CN109851161B - Treatment method of sewage produced in production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde - Google Patents
Treatment method of sewage produced in production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde Download PDFInfo
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Abstract
The invention discloses a method for treating sewage generated in the production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde, which comprises the following steps: neutralizing and centrifuging, removing formaldehyde, MVR evaporating, UASB anaerobic treatment, a hydrolysis acidification tank, contact oxidation, secondary sedimentation tank sedimentation, two-stage flocculation sedimentation, ozone oxidation, biological filter aeration treatment, ammonia removal treatment and sludge treatment. Compared with the prior art, the invention has the beneficial effects that: the lowest operation cost and the best solution are used for achieving the evaporation separation effect, so that the production cost is reduced, after advanced treatment and transformation, the COD discharge concentration of the wastewater is reduced from 500mg/L to 200mg/L, the ammonia nitrogen discharge concentration is reduced from 40mg/L to 25mg/L, and the wastewater pollutant discharge meets the standard and reaches the standard.
Description
Technical Field
The invention belongs to the field of sewage treatment, and relates to a method for treating sewage produced in the production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde.
Background
A certain chemical engineering science and technology company originally has a fluorescent whitening agent production line, and then a biphenyl dichlorobenzyl production line and an o-sodium sulfonate benzaldehyde production line are added.
As shown in fig. 1, the existing sewage treatment process is: the fluorescent whitening agent wastewater sequentially enters a comprehensive regulating tank and a neutralization tank for treatment, then is subjected to filter pressing by a plate-and-frame filter press, sludge enters a sludge concentration tank, filtrate sequentially enters a hydrolysis acidification tank, a contact oxidation tank, a secondary sedimentation tank and a two-stage flocculation sedimentation tank, and finally enters a standard-reaching discharge tank, sludge generated in the secondary sedimentation tank and the two-stage flocculation sedimentation tank also enters the sludge concentration tank, the sludge concentration tank is subjected to filter pressing by the filter press, supernatant enters the comprehensive regulating tank, and the sludge is transported and disposed.
However, the wastewater generated by producing the whitening agent, the o-sodium sulfonate benzaldehyde and the biphenyl dichlorobenzyl belongs to high-salt wastewater, the existing sewage treatment system main body adopts a process of 'hydrolytic acidification + contact oxidation + two-stage flocculation precipitation', salt needs to be removed in the wastewater treatment process, dichlorobenzyl wastewater is newly added in the wastewater treatment process, the wastewater contains a large amount of zinc mud, salt and formaldehyde, the existing triple-effect evaporation treatment has high energy consumption and insufficient treatment capacity, great pressure is applied to the whole wastewater treatment system, and the system cannot normally operate easily; in addition, the existing sewage system does not remove formaldehyde; the pretreated wastewater has large molecular weight and is difficult to degrade; the original effluent discharge take-over standard of the park is COD <500mg/L and ammonia nitrogen <40mg/L, and the new park effluent take-over standard is changed into COD <200mg/L and ammonia nitrogen <25mg/L, therefore, the chemical company urgently needs to upgrade and reform the existing sewage treatment system.
Disclosure of Invention
The present invention aims at solving the above problems in the prior art and provides a method for treating sewage produced in the production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde.
In order to solve the technical problems, the invention adopts the technical scheme that:
the treatment method of sewage produced by producing biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde comprises the following steps:
(1) firstly, carrying out neutralization reaction on dichlorobenzyl wastewater generated in the production of biphenyl dichlorobenzyl and fluorescer wastewater generated in the production of fluorescer to lead ph to be 7, and centrifuging the neutralized dichlorobenzyl wastewater by adopting a centrifugal machine to remove zinc-containing sludge in the neutralized dichlorobenzyl wastewater;
(2) after removing zinc mud, introducing the dichlorobenzyl wastewater and the fluorescer wastewater into a formaldehyde oxidation device for oxidation, adding 1-3% hydrogen peroxide in the oxidation process, removing formaldehyde and salt substances in the wastewater to obtain pretreated dichlorobenzyl wastewater and fluorescer wastewater, and introducing sludge generated in the formaldehyde oxidation process into a sludge concentration tank;
(3) the pretreated dichlorobenzyl wastewater and the fluorescer wastewater enter a homogenizing tank after being evaporated by an MVR falling film evaporator, and wastewater generated after sulfonic acid aldehyde wastewater generated by producing o-sodium sulfonate benzaldehyde is evaporated by an MVR forced evaporator, workshop equipment rinsing water, domestic sewage and wastewater after flocculation precipitation all enter the homogenizing tank to be mixed to obtain mixed wastewater;
(4) the mixed wastewater enters an up-flow anaerobic sludge bed reactor UASB for anaerobic reaction to remove organic matters in the mixed wastewater;
(5) the mixed wastewater after UASB anaerobic treatment sequentially enters a hydrolytic acidification tank and a contact oxidation tank for hydrolytic acidification and contact oxidation treatment, and organic matters in the mixed wastewater are further removed;
(6) the mixed wastewater after the contact oxidation treatment enters a secondary sedimentation tank for sedimentation, and then sequentially enters a primary flocculation sedimentation tank and a secondary flocculation sedimentation tank for two-stage flocculation sedimentation to remove insoluble substances, and the sludge generated in the secondary sedimentation tank and the sludge generated in the two-stage flocculation sedimentation tank both enter a sludge concentration tank;
(7) the mixed wastewater after flocculation and precipitation enters an ozone oxidation pond for oxidation treatment;
(8) the mixed wastewater after ozone oxidation enters an aeration biological filter to carry out aeration degradation on wastewater COD, and the COD is tested whether to reach the standard or not through an aeration biological filter experiment, and is discharged after reaching the standard;
(9) and (4) enabling the supernatant of the sludge concentration tank to enter the homogenization tank in the step (3), compressing the sludge in the sludge concentration tank by using a plate-and-frame filter press to generate sludge, transporting the sludge out, and treating the sludge out.
