CN113912251A - Treatment process of high-concentration degradation-resistant pickling wastewater - Google Patents
Treatment process of high-concentration degradation-resistant pickling wastewater Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 79
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- 238000006731 degradation reaction Methods 0.000 title claims abstract description 14
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 115
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- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
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- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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Abstract
The invention relates to the technical field of wastewater treatment, and discloses a treatment process of high-concentration degradation-resistant pickling wastewater. According to the treatment process, the pickling wastewater is pretreated and then sequentially subjected to ozone air flotation pretreatment, ozone heterogeneous catalytic oxidation treatment and ozone photocatalytic oxidation treatment, high-concentration organic matters in the pickling wastewater are efficiently degraded to meet the requirement of evaporative crystallization through ozone advanced oxidation in three links, so that salt in the pickling wastewater is evaporated and separated, and meanwhile, condensed water generated by evaporation can be treated again through a low-cost biochemical system, so that higher emission or recycling requirements are met. The treatment process provided by the invention can obviously improve the degradation efficiency of organic matters in the pickling wastewater, reduces the investment and operation cost on the premise of ensuring the treatment effect, and ensures the overall operation stability of the system.
Description
Technical Field
The application relates to the technical field of wastewater treatment, in particular to a treatment process of high-concentration degradation-resistant pickling wastewater.
Background
The preserved szechuan pickle industry belongs to the vegetable food industry for pickling with salt in the pickle industry. A large amount of high-salinity wastewater is generated in the process of producing the tuber mustard. Generally, the high-salinity wastewater has adverse effects on the ecological environment, which are mainly shown in the following steps: the high-salinity wastewater flows into rivers and branches to directly change the water quality; high-salinity wastewater permeates into the underground to cause underground water pollution and land salinization; the running efficiency of the biochemical process is low because the high-concentration sodium chloride enters a town sewage treatment plant to inhibit the metabolic activity of microorganisms. Toxic substances in high-salinity wastewater are remained and enriched in animals and plants, and the toxic substances finally enter human bodies indirectly through food chains. Therefore, the problem of the pollution of the preserved szechuan pickle waste water, in particular the influence of chloride ions on a water source area is concerned by various countries and industries.
The preserved szechuan pickle industry still has a large number of production workshops with small scale and poor benefit, so that the problems of disordered preserved szechuan pickle wastewater discharge, excessive resource waste, serious disordered competition in the industry and the like are increasingly prominent. Therefore, the industrial structure optimization is necessary for medium and small sized preserved szechuan pickle enterprises which have laggard production equipment, weak technical and management strength, incapability of comprehensively utilizing byproducts, waste of raw materials and serious environmental pollution. The clean production technology is a feasible technical way for solving the problem of production pollution of tuber mustard enterprises in China and improving the product quality and economic benefit. The production of the preserved szechuan pickle starts with the clean production technology from the production source, the production process and the tail end of the preserved szechuan pickle, forms a low-salt production mode, reduces the salt content of the preserved szechuan pickle wastewater, fully recycles the high-salt water wastewater, and explores a tail end treatment technology suitable for the water quality of the preserved szechuan pickle wastewater.
Generally, the production process of the preserved szechuan pickle is divided into three steps of pickling and three squeezing, and mainly comprises five stages: a pickling stage; pruning and elutriating; cutting and desalting; mixing and packaging; and (5) sterilizing and cooling. The time required by primary curing is about 7-10 days, a large amount of salt needs to be added in the curing process, the generated curing wastewater contains a large amount of salt, the content of the salt in the primary curing wastewater is detected to be about 10%, the content of organic matters is up to more than 30000mg/l, the content of ammonia nitrogen is up to more than 1000mg/l, the content of total phosphorus is up to more than 400mg/l, and the total nitrogen is up to more than 2000mg/l, and belongs to typical three-high wastewater with high salt, high organic matters and high ammonia nitrogen. Because the waste water contains a large amount of salt and can not be biochemically treated, organic matters in the waste water can not be removed, and the high-concentration organic matters can not be evaporated and crystallized without being degraded, so that the core of the preserved szechuan pickle waste water treatment process is to efficiently degrade the high-concentration organic matters in the waste water to a certain degree by adopting which process is then evaporated and crystallized.
