CN109970278B - Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater - Google Patents
Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater Download PDFInfo
- Publication number
- CN109970278B CN109970278B CN201910285382.XA CN201910285382A CN109970278B CN 109970278 B CN109970278 B CN 109970278B CN 201910285382 A CN201910285382 A CN 201910285382A CN 109970278 B CN109970278 B CN 109970278B
- Authority
- CN
- China
- Prior art keywords
- tank
- wastewater
- sedimentation tank
- antimony
- aerobic biochemical
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
-
- 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
- C02F1/52—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
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F1/52—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
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/30—Nature of the water, waste water, sewage or sludge to be treated from the textile industry
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/12—Sludge, slurries or mixtures of liquids
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention discloses a method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater, wherein the wastewater enters a reaction tank from an adjusting tank, and acid dissolved with ferrous sulfate, slaked lime and anionic polyacrylamide are sequentially added into the reaction tank for coagulation reaction; after reaction, the wastewater enters a primary sedimentation tank, the precipitated sludge is subjected to plate-and-frame filter pressing, and the separated wastewater enters an aerobic biochemical tank; after biochemical treatment, the sewage enters a secondary sedimentation tank, the separated sludge flows back to the biochemical tank, and the wastewater is introduced into a secondary biochemical tank; and (3) after treatment, the wastewater enters a final sedimentation tank, the separated wastewater reaches a standard and is contained in a pipe or is further treated and recycled to a workshop, and the residual sludge is subjected to plate-frame filter pressing and then is subjected to incineration treatment. The method has the advantages of simple operation, low medicament cost and obvious antimony removal effect, the final antimony concentration of the wastewater can be stably reduced to be below 100 mu g/L, the aeration of the aerobic sludge tank is fully utilized, the oxidation of ferrous iron in the wastewater into ferric iron is promoted, and the complexation and precipitation performance between the iron oxide and the antimonate are enhanced.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater.
Background
Antimony is a typical toxic and harmful heavy metal element, and researches show that antimony has chronic toxicity and carcinogenicity to organisms and human bodies and is included in the pollutant priority control category by the United States Environmental Protection Agency (USEPA) and the European Union (EU). With the rapid development of textile and printing and dyeing industries, antimony and compounds thereof are widely applied in the industry, and the problems of heavy metal antimony emission and pollution become more serious day by day. In 2015, the discharge standard of pollutants in textile dyeing and finishing industry water (GB 4287-: waste in the enterpriseThe standard direct discharge and indirect discharge limits of the total water discharge port and the total antimony are all 100 mu g.L-1。
The coagulating sedimentation method is one of the most common processes for treating the antimony-containing wastewater, and aiming at the problem of antimony pollution of the printing and dyeing wastewater at present, ferric salts such as polymeric ferric sulfate, ferrous sulfate and the like are often used as an antimony removal coagulant, and iron oxide or iron hydroxide formed by hydrolysis of the polymeric ferric sulfate, ferrous sulfate and the like can be effectively complexed with antimonate, so that solid-liquid separation of antimony pollution is realized. The polymeric ferric sulfate coagulation antimony removal efficiency is high, but the method needs to repeatedly adjust the pH value, the cost of the medicament is high, and the cost performance is low; the ferrous sulfate is low in price, but the treatment efficiency is low, and the discharge reaching the standard can be realized only by adding a large amount of the ferrous sulfate.
