CN211595362U - High-salt-content high-organic-matter chemical wastewater treatment device - Google Patents
High-salt-content high-organic-matter chemical wastewater treatment device Download PDFInfo
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- CN211595362U CN211595362U CN201922405357.9U CN201922405357U CN211595362U CN 211595362 U CN211595362 U CN 211595362U CN 201922405357 U CN201922405357 U CN 201922405357U CN 211595362 U CN211595362 U CN 211595362U
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Abstract
The utility model provides a high organic matter chemical wastewater treatment device that contains salt belongs to sewage treatment technical field, the utility model provides a device is including the waste water equalizing basin, the acid adjusting pond, the fenton tower, the pond of degasifying, reaction tank, sedimentation tank, evaporation distribution tank, vaporization system, anaerobism distribution tank, UASB anaerobic tower, oxygen deficiency pond, good oxygen pond, two heavy ponds, reaction tank, materialization sedimentation tank and the clean water basin that connect in order. The device provided by the utility model successfully solves the difficult problem of high-salt and high-organic chemical wastewater treatment, does not produce biochemical sludge, and has the characteristics of low operating cost, stable operation and the like.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, especially, relate to a contain salt organic chemical industry waste water processing apparatus up to standard.
Background
At present, about 3 thousands of chemical enterprises exist in China, and account for about 70 percent of the total number of the industrial enterprises. Although the chemical enterprises in China have different scales, some obvious commonalities exist: such as strong resource dependence, strong technical dependence, special production flow, large-scale production and the like, and can find that a common chemical plant can generate a large amount of wastewater. The consumption of tap water in a chemical plant as a water consumer is generally hundreds of thousands of cubic meters per year, the reuse rate of water is low, and simultaneously, the discharged sewage is hundreds of thousands of cubic meters, so that a large amount of water resources are wasted, the environmental pollution is caused, and the shortage of water resources at present threatens the production of the industrial water consumers. In order to maintain the sustainable development of enterprises, reduce the waste of water resources, reduce the production cost and improve the economic benefit and social benefit of the enterprises, the salt-containing organic chemical wastewater needs to be subjected to advanced treatment.
The treatment of the salt-containing organic chemical wastewater mainly treats the high-salt high-concentration organic wastewater, but the high-salt high-organic wastewater is always a big difficulty in domestic environment treatment. Whether the salt-containing organic chemical wastewater can be stably treated and discharged after reaching standards becomes a bottleneck for restricting the continuous vigorous development of chemical enterprises. The quality of water discharged after the traditional salt-containing organic chemical wastewater treatment process is not stable and reaches the standard, and the environment is easily influenced.
SUMMERY OF THE UTILITY MODEL
In view of this, the present invention is directed to a process route mainly comprising "adjustment + fenton pretreatment + evaporation + anaerobic + biochemical + physical chemical treatment" to classify the production wastewater into high-salinity wastewater, low-salinity wastewater, alkaline wastewater, acidic wastewater and oily wastewater; adding acidic wastewater into the high-salinity wastewater and the oily wastewater subjected to air floatation treatment in an acid regulating tank to regulate the pH value to acidity, performing Fenton tower and degassing reaction, adding alkaline wastewater to regulate the pH value to neutrality, adding PAM (polyacrylamide) to perform coagulation reaction and precipitation, and collecting sludge and overflow liquid; pumping the overflow liquid into an evaporator to remove salt; mixing the evaporated wastewater with low-salt wastewater in a distribution tank, performing biochemical treatment, namely anaerobic treatment, anoxic treatment, aerobic treatment and secondary sedimentation, and performing coagulation reaction and sedimentation to obtain effluent reaching the standard; the device provided by the utility model successfully solves the difficult problem of high-salt and high-organic chemical wastewater treatment, does not produce biochemical sludge, and has the characteristics of low operating cost, stable operation and the like. The device can synchronously remove fluorine substances, salt inorganic substances and COD, can effectively solve the problem that the salt-containing organic chemical wastewater is high in salt and organic substances and difficult to treat, thoroughly degrades the organic substances in the salt-containing organic chemical wastewater, effectively removes total nitrogen, has small sludge production amount in the whole process, can eliminate sludge in a system by biochemical sludge, and effectively reduces the investment and operating cost of sludge treatment; the method has the advantages of low operation cost, simple operation management and the like.
