipitation treatment.

S4. The effluent from the iron-carbon sedimentation tank enters the intermediate tank. In the intermediate pool, domestic wastewater with low concentration COD is mixed with production wastewater with high concentration COD. A hydraulic agitator or aeration agitator is installed in the intermediate pool, which can make the high-concentration production wastewater and low-concentration domestic wastewater mix evenly, and avoid fluctuations in the concentration of COD that are too high or too low. In addition, an on-line COD monitor is also set up in the intermediate pool to monitor the COD content of wastewater in real time.

S5. The effluent from the intermediate tank enters the hydrolysis and acidification tank. In the hydrolysis and acidification tank, the hydrolysis and acidification of anaerobic microorganisms are used to decompose some refractory organic substances into easily degradable organic substances, and part of macromolecular organic substances are decomposed into small molecular organic substances, Thus, the B/C ratio of the wastewater is improved, and at the same time, part of the COD (about 20%) can also be removed. The pH of the hydrolysis and acidification pool should be controlled between 6.0-7.0.

S6. The effluent from the hydrolysis and acidification tank is pumped into the UASB anaerobic tower. Through the biodegradation of anaerobic bacteria, the refractory pollutants are degraded into easily degradable pollutants, and the macromolecular pollutants are degraded into small molecular pollutants. , and further improve the B/C ratio of wastewater. Small molecular pollutants are largely removed by the action of anaerobic bacteria in the anaerobic reactor, producing biogas and realizing the energy of organic matter. There is an anaerobic reflux pipeline at the outlet of the UASB anaerobic tower, and part of the effluent from the UASB anaerobic tower is returned to the hydrolysis and acidification tank. The pH of the UASB anaerobic tower needs to be controlled between 6.5-7.5. If the pH is greater than 8 or less than 6, the activity of anaerobic bacteria is inhibited and tends to stop. Preferably, 50% of the effluent from the UASB anaerobic tower is returned to the hydrolysis and acidification tank, and 50% of the effluent enters the anoxic tank.

S7.UASB anaerobic tower effluent flows into the anoxic tank by itself. In the anoxic tank, the organic pollutants in the wastewater are degraded by anaerobic and hydrolysis, so that the macromolecular pollutants in the wastewater become small molecular pollutants, and the refractory pollutants become easily degradable pollutants, thereby reducing the amount of pollution. The organic load and operating cost of the A/O aerobic system increase the B/C ratio of the wastewater.

The hydraulic retention time of the anoxic tank is about 1d, and it is equipped with a submersible mixer with a power of 6-12 (W/m ³ tank body).

S8. The effluent from the anoxic pool enters the A/O aerobic pool. The wastewater has been pretreated before, and the biodegradability (B/C ratio) of the wastewater is greatly improved. Therefore, in the A/O aerobic tank, the aeration system is blown to maintain the aerobic environment in the reaction tank and maintain a certain dissolved oxygen concentration. . Preferably, the dissolved oxygen (DO) of the A/O aerobic pool is preferably controlled above 2 mg/L. In an aerobic environment, aerobic microorganisms fully degrade the remaining small molecular organic matter, carry out denitrification and phosphorus removal, and can quickly adsorb and dilute the organic matter at the inlet end, so that the COD of the wastewater reaches the index value, which has the advantages of low sludge yield, It has the advantages of less sludge discharge, good removal effect and simple operation.

In the present invention, the outlet of the A/O aerobic tank is provided with a nitrification return line, and part of the effluent is returned to the anoxic tank to realize biological denitrification. Returning the nitrification solution after aerobic treatment to the anoxic tank is beneficial to meet the demand of NO ₃ ^- for denitrification by anaerobic bacteria under anoxic conditions, and is beneficial to reduce energy consumption. Preferably, the reflux ratio of the nitrification solution from the A/O aerobic tank to the anoxic tank is 1:1.

In the present invention, the sedimentation ratio (SV30) of the sludge is preferably controlled to 50 to 70%. A thermometer is set in the A/O aerobic tank, and the temperature in the reaction tank is controlled to be 10-30°C.