Disclosure of Invention
The invention aims to provide a method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater by combining the existing treatment facilities of enterprises, and the method and equipment are high in treatment efficiency and low in medicament cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for efficiently and economically removing antimony in printing and dyeing wastewater comprises the following steps:
(1) the antimony-containing printing and dyeing wastewater enters a reaction tank from a regulating tank, acid dissolved with ferrous sulfate or acid dissolved with ferrous sulfate and potassium permanganate is added into the reaction tank, and then slaked lime and anionic polyacrylamide are added for coagulation reaction;
(2) the wastewater after reaction enters a primary sedimentation tank from a reaction tank, the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank, and the precipitated sludge in the primary sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated;
(3) the wastewater after biochemical treatment enters a secondary sedimentation tank from an aerobic biochemical tank, the wastewater separated from the secondary sedimentation tank is introduced into a secondary aerobic biochemical tank, partial sludge in the secondary sedimentation tank flows back to the aerobic biochemical tank, and the residual sludge in the secondary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
(4) and (3) the wastewater after the second-stage biochemical treatment enters a final sedimentation tank from a second-stage aerobic biochemical tank, the wastewater separated from the final sedimentation tank is the wastewater (reaching a standard for receiving pipes or being further treated and recycled to a workshop) from which the antimony is removed, part of sludge in the final sedimentation tank flows back to the second-stage aerobic biochemical tank, and the residual sludge in the final sedimentation tank is subjected to plate-frame filter pressing and then is burnt.
The following are preferred technical schemes of the invention:
in the step (1), the acid in which ferrous sulfate is dissolved is hydrochloric acid, the adding amount of the ferrous sulfate is 150 to 200 times (more preferably 180 to 200 times) of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, the adding amount of the ferrous sulfate is 300ppm to 700ppm (more preferably 550ppm to 600ppm), the mass ratio of the ferrous sulfate in the acid in which the ferrous sulfate is dissolved to the mass of the antimony-containing printing and dyeing wastewater is 300ppm to 700ppm (more preferably 550ppm to 600ppm), the acid in which the ferrous sulfate and potassium permanganate are dissolved is hydrochloric acid, the adding amount of the ferrous sulfate is 50 to 90 times (more preferably 60 to 80 times) of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, the adding amount of the ferrous sulfate is 150ppm to 250ppm (more preferably 160ppm to 200ppm), and the mass ratio of the ferrous sulfate in the acid in which the ferrous sulfate and potassium permanganate are dissolved to the mass ratio of the antimony-containing printing and dyeing wastewater is 150ppm ppm-250 ppm (more preferably 160 ppm-200 ppm), the adding amount of the potassium permanganate is 0.5-0.6 times of that of ferrous sulfate, the adding amount of the potassium permanganate is 75 ppm-150 ppm (more preferably 80 ppm-120 ppm), namely the mass ratio of ferrous sulfate in acid dissolved with ferrous sulfate and potassium permanganate to the mass of antimony-containing printing and dyeing wastewater is 75 ppm-150 ppm (more preferably 80 ppm-120 ppm), and the lower concentration of the acid dissolved with ferrous sulfate and potassium permanganate can generate better antimony removal effect.
The addition amount of the slaked lime is 30ppm to 100ppm (more preferably 50ppm to 80ppm), namely, the slaked lime accounts for 30ppm to 100ppm (more preferably 50ppm to 80ppm) by mass of the antimony-containing printing and dyeing wastewater, the addition amount of the anionic polyacrylamide is 1ppm to 10ppm (more preferably 2ppm to 3ppm), and the addition amount of the anionic polyacrylamide and the antimony-containing printing and dyeing wastewater is 1ppm to 10ppm (more preferably 2ppm to 3ppm) by mass.
The coagulation reaction specifically comprises the following steps: and (3) quickly stirring and mixing for reaction for 1-10 min at the speed of 100-300 r/min, further preferably, quickly stirring and mixing for reaction for 1-5 min at the speed of 150-250 r/min, and most preferably, quickly stirring and mixing for reaction for 2min at the speed of 200 r/min.
In the step (2), the pH value of the effluent of the primary sedimentation tank is 7-8.
In the step (2), the hydraulic retention time of the aerobic biochemical pool is 4.5-7 h, and the concentration of dissolved oxygen in the aerobic biochemical pool is 2.0-5.5 mg/L. Further preferably, the hydraulic retention time of the aerobic biochemical pool is 4.5-5 h, and the dissolved oxygen concentration in the aerobic biochemical pool is 3.0-4.0 mg/L.
