CN108178389B - Treatment process of preserved fruit wastewater - Google Patents

Treatment process of preserved fruit wastewater Download PDF

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Publication number
CN108178389B
CN108178389B CN201810076708.3A CN201810076708A CN108178389B CN 108178389 B CN108178389 B CN 108178389B CN 201810076708 A CN201810076708 A CN 201810076708A CN 108178389 B CN108178389 B CN 108178389B
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treatment
wastewater
preserved fruit
membrane
activated carbon
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CN108178389A (en
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曾孟祥
马仁杰
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Xiamen University of Technology
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Xiamen University of Technology
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water, or sewage
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/001Processes for the treatment of water whereby the filtration technique is of importance
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/46Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104Devices therefor; Their operating or servicing
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5281Installations for water purification using chemical agents
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters

Abstract

The invention provides a treatment process of preserved fruit wastewater, and relates to the technical field of water treatment. The treatment process of the preserved fruit wastewater comprises the following steps: adding a coagulant into the preserved fruit wastewater, stirring and reacting for 20-40 min, and then placing the mixture into a sedimentation tank to remove sediments. And then transferring the water subjected to precipitation treatment to a sand filter, and enabling the wastewater subjected to sand filtration to enter an activated carbon filter to remove suspended matters and viscose particles in the water. And separating the coarsely filtered wastewater by an ultrafiltration membrane, separating by a nanofiltration membrane, and removing particles, colloids, bacteria and organic matters in the water, wherein concentrated solution obtained by interception by the ultrafiltration membrane and the microfiltration membrane is subjected to micro-electrolysis treatment, and then returned to the membrane separation step for treatment. The membrane pollution can be effectively reduced by pre-treatment such as coagulating sedimentation, sand filtration, activated carbon filtration and the like, and then the concentrated solution after membrane separation is subjected to centralized treatment, so that the discharge of high-salinity wastewater pollutants is reduced.

Description

Treatment process of preserved fruit wastewater
Technical Field
The invention relates to the technical field of water treatment, and particularly relates to a treatment process of preserved fruit wastewater.
Background
The waste water of the preserved fruit, namely the waste water generated in the process of producing the preserved fruit, is not suitable for the survival of microorganisms due to the characteristics of the waste water of the preserved fruit, and the biological method is greatly restricted in treating the waste water of the preserved fruit. In the prior art, a physical method is generally adopted to treat the preserved fruit wastewater, and the method specifically comprises the following treatment processes:
(1) the process for treating the jujube production wastewater by using the pre-aeration adjusting tank, IC, A/O, active sand filtration and multi-medium filtration utilizes the anaerobic biological reaction of the wastewater in an IC reactor to reduce the COD index of water, and utilizes microorganisms in the water to adsorb pollutants through the subsequent anaerobic-aerobic biological treatment. However, the IC reactor has a problem that the hydraulic retention time is short, and the burden on the aerobic stage is increased. Because the internal circulation of the gas of the IC reactor makes the quality of the effluent unstable, the subsequent treatment effect is influenced, and the final effluent quality is unstable. In addition, the process requires professional personnel to maintain and operate, and the operation cost is high.
(2) The technology for treating high-salt preserved fruit by electrochemical, medicament clarification and MBR (membrane bioreactor) utilizes an iron-carbon micro-electrolysis reactor based on the principle of a primary battery to perform an oxidation-reduction reaction under an acidic condition so as to convert substances which are difficult to biodegrade into substances which are easy to biodegrade. Then, partial chloride ions in the wastewater are removed by utilizing the characteristics of the modified diatomite, and the salt concentration is reduced. And finally, MBR is selected to replace a secondary sedimentation tank, so that the removal rate of pollutants is improved. But the electrochemical method and the MBR are processing methods with high investment, energy consumption and high processing cost. In the operation process, the electrochemical method is easily polluted by electrodes, the MBR is easily polluted by membranes, and the operation cost of the process is increased.