The effluent from the S9.A/O aerobic tank enters the secondary sedimentation tank. In the secondary sedimentation tank, part of the settled sludge is returned to the aerobic tank, anaerobic tower and hydrolysis tank through the return pipeline to maintain the biomass concentration in each biochemical tank. The remaining activated sludge enters the sludge thickening tank through the pipeline and plays a role in metabolism. Preferably, the sludge in the lower layer of the secondary sedimentation tank is returned to the hydrolysis acidification tank, the anoxic tank and the A/O aerobic tank at a weekly rate of 20%, and the excess sludge is pumped into the sludge thickening tank. The sludge in the sludge thickening tank is further processed by pressure filtration, and the resulting mud cake is transported and disposed of.

The standard treatment method of the present invention can achieve a removal rate of more than 98% for COD in the di-tert-butyl dicarbonate wastewater.

In order to make the objectives and technical solutions of the present invention clearer, the following are specific examples to further describe the present invention in detail. It should be understood that the specific embodiments described herein are only used to explain the present invention, but not to limit the present invention.

Example

The invention provides a standard treatment method for di-tert-butyl dicarbonate wastewater, comprising the following steps:

S1. High-salt wastewater and low-salt wastewater in the production process of di-tert-butyl dicarbonate flow into the comprehensive adjustment tank through the workshop pipe network, and start the hydraulic mixer to stir evenly. The COD value of the mixed wastewater is about 20000mg/L.

S2. The effluent from the comprehensive adjustment tank enters the iron-carbon electrochemical reaction tank. In order to maintain the electrochemical reaction, the solution needs to be controlled in an acidic condition, so that the pH is reduced to below 4-5, and the iron-carbon micro-electrolysis reaction is carried out. After the wastewater undergoes iron-carbon electrochemical reaction, the COD content is reduced from about 20,000 mg/L to about 16,000 mg/L, and the COD removal rate is about 20%.

S3. After the wastewater passes through the iron-carbon sedimentation tank, it enters the intermediate tank, mixes with domestic wastewater, and starts the hydraulic mixer to mix evenly.

S4. The effluent from the intermediate tank enters the hydrolysis and acidification tank, and controls the pH of the waste water to be within the range of 6.0-7.0, and conducts the hydrolysis acidification reaction to improve the biodegradability of the waste water. The COD content is reduced from about 16000mg/L to about 12800mg/L. The removal rate is about 20%, and the B/C ratio is increased from 0.2 to 0.25, an increase of about 25%.

S5. The effluent from the hydrolysis and acidification tank enters the UASB anaerobic tower, and the biodegradation reaction of anaerobic bacteria occurs. The refractory pollutants are degraded into easily degradable pollutants, and the macromolecular pollutants are degraded into small molecular pollutants; some small molecular pollutants are degraded. The pollutants are removed by the anaerobic bacterial reaction in the anaerobic reactor to produce biogas. The outlet of the UASB anaerobic tower is set with an anaerobic return line, which returns to the hydrolysis and acidification tank. Among them, the UASB anaerobic tower needs to take internal anti-corrosion and external thermal insulation measures, and set up two layers of thermometers, and the operating temperature is 35 ~ 38 ℃. The hydraulic retention time is about 2d, and the suitable pH is 6.5-7.5. The COD content was reduced from about 12800mg/L to about 10000mg/L, and the removal rate of COD was about 20%, and the B/C ratio was increased from 0.25 to 0.5, an increase of about 100%.

S6. The effluent from the UASB anaerobic tower enters the anoxic pool. In the anoxic tank, the organic pollutants in the wastewater are degraded by the action of anaerobic microorganisms, so that the macromolecular pollutants in the wastewater become small molecular pollutants, and the refractory pollutants become easily degradable pollutants. The hypoxia tank is equipped with a submersible mixer, and the hydraulic retention time is about 1d.