In the step (3), the hydraulic retention time of the second-stage aerobic biochemical pool is 4.5-7 h, and the concentration of dissolved oxygen in the second-stage aerobic biochemical pool is 2.0-5.5 mg/L. Preferably, the hydraulic retention time of the second-stage aerobic biochemical pool is 6-7 h, and the concentration of dissolved oxygen in the second-stage aerobic biochemical pool is 2.5-3.8 mg/L.
An apparatus for efficiently and economically removing antimony from printing and dyeing wastewater, comprising:
a regulating tank for receiving the antimony-containing printing and dyeing wastewater;
the reaction tank is connected with the regulating tank;
the primary sedimentation tank is connected with the reaction tank;
the aerobic biochemical tank is connected with the primary sedimentation tank;
the secondary sedimentation tank is connected with the aerobic biochemical tank;
the two-section aerobic biochemical tank is connected with the secondary sedimentation tank;
the final sedimentation tank is connected with the two sections of aerobic biochemical tanks;
the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank, and the precipitated sludge in the primary sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated;
introducing the wastewater separated by the secondary sedimentation tank into a second-stage aerobic biochemical tank, refluxing partial sludge in the secondary sedimentation tank to the aerobic biochemical tank, and incinerating residual sludge in the secondary sedimentation tank after plate-frame filter pressing;
the waste water separated from the final sedimentation tank is waste water for removing antimony, partial sludge in the final sedimentation tank flows back to the two-stage aerobic biochemical tank, and residual sludge in the final sedimentation tank is subjected to plate-frame filter pressing and then is burnt.
Compared with the prior art, the invention has the following advantages:
1. according to the invention, hydrated lime is added to increase the calcium ion concentration, so that the antimony removing effect of ferrous sulfate coagulation is enhanced, aeration and oxygenation in the aerobic tank are effectively utilized, the antimony is efficiently removed by using ferrous sulfate with lower dosage, and the medicament cost is reduced.
2. The method has the advantages of simple operation, low medicament cost and obvious antimony removal effect, the final antimony concentration of the wastewater can be stably reduced to be below 100 mu g/L, the aeration of the aerobic sludge tank is fully utilized, the oxidation of ferrous iron in the wastewater into ferric iron is promoted, and the complexation and precipitation performance between the iron oxide and the antimonate are enhanced.
3. The process and equipment applied by the method are conventional processes and devices of printing and dyeing enterprises or sewage treatment plants, and can be realized by changing the medicament, so that the method is convenient to popularize and apply.
Drawings
FIG. 1 is a schematic diagram of the method for efficiently and economically removing antimony from printing and dyeing wastewater according to the invention.
Detailed Description
The present invention will be further described with reference to the following examples.