In order to realize the purpose of the utility model, the utility model provides a following technical scheme:
the utility model provides a salt-containing organic chemical industry wastewater standard treatment device, which comprises a wastewater adjusting tank, an acid regulating tank, a Fenton tower, a degassing tank, a reaction tank, a sedimentation tank, an evaporation water distribution tank, an evaporation system, an anaerobic water distribution tank, a UASB anaerobic tower, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a reaction tank, a physicochemical sedimentation tank and a clean water tank which are connected in sequence; the wastewater adjusting tank comprises an alkaline wastewater adjusting tank, a high-salinity wastewater adjusting tank, an acidic wastewater adjusting tank, a low-salinity wastewater adjusting tank and an oily wastewater adjusting tank which are connected in parallel; an air floatation tank is also arranged between the oily wastewater regulating tank and the acid regulating tank; the air flotation tank, the sedimentation tank and the physicochemical sedimentation tank are respectively connected with the sludge tank.
The device carries out a front-section treatment process route mainly comprising water quality regulation, Fenton pretreatment and evaporation aiming at the characteristics of high-salinity and high-organic matters in chemical wastewater; the biological treatment process of anaerobic treatment, anoxic treatment, aerobic treatment and sedimentation treatment is adopted as a core, wherein the anoxic and aerobic comprehensive treatment can synchronously perform denitrification and dephosphorization, remove COD (chemical oxygen demand) and reduce chroma, and the problems of difficult treatment of nitrogen and phosphorus in the wastewater and the like are effectively solved; the utility model discloses the COD in the chemical industry waste water can be reduced to below 500mg/L from 30000mg/L to the device, reduces the TDS in the waste water to below 3000mg/L from 40000mg/L, reduces the fluorine content in the waste water to below 20mg/L from 5000mg/L simultaneously. The effluent can reach the B-level standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 45mg/L, total nitrogen is less than or equal to 70mg/L, and F is less than or equal to 20mg/L) in the water quality standard for sewage discharge into cities and towns (GB/T31962-2015), the sludge yield of the whole process is small, the investment and the operation cost of sludge treatment are effectively reduced, and the method has the advantages of low power consumption, low operation cost, simplicity in operation and management, stability in operation and the like.
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Fig. 1 is a device and a process flow chart of the present invention.
Detailed Description
Example (b): the following description is provided for illustrative embodiments of the present invention, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein.
Referring to fig. 1, which is a schematic structural diagram of an embodiment of the present invention, the present invention includes a wastewater adjusting tank, an acid adjusting tank, a fenton tower, a degassing tank, a reaction tank, a sedimentation tank, an evaporation distribution tank, an evaporation system, an anaerobic distribution tank, a UASB anaerobic tower, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a reaction tank, a physicochemical sedimentation tank, and a clean water tank, which are connected in sequence; the wastewater adjusting tank comprises an alkaline wastewater adjusting tank, a high-salinity wastewater adjusting tank, an acidic wastewater adjusting tank, a low-salinity wastewater adjusting tank and an oily wastewater adjusting tank which are connected in parallel; an air floatation tank is also arranged between the oily wastewater regulating tank and the acid regulating tank; the air flotation tank, the sedimentation tank and the physicochemical sedimentation tank are respectively connected with the sludge tank.
The utility model discloses in, the equalizing basin is used for adjusting the quality of water and the water yield of waste water, the subsequent processing of being convenient for. The utility model discloses it is preferred install aeration agitating unit in the equalizing basin, be convenient for carry out aeration pretreatment smoothly. The utility model discloses right aeration stirring apparatus's specification and mounted position do not have special injecing, can guarantee to carry out smoothly aeration pretreatment can.
In the utility model, an anaerobic lift pump is arranged between the anaerobic distribution tank and the anaerobic tower and is used for pumping the effluent of the regulating tank into the anaerobic tower; the anaerobic lift pump is preferably a stainless steel transfer pump.
In the utility model, the water outlet of the anaerobic tower is communicated with the water inlet of the anoxic pond; the anaerobic tower and the anoxic tank are respectively used for anaerobic treatment and anoxic treatment.
The utility model discloses in, be provided with muddy water mixed liquid reflux unit between oxygen deficiency pond and the anaerobism tower to realize that the muddy water mixed liquid that the oxygen deficiency was handled and is produced flows back in the anaerobism tower in the oxygen deficiency pond. The utility model discloses it is preferred the delivery port end in oxygen deficiency pond sets up the muddy water mixed liquid backwash pump, makes muddy water mixed liquid flow back in the anaerobism tower through the pipeline.
The utility model discloses in, good oxygen pond and oxygen deficiency pond between be provided with and nitrify liquid reflux unit to realize that the liquid that nitrifies that aerobic treatment produced flows back in the oxygen deficiency pond. In the utility model, the preferable delivery port end of the aerobic tank is provided with a nitrifying liquid reflux pump, so that nitrifying liquid flows back to the anoxic tank through the pipeline.