Disclosure of Invention
In view of the above, the present invention aims to provide a treatment process for high-concentration degradation-resistant pickling wastewater, such that the treatment process can significantly improve the degradation efficiency of organic matters in the pickling wastewater of preserved szechuan pickle.
In order to solve the above technical problems/achieve the above object or to at least partially solve the above technical problems/achieve the above object, the present invention provides a process for treating high-concentration degradation-resistant pickling wastewater, comprising:
step 1, solid-liquid separation;
collecting pickling wastewater, homogenizing and homogenizing, and then carrying out solid-liquid separation;
step 2, coagulating sedimentation;
after solid-liquid separation, carrying out coagulating sedimentation treatment on the pickling wastewater;
step 3, ozone air flotation pretreatment;
combining ozone oxidation and air flotation, adjusting the pH value of the pickling wastewater to 11-12 before reaction, dissolving ozone in the pickling wastewater through an air flotation air dissolving device and releasing the ozone, and performing contact and reaction with the pickling wastewater after coagulating sedimentation to remove generated foam and suspended matters; detecting the pH value in the reaction process, and adjusting the pH value to be between 11 and 12 when the pH value is lower than 11;
step 4, ozone heterogeneous catalytic oxidation;
after ozone air flotation pretreatment, adopting ozone and a heterogeneous catalyst to carry out combined treatment on the pickling wastewater; adjusting the pH value of the curing wastewater to 7.5-8.5 before reaction, and detecting the pH value in the reaction process to maintain the pH value of the wastewater at 7.5-8.5;
step 5, carrying out photocatalytic oxidation on ozone;
after ozone heterogeneous catalytic oxidation, treating pickling wastewater by combining ultraviolet light and ozone; adjusting the pH value of the curing wastewater to 11-12 before reaction, detecting the pH value in the reaction process, and adjusting the pH value to 11-12 when the pH value is lower than 11;
and 6, after the photocatalytic oxidation by ozone, evaporating and crystallizing the pickling wastewater, and separating salt from the pickling wastewater.
Compared with the waste water produced by the production of the preserved szechuan pickle by enterprises, the waste water with high salinity and high COD content produced by small workshops and scattered households of the preserved szechuan pickle is difficult to treat, and aiming at the difficult-to-degrade pickling waste water from the same source, the organic matters are efficiently degraded by using the combination of ozone oxidation and air flotation, a heterogeneous catalyst and ultraviolet light through a special process; in addition, the pH value of the wastewater can be gradually reduced in the treatment process, the pH value of the wastewater is only adjusted before treatment in the existing ozone oxidation, and the pH value is not monitored and regulated in the treatment process.
In the process of adjusting the pH value of the pickling wastewater, the alkali is preferably sodium hydroxide and/or calcium hydroxide;
preferably, the pH of the curing waste water is adjusted to 11.0, 11.1, 11.2, 11.3, 11.4, 11.5, 11.6, 11.7, 11.8, 11.9 or 12.0 before the reaction in the step 3 and the step 5, the pH value is detected in the reaction process, and when the pH value is lower than 11, the pH of the curing waste water is adjusted to 11.0, 11.1, 11.2, 11.3, 11.4, 11.5, 11.6, 11.7, 11.8, 11.9 or 12.0;
preferably, the pH value of the curing wastewater is adjusted to 7.5, 7.6, 7.7, 7.8, 7.9, 8.0, 8.1, 8.2, 8.3, 8.4 or 8.5 before the reaction in the step 4, and the pH value is detected during the reaction, so that the pH value of the wastewater is maintained at 7.5, 7.6, 7.7, 7.8, 7.9, 8.0, 8.1, 8.2, 8.3, 8.4 or 8.5;
in the treatment process, the curing wastewater from various sources is collected, stored and stirred, and related operations can be performed by using an existing homogenizing tank and an amount equalizing tank, or a homogenizing tank, such as a device provided by the existing patent CN203741133U or CN205634942U, so that the effect of homogenizing and equalizing the wastewater is achieved, and the continuous and stable operation of a subsequent wastewater treatment system is facilitated. The process does not need to add other medicaments and treat, and mainly mixes the pickling wastewater from different sources.