S7. The effluent of the anoxic tank enters the A/O aerobic tank. In the A/O aerobic tank, aerobic microorganisms can degrade most of the organic pollutants in the wastewater, carry out denitrification and phosphorus removal, and can quickly adsorb and dilute the water at the inlet end. Organic matter, it has the advantages of low sludge yield, less sludge discharge, good removal effect and simple operation. A nitrification return line is set at the outlet of the A/O aerobic tank, and the nitrification liquid is returned to the anoxic tank through the nitrification return line, and the return ratio is 1:1 to realize biological denitrification. The indicators of the A/O aerobic tank are as follows: dissolved oxygen: DO control above 2mg/L; sludge concentration: sedimentation ratio, settling 30min to control 50-70%; the reaction tank is set with a thermometer to control the temperature of the reaction tank to 10-30 °C.

After the sewage passes through the A/O aerobic tank, the COD removal rate can be greater than 95%.

The effluent from the S8.A/O aerobic tank enters the secondary sedimentation tank. In the secondary sedimentation tank, the lower sludge of the secondary sedimentation tank is returned to the aerobic tank, anaerobic tower and hydrolysis tank at a weekly rate of 20% to maintain the biomass concentration in each biochemical tank, and the remaining activated sludge is fed into the sludge. In the thickening tank, it plays a role of metabolism, and the sludge in the sludge thickening tank is processed and disposed of by pressure filtration.

In summary, the present invention provides a standard treatment method for di-tert-butyl dicarbonate wastewater, which can reduce the COD of wastewater from 15,000-20,000 mg/L in influent to less than 500 mg/L in effluent, and achieve a COD removal rate of more than 98%.

The above-mentioned embodiments are only preferred embodiments for fully illustrating the present invention, and the protection scope of the present invention is not limited thereto. Equivalent substitutions or transformations made by those skilled in the art on the basis of the present invention are all within the protection scope of the present invention. The protection scope of the present invention is subject to the claims.

Claims (9)

1. The utility model provides a di-tert-butyl dicarbonate waste water processing apparatus up to standard, a serial connection's comprehensive equalizing basin, indisputable carbon electrochemical reaction pond, indisputable carbon sedimentation tank, middle pond, hydrolysis-acidification pool, UASB anaerobic tower, oxygen deficiency pond, AO aerobic tank, two heavy ponds and clean water basin in proper order through the pipeline, wherein, high salt waste water and the low salt waste water of di-tert-butyl dicarbonate in the production process get into through comprehensive equalizing basin up to standard processing apparatus, domestic sewage gets into through middle pond up to standard processing apparatus, the non-water after the processing enters into the clean water basin.

2. The di-tert-butyl dicarbonate wastewater standard treatment device according to claim 1, characterized in that aeration stirring systems are arranged in the comprehensive adjusting tank and the intermediate water tank.

3. The device for treating di-tert-butyl dicarbonate wastewater reaching the standard according to claim 1, wherein an anaerobic return line is arranged at the outlet of the UASB anaerobic tower and is used for returning effluent to the hydrolysis acidification tank; and a nitrification return pipeline is arranged at an outlet of the A/O aerobic tank and is used for returning the effluent to the anoxic tank.

4. The di-tert-butyl dicarbonate wastewater standard treatment device according to claim 1, wherein a sludge return line is arranged at the outlet of the secondary sedimentation tank, and the sludge deposited in the secondary sedimentation tank flows back to the hydrolysis acidification tank, the anoxic tank and the A/O aerobic tank through the return line.

5. The di-tert-butyl dicarbonate wastewater standard-reaching treatment device according to claim 1, characterized in that the standard-reaching treatment device further comprises a sludge concentration tank, the sludge concentration tank is communicated with the secondary sedimentation tank through a pipeline, and the residual sludge in the secondary sedimentation tank is conveyed into the sludge concentration tank through a sludge pump.

6. The di-tert-butyl dicarbonate wastewater standard treatment device according to claim 1, characterized in that a plate-and-frame filter press is connected behind the sludge concentration tank.