The utility model discloses in, the bottom in two heavy ponds sets up the mud backwash pump of setting that mud mouth is preferred, makes sediment mud flow back in anaerobism tower, oxygen deficiency pond and aerobic tank through the pipeline.
In the utility model, the secondary sedimentation tank is communicated with a sludge tank, preferably, a sludge outlet of the secondary sedimentation tank is communicated with a sludge inlet of the sludge tank; the sludge tank is used for carrying out filter-pressing concentration treatment on the sludge so as to realize reduction of the sludge and facilitate outward transportation and disposal.
In the utility model, the biochemical treatment device further comprises a reaction tank and a physicochemical sedimentation tank, specifically, the water inlet of the reaction tank is communicated with the water outlet of the secondary sedimentation tank, and the water outlet of the reaction tank is communicated with the water inlet of the physicochemical sedimentation tank; the reaction tank and the physical and chemical sedimentation tank are used for performing flocculation sedimentation treatment on the effluent of the secondary sedimentation tank.
The utility model discloses in, materialization sedimentation tank's mud discharging port with mud thickening's mud inlet intercommunication to the realization carries out filter-pressing concentration with the materialization sediment mud that produces in the materialization sedimentation tank and handles.
The utility model discloses in, what biochemical treatment device was preferred still includes the clean water basin, the water inlet of clean water basin with the delivery port intercommunication of materialization sedimentation tank for hold materialization sedimentation tank exhaust up to standard and go out water, and further will up to standard goes out water and discharges.
In the utility model, if no special description is provided between the processing devices, the processing devices are connected by adopting the conventional realizable connection mode in the field; such as a pipe connection.
The utility model discloses right the shape and the size etc. of each processing pond do not have special injecions among the biochemical treatment device, according to handling the water yield, guarantee corresponding processing procedure go on smoothly can.
As shown in figure 1, the method for carrying out standard treatment on the high-salt and high-organic chemical wastewater comprises the following steps:
s1: respectively introducing alkaline wastewater, high-salt wastewater, low-salt wastewater, acidic wastewater and oily wastewater into corresponding regulating ponds through pipelines to homogenize the quality of the wastewater;
s2: most of oily substances and suspended matters in the oily wastewater are separated by air flotation, so that the influence of the floating oil on subsequent treatment is reduced;
s3: respectively pumping the oily wastewater and the high-salinity wastewater which are treated by the air floatation tank into an acid regulating tank for mixing, and regulating the pH value of the wastewater by using acidic wastewater and supplemented sulfuric acid;
s4: pumping the wastewater in the acid adjusting tank into a Fenton tower, adding hydrogen peroxide and ferrous sulfate to form a Fenton reagent, and carrying out advanced oxidation reaction to strongly oxidize organic matters in the wastewater;
s5: overflowing the effluent of the Fenton tower to a degassing tank for degassing reaction, and removing excessive hydrogen peroxide;
s6: enabling the effluent of the degassing tank to automatically flow to a dosing reaction tank, adjusting the pH of the wastewater to be neutral by adding alkaline wastewater and lime to form insoluble or slightly soluble substances such as calcium carbonate, calcium sulfate, calcium fluoride and the like, and then adding PAM (polyacrylamide) to perform a coagulation reaction to form larger alum floc;
s7: discharging the effluent treated by the reaction tank into a sedimentation tank for mud-water separation, precipitating calcium carbonate, calcium sulfate and calcium fluoride, clarifying the effluent, and pumping the generated sludge, calcium sulfate, calcium carbonate, calcium sulfate and calcium fluoride into a sludge tank;
s8: the effluent of the sedimentation tank overflows to an evaporation distribution tank;
s9: the water in the evaporation distribution pool enters an evaporation system to evaporate the wastewater, and salt such as sodium chloride and calcium chloride and partial organic matters which are difficult to be oxidized in a higher order and have low boiling point are removed;
s10: the effluent of the evaporation system automatically flows into an anaerobic distribution tank, is mixed with low-salt wastewater, controls the temperature of the wastewater, and then is pumped into a UASB (upflow anaerobic sludge blanket) anaerobic tower, wherein macromolecular pollutants in the wastewater in the anaerobic reactor become micromolecular pollutants, and pollutants which are difficult to degrade become pollutants which are easy to degrade, so that the biodegradability of the sewage is improved, and organic matters are removed in the anaerobic reactor to generate methane. The temperature is reduced in winter, and the temperature of the anaerobic reactor is ensured to be between 35 and 40 ℃ by controlling the temperature of the anaerobic distribution tank;