The homogenized and equalized waste water is passed through a screening device, such as a hydraulic screen, to make solid-liquid separation of some large-particle preserved szechuan pickle residues in the waste water, so as to reduce the subsequent treatment load.
Preferably, step 2 of the treatment process is: after solid-liquid separation, the liquid is adjusted from acidity to alkalescence by adding alkali, the pH value can be generally adjusted to 7-9, and then the total phosphorus and suspended pollutants are removed by adding medicine. Wherein the alkali can be selected from calcium hydroxide and/or sodium hydroxide, and the total phosphorus removing medicine is PAC (polyaluminium chloride) and/or PFC (polyferric chloride); meanwhile, in the step 2, hardness-removing medicines can be added according to needs, magnesium ions and calcium ions are removed in a precipitation mode in principle, for example, calcium carbonate, magnesium hydroxide and the like are formed to remove hardness, and calcium fluoride can be formed by adding calcium hydroxide to achieve the aim of removing fluorine. The medicament for removing the suspended pollutants is a polymeric flocculant PAM (polyacrylamide). More preferably, the ratio of phosphorus: the concentration of the medicament for removing the suspended pollutants is 2mg/L to 5mg/L except total phosphorus medicament (molar ratio) =1:0.8 to 1: 1. In a specific embodiment of the invention, the ratio of phosphorus: the concentration of the drug for removing suspended pollutants is 3mg/L except total phosphorus medicament (molar ratio) =1: 0.9.
Preferably, the concentration of the ozone in the steps 3-5 is independently selected from 100-120mg/L, further, the concentration of the ozone in the step 3 is 100-120mg/L, and the concentrations of the ozone in the steps 4 and 5 are independently selected from 100-110 mg/L; the ozone may be provided by an oxygen source ozone generating device. In a specific embodiment, the concentration of ozone in step 3 is 110mg/L, and the concentration of ozone in step 4 and step 5 is 100 mg/L.
Preferably, the treatment time of the three ozone treatment links in the steps 3-5 is independently selected from 4-10h, further, the treatment time of the step 3 is 8-10h, the treatment time of the step 4 is 6-8h, and the treatment time of the step 5 is 4-6 h; in the specific embodiment of the invention, the treatment time of step 3 is 8h, the treatment time of step 4 is 8h, and the treatment time of step 5 is 4 h.
Preferably, the heterogeneous catalyst in step 3 is a carbon-based catalyst and/or an aluminum-based catalyst, such as commercially available silica-alumina catalysts and activated carbon catalysts.
The wavelength of the ultraviolet light in step 5 of the present invention can adopt any wavelength band capable of promoting the ozone oxidation activity, and the wavelength of the ultraviolet light in the present embodiment is 185nm-254 nm.
In the treatment process, the MVR evaporator is adopted for evaporative crystallization, the wastewater after pretreatment and three-step ozone oxidation treatment is concentrated, evaporated and crystallized through the MVR evaporator, salt such as sodium chloride and the like generated by evaporation enters a salt separation system for purification, the economic value is improved, the mother liquor generated by evaporation can be separately treated, and can also be returned to the step 1 for retreatment, so that the circulation treatment is formed, and the treatment efficiency is improved. And various conditions of MVR water inflow are controlled, and the long-term stable operation of the evaporation system is kept.
The condensate generated by evaporation can be further treated according to the needs, for example, the condensate can be further treated by an economic and reliable biochemical system, and the organic matters are further decomposed by microorganisms, so that the higher emission requirement is met, and the investment and the operation cost are greatly reduced. The biochemical condensate water retreatment system is one or more than two of AAO, AO, MBR, MBBR and BAF.
Tests prove that the effect is poor when organic matters in the pickling wastewater are degraded through pure Fenton oxidation or adjustment of the three-step ozone oxidation process; moreover, the regulation and control of the pH value in the treatment process can obviously influence the removal rate of COD. The catalytic ozonation mainly comprises three different catalytic ozonation processes, namely an ozone air flotation pretreatment process, heterogeneous catalytic ozonation and photocatalytic ozonation, and the three catalytic ozonation processes are combined, so that the high-concentration organic matters in the wastewater can be reduced to the concentration meeting the evaporation condition by adjusting and controlling the reaction condition, the time and various technical parameters, and the oxidation efficiency is improved.