The first embodiment is as follows: in this embodiment, a method for efficiently and economically removing antimony from printing and dyeing wastewater, which is to treat printing and dyeing wastewater of a certain printing and dyeing enterprise according to the process shown in fig. 1, wherein the antimony concentration in the antimony-containing printing and dyeing wastewater is 3330.6 μ g/L, includes the following steps:
(1) the method comprises the following steps of (1) enabling antimony-containing printing and dyeing wastewater to enter a reaction tank from an adjusting tank, firstly adding hydrochloric acid dissolved with ferrous sulfate into the reaction tank, wherein the adding amount of the ferrous sulfate is 180.1 times (600 ppm) of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, namely the mass ratio of the ferrous sulfate in the hydrochloric acid dissolved with the ferrous sulfate to the antimony-containing printing and dyeing wastewater is 600ppm, then adding slaked lime and anionic polyacrylamide (PAM, Henan Hai Yun environmental protection science and technology Limited), wherein the adding amounts are 60ppm and 2ppm respectively, namely the mass ratio of the slaked lime to the antimony-containing printing and dyeing wastewater is 60ppm, the mass ratio of the anionic polyacrylamide to the antimony-containing printing and dyeing wastewater is 2ppm, and carrying out rapid stirring and mixing reaction for 2min at;
(2) the wastewater after reaction enters a primary sedimentation tank from a reaction tank, the pH of the effluent of the primary sedimentation tank is 7.3, the concentration of antimony is 282.0 mu g/L, the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank (called aerobic tank for short), the hydraulic retention time of the aerobic biochemical tank is 4.7h, the dissolved oxygen in the aerobic biochemical tank is 3.5mg/L, and the precipitated sludge in the primary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
(3) after biochemical treatment, the wastewater enters a secondary sedimentation tank from an aerobic biochemical tank, the concentration of antimony in the effluent of the secondary sedimentation tank is 103.2 mu g/L, the wastewater separated by the secondary sedimentation tank is introduced into a secondary aerobic tank (namely a secondary aerobic biochemical tank), the hydraulic retention time of the secondary aerobic biochemical tank is 6.5h, and the dissolved oxygen in the secondary aerobic biochemical tank is 2.7 mg/L; part of sludge in the secondary sedimentation tank flows back to the aerobic biochemical tank, and the rest sludge in the secondary sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated;
(4) after two-stage biochemical treatment, the wastewater enters a final sedimentation tank from a two-stage aerobic biochemical tank, the concentration of antimony in the supernatant of the wastewater separated from the final sedimentation tank is 86.8 mu g/L, the removal rate of antimony in the process is 97.4 percent, and the standard that the total antimony emission limit value is 100 mu g/L after the modification of the textile dyeing and finishing industry water pollutant emission standard (GB 4287-. And part of sludge in the final sedimentation tank flows back to the two-stage aerobic biochemical tank, and the residual sludge in the final sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated.
Example two: in this embodiment, a method for efficiently and economically removing antimony from printing and dyeing wastewater, which is to treat antimony-containing printing and dyeing wastewater of a certain printing and dyeing enterprise according to the process shown in fig. 1, wherein the antimony concentration in the antimony-containing printing and dyeing wastewater is 2822.5 μ g/L, includes the following steps:
(1) antimony-containing printing and dyeing wastewater enters a reaction tank from an adjusting tank, hydrochloric acid dissolved with ferrous sulfate is firstly added into the reaction tank, the adding amount of the ferrous sulfate is 194.9 times of the mass concentration of antimony in the wastewater, namely 550ppm, slaked lime and anionic polyacrylamide (PAM, river south China sea charm environmental protection technology Co., Ltd.) are then added, the adding amounts are 80ppm and 3ppm respectively, and 200r/min is quickly stirred and mixed for reaction for 2 min;
(2) the wastewater after reaction enters a primary sedimentation tank, the pH of the effluent of the primary sedimentation tank is 7.5, the concentration of antimony is 258.3 mu g/L, the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank (called aerobic tank for short), the hydraulic retention time of the aerobic biochemical tank is 4.7h, the dissolved oxygen in the aerobic biochemical tank is 3.3mg/L, and the precipitated sludge in the primary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
(3) after biochemical treatment, the wastewater enters a secondary sedimentation tank from an aerobic biochemical tank, the concentration of antimony in the effluent of the secondary sedimentation tank is 81.8 mu g/L, the wastewater separated by the secondary sedimentation tank is introduced into a second-stage aerobic tank (namely a second-stage aerobic biochemical tank), the hydraulic retention time of the second-stage aerobic biochemical tank is 6.5h, the dissolved oxygen in the second-stage aerobic biochemical tank is 3.6mg/L, part of sludge in the secondary sedimentation tank flows back to the aerobic biochemical tank, and the rest sludge in the secondary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
(4) after two-stage biochemical treatment, the wastewater enters a final sedimentation tank from a two-stage aerobic biochemical tank, the concentration of antimony in the supernatant of the wastewater separated from the final sedimentation tank is 69.2 mu g/L, the removal rate of antimony in the process is 97.5 percent, and the standard that the total antimony emission limit value is 100 mu g/L after modification of the discharge standard of pollutants for textile dyeing and finishing industry (GB 4287-. And part of sludge in the final sedimentation tank flows back to the two-stage aerobic biochemical tank, and the residual sludge in the final sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated.