s11: enabling the effluent of the UASB anaerobic tower to automatically flow into an anoxic tank and then automatically flow into an aerobic tank, simultaneously performing denitrification and dephosphorization reaction to remove ammonia nitrogen, total nitrogen and a small amount of phosphorus, controlling the hydraulic retention time HRT of the anoxic tank to be 16hr and controlling the hydraulic retention time HRT of the aerobic tank to be 4-5.5 d;
s12: the effluent of the aerobic tank also automatically flows into a secondary sedimentation tank for sludge-water separation, the clear water at the upper layer enters a reaction tank, and the sludge at the lower layer partially flows back to the anoxic tank, the aerobic tank and the UASB anaerobic tower; separating mud and water in a secondary sedimentation tank, feeding clear water at the upper layer into a reaction tank, refluxing part of sludge at the lower layer into an anoxic tank and an aerobic tank, pumping part of sludge into a sludge tank, and loading the surface of the secondary sedimentation tank at 0.6-0.8 m3/(m2H). The sludge in the secondary sedimentation tank flows back to the anoxic tank and the aerobic tank, and the excess sludge is discharged into the sludge tank;
s13: flocculating agent is added into the reaction tank to further perform coagulation reaction on organic matters and suspended matters in the wastewater, and PAC flocculating agent is Al2O3The dosage of the polyaluminium chloride with the content of 24 percent is 0.5-1 kg/(m)3Wastewater), PAM is anion with the molecular weight of 1200 ten thousand, and the dosage is 0.005-0.01 kg/(m)3Wastewater), suspended substances SS and chroma of effluent of a biochemical system are removed to achieve clarified effluent, and the chroma of the treated sewage is up to 80 times or less;
s14: after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank for mud-water separation, clear water is discharged into a clear water tank to be discharged after reaching the standard, and precipitated sludge is discharged into a sludge tank;
s15: and (3) carrying out filter pressing on the sludge in the sludge pool, wherein the water content of the sludge is 70% after the sludge is subjected to filter pressing by a plate-and-frame filter press, and the sludge cake is transported and disposed.
S14: automatically flowing the effluent of the secondary sedimentation tank to a dosing reaction tank;
s15: after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank for mud-water separation, clear water is discharged into a clear water tank to be discharged after reaching the standard, and precipitated sludge is discharged into a sludge tank;
the utility model discloses well step S1 to step S9 are the anterior segment treatment process route that the core system "adjusts + fenton preliminary treatment + evaporation" of the high organic matter chemical wastewater standard treatment' S of high salt content method is given first place to. Mainly removes high-content salt in the wastewater and fluoride in the wastewater. Meanwhile, the middle step S10 to the step S12 of the utility model are a back-end 'anaerobic + anoxic + aerobic + secondary sedimentation' biochemical treatment process system of the method for standard treatment of the high-salt and high-organic chemical wastewater.
In the utility model, the oily wastewater is preferably subjected to air floatation separation to separate most of oily substances and suspended matters, so that the influence of floating oil on subsequent treatment is reduced; the utility model discloses it is right the parameter of air supporting does not have special restriction, adopt the air supporting parameter of this area conventionality can. In the utility model discloses, water quality control is preferred to be with alkaline waste water, high salt waste water, low salt waste water, acid waste water and oily waste water adjust respectively.
The utility model discloses obtaining behind the pending waste water, adjust the pH valve of pending waste water is 4 ~ 5 backs to pH value, carries out the waste water after strong oxidation obtains the oxidation through the Fenton tower. In the present invention, the step of adjusting the ph of the wastewater to be treated is preferably to add acidic wastewater to the wastewater to be treated. In the present invention, the strong oxidizing agent preferably includes hydrogen peroxide and ferrous sulfate; the addition amount of the hydrogen peroxide is preferably 0.5-1 kg/m3The addition amount of the ferrous sulfate is preferably 0.5-1 kg/m3And (4) waste water. The utility model discloses in carry out the fenton reaction in the fenton tower and can oxidize most organic matters in the waste water.