According to the technical scheme, the pickling wastewater is pretreated and then sequentially subjected to ozone air flotation pretreatment, ozone heterogeneous catalytic oxidation treatment and ozone photocatalytic oxidation treatment, high-concentration organic matters in the pickling wastewater are efficiently degraded to meet the requirement of evaporative crystallization through ozone advanced oxidation in three links, so that salt in the pickling wastewater is evaporated and separated, and meanwhile, condensed water generated by evaporation can be reprocessed through a low-cost biochemical system to meet the higher emission or recycling requirement. The treatment process provided by the invention can obviously improve the degradation efficiency of organic matters in the pickling wastewater, reduces the investment and operation cost on the premise of ensuring the treatment effect, and ensures the overall operation stability of the system.
Drawings
FIG. 1 is a schematic flow diagram of the treatment process of the present invention.
Detailed Description
The invention discloses a treatment process of high-concentration degradation-resistant pickling wastewater, and a person skilled in the art can realize the treatment process by properly improving process parameters by referring to the content. It is expressly intended that all such similar substitutes and modifications which would be obvious to one skilled in the art are deemed to be included in the invention. While the processes and applications of this invention have been described in terms of preferred embodiments, it will be apparent to those of ordinary skill in the art that variations and modifications in the processes and applications described herein, as well as other suitable variations and combinations, may be made to implement and use the techniques of this invention without departing from the spirit and scope of the invention. It should be apparent that the described embodiments are only some of the embodiments of the present application, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
It is noted that, in this document, relational terms such as "first" and "second", "step 1" and "step 2", and "(1)" and "(2)" are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The process flow schematic diagram of the treatment process is shown in figure 1, in the specific treatment process, a tank truck is adopted to collect primary preserved szechuan pickle curing wastewater intermittently generated by each scattered household and farmer and transport the primary preserved szechuan pickle curing wastewater to a centralized wastewater treatment station, characteristics such as wastewater quantity and discharge period of the preserved szechuan pickle curing wastewater are comprehensively considered, a collection system with a certain volume is designed, the preserved szechuan pickle curing wastewater is collected and transported to the collection system of the centralized wastewater treatment station through the tank truck, the wastewater is stored in the collection system, meanwhile, the water quality and the water quantity are regulated and homogenized, and a transportation device and the collection system both need to consider the anti-corrosion requirement.
The waste water after being regulated is pumped into a screening system, the screening system mainly carries out solid-liquid separation on a large-particle tuber mustard residue and the like in tuber mustard waste water through a hydraulic screen, the subsequent treatment load is reduced, and the screening system needs to consider the anti-corrosion requirement.
The waste water is screened to remove large-particle preserved szechuan pickle residues and then enters an alkali-adding coagulating sedimentation system, relevant system equipment can adopt devices in the existing waste water treatment industry, such as a coagulating and flocculating device in CN108383296A, the system mainly removes suspended pollutants and total phosphorus in the waste water, preconditions are made for subsequent advanced oxidation treatment, the system needs to control the pH value in the waste water to be slightly alkaline, and agents for removing hardness, fluorine and the like can be added as required.
The wastewater enters an advanced oxidation system after being pretreated, the advanced oxidation system comprises an ozone air flotation pretreatment system, an ozone heterogeneous catalytic oxidation system and an ozone photocatalytic oxidation system, and through the cooperation of special procedures of three oxidation stages in the ozone advanced oxidation, the wastewater is firstly subjected to ozone air flotation to remove suspended matters and bubbles in the wastewater, so that the influence on the activity of a subsequent heterogeneous catalyst is avoided; through ozone air flotation and ozone heterogeneous catalytic oxidation, the water color of the preserved szechuan pickle wastewater can be clarified, the subsequent treatment effect of ozone photocatalytic oxidation is promoted, three-step oxidation is cooperated to degrade high-concentration organic matters in the wastewater to the requirement of entering evaporation crystallization, and meanwhile, the evaporation crystallization system can be stably operated for a long time. On the premise of reducing the investment and the operation cost of the advanced oxidation system to the maximum extent, the effective and stable control of the organic matters in the advanced oxidation effluent is ensured, thereby ensuring that the evaporative crystallization system can stably and well operate for a long time.