(3) The process for treating the preserved bean curd process wastewater by the combination of air floatation, anaerobic hydrolysis acidification and SBR has the advantages that when the preserved bean curd process wastewater is treated, due to low pH value, high salinity, high molecular mass of organic pollutants and high osmotic pressure, microbial cells are dehydrated to cause cell plasma separation, the activity of dehydrogenase is reduced by salting-out, and activated sludge is easy to float upwards and run off due to the increase of the density of the wastewater, so that the biological treatment effect is seriously influenced. And the biological method occupies a large area and needs professional personnel to maintain and operate.
(4) The Fenton oxidation method is used for treating the organic high-salt wastewater, not only utilizes a technology of treating organic matters by hydroxyl radicals generated by hydrogen peroxide through the action of a catalyst, light radiation or electrochemistry, but also has unique advantages when treating refractory organic matters, and is a high-salt organic wastewater treatment technology with a very promising prospect. However, the use of Fenton reagent can be costly due to the large amounts of ferrous salt and hydrogen peroxide.
Disclosure of Invention
The invention aims to provide a treatment process of preserved fruit wastewater, which is simple, easy to operate, low in one-time investment cost and good in treatment effect.
The technical problem to be solved by the invention is realized by adopting the following technical scheme.
The invention provides a treatment process of preserved fruit wastewater, which comprises the following steps:
coagulating sedimentation: adding a coagulant into the preserved fruit wastewater, stirring and reacting for 20-40 min, and then placing the mixture into a sedimentation tank to remove sediments;
and (3) coarse filtration: transferring the water subjected to precipitation treatment to a sand filter, and enabling the wastewater subjected to sand filtration to enter an activated carbon filter to remove suspended matters and viscose particles in the water;
a membrane separation step: and (3) separating the coarsely filtered wastewater by an ultrafiltration system, separating by a nanofiltration system, and removing particles, colloids, bacteria and organic matters in the water, wherein concentrated solution obtained by interception by the ultrafiltration system and the microfiltration system is subjected to micro-electrolysis treatment, and then returned to the membrane separation step for treatment.
The treatment process of the preserved fruit wastewater provided by the embodiment of the invention has the beneficial effects that:
compared with the prior biological methods such as an IC reactor and the like, the method has the advantages that the pollution components in the preserved fruit wastewater are directly removed mainly in a logistics interception mode, and the method is simple in treatment process operation and higher and more stable in effluent quality. Meanwhile, in the treatment process, a treatment method which is adaptive to the characteristics of the preserved fruit wastewater is designed, and due to the fact that the content of suspended matters such as pectin in the preserved fruit wastewater is high and the viscosity of the preserved fruit wastewater is high, the preserved fruit wastewater is subjected to multiple pre-treatments including coagulating sedimentation, sand filtration and activated carbon filtration, membrane pollution components with large particle sizes are effectively intercepted, then membrane separation treatment is carried out, the risks of membrane pollution and blockage are greatly reduced, and the membrane cleaning and repairing cost in the membrane separation treatment process is reduced.
In addition, the concentrated solution intercepted by the membrane separation treatment is subjected to micro-electrolysis treatment, compared with preserved fruit wastewater, the concentrated solution is greatly reduced in volume and contains high-concentration organic matters, the micro-electrolysis treatment is performed on the concentrated solution, then the membrane separation treatment is performed on the concentrated solution, pollutants are effectively reduced, and the requirement on micro-electrolysis equipment is greatly reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a process flow diagram of example 1 of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
The treatment process of the waste water of preserved fruit according to the embodiment of the present invention will be specifically described below.
The embodiment of the invention provides a treatment process of preserved fruit wastewater, which comprises the following steps:
coagulating sedimentation: adding a coagulant into the preserved fruit wastewater, stirring and reacting for 20-40 min, and then placing the mixture into a sedimentation tank to remove sediments;
and (3) coarse filtration: transferring the water subjected to precipitation treatment to a sand filter, and enabling the wastewater subjected to sand filtration to enter an activated carbon filter to remove suspended matters and viscose particles in the water;
a membrane separation step: and (3) separating the coarsely filtered wastewater by an ultrafiltration system, separating by a nanofiltration system, and removing particles, colloids, bacteria and organic matters in the water, wherein concentrated solution obtained by interception by the ultrafiltration system and the microfiltration system is subjected to micro-electrolysis treatment, and then returned to the membrane separation step for treatment.