In the step (1), the pH of the dichlorobenzyl wastewater is adjusted to 3 by using 30-40% liquid alkali, and then the pH of the wastewater is adjusted to 7 by using soda ash.
And (3) homogenizing the waste water after the sulfonic acid aldehyde waste water is evaporated by the MVR forced evaporator, the flushing water of workshop equipment, the domestic sewage and the flocculated and precipitated waste water.
In the step (7), the gas production rate of the ozone generator in the ozone oxidation pond is 3 kg/h.
And (4) arranging an ammonia elimination agent adding device behind the biological aerated filter in the step (8) to remove ammonia nitrogen in the wastewater.
The evaporation speed of the MVR falling-film evaporator is 6.8t/h, and the evaporation speed of the MVR forced evaporator is 3.0 t/h.
In the step (3), the evaporation temperature of the MVR forced evaporator is set to be 85 ℃, and the temperature can be increased to 90-95 ℃ after the secondary steam is compressed.
Compared with the prior art, the invention has the beneficial effects that: the lowest operation cost and the best solution are used for achieving the evaporation separation effect, so that the production cost is reduced, the waste water is subjected to MVR falling film (6.8t/h) + MVR forcing (3.0t/h) + UASB + hydrolytic acidification + contact oxidation + secondary flocculation precipitation + ozone generator (3kg/h) + biological aerated filter + ammonia elimination device, after advanced treatment and modification, the COD discharge concentration of the waste water is reduced from 500mg/L to 200mg/L, the ammonia nitrogen discharge concentration is reduced from 40mg/L to 25mg/L, and the waste water pollutant discharge meets the standard and reaches the standard.
The MVR falling film evaporator and the MVR forced evaporator thoroughly solve the defects of triple-effect evaporation, enhance the pretreatment capacity of high-salt wastewater and relieve the wastewater treatment pressure of a system.
The formaldehyde oxidation device destroys formaldehyde in the wastewater under the high-temperature condition, enhances the pretreatment capacity of high-concentration wastewater, and reduces the treatment load of a subsequent biochemical system.
The UASB anaerobic equipment further degrades COD aiming at high-COD waste water with large molecular weight and difficult degradation, and relieves the biochemical treatment pressure.
The ozone generator and the ammonia elimination device effectively reduce COD and ammonia nitrogen, and the effluent meets the new pipe connection standard. If the standard COD of the sewage in the park is less than 500mg/L and the ammonia nitrogen is less than 25mg/L, the ozone oxidation system stops running.
Drawings
FIG. 1 is a schematic flow diagram of a conventional wastewater treatment process of the chemical plant;
FIG. 2 is a schematic flow chart of the method for treating sewage produced in the production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde according to the present invention.
Detailed Description
The present invention will now be described in further detail with reference to examples and the accompanying drawings. The drawings are simplified schematic views illustrating only the basic structure of the present invention in a schematic manner, and thus show only the constitution related to the present invention.