Example three: in this embodiment, a method for efficiently and economically removing antimony from printing and dyeing wastewater, which is to treat antimony-containing printing and dyeing wastewater of a certain printing and dyeing enterprise according to the process shown in fig. 1, wherein the antimony concentration in the antimony-containing printing and dyeing wastewater is 2525.4 μ g/L, includes the following steps:
(1) antimony-containing printing and dyeing wastewater enters a reaction tank from an adjusting tank, hydrochloric acid dissolved with ferrous sulfate and potassium permanganate is mixed and added into the reaction tank, wherein the adding amount of the ferrous sulfate is 71.3 times of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, namely 180ppm, and the adding amount of the potassium permanganate is 0.56 times of the adding amount of the ferrous sulfate, namely 100ppm, slaked lime and anionic polyacrylamide (PAM, river-south sea charm environmental protection technology limited company) are added, the adding amounts are 50ppm and 2ppm respectively, and the stirring and mixing reaction is carried out for 2min at a speed of 200 r/min;
(2) the wastewater after reaction enters a primary sedimentation tank from a reaction tank, the pH of the effluent of the primary sedimentation tank is 7.2, the concentration of antimony is 148.1 mu g/L, the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank (called aerobic tank for short), the hydraulic retention time of the aerobic biochemical tank is 4.7h, the dissolved oxygen in the aerobic biochemical tank is 3.3mg/L, and the precipitated sludge in the primary sedimentation tank is subjected to plate-and-frame filter pressing and then is burnt;
(3) after biochemical treatment, the wastewater enters a secondary sedimentation tank from an aerobic biochemical tank, the concentration of antimony in the effluent of the secondary sedimentation tank is 48.2 mu g/L, the wastewater separated by the secondary sedimentation tank is introduced into a second-stage aerobic tank (namely a second-stage aerobic biochemical tank), the hydraulic retention time of the second-stage aerobic biochemical tank is 6.5h, the dissolved oxygen in the second-stage aerobic biochemical tank is 3.2mg/L, part of sludge in the secondary sedimentation tank flows back to the aerobic biochemical tank, and the rest sludge in the secondary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
(4) after two-stage biochemical treatment, the wastewater enters a final sedimentation tank from a two-stage aerobic biochemical tank, the concentration of antimony in the supernatant of the wastewater separated from the final sedimentation tank is 29.6 mu g/L, the removal rate of antimony in the process is 98.8 percent, and the standard that the total antimony emission limit value is 100 mu g/L after the modification of the emission standard of pollutants for textile dyeing and finishing industry (GB 4287-. And part of sludge in the final sedimentation tank flows back to the two-stage aerobic biochemical tank, and the residual sludge in the final sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated.