Further, in a preferred embodiment of the present invention, the method further comprises a preprocessing step: and the preserved fruit wastewater enters an adjusting tank after being separated by a grid, and the pH value of the preserved fruit wastewater is adjusted to 6-8.
Further, in the preferred embodiment of the present invention, in the coagulating sedimentation step, the coagulant is selected from one or more of ammonium ferrous sulfate heptahydrate, aluminum sulfate, ferric chloride, ferrous sulfate and potassium aluminum sulfate, the feeding amount of the coagulant is 0.3-0.5 g/L, further, the coagulant is selected from ammonium ferrous sulfate heptahydrate, the feeding amount is 0.4 g/L, the stirring speed is controlled at 50r/min, the reaction time is 25min, the fully coagulated water is placed into a sedimentation tank, and coagulation and sedimentation can remove most of suspended matters and pectin, and also can remove a part of COD and ammonia nitrogen.
Furthermore, in the preferred embodiment of the invention, in the rough filtration step, the filler of the sand filter is quartz sand with the particle size of 3-5 mm, preferably, a pressure type sand filter is selected, the preserved fruit wastewater passes through the filter material from top to bottom, so that pollutants in the water are intercepted by the filter layer and purified, when the pressure difference △ P between the inlet and the outlet of the filter is more than or equal to 0.05-0.07 MPa, the sand filter needs backwashing, and the backwashing flow is controlled to be well backwashing until the water quality transparency of the inlet water and the outlet water is similar, the backwashing flow is continuously reduced, so that the filter material is layered and settled according to the particle size.
Further, in a preferred embodiment of the present invention, in the rough filtration step, the filler of the activated carbon filter is shell activated carbon with a particle size of 0.4-2.4 mm, and the activated carbon is cylindrical, spherical, hollow spherical or hollow column. Preferably, a fixed bed type activated carbon filter is selected, the effluent of the activated carbon filter is detected periodically, and when the activated carbon adsorption is saturated, the activated carbon is replaced in time.
Further, in the preferred embodiment of the present invention, in the membrane separation step, the ultrafiltration system uses an ultrafiltration-grade ceramic membrane as the membrane module, and the pore size of the ceramic membrane is 10-90 nm. Preferably, the selected ultrafiltration membrane is a 181-tube ultrafiltration ceramic membrane, and a cross-flow filtration mode is adopted for carrying out, the wastewater forms cross-flow filtration on the inner surface of the tube-type ceramic membrane, one part of the wastewater is filtered in a tangential-flow passing mode, the other part of the wastewater forms turbulence in a pipeline, the inner surface of the ceramic membrane is continuously washed, a small amount of solid matters attached to the membrane are taken away, the blockage of the ceramic membrane is effectively prevented, and the smooth operation of the membrane separation process is ensured. Furthermore, the working pressure of the ultrafiltration system is 0.05-0.3 MPa, and the membrane separation effect is further improved.
Further, in a preferred embodiment of the present invention, in the membrane separation step, the nanofiltration system employs a composite nanofiltration membrane with a pore size of 0.1 to 1 nm. The composite nanofiltration membrane in the embodiment can use the existing 250 composite membranes, and can also adopt a self-made composite nanofiltration membrane. Preferably, the self-made composite nanofiltration membrane is prepared by the following steps:
(1) dissolving 0.3 wt% piperazine and 0.2 wt% sodium hydroxide in deionized water, and adding0-0.07 wt% of modified nano TiO2Performing ultrasonic treatment for 10 min; soaking the wet polysulfone support membrane for 5min, taking out, rolling the surface of the support membrane by a rubber roller, and squeezing. Wherein, the modified nano TiO2The preparation method comprises the following steps: TiO with the content of 1 wt%2Ultrasonically dispersing in water solution, adding 2.5 wt% tannic acid solution, ultrasonically treating for 20min, adding 5 wt% ferric trichloride solution, reacting for 2min under stirring, centrifuging, cleaning, and drying to obtain modified TiO2
(2) Dissolving trimesoyl chloride with the concentration of 0.15 weight percent in cyclohexane; immersing the membrane material prepared in the step (1) in the solution, taking out the membrane material after the reaction time is 0.5min, and carrying out heat treatment on the membrane material in an oven at the temperature of 60 ℃ for 30 min. Rinsing with deionized water for several times to obtain the product containing TiO2The composite nanofiltration membrane.