The ozone air-flotation pretreatment system mainly combines ozone oxidation and air flotation, and ozone is dissolved in water and released through the air dissolving device to contact and react with wastewater. The upper foam scraping and deslagging device removes foam and suspended matters generated in the reaction process. The reaction devices are made of ozone corrosion resistant materials. .
The ozone heterogeneous catalytic oxidation system adopts ozone and heterogeneous catalyst to combine, and compared with the ozone which is used as a single oxidant, the ozone forms [. OH under the action of the catalyst]The reaction rate with organic matters is higher, the oxidizability is stronger, and almost all the organic matters can be oxidized. The catalyst can directly oxidize the organic matters in the water into CO by utilizing the strong oxidizing property of the ozone2And H2O, or organic matter of large moleculeOxidative decomposition into small molecules makes it more susceptible to decomposition into small molecules, making it more susceptible to degradation. The ozone heterogeneous catalytic oxidation technology has the advantages of strong oxidation capacity, reduction of ozone adding amount, particularly remarkable improvement of mineralization rate of organic matters, and the like, and can greatly reduce the content of the organic matters in wastewater and improve the oxidation efficiency. The integral device needs to consider the anti-corrosion requirement.
The ozone photocatalytic oxidation system combines ultraviolet light and ozone, and through repeated tests, the combination of the ultraviolet light with proper wavelength and the ozone is determined to react with the wastewater, so that organic matters in the wastewater are further treated in an advanced manner. The integral device needs to consider the anti-corrosion requirement, and a cooling device can be arranged during the operation of the system, so that the treatment effect is further ensured, and the equipment maintenance rate is reduced.
The treatment time and the ozone concentration of the three-step ozone catalytic oxidation link of the invention can be independently selected from corresponding parameters, namely the treatment time and the ozone concentration in the step 3, the step 4 and the step 5 are not necessarily the same, and the treatment time and the ozone concentration can be respectively selected from completely the same, partially the same, completely different or partially different parameters within the limited parameter range.
After most of organic matters, ammonia nitrogen and total phosphorus in the wastewater are removed through pretreatment and advanced oxidation treatment, the wastewater enters an evaporation crystallization system, the evaporation crystallization system mainly separates salt in the wastewater from the wastewater, and the separated salt can be purified and reused and generates economic value.
Condensed water generated by evaporation is further subjected to advanced treatment through a condensed water biochemical retreatment system, so that higher discharge or recycling requirements are met, partial organic matters can be remained in the condensed water, and the organic matters in the condensed water are further degraded through low-cost biochemical treatment. The condensate water biochemical retreatment system selects a biochemical and advanced treatment combined process for further treatment according to the actual conditions and the water quality discharge requirements of projects, and achieves higher discharge or recycling requirements.
Compared with the prior conventional ozone oxidation technology, the invention has the beneficial effects that:
by adopting a combined process of three ozone catalytic oxidations in a specific procedure and controlling the pH value in the three ozone catalytic oxidations, high-concentration organic matters in the wastewater can be efficiently reduced to a concentration meeting the evaporation condition, and the oxidation efficiency is improved.
The organic matter in the waste water is reduced to meet the evaporation entry condition through ozone catalytic oxidation, salt is separated from the waste water, the residual organic matter is converted into condensed water, and the residual organic matter in the condensed water is biochemically decomposed through microorganisms through an economically reliable biochemical process, so that the higher emission requirement is met, and the investment and the operation cost are greatly reduced.
In the comparative experiment in the embodiment of the present invention, except for the differences of the groups, the process environments, the reagent materials, and the like, which are not explicitly described, are kept consistent;
the treatment process of the high-concentration degradation-resistant pickling wastewater provided by the invention is further explained below.
Example 1: the invention relates to a treatment process of high-concentration degradation-resistant pickling wastewater
The method is characterized in that a tank truck is adopted to collect primary preserved szechuan pickle curing wastewater generated by scattered farmers intermittently and transport the primary preserved szechuan pickle curing wastewater to a centralized wastewater treatment station, characteristics such as wastewater volume and discharge period of the preserved szechuan pickle curing wastewater are comprehensively considered, a collection system with a certain volume is designed, the preserved szechuan pickle curing wastewater is collected by the tank truck and transported to the collection system of the centralized wastewater treatment station, and the wastewater is stored in the collection system while the water quality and the water volume are homogenized.