The utility model obtains the oxidized waste water, and the oxidized waste water is aerated and iron is added in sequenceAnd (4) separating mud and water after the mud removing coagulation reaction, and collecting the mud and the overflow liquid. In the utility model, the aeration strength is preferably 5-10 m3/(m2H), more preferably 6 to 9m3/(m2H); the aeration time is preferably 4 hr; in the utility model, the aeration is used for removing the excessive hydrogen peroxide remained in the previous step. In the utility model, lime and PAM are added in the iron mud coagulation reaction process; the addition amount of the lime is preferably 0.01-1 kg/m3Waste water, more preferably 0.5kg/m3Waste water; the preferable addition amount of the PAM is 0.005-0.01 kg/m3Waste water; more preferably 0.006 to 0.009kg/m3And (4) waste water. The pH value of the iron mud coagulation reaction process is preferably adjusted to 6-7; in the iron mud coagulation reaction process of the utility model, the lime is ionized into Ca2+Under the condition that the pH value is 6.5-6.8, reacting with F in the wastewater-Rapid association to form CaF2Precipitation, effective removal of F-。
The utility model carries out mud-water separation after the iron mud coagulation removal reaction, the mud-water separation is preferably carried out in the sedimentation tank, the sludge generated by the mud-water separation is preferably pumped into the sludge tank, and the main components of the sludge comprise lime, calcium fluoride, sundries and the like; the sludge pump is preferably a sludge screw pump.
The utility model discloses will the overflow liquid that mud-water separation produced carries out waste water evaporation and obtains the waste water after the evaporation the utility model discloses in, the preferred adoption four-effect evaporator of waste water evaporation goes on, the effect of waste water evaporation is for getting rid of most salinity and partial organic matter, can reach the effect of clarification play water simultaneously.
After the evaporated wastewater is obtained, the wastewater after the evaporation is subjected to biochemical treatment to obtain the wastewater after the biochemical treatment; the biochemical treatment comprises anaerobic treatment, anoxic treatment and aerobic treatment which are connected in series.
In the utility model, the temperature of anaerobic treatment is preferably 35-37 ℃; the pH value of the anaerobic treatment is preferably 7.0-8.0, and the Hydraulic Retention Time (HRT) of the anaerobic treatment is preferably 2-3d, and more preferably 2.5 d; the sludge settlement ratio (SV30) of the anaerobic treatment is preferably 80-90%; the utility model discloses preferentially, the mud settlement ratio through control anaerobic treatment is in above-mentioned within range to cooperate follow-up oxygen deficiency treatment and aerobic treatment in-process mud settlement ratio simultaneously, be favorable to guaranteeing to fully get rid of ammonia nitrogen and total nitrogen in the waste water, if anaerobic treatment's mud settlement ratio is low excessively, easily leads to finally going out aquatic ammonia nitrogen and/or total nitrogen not up to standard. Among the anaerobic treatment process, the macromolecular pollutant in the waste water becomes the micromolecular pollutant, and the pollutant of difficult degradation becomes the pollutant of easy degradation, improves the biodegradability of sewage, and the organic matter is got rid of in anaerobic reactor, produces marsh gas. The utility model discloses in, when temperature declined in winter, the preferred temperature of anaerobic distribution tank through control, guaranteed that anaerobic reactor's temperature is between 35 ~ 40 ℃.
After the anaerobic treatment, the utility model carries out anoxic treatment on the obtained wastewater, and preferably reflows the muddy water mixed liquid to the anaerobic treatment process; the reflux ratio of the mud-water mixed liquid is preferably 100-150%. The utility model discloses the reflux ratio of preferred control muddy water mixed liquid is favorable to alleviateing follow-up oxygen deficiency, aerobic treatment's operating load at above-mentioned within range, and then influences the nitrification in the aerobic treatment stage.
In the utility model, the Dissolved Oxygen (DO) of the anoxic treatment is preferably less than or equal to 0.2mg/L, and more preferably 0.05-0.15 mg/L; the carbon-nitrogen ratio (abbreviated as C/N, specifically the mass ratio of COD to ammonia nitrogen) of the anoxic treatment is preferably (4-5): 1, more preferably 4.5:1, the utility model discloses preferred through the carbon-nitrogen ratio of control oxygen deficiency processing system, can satisfy the demand of denitrifying bacteria to the carbon source under the oxygen deficiency condition, improve denitrification efficiency. The utility model discloses in, the preferred carbon source of throwing through throwing satisfies carbon nitrogen ratio, the carbon source is preferred to include glucose or sodium acetate, throws the volume of adding in order to satisfy carbon nitrogen ratio requires to be suitable, and is concrete, if according to per cubic meter waste water meter, throws 0.8kg glucose or 1.0kg sodium acetate. In the utility model discloses, the water conservancy dwell time of oxygen deficiency treatment is preferred 9 ~ 20h, more preferably 16 h. In the utility model, the sludge sedimentation ratio (SV30) of the anoxic treatment is preferably 80-90%; the utility model discloses preferentially, the sludge sedimentation ratio through control oxygen deficiency treatment is in above-mentioned within range to cooperate simultaneously aforementioned anaerobic treatment and follow-up aerobic treatment in-process sludge sedimentation ratio, be favorable to guaranteeing to fully get rid of ammonia nitrogen and total nitrogen in the waste water, if the sludge sedimentation ratio of oxygen deficiency treatment is low excessively, easily lead to finally go out aquatic ammonia nitrogen and/or total nitrogen not up to standard.