Using tannic acid and Fe3+The functional surface layer is formed on the nano particles through chelation crosslinking, and the modified nano particles are loaded on the polysulfone support membrane through an interfacial polymerization method, so that the structure is stable, the hydrophilicity is better, the membrane separation effect is better, and the service life is long.
Further, the operating pressure of the nanofiltration system is 0.2-0.7 MPa, and the removal rate of pollutants in the wastewater can be improved under the operating pressure.
Further, in a preferred embodiment of the invention, the micro-electrolysis treatment of the concentrated solution (including the concentrated solution intercepted by the ultrafiltration system and the concentrated solution intercepted by the nanofiltration system) obtained by membrane separation comprises the steps of enabling the concentrated solution to enter an iron-carbon packed tower, enabling the retention time (HRT) to be 30-60 min, adjusting the pH of the concentrated solution to be 4-10, enabling the iron-carbon mass ratio to be 1-3: 1, enabling the aeration amount to be 1.5-3L/min, and simultaneously conducting the micro-electrolysis treatment of the aerated iron-carbon, so that the hardening effect of iron can be effectively prevented, the removal rate of COD can be improved, further, enabling the pH value to be 4, enabling the Fe/C to be 1, enabling the HRT to be 45min and enabling the aeration size to be 3L/min, and achieving the optimal effect.
More preferably, iron powder, activated carbon and a catalyst in a mass ratio of 1:1:0.01 are added in H in advance2In the atmosphere, sintering is carried out for 1-1.5 h at 850-1000 ℃, then sodium borohydride with 0.1% of iron powder mass is added, and grinding is carried out for 1-2 h to obtain a mixture which is used as an iron-carbon fillerThe catalyst is preferably L n2O3. The mixture forms a micro-battery system of zero-valent iron, catalyst, reducing agent and active carbon, can improve the treatment efficiency of wastewater, and effectively overcomes the defects of slow reaction speed, easy passivation and hardening and the like of the existing iron-carbon micro-electrolysis material in the wastewater treatment process.
The features and properties of the present invention are described in further detail below with reference to examples.
Example 1
As shown in FIG. 1, in the treatment process of wastewater from preserved fruit provided in this example, the water quality of wastewater from a preserved fruit processing plant is shown in Table 1:
TABLE 1
The waste water of the preserved fruit in the waste water pool enters a grid pool and then enters a regulating pool, and Na is used2CO3Adjusting the pH value to about 6.5, adding ammonium ferrous sulfate heptahydrate into a coagulation tank according to the feeding amount of 0.4 g/L, stirring and reacting for 25min under the condition of 50r/min, placing the coagulation tank into a sedimentation tank, removing sediment, enabling the wastewater to pass through a filter material of a sand filter from top to bottom, wherein the filter material is quartz sand with the particle size of 3-5 mm, enabling the wastewater flowing out of the sand filter to pass through an activated carbon fixed bed filter, the filter material is shell activated carbon with the particle size of 0.4-2.4 mm, enabling the wastewater flowing out of the activated carbon fixed bed filter to enter an ultrafiltration system, wherein the intercepted molecular weight is 6000-20000, the operating pressure is 0.1MPa, then enabling the wastewater to enter a nanofiltration system, the intercepted molecular weight is 800-1000, the operating pressure is 0.5MPa, enabling concentrated liquid intercepted by the ultrafiltration system and the nanofiltration system to enter an iron carbon packed tower, adjusting the pH value to be 4, Fe/C to be 1, HRT to be 45min, and aerating to be 3L/min.