7. The standard-reaching treatment method of di-tert-butyl dicarbonate wastewater is characterized by comprising the following steps:

s1, introducing high-salinity wastewater and low-salinity wastewater generated in the production process of di-tert-butyl dicarbonate into a comprehensive regulating reservoir for mixing, and homogenizing the water quality of the wastewater;

s2, allowing effluent of the comprehensive regulating reservoir to enter an iron-carbon electrochemical reaction tank for micro-electrolysis reaction, and oxidizing and decomposing macromolecular organic matters in wastewater into micromolecular organic matters;

s3, enabling the effluent of the iron-carbon electrochemical reaction tank to enter an iron-carbon sedimentation tank, carrying out mud-water separation, and clarifying the effluent;

s4, enabling the effluent of the iron-carbon sedimentation tank to enter an intermediate water tank, mixing the effluent with domestic sewage, and homogenizing the wastewater;

s5, enabling the effluent of the intermediate water tank to enter a hydrolysis acidification tank, and improving the B/C ratio of the wastewater through the hydrolysis and acidification effects of anaerobic microorganisms;

s6, pumping the effluent of the hydrolysis acidification tank into a UASB anaerobic tower for anaerobic biochemical reaction, and further improving the B/C ratio of the wastewater; part of effluent of the UASB anaerobic tower flows back to the hydrolysis acidification tank through an anaerobic return pipeline;

s7, enabling part of effluent of the UASB anaerobic tower to enter an anoxic tank, removing organic matters in the wastewater in an anaerobic and hydrolytic mode, and improving the B/C ratio of the wastewater;

s8, enabling the effluent of the anoxic tank to enter an A/O aerobic tank for aerobic biochemical reaction to degrade the residual micromolecular organic matters; the nitrifying liquid after the aerobic treatment flows back to the anoxic tank, and the mixed liquid of the nitrifying liquid flows back;

s9, enabling the effluent of the A/O aerobic tank to enter a secondary sedimentation tank for sludge-water separation, enabling the upper clear water to flow into a clear water tank for discharge after reaching the standard, and enabling the lower sludge to partially flow back to a hydrolysis acidification tank, an anoxic tank and the A/O aerobic tank, and pumping part of the lower sludge into a sludge concentration tank;

s10, performing filter pressing on the sludge in the sludge concentration tank, returning the supernatant to the regulating tank for treatment, and transporting the formed sludge cake to the outside.

8. The method for treating di-tert-butyl dicarbonate wastewater reaching the standards according to claim 4,

in step S1, after the high-salt wastewater and the low-salt wastewater are mixed, the COD value of the wastewater is 20000mg/L, and the pH value is 6-7;

in the step S2, controlling the pH value in the iron-carbon electrochemical reaction tank to be below 4-5, and reducing the COD of the wastewater to be below 16000mg/L after the micro-electrolysis reaction;

in step S4, adjusting the pH of the wastewater in the intermediate water pool to 6.5-7.0 by alkali;

in step S5, the pH value of the wastewater in the hydrolysis acidification tank is 6.0-7.0;

in the step S6, the operation temperature of the UASB anaerobic tower is 35-38 ℃, the hydraulic retention time is 2d, and the pH value of the wastewater is controlled to be 6.5-7.5; 50% of effluent of the UASB anaerobic tower flows back to the hydrolysis acidification tank, and 50% of effluent enters the anoxic tank;

in step S7, the hydraulic retention time of the anoxic pond is 1 d;

in the step S8, the content of dissolved oxygen in the A/O aerobic pool is controlled to be more than 2mg/L, the temperature is controlled to be 10-30 ℃, and the sedimentation ratio of the sludge after 30min of sedimentation is 50-70%; the reflux ratio of the nitrified liquid in the A/O aerobic pool to the anoxic pool is 1: 1;

in step S9, the sludge at the lower layer of the secondary sedimentation tank flows back to the hydrolytic acidification tank, the anoxic tank and the A/O aerobic tank by 20% of the amount of sludge per week, and the residual sludge is pumped into a sludge concentration tank.

9. The method for treating di-tert-butyl dicarbonate wastewater to reach the standard according to claim 7, characterized in that the removal rate of COD in the wastewater reaches more than 98% after the treatment.

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