The embodiments of the present invention have been described with reference to the accompanying drawings, but the present invention is not limited to the embodiments, and any modifications, equivalent substitutions, improvements, etc. within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A method for efficiently and economically removing antimony in printing and dyeing wastewater is characterized by comprising the following steps:
(1) the antimony-containing printing and dyeing wastewater enters a reaction tank from a regulating tank, acid dissolved with ferrous sulfate or acid dissolved with ferrous sulfate and potassium permanganate is added into the reaction tank, and then slaked lime and anionic polyacrylamide are added for coagulation reaction;
in the acid dissolved with ferrous sulfate, the acid is hydrochloric acid, the addition amount of the ferrous sulfate is 150-200 times of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, and the addition amount of the ferrous sulfate is 300-700 ppm;
in the acid dissolved with ferrous sulfate and potassium permanganate, the acid is hydrochloric acid, the addition amount of the ferrous sulfate is 50-90 times of the mass concentration of antimony in the antimony-containing printing and dyeing wastewater, the addition amount of the potassium permanganate is 0.5-0.6 times of the addition amount of the ferrous sulfate, the addition amount of the ferrous sulfate is 150-250 ppm, and the addition amount of the potassium permanganate is 75-150 ppm;
the addition amount of the hydrated lime is 30ppm to 100 ppm;
the dosage of the anionic polyacrylamide is 1ppm to 10 ppm;
(2) the wastewater after reaction enters a primary sedimentation tank from a reaction tank, the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank, and the precipitated sludge in the primary sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated;
(3) the wastewater after biochemical treatment enters a secondary sedimentation tank from an aerobic biochemical tank, the wastewater separated from the secondary sedimentation tank is introduced into a secondary aerobic biochemical tank, partial sludge in the secondary sedimentation tank flows back to the aerobic biochemical tank, and the residual sludge in the secondary sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
the hydraulic retention time of the aerobic biochemical tank is 4.5-7 h, and the concentration of dissolved oxygen in the aerobic biochemical tank is 2.0-5.5 mg/L;
(4) the wastewater after the second-stage biochemical treatment enters a final sedimentation tank from a second-stage aerobic biochemical tank, the wastewater separated from the final sedimentation tank is the wastewater subjected to antimony removal, the wastewater reaches a standard for containing pipes or is further treated and recycled to a workshop, part of sludge in the final sedimentation tank flows back to the second-stage aerobic biochemical tank, and the residual sludge in the final sedimentation tank is subjected to plate-frame filter pressing and then is burnt;
the hydraulic retention time of the second-stage aerobic biochemical tank is 4.5-7 h, and the dissolved oxygen concentration in the second-stage aerobic biochemical tank is 2.0-5.5 mg/L.
2. The method for efficiently and economically removing antimony in printing and dyeing wastewater according to claim 1, wherein in the step (1), the coagulation reaction is specifically as follows: stirring and mixing the mixture for reaction for 1-10 min at a speed of 100-300 r/min.
3. The method for efficiently and economically removing antimony from printing and dyeing wastewater according to claim 1, wherein in the step (2), the hydraulic retention time of the aerobic biochemical pool is 4.5-5 h, and the dissolved oxygen concentration in the aerobic biochemical pool is 3.0-4.0 mg/L;
in the step (3), the hydraulic retention time of the second-stage aerobic biochemical pool is 6-7 h, and the concentration of dissolved oxygen in the second-stage aerobic biochemical pool is 2.5-3.8 mg/L.
4. The method for efficiently and economically removing antimony from printing and dyeing wastewater according to claim 1, wherein the equipment for efficiently and economically removing antimony from printing and dyeing wastewater is used and comprises:
a regulating tank for receiving the antimony-containing printing and dyeing wastewater;
the reaction tank is connected with the regulating tank;
the primary sedimentation tank is connected with the reaction tank;