The utility model discloses in anaerobism-oxygen deficiency is handled, can make anaerobic treatment and the heterotrophic fungus of oxygen deficiency treatment cultivation fully hydrolyze floaters such as batting, fibre and soluble organic matter in the waste water for organic acid, and macromolecule organic matter decomposes into the micromolecule organic matter, and insoluble organic matter converts soluble organic matter into, is convenient for carry out follow-up aerobic treatment.
The utility model preferably adjusts the pH value to 7.5-8.5 after the anaerobic-anoxic treatment and before the aerobic treatment. In the present invention, the pH adjustment is preferably performed using an alkaline reagent; the utility model discloses to the kind of alkali reagent does not have special restriction, can guarantee that pH value is in required scope can, specifically be 30% NaOH solution as mass concentration. The utility model discloses adjust pH value to 7.5 ~ 8.5, be favorable to satisfying the demand of autotrophic bacteria nitrification to basicity under the follow-up oxygen suppliment condition.
In the process of anoxic and aerobic treatment, the dissolved oxygen of the anoxic treatment is preferably less than or equal to 0.2mg/L, and the aeration rate of the anoxic treatment is preferably 0.5-1.0 m3/(m2H); the dissolved oxygen of the aerobic treatment is preferably 3-5 mg/L, and the aeration rate of the aerobic treatment is preferably 5-6 m3/(m2·h)。
In the utility model, the hydraulic retention time of the aerobic treatment is preferably 5.0 days, and the hydraulic retention time of each treatment stage is preferably equal. In the utility model, the sludge sedimentation ratio (SV30) of the anoxic and aerobic comprehensive treatment is preferably 70-80%; the utility model discloses preferentially, the mud settlement ratio through control oxygen deficiency, good oxygen integrated treatment is in above-mentioned within range to cooperate simultaneously among the aforementioned anaerobic treatment mud settlement ratio, be favorable to guaranteeing fully to get rid of the ammonia nitrogen and total nitrogen in the waste water, if oxygen deficiency, good oxygen integrated treatment's mud settlement ratio cross lowly, easily lead to finally go out aquatic ammonia nitrogen and/or total nitrogen not up to standard.
In the utility model, the preferable nitrifying liquid generated in the aerobic treatment flows back to the anoxic treatment process. The utility model discloses it is preferred will nitrify liquid is 100 ~ 300%, more preferably 200 ~ 250% according to the reflux ratio. The utility model discloses preferably will nitrify liquid and flow back to the oxygen deficiency treatment process under above-mentioned reflux ratio condition, be favorable to satisfying under the oxygen deficiency condition that the effect of heterotroph denitrification is to NO3 -And is beneficial to reducing energy consumption. If the reflux ratio of the nitrifying liquid is too low or too high, the denitrification effect in the anoxic treatment stage is not fully ensured, so that the removal rate of nitrogen in the final effluent is low; moreover, the reflux ratio of the nitrified liquid is too high, so that the hydraulic retention time in the anoxic treatment stage is shortened, and the effluent quality is influenced.
In the utility model, after the anaerobic treatment, the wastewater has higher biodegradability in the anoxic and aerobic treatment stages. In the anoxic treatment stage, heterotrophic bacteria ammoniate contaminants such as proteins and fats (nitrogen in the organic chain or amino groups in amino acids) to release ammonia (NH)4 +) Then under the condition of sufficient oxygen supply in the aerobic treatment stage, NH is nitrified by autotrophic bacteria3-N(NH4 +) Oxidation to NO3 -(ii) a And refluxing the nitrified liquid to the anoxic treatment process. Under the anoxic condition, NO is generated by the denitrification of the heterotrophic bacteria3 -Reduced to molecular nitrogen (N)2) And C, N and O ecological cycle is completed, and harmless and standard treatment of wastewater is realized. After the oxygen-poor and aerobic treatment, most of the organic matters in the wastewater are degraded. In the utility model, after the anoxic and aerobic treatments, the chemical oxygen demand of the wastewater is less than 200mg/L, the ammonia nitrogen concentration is less than 20mg/L, the total nitrogen concentration is less than 30mg/L, and the total phosphorus concentration is less than 1.5 mg/L.
The utility model discloses behind the biochemical treatment, it will be preferred waste water after the biochemical treatment carries out the sedimentation treatment, obtains waste water and sediment mud after the sedimentation treatment. The utility model discloses in, sedimentation treatment's effect is realized mud-water separation, makes the water clear more, avoids mud to run off. The present invention has no particular limitation on the specific operating conditions of the precipitation treatment, and may employ operating conditions known to those skilled in the art.