The waste water after being regulated is pumped into a screening system, and the screening system mainly carries out solid-liquid separation on a large part of tuber mustard residues and the like in the tuber mustard waste water through a hydraulic screen so as to reduce the subsequent treatment load.
The waste water is screened to remove large-particle preserved szechuan pickle residues and then enters an alkali-adding coagulating sedimentation system, and the system mainly removes suspended pollutants and total phosphorus in the waste water and makes preconditions for subsequent advanced oxidation treatment. Firstly, adding calcium hydroxide to adjust the pH value of the wastewater to 7-8, wherein the phosphorus removal agent is polyaluminium, and the addition amount is as follows: polyaluminium (molar ratio) =1:0.9, adding polyaluminium, rapidly stirring for 0.5h, adding PAM 3mg/L, slowly stirring for 1min, and finally precipitating for 1.5-2 h.
The wastewater enters an advanced oxidation system after being pretreated, the advanced oxidation system comprises an ozone air flotation pretreatment system, an ozone heterogeneous catalytic oxidation system and an ozone photocatalytic oxidation system, high-concentration organic matters in the wastewater are degraded to meet the requirement of entering evaporative crystallization through ozone advanced oxidation, and meanwhile, the evaporative crystallization system can stably run for a long time.
The ozone air-flotation pretreatment system mainly combines ozone oxidation and air flotation, and ozone is dissolved in water and released through the air dissolving device to contact and react with wastewater. The upper foam scraping and deslagging device removes foam and suspended matters generated in the reaction process. The reaction devices are made of ozone corrosion resistant materials. The ozone generator adopts an oxygen source, and the concentration of ozone is 110 mg/L. Adding calcium hydroxide to adjust the pH value of the wastewater to 12 before reaction, detecting the pH value in the reaction process, adding sodium hydroxide to adjust the pH value of the wastewater to 12 when the pH value is reduced to 7.5, and after ozone air flotation treatment is carried out for 8 hours, feeding the wastewater into an ozone heterogeneous catalytic oxidation system.
The filling volume of the heterogeneous catalyst (silicon-aluminum catalyst, Longantai LCO type) accounts for 55-70 percent of the volume of the ozone generator, preferably 60 percent, the ozone generator adopts an oxygen source, and the concentration of the ozone is 100 mg/L. Adding calcium hydroxide to adjust the pH value of the wastewater to 8 before reaction, detecting the pH value in the reaction process, maintaining the pH value of the wastewater at about 8 by adding sodium hydroxide, and after carrying out heterogeneous ozone catalytic oxidation treatment for 8 hours, allowing the wastewater to enter an ozone photocatalytic oxidation system.
The ozone photocatalytic oxidation system further deeply treats organic matters in the wastewater by combining ultraviolet light and ozone. The ozone generator adopts an oxygen source, the concentration of ozone is 100mg/L, and the wavelength of ultraviolet light is 185 nm. Adding calcium hydroxide to adjust the pH value of the wastewater to 12 before reaction, detecting the pH value in the reaction process, adding sodium hydroxide to adjust the pH value of the wastewater to 12 when the pH value is reduced to 7.5, and carrying out ozone photocatalytic oxidation treatment for 4 hours.
After most of organic matters, ammonia nitrogen and total phosphorus in the wastewater are removed through pretreatment and advanced oxidation treatment, the wastewater enters an evaporation crystallization system, the evaporation crystallization system mainly separates salt in the wastewater from the wastewater, and the separated salt can be purified and reused and generates economic value.
The condensed water generated by evaporation passes through a condensed water biochemical retreatment system, and the condensed water is further deeply treated by adopting AAO, so that the higher discharge or recycling requirement is met, partial organic matters can be remained in the condensed liquid, and the organic matters in the condensed water are further degraded by low-cost biochemical treatment.