The water quality after treatment is shown in Table 2.
TABLE 2
The treatment cost was as follows:
power consumption: the total installed power of a set of membrane system with the wastewater treatment capacity of 40t/h is about 125kW, and according to the electric charge of 0.6 yuan/meter, the electric charge required by each ton of wastewater is as follows: 1.875 yuan.
The labor cost of wastewater treatment operators is 2, wherein the work time of the operators is 1 in white class and 1 in night class, the work time of each operator is 2500 yuan/month, the membrane treatment equipment is started for 16 hours each day on average, and the labor cost of each ton of wastewater is 2500 × 2/30/40/16/0.26 yuan/ton.
The cost of the drug is calculated as shown in table 3:
TABLE 3
Accounting of depreciation cost:
the ultrafiltration membrane is a ceramic membrane, the replacement period is generally 5 years, the price for replacing a set of membrane system of 40t/h is about 200000 yuan, and the membrane loss per ton of water is as follows: 200000/365/5/40/16 is 0.16 yuan.
The nanofiltration membrane ultrafiltration membrane is a composite membrane system, the replacement period is generally 3 years, the price for replacing a set of 40t/h membrane system is about 600000 yuan, and the membrane loss per ton of water is as follows: 600000/365/3/40/16 is 0.85 yuan.
The micro-electrolysis equipment is an iron-carbon packed tower, the treatment cost per ton of water is 0.5 yuan, about 0.07 ton of concentrated solution is generated per ton of wastewater, and the micro-electrolysis loss per ton of water is as follows: 0.5 x 0.07 ═ 0.035 yuan.
In total, the cost of treating one ton of water is about 3.84 yuan.
Test examples the microelectrolytic conditions of the concentrates were investigated
1. Orthogonal assay analysis
Orthogonal test: four factors were determined to be Fe/C, pH values, HRT and aeration, and three level conditions were determined for each factor to measure the effect of these factors, with the design results shown in table 4.5 below:
TABLE 4 Quadrature test four factors and three levels
TABLE 5 results of orthogonal experiments
From table 5, we obtain: the orthogonal test result of the iron-carbon micro-electrolysis treatment nanofiltration concentrated solution shows that the degrees of COD removal rate under the four conditions are respectively pH value > Fe/C > HRT > aeration rate. Wherein, the influence of the hydrogen ion concentration index is the largest, the optimal combination condition is that the pH value is 4, the Fe/C is 1, the HRT is half an hour, the aeration size is 1.50 liters/minute, and the COD degradation rate is 60.25 percent.
2. Single factor variable experiment influence analysis
2.1pH Single factor variable Experimental analysis
The experiment fixes the mass ratio of iron to carbon as 1 and fills the iron to carbon into 5 beakers respectively filled with L solutions of 100m, the mass of the fixed active carbon is 2g, the HRT is controlled to be 0.5h, the aeration rate is 1.5L/min, five groups of experiments are respectively carried out under the conditions that the pH value is 3, 4, 7, 8 and 10, and a proper amount of water samples after the experiments are taken to detect the COD of the water samples.
Under the conditions of pH values of 3, 4, 7, 8 and 10, the removal rates of COD are respectively 53.33%, 58.46%, 37.95%, 33.85% and 27.69%. Under the condition of weak acid, the potential difference between iron and carbon is increased, the cathode and anode reaction speed is increased, and the micro-electrolysis treatment efficiency is higher. When the pH value is 4, the COD removal rate is the best, and is 58.46%. When the pH exceeds 4, the amount of COD degradation is reduced because the too high alkalinity lowers the reaction capability of the primary battery, and adversely affects the removal capability of COD. However, when the pH is too low, not only is iron consumed, but also hydrogen gas generated by the electrode reaction is attached to the electrode surface, and a film formed between the electrodes inhibits the reaction between iron and carbon, and eventually, the reaction ability is also lowered. The experimental results show that: the nanofiltration concentrate has the best decontamination effect when the pH value is 4.