After the precipitated sludge is obtained, part of the precipitated sludge is refluxed to the anaerobic treatment and anoxic and aerobic treatment processes, and the residual precipitated sludge is subjected to filter pressing concentration treatment; preferably, the part of the precipitated sludge is refluxed to the three treatment processes, wherein the first treatment process is an anaerobic treatment process; the second is in the anoxic treatment process; the third is in the aerobic treatment stage. The utility model preferably reflows the precipitated sludge to the anaerobic treatment, anoxic treatment and aerobic treatment processes according to the reflow ratio of 150 to 300 percent; in the utility model, the volume ratio of the precipitated sludge that flows back to the anaerobic treatment, anoxic treatment and aerobic treatment process is preferably 1: (0.9-1.1): (2.5 to 3.5), more preferably 1: 1: 3. the utility model discloses it is preferred through above-mentioned processing, be favorable to reducing excess sludge by a wide margin, be convenient for carry out follow-up filter-pressing concentrated treatment. The utility model discloses in, the press filtration is concentrated and is handled preferred adoption plate and frame filter press right the sediment mud carries out the filter-pressing. The utility model discloses to the specific operation mode of filter-pressing concentrated treatment does not have special restriction, adopts the mode that technical personnel in the field are familiar with can. After the filter-pressing concentration treatment is finished, the water content of the obtained concentrated sludge is about 70 percent; in the present invention, the concentrated sludge can be further treated as a general solid waste.
The utility model discloses behind the biochemical treatment, will waste water after the biochemical treatment flocculates, mud-water separation obtains effluent up to standard. In the utility model, a flocculating agent and a coagulant are preferably added into the wastewater in the flocculation treatment process; the present invention has no special limitation on the kinds of the flocculant and the coagulant, and can adopt reagents well known to those skilled in the art, and in the embodiment of the present invention, polyaluminium chloride (PAC) flocculant and anionic polyacrylamide (P) are preferably adoptedAM) coagulant, Al in PAC flocculant2O3The content is preferably 24%, and the molecular weight of the PAM coagulant is preferably 1200 ten thousand. In the utility model, the addition amount of the PAC flocculating agent is preferably 0.5-1.0 kg, more preferably 0.6-0.9 kg, calculated by per cubic meter of water; the addition amount of the PAM coagulant is preferably 0.005-0.010 kg, and more preferably 0.006-0.009 kg. The utility model discloses a flocculation treatment gets rid of Suspended Solid (SS) and reduces the colourity in the waste water, makes the sewage colourity after handling reach below 80 times.
The utility model discloses in, the purpose of materialization sedimentation treatment is to realize mud-water separation, makes the play water more limpid, avoids mud to run off. The utility model discloses to concrete operating condition of mud-water separation does not have special restriction, adopt the operating condition that technical personnel in the field are familiar with can. The utility model discloses after the materialization is deposited and is handled, the gained effluent reaches emission standard promptly, can directly discharge.
In the utility model, the physicochemical precipitated sludge is obtained after the physicochemical precipitation treatment, and the utility model preferably carries out the filter-pressing concentration treatment on the physicochemical precipitated sludge; the utility model discloses right the filter-pressing concentrated treatment does not have special injecing, refer to the above-mentioned method that carries out filter-pressing concentrated treatment to deposiing mud can. The utility model discloses in, the materialization deposits mud and carries out filter-pressing concentration treatment after, and the concentrated mud moisture content that obtains is about 70%, can regard as general solid waste to further handle. Adopt the method, every 1000 tons of salt-containing chemical wastewater is treated, the generated physicochemical precipitated sludge is subjected to filter-pressing concentration treatment to obtain 0.4-0.6 tons of concentrated sludge, and the investment and the operating cost of sludge treatment are effectively reduced.