As shown in figure 2, the treatment method of the sewage produced by the production of the biphenyl dichlorobenzyl and the o-sodium sulfonate benzaldehyde comprises the following steps:
(1) firstly, carrying out neutralization reaction on dichlorobenzyl wastewater generated in the production of biphenyl dichlorobenzyl and fluorescer wastewater generated in the production of fluorescer, firstly adjusting the pH of the dichlorobenzyl wastewater to 3 by using liquid caustic soda with the concentration of 30-40%, then adjusting the pH of the wastewater to 7 by using soda ash, and centrifuging the neutralized dichlorobenzyl wastewater by using a centrifugal machine to remove zinc-containing sludge;
(2) after removing zinc mud, introducing the dichlorobenzyl wastewater and the fluorescer wastewater into a formaldehyde oxidation device for oxidation, adding 1-3% hydrogen peroxide in the oxidation process, removing formaldehyde and salt substances in the wastewater to obtain pretreated dichlorobenzyl wastewater and fluorescer wastewater, and introducing sludge generated in the formaldehyde oxidation process into a sludge concentration tank;
(3) the method comprises the following steps that pretreated waste water of dichlorobenzyl and fluorescent agent enters a homogenizing tank after being evaporated by an MVR falling-film evaporator, waste water, workshop equipment flushing water, domestic sewage and waste water after flocculation precipitation, which are generated during production of o-sodium sulfonate benzaldehyde, enter the homogenizing tank to be mixed, the evaporation speed of the MVR falling-film evaporator is 6.8t/h, the evaporation temperature of the MVR forced evaporator is 85 ℃, the temperature can be increased to 90-95 ℃ after secondary steam is compressed, the evaporation speed of the MVR forced evaporator is 3.0t/h, and the waste water, the workshop equipment flushing water, the domestic sewage and the waste water after flocculation precipitation, which are evaporated by the MVR forced evaporator, are homogenized to obtain mixed waste water;
(4) the mixed wastewater enters an up-flow anaerobic sludge bed reactor UASB for anaerobic reaction to remove organic matters in the mixed wastewater,
(5) the mixed wastewater after UASB anaerobic treatment sequentially enters a hydrolytic acidification tank and a contact oxidation tank for hydrolytic acidification and contact oxidation treatment, and organic matters in the mixed wastewater are further removed;
(6) the mixed wastewater after the contact oxidation treatment enters a secondary sedimentation tank for sedimentation, and then sequentially enters a primary flocculation sedimentation tank and a secondary flocculation sedimentation tank for two-stage flocculation sedimentation to remove insoluble substances, and the sludge generated in the secondary sedimentation tank and the sludge generated in the two-stage flocculation sedimentation tank both enter a sludge concentration tank;
(7) the mixed wastewater after flocculation and precipitation enters an ozone oxidation pond for oxidation treatment, and the gas production rate of an ozone generator in the ozone oxidation pond is 3 kg/h;
(8) the mixed wastewater after ozone oxidation enters an aeration biological filter to carry out aeration degradation on wastewater COD, and the COD is tested whether to reach the standard or not through an aeration biological filter experiment, and is discharged after reaching the standard; a set of ammonia removing agent adding device is arranged behind the biological aerated filter to remove ammonia nitrogen in the wastewater; the ammonia-eliminating pesticide can ensure that the wastewater reaches the standard and is discharged in a short time, so when the ammonia nitrogen in the effluent of the aeration biological filter tank reaches less than 25mg/L, the ammonia-eliminating pesticide is directly added, and when the effluent of the filter tank reaches the standard, the ammonia-eliminating pesticide is used as an emergency pesticide;
(9) and (4) enabling the supernatant of the sludge concentration tank to enter the homogenization tank in the step (3), compressing the sludge in the sludge concentration tank by using a plate-and-frame filter press to generate sludge, transporting the sludge out, and treating the sludge out.
Example 1
The following table is used for determining the partial indexes of the wastewater after detecting a water sample (after the workshop production wastewater is subjected to reduced pressure evaporation) provided by the chemical company:
TABLE 1.1 raw Water quality index List
The effluent index is the water quality index which is required by the local environmental protection department and discharged to the municipal sewage treatment plant, and is detailed in the following table:
TABLE 1.2 Water quality index List
| COD(mg/L) | NH3-N(mg/L) | pH | Whole salt (mg/L) | Total phosphorus (mg/L) |
| ≤500 | ≤40 | 6～8 | ≤5000 | ≤1.0 |
Experimental process and data for wastewater treatment
(1) And (3) neutralization and centrifugation, namely performing a neutralization experiment on the wastewater by using liquid caustic soda, adjusting the pH to 3 by using liquid caustic soda with the concentration of 30-40%, adjusting the pH of the wastewater to 7 by using sodium carbonate, and performing suction filtration on the dichlorobenzyl wastewater, wherein the suction filtration has the same centrifugal filtration effect. Taking supernatant to detect the content of COD and formaldehyde in the wastewater.
(2) And (3) evaporation: the supernatant was evaporated. And (3) adding 2% and 3% hydrogen peroxide into the wastewater under the condition that the pH is 7 to perform evaporation experiments respectively, and monitoring the COD (chemical oxygen demand) and formaldehyde content in the wastewater after evaporation.
The temperature is firstly preserved for 2 hours at 70 ℃, and the detection data are as follows:
| water sample | Formaldehyde number | Removal rate of formaldehyde | COD value | COD removal rate |
| Neutralized waste water | 12678 | 15530 | ||
| After 2% hydrogen peroxide is evaporated | 2307 | 81.8％ | ||
| After 3% hydrogen peroxide is evaporated | 326 | 97.5％ | 4369 | 71.8％ |
| Water collecting sample of sewage station | 124.2 | 3333.5 | ||
| After the collected water sample of the sewage station is evaporated | 122.3 | 1.5％ | 1674.5 | 49.8％ |
After 2% and 3% hydrogen peroxide are respectively used for evaporating the neutralized wastewater, the ammonia nitrogen removal rate of the 3% hydrogen peroxide is much higher than that of the 2%, and a water sample evaporated by the 3% hydrogen peroxide can be directly used for an anaerobic experiment in indexes.