2.2 Single factor variable Experimental analysis of iron to carbon Mass ratio
In the experiment, HRT is controlled to be half an hour, pH value is 4, 100 ml of solution is taken, the mass of fixed active carbon is 2g, aeration amount is 1.5L/min, five groups of experiments are carried out under the condition that Fe/C is respectively controlled to be 0.5, 1, 2, 3 and 4, and a proper amount of water sample after the experiment is taken to detect COD.
When the mass ratios of the iron and carbon are 0.5, 1, 2, 3 and 4, the corresponding COD removal rates are 58.21%, 58.46%, 55.90%, 48.21% and 43.08%, respectively. The larger the Fe/C value is, the COD degradation amount is increased and then gradually reduced. The reason is as follows: the iron and the activated carbon in the solution can form a primary battery, the mass ratio of the iron to the carbon is increased, the primary batteries of the iron and the activated carbon are increased to a certain extent, the electrode reaction is accelerated, and the pollution degradation is strong. Oxidation of excess Fe alone to produce excess Fe2+The subsequent process is complicated. The experimental results can be obtained as follows: the mass ratio of the iron to the carbon is set to be 1:1, and the decontamination effect of the concentrated solution is best.
2.3 Single factor variable Experimental analysis of HRT
100 ml of the solution was taken and the mass of the fixed activated carbon was 2 g. In the experiment, the pH value is controlled to be 4, the Fe/C is 1, the aeration rate is 1.5 liters/min, and the chemical oxygen demand of the solution is detected by taking a proper amount of the solution under the conditions that the HRT is respectively 10 minutes, 20 minutes, 30 minutes, 45 minutes and 60 minutes.
The removal rates of COD were 40.51%, 51.79%, 58.46%, 59.82% and 58.69% at HRT of 10min, 20min, 30 min, 45min and 60min, respectively. The removal rate increased all the time within 10-45 minutes of the experiment. After more than 45min, the COD removal rate is slightly reduced. The reason is that according to the principle of micro-electrolysis reaction, as the reaction proceeds, H in the cathode+Electrons are obtained to form hydrogen, H+The reduction in (b) increases the cell alkalinity, resulting in slower cell reactions and slower COD removal efficiency. From this, experimental results can be obtained: HRT is set to 45 minutes, and the decontamination effect of the concentrated solution is best。
2.4 Single factor variable Experimental analysis of aeration
In the experiment, the pH value is controlled to be 4, the Fe/C is 1, the HRT is controlled to be half an hour, 100 ml of concentrated solution is taken, and the mass of the fixed active carbon is 2 g. The chemical oxygen demand of the solution was measured by taking an appropriate amount of the solution under conditions of five experiments with aeration amounts of 0.00 l/min, 0.75 l/min, 1.50 l/min, 2.25 l/min and 3.00 l/min, respectively. The larger the aeration amount is, the larger the removal amount of the corresponding contaminant is. The COD removal rates at aeration rates of 0.00L/min, 0.75L/min, 1.50L/min, 2.25L/min, and 3.00L/min were 37.46%, 46.03%, 57.46%, 58.72%, and 59.50%, respectively. The reason for this is that the increase of the aeration amount increases O2The dissolution amount and the oxidation effect are enhanced, and the coagulation of the scrap iron is effectively hindered. In addition, the bubbles generated by aeration can also accelerate the reaction of the primary battery. The aeration rate is set to 3.00L/min, and the decontamination effect of the nanofiltration concentrated solution is the best.
2.5 validation of optimal Experimental conditions
The optimal experimental conditions of micro-electrolysis are obtained by the single-factor variable experiment for controlling the micro-electrolysis of the iron and the carbon, wherein the pH value is 4, the mass ratio of the iron to the carbon is 1, the HRT is 45 minutes, and the aeration size is 3.00 liters per minute. A set of validation experiments under the above optimal experimental conditions resulted in COD values as shown in table 6 below:
TABLE 6
The embodiments described above are some, but not all embodiments of the invention. The detailed description of the embodiments of the present invention is not intended to limit the scope of the invention as claimed, but is merely representative of selected embodiments of the invention. 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 invention.