Example 2: comparison of Fenton Oxidation and ozone Oxidation according to the invention
Referring to the treatment method of example 1, only the oxidation step is completed, the control group adopts the fenton oxidation process, and the two groups are treated by using the preserved szechuan pickle wastewater with the same source and COD value as raw water, and the results are shown in Table 1;
TABLE 1
As can be seen from table 1, the removal rate of COD is only 7% by fenton oxidation process, which is far from meeting the treatment requirement of pickling wastewater, and subsequent evaporative crystallization desalination cannot be performed; through the three-step ozone oxidation process, the final removal rate of COD reaches about 65%, most organic matters are efficiently degraded, and the requirement of evaporative crystallization can be met.
Example 3: influence of ozone oxidation pH value and process on COD removal effect
1. Ozone oxidation pH value
Referring to the treatment mode of example 1, only the oxidation step is completed, and each group is treated by wastewater with the same source and COD value;
TABLE 2
As can be seen from Table 2, if the pH value is not adjusted to the proper value along with the change of the pH value in the ozone oxidation process, the removal rate of COD in the wastewater by the three-step ozone oxidation is only 40%, while the pH value is continuously adjusted along with the change of the pH value in the reaction process, the removal rate of COD in the wastewater by the three-step ozone oxidation is about 65%, and compared with the case that the pH value is not adjusted in the reaction process, the treatment effect on the wastewater is obviously improved. 2. Influence of ozone Oxidation Process
Referring to the treatment method of example 1, the oxidation step is only completed;
(1) ozone photocatalytic oxidation-ozone air flotation oxidation-ozone heterogeneous catalytic oxidation process
TABLE 3
The process has the following defects: the photocatalytic oxidation has requirements on water quality chromaticity, the waste water is required to be colorless, but the preserved szechuan pickle waste water is yellow, and if the first process adopts photocatalytic ozone oxidation, the treatment effect on the preserved szechuan pickle waste water is basically not achieved. Under the same treatment time, the treatment effect is not as good as that of the ozone oxidation-heterogeneous ozone catalytic oxidation-photocatalytic ozone oxidation process.
(2) Ozone heterogeneous catalytic oxidation-ozone air flotation oxidation-ozone photocatalytic oxidation process
TABLE 4
The process has the following defects: contain a large amount of gases in the preserved szechuan pickle waste water, can produce a large amount of bubbles in the early stage processing procedure, if first technology adopts heterogeneous ozone catalytic oxidation, the bubble can be attached to the catalyst surface, wraps up the catalyst, influences the catalyst effect, and then influences the treatment effect of heterogeneous ozone catalytic oxidation to the preserved szechuan pickle waste water. Under the same treatment time, the treatment effect is not as good as that of the ozone oxidation-heterogeneous ozone catalytic oxidation-photocatalytic ozone oxidation process.
The foregoing are merely exemplary embodiments of the present invention, which enable those skilled in the art to understand or practice the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A treatment process of high-concentration degradation-resistant pickling wastewater is characterized by comprising the following steps:
step 1, solid-liquid separation;
collecting pickling wastewater, homogenizing and homogenizing, and then carrying out solid-liquid separation;
step 2, coagulating sedimentation;
after solid-liquid separation, carrying out coagulating sedimentation treatment on the pickling wastewater;
step 3, ozone air flotation pretreatment;
combining ozone oxidation and air flotation, adjusting the pH value of the pickling wastewater to 11-12 before reaction, dissolving ozone in the pickling wastewater through an air flotation air dissolving device and releasing the ozone, and performing contact and reaction with the pickling wastewater after coagulating sedimentation to remove generated foam and suspended matters; detecting the pH value in the reaction process, and adjusting the pH value to be between 11 and 12 when the pH value is lower than 11;
step 4, ozone heterogeneous catalytic oxidation;
after ozone air flotation pretreatment, adopting ozone and a heterogeneous catalyst to carry out combined treatment on the pickling wastewater; adjusting the pH value of the curing wastewater to 7.5-8.5 before reaction, and detecting the pH value in the reaction process to maintain the pH value of the wastewater at 7.5-8.5;
step 5, carrying out photocatalytic oxidation on ozone;
after ozone heterogeneous catalytic oxidation, treating pickling wastewater by combining ultraviolet light and ozone; adjusting the pH value of the curing wastewater to 11-12 before reaction, detecting the pH value in the reaction process, and adjusting the pH value to 11-12 when the pH value is lower than 11;
step 6, evaporating and crystallizing;
after the ozone photocatalytic oxidation, the pickling wastewater is evaporated and crystallized, and the salt is separated from the pickling wastewater.