(3) Anaerobic experiment: 500mL of granular sludge was added to a 1L volumetric flask, and the water sample was added to the volumetric flask until the volumetric flask was full. And mixing the water sample of the dichlorobenzyl wastewater evaporated by 3% of hydrogen peroxide with the water sample of the sulfonic acid aldehyde wastewater evaporated by 1:1, and respectively performing a group of anaerobic experiments on the water samples evaporated by 3% of hydrogen peroxide. The change of COD and PH of the wastewater was monitored daily and when the pH of the wastewater was below 7, the pH was adjusted back to 7-8 by adding caustic soda solution to the flask. The volumetric flask needs to rock 3 times every day, rocks every time and needs to evenly mix mud and waste water in the waste water.
The wastewater indexes after 48 hours of fermentation are shown in the following table:
the experimental result shows that the ammonia nitrogen value cannot be removed by anaerobic treatment, the higher ammonia nitrogen value can influence the removal rate of anaerobic bacteria to the COD value, the reaction is more severe in the first 24 hours from the start of the anaerobic treatment, more methane bubbles are generated, and the reaction rate tends to be stable along with the time extension.
(4) Through simulating the existing sewage station process, hydrolyzing and acidifying sludge in an anoxic tank, performing aerobic treatment on sludge in an aerobic tank, performing flocculation and precipitation by using PAC and PAM, and obtaining the ammonia nitrogen value and COD value conditions of a water sample as follows:
| water sample | Ammonia nitrogen value | Ammonia nitrogen removal rate | COD value | COD removal rate |
| After 3% hydrogen peroxide evaporates water and is anaerobic | 330.5 | 1901.5 | ||
| After hydrolytic acidification | 210.8 | 36.2％ | 1391.5 | 26.8％ |
| After aerobic treatment | 41.3 | 80.4％ | 1084.0 | 22.1％ |
| After flocculation and precipitation | 28.9 | 30.0％ | 339.8 | 68.7％ |
As can be seen from the data in the table, the data result obtained by the simulation experiment is close to the predicted proportion, and the ammonia nitrogen value and the COD value of the final effluent can reach the discharge standard.
Example 2
The water quantity and quality of various waste water of the chemical plant
TABLE 2.1 quality and quantity of water from waste water of benzyl dichloride and sulfonic acid aldehyde
TABLE 2.2 quality and quantity of other waste waters
Wastewater characteristic contaminant factor detection
| Product name | Characteristic factor of waste water |
| O-sodium sulfonate benzaldehyde | COD, SS, total salt |
| Biphenyl dichloro benzyl | COD, formaldehyde, toluene, total zinc and total phosphorus |
Local discharge requirements
According to the requirements of local environmental protection departments, the wastewater discharge index is a water quality index discharged to a park sewage treatment plant, and specifically comprises the following steps:
the wastewater treatment steps are as follows:
step one, neutralization and centrifugation
And (2) carrying out neutralization reaction on the dichlorobenzyl wastewater and the fluorescer wastewater entering a water collecting tank of the sewage station to ensure that the ph is 7, centrifuging the neutralized dichlorobenzyl wastewater by adopting a centrifugal machine to remove zinc-containing sludge, and feeding the centrifuged wastewater into a wastewater collecting tank.
Step two, formaldehyde oxidation
Wastewater in the wastewater collection pool enters a formaldehyde oxidation device for oxidation, hydrogen peroxide with the concentration of 3% is added in the oxidation process, formaldehyde and salt substances in the wastewater are removed, pretreated dichlorobenzyl wastewater and fluorescer wastewater are obtained, and sludge generated in the formaldehyde oxidation process enters a sludge concentration pool.
Step three, MVR treatment process flow
And (4) feeding the pretreated dichlorobenzyl wastewater and the fluorescent agent wastewater into an MVR falling film evaporator for evaporation, and feeding the sulfonic acid aldehyde wastewater into an MVR forced evaporator for evaporation.
The purpose of the scheme is as follows: the evaporation separation effect is achieved with the lowest operation cost and the best solution, so that the production cost is reduced.
The MVR process is described as follows:
the solubility of the solute does not change much with temperature in the vaporization temperature range and the boiling point of the material rises high. The solution boiling point rise with the highest boiling point in the normal pressure saturated state is taken as a theoretical basis in the scheme stage. The values in the scheme are that the boiling point rising end point of a saturated sodium chloride solution of a material is about 10 ℃, and the boiling point rising end point of an ammonium chloride solution is about 15 ℃.
The MVR-FC continuous crystallization system is used for processing, the MVR system is coupled with the FC crystallizer, a mixed flow pump is selected for the system, the scaling tendency is reduced due to the large flow rate, and the cleaning period is prolonged. And the mixed flow pump has larger and proper flow which is also a necessary condition for controlling the metastable zone of material crystallization, thereby creating conditions for growing crystals with proper scale.