The utility model discloses in, control anaerobism, the sludge concentration of oxygen deficiency and good oxygen is in suitable within range, be favorable to guaranteeing to carry out effective denitrogenation to waste water, it is specific, the sludge settlement ratio of anaerobism (SV30) is at 50 ~ 60%, the sludge settlement ratio of oxygen deficiency treatment is at 80 ~ 90%, the sludge settlement ratio of aerobic treatment is at 70 ~ 80%, the aquatic ammonia nitrogen that reachs after the materialization precipitation treatment and total nitrogen reduce respectively to below 20mg/L and below 30mg/L, accord with emission standard;
if the sludge settlement ratio of anaerobic treatment is 20-30%, the sludge settlement ratio of anoxic treatment is 50-60% and the sludge settlement ratio of aerobic treatment is 50-60%, the ammonia nitrogen in effluent of physical and chemical precipitation treatment can still be reduced to be below 20mg/L, but the total nitrogen is about 31-60 mg/L, and the total nitrogen does not reach the standard;
if the sludge settlement ratio of anaerobic treatment is 30-40%, the sludge settlement ratio of anoxic treatment is 30-40%, the sludge settlement ratio of aerobic treatment is 30-40%, the ammonia nitrogen in effluent of physical and chemical precipitation treatment is about 21-30 mg/L, and the total nitrogen is about 61-90 mg/L, the ammonia nitrogen and the total nitrogen do not reach the standard.
In the utility model, in order to ensure that the sludge concentration of anaerobic, anoxic and aerobic treatment is in a proper range, activated sludge in a sludge tank of a municipal sewage treatment plant is preferably adopted when a system is started, so that the sludge in the starting period meets the requirement of the sludge concentration; the present invention does not limit the specific operation manner of the related steps, and can adopt the manner known to those skilled in the art.
In the utility model, heterotrophic bacteria cultured in the anaerobic tank and the anoxic tank hydrolyze macromolecular organic matters, suspended pollutants and soluble organic matters in the sewage into organic acid, so that the macromolecular organic matters are decomposed into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, and when products after anoxic hydrolysis enter the aerobic tank for aerobic treatment, the biodegradability of the sewage can be improved; in the anoxic zone, heterotrophic bacteria ammoniate contaminants such as protein and fat (N in the organic chain or amino groups in amino acids) to release ammonia (NH)4 +) Under the condition of sufficient oxygen supply, the nitrification of autotrophic bacteria can react NH3-N(NH4 +) Oxidation to NO3 -And the effect of removing total nitrogen of ammonia nitrogen is achieved. Then the wastewater is discharged through a reaction tank-a physical and chemical sedimentation tank which reaches the standard.
The utility model discloses can reduce the COD in the chemical industry waste water to below 500mg/L from 30000mg/L, reduce TDS in the waste water to below 3000mg/L from 40000mg/L, reduce the fluorine content in the waste water to below 20mg/L from 5000mg/L simultaneously. The effluent can reach the B-level standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 45mg/L, total nitrogen is less than or equal to 70mg/L, and F is less than or equal to 20mg/L) in the water quality standard for sewage discharge into cities and towns (GB/T31962-2015), the sludge yield of the whole process is small, the investment and the operating cost of sludge treatment are effectively reduced, and meanwhile, the system is low in power consumption, low in operating cost, simple in operation and management and stable in operation.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (4)
1. A high-salt-content high-organic-matter chemical wastewater treatment device is characterized by comprising a wastewater adjusting tank, an acid regulating tank, a Fenton tower, a degassing tank, a reaction tank, a sedimentation tank, an evaporation water distribution tank, an evaporation system, an anaerobic water distribution tank, a UASB anaerobic tower, an anoxic tank, an aerobic tank, a secondary sedimentation tank, a reaction tank, a physicochemical sedimentation tank and a clean water tank which are connected in sequence;
the wastewater adjusting tank comprises an alkaline wastewater adjusting tank, a high-salinity wastewater adjusting tank, an acidic wastewater adjusting tank, a low-salinity wastewater adjusting tank and an oily wastewater adjusting tank which are connected in parallel;
an air floatation tank is also arranged between the oily wastewater regulating tank and the acid regulating tank;
the air flotation tank, the sedimentation tank and the physicochemical sedimentation tank are respectively connected with the sludge tank.
2. The apparatus according to claim 1, wherein an aeration stirring device is installed in the conditioning tank.
3. The apparatus of claim 1, wherein an anaerobic lift pump is provided between the anaerobic distribution tank and the UASB anaerobic tower.
4. The device according to claim 1, wherein a sludge-water mixed liquor reflux device is arranged between the anoxic pond and the UASB anaerobic tower.
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| CN117142728A (en) * | 2023-10-27 | 2023-12-01 | 珙县华洁危险废物治理有限责任公司成都分公司 | Method for treating waste water after oil-based rock debris thermal desorption |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117142728A (en) * | 2023-10-27 | 2023-12-01 | 珙县华洁危险废物治理有限责任公司成都分公司 | Method for treating waste water after oil-based rock debris thermal desorption |
| CN117142728B (en) * | 2023-10-27 | 2024-02-27 | 珙县华洁危险废物治理有限责任公司成都分公司 | Method for treating waste water after oil-based rock debris thermal desorption |
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