2. The treatment process according to claim 1, wherein the step 2 is:
after solid-liquid separation, the pH value of the liquid is adjusted to 7-9 by adding alkali, and then the total phosphorus, the hardness and the suspended pollutants are removed by adding chemicals.
3. The process of claim 2 wherein the total phosphorus removal agent is PAC and/or PFC.
4. The process of claim 2, wherein the hardness-removing agent is sodium carbonate; and/or the medicament for removing the suspended pollutants is PAM; and/or, the heterogeneous catalyst in the step 3 is a carbon-based catalyst and/or an aluminum-based catalyst.
5. The process of claim 1, wherein the treatment time of steps 3-5 is independently selected from 4-10 hours.
6. The process of claim 1, wherein the ultraviolet light of step 5 has a wavelength of 185nm to 254 nm.
7. The process as claimed in claim 1, wherein the concentration of ozone in steps 3-5 is selected from 100-120 mg/L.
8. The treatment process according to any one of claims 1 to 7, further comprising removing residual organic matters from the condensed water produced by evaporative crystallization through a biochemical treatment process.
9. The treatment process according to claim 8, wherein the biochemical treatment process is one or more selected from AAO, AO, MBR, MBBR, and BAF.
10. The process according to any one of claims 1 to 7, further comprising returning the mother liquor from the evaporative crystallization to step 1 for reprocessing.
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|---|---|---|---|---|
| CN115259554A (en) * | 2022-07-26 | 2022-11-01 | 山东海科创新研究院有限公司 | Treatment method of epoxy resin wastewater |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591463A (en) * | 2015-01-19 | 2015-05-06 | 重庆华绿环保科技发展有限责任公司 | Method for treating preserved vegetable production wastewater |
| CN207933190U (en) * | 2018-01-31 | 2018-10-02 | 湖南平安环保股份有限公司 | A kind of ozone oxidation air-floating apparatus |
| CN110054331A (en) * | 2019-04-23 | 2019-07-26 | 苏州劼平泰环保科技有限公司 | A kind of Die Casting Plant wastewater treatment method |
| CN212334890U (en) * | 2020-04-27 | 2021-01-12 | 上海湘伊实业有限公司 | Textile wastewater treatment device |
-
2021
- 2021-12-14 CN CN202111523521.1A patent/CN113912251A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591463A (en) * | 2015-01-19 | 2015-05-06 | 重庆华绿环保科技发展有限责任公司 | Method for treating preserved vegetable production wastewater |
| CN207933190U (en) * | 2018-01-31 | 2018-10-02 | 湖南平安环保股份有限公司 | A kind of ozone oxidation air-floating apparatus |
| CN110054331A (en) * | 2019-04-23 | 2019-07-26 | 苏州劼平泰环保科技有限公司 | A kind of Die Casting Plant wastewater treatment method |
| CN212334890U (en) * | 2020-04-27 | 2021-01-12 | 上海湘伊实业有限公司 | Textile wastewater treatment device |
Non-Patent Citations (7)
| Title |
|---|
| 中国环境科学学会: "《中国环境科学学会学术年会论文集 2010 第3卷》", 31 August 2010, 北京：中国环境科学出版社 * |
| 崔节虎: "《氨基酚类有机废水处理技术研究》", 31 December 2018, 郑州：黄河水利出版社 * |
| 本书编委会: "《钻井废水处理技术及工程实例》", 31 May 2017, 成都：四川科学技术出版社 * |
| 李育基: "《企业环保基础知识》", 31 December 2017, 北京：中国计量出版社 * |
| 水工业市场编: "《"十一五"水处理关键技术与工程应用案例大全》", 31 October 2010, 北京：中国环境科学出版社 * |
| 祁鲁梁等: "《水处理工艺与运行管理实用手册》", 31 May 2002, 北京：中国石化出版社 * |
| 魏健编: "《辽河流域石化废水处理技术及工程实例》", 28 February 2018, 中国环境出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259554A (en) * | 2022-07-26 | 2022-11-01 | 山东海科创新研究院有限公司 | Treatment method of epoxy resin wastewater |
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