The vapor compressor adopts a single positive displacement compressor, and when fluid enters the vapor-liquid crystallizer from the heat exchanger, a central feeding mode is adopted. Because the incoming material has no heat sensitivity, the optional evaporation temperature is arbitrary, and the design is temporarily set to be 85 ℃. The higher centrifugation temperature can reduce the moisture content of the material, so the high-temperature centrifugation mode is selected, and the centrifugation temperature is 85 ℃.
Basic flow feed liquid flow of MVR evaporator
The feed liquid with the pH value of 7 is firstly recycled by a preheater to recover the sensible heat of the condensate, the feed liquid is pumped into a circulating pipe of a circulating heat exchanger by a raw material pump, the feed liquid is heated by the circulating pipe and then enters a separator for evaporation, the solution is flashed at a two-phase interface, the evaporated solution immediately flows downwards under the suction of a circulating pump to be mixed with the fresh feed liquid to enter the next circulation, and the feed liquid is discharged after the discharge requirement is met.
Steam flow
The secondary steam in the circulation separator moves upwards to enter the roots type steam compressor, the roots type steam compressor compresses the secondary steam to the process design temperature and then returns to the shell pass of the circulation heat exchanger to release latent heat, and condensed water enters the condensate collecting tank.
Crystallizer/separator
The material liquid is heated by the circulating heat exchanger and enters the crystallizer/separator for evaporation, the evaporation process is continuously carried out in a fully closed state, and the temperature, the pressure and the material liquid concentration in the equipment can be kept in the state which is most suitable for evaporation. The crystallizer/separator is internally provided with the high-efficiency foam catcher, so that the vapor-liquid separation efficiency can be improved, and the entrainment can be reduced.
The spraying device is arranged in the crystallizer/separator and has two functions, namely, a foam catcher is washed, and the material is prevented from being hung on the wall.
Circulating heat exchanger
A tube-plate heat exchanger is adopted. Due to the function of MVR, the device is not only a material heater, but also a condenser of secondary steam. The heat transfer efficiency is high, the floor area is small, and the equipment price is low.
In the process of evaporation, partial organic matters can gradually adhere to the inner wall of the heat exchange tube to cause the reduction of the convection heat transfer coefficient in the tube, so that the K value is greatly reduced, and the heat exchanger is convenient to use a short tube which is convenient to disassemble and maintain in the future in the design for cleaning in the running process in future.
The heater tube side material is Ta2, and the shell side material is 316L.
Vapor compressor
The full stainless steel vapor compressor specially designed for vapor compression is adopted, and the full stainless steel vapor compressor has the advantages of low noise, low vibration, high reliability and the like.
Explanation of the procedure
The feed liquid to be treated is pumped into the evaporation system by a pump. The feed liquid is pumped into the tube-plate heat exchanger by a feed pump, the feed liquid in the tube-plate heat exchanger exchanges heat with steam condensate water in the evaporator, and the feed liquid enters the crystallizer/separator for evaporation after being preheated.
The secondary vapor from the crystallizer/separator enters the MVR compression system. After the secondary steam is compressed, the temperature can be raised to about 91 ℃, and the compressed steam enters a circulating heat exchanger to heat materials. In the process of heating the materials, the steam is condensed into water and discharged by a water pump, the temperature of the water is about 91 ℃, and at the moment, the circulating heat exchanger is used as a material heater and a pressed steam cooler.
After the preheated material enters the circulating heat exchanger, the preheated material exchanges heat with the compressed secondary steam after temperature rise, the whole system reaches heat balance, the external fresh steam is not needed to be heated at the moment, and only the compressor is needed to maintain the heat balance of the whole system.
And step four, the wastewater of the dichlorobenzyl wastewater and the fluorescent agent wastewater pretreated by the homogenizing tank and evaporated by an MVR falling film evaporator enters the homogenizing tank, the wastewater of the sulfonic acid aldehyde wastewater generated in the production of o-sodium sulfonate benzaldehyde is evaporated by an MVR forced evaporator, the flushing water of workshop equipment, domestic sewage and the wastewater after flocculation precipitation all enter the homogenizing tank to be mixed, mixed wastewater is obtained, and the mixed wastewater is homogenized.
Step five, biochemical treatment process
The anaerobic treatment of the mixed wastewater adopts an upflow anaerobic sludge reactor (UASB) for treatment.
The upflow anaerobic sludge reactor (UASB) technology has been developed at home and abroad as one of the mainstream technologies for anaerobic treatment, the UASB has no carrier, sewage uniformly enters from the bottom and flows upwards, and granular sludge (sludge floc) is in a suspension state under the action of rising water flow and air bubbles. The lower part of the reactor is a sludge bed with higher concentration, and the upper part is a suspended sludge layer with lower concentration, and organic matters are converted into methane and carbon dioxide gas. In the upper part of the reactor there is a three-phase separator, which allows degassing and settling of the sludge back into the reactor. The UASB has higher COD load, and the sludge concentration in the reactor reaches 100-150 g/L, so the COD removal efficiency is three times higher than that of the common anaerobic reactor and can reach 80-95 percent. The starting time is short, the device can run discontinuously or seasonally, the investment is low, and the operation management is simple.