Claims (8)

1. The treatment process of the preserved fruit wastewater is characterized by comprising the following steps of:
coagulating sedimentation: adding a coagulant into the preserved fruit wastewater, stirring and reacting for 20-40 min, and then placing the mixture into a sedimentation tank to remove sediments;
and (3) coarse filtration: transferring the water subjected to precipitation treatment to a sand filter, and enabling the wastewater subjected to sand filtration to enter an activated carbon filter to remove suspended matters and viscose particles in the water;
a membrane separation step: separating the coarsely filtered wastewater by an ultrafiltration system, separating by a nanofiltration system, and removing particles, colloids, bacteria and organic matters in the water, wherein concentrated solution obtained by interception by the ultrafiltration system and the nanofiltration system is subjected to micro-electrolysis treatment and then returns to the membrane separation step for treatment;
the micro-electrolysis treatment of the concentrated solution comprises the steps of enabling the concentrated solution to enter an iron-carbon packed tower, enabling the concentrated solution to stay for 30-60 min, adjusting the pH of the concentrated solution to be 4-10, enabling the mass ratio of iron to carbon to be 1-3: 1, enabling the aeration rate to be 1.5-3L/min, and enabling iron powder, activated carbon and a catalyst to be mixed in an H mode in advance, wherein the mass ratio of the iron powder to the activated carbon to be 1:1:0.012In the atmosphere, sintering is carried out for 1-1.5 h at 850-1000 ℃, then sodium borohydride with 0.1% of iron powder by mass is added, and grinding is carried out for 1-2 h to obtain a mixture which is used as a filler of the iron-carbon packed tower, wherein the catalyst is L n2O3
2. The treatment process of preserved fruit wastewater according to claim 1, further comprising a pretreatment step of: and the preserved fruit wastewater enters an adjusting tank after being separated by a grid, and the pH value of the preserved fruit wastewater is adjusted to 6-8.
3. The treatment process of preserved fruit wastewater according to claim 1, wherein in the coagulating sedimentation step, the coagulant is one or more selected from ammonium ferrous sulfate heptahydrate, aluminum sulfate, ferric chloride, ferrous sulfate and potassium aluminum sulfate, and the feeding amount of the coagulant is 0.3-0.5 g/L.
4. The treatment process of preserved fruit wastewater according to claim 1, wherein in the rough filtration step, the filler of the sand filter is quartz sand with a particle size of 3-5 mm.
5. The treatment process of preserved fruit wastewater according to claim 1, wherein in the rough filtration step, the filler of the activated carbon filter is shell activated carbon with a particle size of 0.4-2.4 mm, and the activated carbon is cylindrical, spherical, hollow spherical or hollow column.
6. The treatment process of preserved fruit wastewater according to claim 1, wherein in the membrane separation step, the ultrafiltration system adopts an ultrafiltration-grade ceramic membrane as a membrane component, and the pore diameter of the ceramic membrane is 10-90 nm.
7. The treatment process of preserved fruit wastewater according to claim 1, wherein in the membrane separation step, the nanofiltration system adopts a composite nanofiltration membrane with a pore diameter of 0.1-1 nm.
8. The treatment process of preserved fruit wastewater according to claim 1, wherein in the membrane separation step, the operating pressure of the ultrafiltration system is 0.05 to 0.3MPa, and the operating pressure of the nanofiltration system is 0.2 to 0.7 MPa.
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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101376546A (en) * 2008-09-02 2009-03-04 北京桑德环保集团有限公司 Coking advanced waste treatment system and processing method
CN105540967A (en) * 2015-12-09 2016-05-04 大唐国际化工技术研究院有限公司 Processing method for reducing and recycling organic waste water and processing system

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101376546A (en) * 2008-09-02 2009-03-04 北京桑德环保集团有限公司 Coking advanced waste treatment system and processing method
CN105540967A (en) * 2015-12-09 2016-05-04 大唐国际化工技术研究院有限公司 Processing method for reducing and recycling organic waste water and processing system

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