Step six, anaerobic and aerobic treatment process of sewage
The mixed wastewater after UASB anaerobic treatment sequentially enters a hydrolytic acidification tank and a contact oxidation tank for hydrolytic acidification and contact oxidation treatment, and organic matters in the mixed wastewater are further removed
The sewage is treated by adopting an anaerobic-aerobic A/O method, because the waste water contains higher organic matters, the simple aerobic biological treatment is difficult to meet the requirements, and in addition, the sludge treatment problem is a big problem which is not solved in the field of waste water treatment, therefore, in order to search for a new waste water treatment technology with high efficiency, low consumption and low investment, a great deal of research is carried out in the aspects of anaerobic and aerobic process combination and aerobic process reinforcement in recent years, and breakthrough progress is made.
The anaerobic-aerobic A/O process utilizes hydrolysis and acidification stages of anaerobic treatment, abandons a methanogenesis (alkaline fermentation) stage, and mainly aims to realize the conversion of organic matters difficult to biodegrade through hydrolysis and non-hydrolysis, and converts organic molecules difficult to biodegrade with complex structures into organic matters capable of being biodegraded slowly or rapidly through molecular structure change (ring opening, bond breaking, cracking, group substitution, reduction and the like), so that the biotreatability and the decoloration effect of sewage are obviously improved, and a final electron acceptor comprises the organic matters difficult to biodegrade (groups or chemical bonds in a molecular structure). The effluent quality is stable, the impact load is reduced, and conditions are created for aerobic treatment. On the other hand, the method is characterized in that the residual sludge generated in the aerobic section completely flows back to the anaerobic section, and because the anaerobic section has enough biological Solid Retention Time (SRT), the sludge can be subjected to thorough anaerobic digestion in the anaerobic section, so that the residual sludge is completely decomposed into H2O and CO2 in the circulation process, the whole system achieves the sludge balance of the whole system, discharges less or no sludge, effectively solves the problem of pulp-dyed wastewater sludge, and simultaneously can play a role in biological denitrification. Therefore, the anaerobic section of the process has double functions, namely, the wastewater is pretreated to improve the biochemical property of the wastewater and absorb and degrade a part of organic matters; secondly, the sludge of the system is digested.
1. The process is characterized in that:
(1) the A/O mostly adopts biological filler with large specific surface area, high porosity and smooth water flow, and is suitable for the inhabitation and proliferation of microorganisms due to the addition of sufficient organic matters and dissolved oxygen, so that the organisms on the biological membrane are abundant, and the bacteria, various protozoa and metazoans can grow filamentous bacteria of the genus corselella with strong oxidizing capability without the sludge bulking phenomenon. A stable ecosystem and food chain can be formed on the biofilm.
(2) The surfaces of the fillers are all densely covered by the biological film to form a main body structure of the biological film, and due to the breeding of a large number of filamentous bacteria, a dense biological net in a three-dimensional structure is possibly formed, so that the purification effect can be effectively improved when the wastewater passes through the biological net.
(3) Because the aeration is carried out, the surface of the biological membrane is continuously subjected to aeration stripping, so that the activity of the biological membrane is favorably kept, the anaerobic membrane is always proliferated, the utilization rate of oxygen is also favorably improved, and the active biomass with higher concentration can be kept. Because of this, the a/O can accept a higher organic load, and the treatment efficiency is higher, contributing to a reduction in the reaction tank volume and the floor space.
2. The characteristics of the operation aspect are as follows: the method has stronger adaptability to impact load, can still keep good treatment effect under the condition of intermittent operation, and has practical significance to enterprises with uneven drainage; the operation is simple, the operation is convenient, the maintenance and the management are easy, the sludge backflow is not needed, and the sludge expansion phenomenon is not generated; the sludge generation amount is small, the sludge particles are large, and the sedimentation is easy.
3. Features in functional terms: has various purification functions, can effectively remove organic pollutants, can be used for denitrification and dephosphorization if properly operated, and can be used as a three-stage treatment technology.
The A/O saves the occupied area, is convenient to operate and has simpler processing flow; the method is simple to operate, easy to maintain and manage, high in microorganism content through film hanging, strong in adaptability to wastewater difficult to treat and good in treatment effect.
Step seven, precipitation and flocculation precipitation
The mixed wastewater after the contact oxidation treatment enters a secondary sedimentation tank for sedimentation, then enters a first-stage flocculation sedimentation tank and a second-stage flocculation sedimentation tank in sequence for two-stage flocculation sedimentation to remove insoluble substances, and the sludge generated in the secondary sedimentation tank and the sludge generated in the two-stage flocculation sedimentation tank both enter a sludge concentration tank.
Step eight, the mixed wastewater after flocculation and precipitation enters an ozone oxidation pond for oxidation treatment; and (3) introducing the mixed wastewater after ozone oxidation into the aeration biological filter for aeration degradation of wastewater COD, and testing whether the COD reaches the standard or not through an aeration biological filter experiment, wherein the COD is discharged after reaching the standard.
And step nine, when the ammonia nitrogen index needs to be adjusted, arranging an ammonia elimination agent adding device behind the biological aerated filter for removing the ammonia nitrogen in the wastewater.
Step ten, sludge treatment
Sludge in the formaldehyde oxidation process, sludge in the secondary sedimentation tank and sludge in the two-stage flocculation sedimentation tank all enter a sludge concentration tank, supernatant of the sludge concentration tank enters a homogenizing tank in the step (3), sludge generated after the sludge in the sludge concentration tank is compressed by a plate-and-frame filter press is transported out, and external treatment is performed
Sludge generated in sewage treatment is concentrated and collected by a sludge concentration tank, dewatered by a plate-and-frame filter press and transported outside.
Operating cost estimation
Oxidation of dichloro-benzaldehyde
1. After neutralizationWaste water 35m3Day, cost of medication: 2% of hydrogen peroxide, and the unit price is 2000 yuan/ton; and (4) converting the medicament cost: 1400 yuan/day.
II, sulfonic acid aldehyde (mother liquor) wastewater: 12m3
Third, forced circulation
1. High-salinity wastewater: 35m of waste water after neutralization of dichlorobenzyl3(ii) a Waste water after sulfonic acid aldehyde concentration is 12m3Total of 47m3. Feed (MVR force) 3.6m per hour3And converting the consumed time: for 13 hours.
2. The steam is calculated according to 198 yuan/ton, 0.2 ton of steam is needed per hour, the steam is operated for 13 hours each day, and the steam consumption cost is reduced: 515 yuan/day.
3. The capacity of the electric machine is 235Kw, the operation is calculated according to 180Kw, the electric charge is calculated according to 0.8 yuan/Kw, the operation is carried out for 13 hours every day, and the consumed electric charge is converted: 1872 yuan/day.
Fourthly, flocculation reaction, biochemical treatment and advanced treatment operation
1. According to 260m per day3The waste water consumes 78kg of PAC and 0.26kg of pAM, and the reduced cost is as follows: 135 yuan/day.
2. The installed capacity of the electricity and ozone generator is 75kw, the other is 120kw, the operation power is 150kw, the electricity is 0.8 yuan/kw, and the electricity cost is converted: 1020 yuan/day.
3. 500 yuan/day for sludge and xiaoailing.
Labor cost
The sewage station (including MVR enforcement and MVR falling film) staffs compile 10 persons, and the wages of the staffs are 180 yuan per person per day. Converting daily labor cost: 1800 yuan.
Totaling the daily sewage treatment cost: 7242 yuan, according to the daily treatment of 110m sewage3Calculating the cost converted into ton waste water treatment: 65.84 yuan, the wastewater treatment cost is very low.
Example 3
In the production process of the fluorescent brightener AMS, wastewater generated in a filter pressing working section is stored in a workshop collecting tank and is pumped into a sewage station collecting tank through a lift pump, and the wastewater is discharged into a sewage treatment plant in a park after being treated to reach the standard through neutralization, centrifugation, a formaldehyde oxidation device, MVR, a homogenization tank, UASB, hydrolytic acidification, contact oxidation, a secondary sedimentation tank, secondary flocculation reaction, ozone oxidation, an ammonia elimination device and a discharge tank. Filter residues generated by filter pressing of the project are treated as hazardous wastes and are disposed outside.
Example 4
In the production process of the fluorescent brightener APC, wastewater generated in a nanofiltration working section is stored in a workshop collecting tank, and is pumped into a sewage station collecting tank through a lifting pump, and the wastewater is discharged into a sewage treatment plant after reaching the standard through neutralization, centrifugation, formaldehyde oxidation device, MVR, homogenization tank, UASB, hydrolytic acidification, contact oxidation, secondary sedimentation tank, secondary flocculation reaction, ozone oxidation, ammonia removal device and discharge tank. Filter residues generated by project filter pressing, and a waste nanofiltration membrane is used as hazardous waste and is disposed outside.
Example 5
In the production process of the fluorescent brightener 357, wastewater generated in a nanofiltration working section is stored in a workshop collecting tank and is pumped into a sewage station collecting tank through a lift pump, and the wastewater is discharged into a sewage treatment plant after reaching the standard through neutralization, centrifugation, a formaldehyde oxidation device, MVR, a homogenization tank, UASB, hydrolysis acidification, contact oxidation, a secondary sedimentation tank, secondary flocculation reaction, ozone oxidation, an ammonia elimination device and a discharge tank. Filter residues generated by project filter pressing, and a waste nanofiltration membrane is used as hazardous waste and is disposed outside.
In light of the foregoing description of the preferred embodiment of the present invention, many modifications and variations will be apparent to those skilled in the art without departing from the spirit and scope of the invention. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims.
Claims (7)
1. The treatment method of the sewage produced by producing the biphenyl dichlorobenzyl and the o-sodium sulfonate benzaldehyde is characterized by comprising the following steps of: the method comprises the following steps:
(1) firstly, carrying out neutralization reaction on dichlorobenzyl wastewater generated in the production of biphenyl dichlorobenzyl and fluorescer wastewater generated in the production of fluorescer to ensure that the pH is =7, and centrifuging the neutralized dichlorobenzyl wastewater by adopting a centrifugal machine to remove zinc-containing sludge in the neutralized dichlorobenzyl wastewater;
(2) after removing zinc mud, introducing the dichlorobenzyl wastewater and the fluorescer wastewater into a formaldehyde oxidation device for oxidation, adding 1-3% hydrogen peroxide in the oxidation process, removing formaldehyde and salt substances in the wastewater to obtain pretreated dichlorobenzyl wastewater and fluorescer wastewater, and introducing sludge generated in the formaldehyde oxidation process into a sludge concentration tank;
(3) the pretreated dichlorobenzyl wastewater and the fluorescer wastewater enter a homogenizing tank after being evaporated by an MVR falling film evaporator, and wastewater generated after sulfonic acid aldehyde wastewater generated by producing o-sodium sulfonate benzaldehyde is evaporated by an MVR forced evaporator, workshop equipment rinsing water, domestic sewage and wastewater after flocculation precipitation all enter the homogenizing tank to be mixed to obtain mixed wastewater;
(4) the mixed wastewater enters an up-flow anaerobic sludge bed reactor UASB for anaerobic reaction to remove organic matters in the mixed wastewater;
(5) the mixed wastewater after UASB anaerobic treatment sequentially enters a hydrolytic acidification tank and a contact oxidation tank for hydrolytic acidification and contact oxidation treatment, and organic matters in the mixed wastewater are further removed;
(6) the mixed wastewater after the contact oxidation treatment enters a secondary sedimentation tank for sedimentation, and then sequentially enters a primary flocculation sedimentation tank and a secondary flocculation sedimentation tank for two-stage flocculation sedimentation to remove insoluble substances, and the sludge generated in the secondary sedimentation tank and the sludge generated in the two-stage flocculation sedimentation tank both enter a sludge concentration tank;
(7) the mixed wastewater after flocculation and precipitation enters an ozone oxidation pond for oxidation treatment;
(8) the mixed wastewater after ozone oxidation enters an aeration biological filter to carry out aeration degradation on wastewater COD, and the COD is tested whether to reach the standard or not through an aeration biological filter experiment, and is discharged after reaching the standard;
(9) and (4) enabling the supernatant of the sludge concentration tank to enter the homogenization tank in the step (3), compressing the sludge in the sludge concentration tank by using a plate-and-frame filter press to generate sludge, transporting the sludge out, and treating the sludge out.
2. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: in the step (1), the pH of the dichlorobenzyl wastewater is adjusted to 3 by using 30-40% liquid alkali, and then the pH of the wastewater is adjusted to 7 by using sodium carbonate.
3. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: and (3) homogenizing the waste water after the sulfonic acid aldehyde waste water is evaporated by the MVR forced evaporator, the flushing water of workshop equipment, the domestic sewage and the flocculated and precipitated waste water.
4. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: in the step (7), the gas production rate of the ozone generator in the ozone oxidation pond is 3 kg/h.
5. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: and (4) arranging an ammonia elimination agent adding device behind the biological aerated filter in the step (8) to remove ammonia nitrogen in the wastewater.
6. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: the evaporation speed of the MVR falling-film evaporator is 6.8t/h, and the evaporation speed of the MVR forced evaporator is 3.0 t/h.
7. The method for treating sewage produced in the production of biphenyl dichlorobenzyl and sodium o-sulfonate benzaldehyde according to claim 1, wherein the method comprises the following steps: in the step (3), the evaporation temperature of the MVR forced evaporator is set to be 85 ℃, and the temperature can be increased to 90-95 ℃ after the secondary steam is compressed.
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| CN111908740A (en) * | 2020-09-06 | 2020-11-10 | 山东蓝城分析测试有限公司 | Method for treating wall imitation stone coating wastewater |
| CN116239264A (en) * | 2023-03-24 | 2023-06-09 | 吴桥县六合德利化工有限责任公司 | Waste water recovery process for preparing sodium o-sulfonate benzaldehyde |
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| CN1792894A (en) * | 2005-11-17 | 2006-06-28 | 中国地质大学（武汉） | Process for treating yellow ginger saponin waste water by hydrochloric acid method |
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| CN1792894A (en) * | 2005-11-17 | 2006-06-28 | 中国地质大学（武汉） | Process for treating yellow ginger saponin waste water by hydrochloric acid method |
| CN101423313A (en) * | 2008-11-14 | 2009-05-06 | 山西大学 | Fluorescent whitening agent production waste water treatment process |
| CN102115291A (en) * | 2009-12-31 | 2011-07-06 | 凯特琳·陈晓英 | Process for treating high-concentration organic wastewater difficult to degrade |
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