the aerobic biochemical tank is connected with the primary sedimentation tank;
the secondary sedimentation tank is connected with the aerobic biochemical tank;
the two-section aerobic biochemical tank is connected with the secondary sedimentation tank;
the final sedimentation tank is connected with the two sections of aerobic biochemical tanks;
the wastewater separated by the primary sedimentation tank enters an aerobic biochemical tank, and the precipitated sludge in the primary sedimentation tank is subjected to plate-and-frame filter pressing and then is incinerated;
introducing the wastewater separated by the secondary sedimentation tank into a second-stage aerobic biochemical tank, refluxing partial sludge in the secondary sedimentation tank to the aerobic biochemical tank, and incinerating residual sludge in the secondary sedimentation tank after plate-frame filter pressing;
the waste water separated from the final sedimentation tank is waste water for removing antimony, partial sludge in the final sedimentation tank flows back to the two-stage aerobic biochemical tank, and residual sludge in the final sedimentation tank is subjected to plate-frame filter pressing and then is burnt.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910285382.XA CN109970278B (en) | 2019-04-10 | 2019-04-10 | Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910285382.XA CN109970278B (en) | 2019-04-10 | 2019-04-10 | Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109970278A CN109970278A (en) | 2019-07-05 |
| CN109970278B true CN109970278B (en) | 2020-11-03 |
Family
ID=67083895
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910285382.XA Active CN109970278B (en) | 2019-04-10 | 2019-04-10 | Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109970278B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112047403A (en) * | 2020-09-07 | 2020-12-08 | 江苏三美化工有限公司 | Treating agent and treating process for fluorine-containing antimony chloride industrial wastewater |
| CN113277689A (en) * | 2021-07-12 | 2021-08-20 | 湖州新利商标制带有限公司 | Device and method for improving biological treatment efficiency of trademark fabric production wastewater |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101708882A (en) * | 2009-11-24 | 2010-05-19 | 锡矿山闪星锑业有限责任公司 | Treating process of waste water containing antimony |
| CN103121763A (en) * | 2012-11-30 | 2013-05-29 | 中南民族大学 | Process for treating high-arsenic and high cadmium waste acid by using three-stage lime-ferric salt method |
| CN105060557A (en) * | 2015-07-31 | 2015-11-18 | 广州大学 | New method for simultaneously and efficiently removing thallium and arsenic from smelting wastewater |
| CN205115188U (en) * | 2015-11-11 | 2016-03-30 | 苏州市环境保护有限公司 | Processing system who contains antimony waste water |
| CN206204074U (en) * | 2016-10-28 | 2017-05-31 | 北京金州恒基环保工程技术有限公司 | A kind of new stibium-containing wastewater processing unit |
| CN206308238U (en) * | 2017-04-07 | 2017-07-07 | 嘉兴市博莱特纸业有限公司 | Sewage disposal system |
| CN107162261A (en) * | 2017-06-01 | 2017-09-15 | 黄山加佳荧光材料有限公司 | A kind of high-efficient treatment method of fluorescent pigment latex waste water |
| CN107512820A (en) * | 2016-06-16 | 2017-12-26 | 吴江市新达印染厂 | The minimizing technology of antimony in a kind of dyeing waste water |
| CN207748994U (en) * | 2017-11-01 | 2018-08-21 | 杭州开源环保工程有限公司 | A kind of printing and dyeing sewage disposal system containing antimony |
-
2019
- 2019-04-10 CN CN201910285382.XA patent/CN109970278B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101708882A (en) * | 2009-11-24 | 2010-05-19 | 锡矿山闪星锑业有限责任公司 | Treating process of waste water containing antimony |
| CN103121763A (en) * | 2012-11-30 | 2013-05-29 | 中南民族大学 | Process for treating high-arsenic and high cadmium waste acid by using three-stage lime-ferric salt method |
| CN105060557A (en) * | 2015-07-31 | 2015-11-18 | 广州大学 | New method for simultaneously and efficiently removing thallium and arsenic from smelting wastewater |
| CN205115188U (en) * | 2015-11-11 | 2016-03-30 | 苏州市环境保护有限公司 | Processing system who contains antimony waste water |
| CN107512820A (en) * | 2016-06-16 | 2017-12-26 | 吴江市新达印染厂 | The minimizing technology of antimony in a kind of dyeing waste water |
| CN206204074U (en) * | 2016-10-28 | 2017-05-31 | 北京金州恒基环保工程技术有限公司 | A kind of new stibium-containing wastewater processing unit |
| CN206308238U (en) * | 2017-04-07 | 2017-07-07 | 嘉兴市博莱特纸业有限公司 | Sewage disposal system |
| CN107162261A (en) * | 2017-06-01 | 2017-09-15 | 黄山加佳荧光材料有限公司 | A kind of high-efficient treatment method of fluorescent pigment latex waste water |
| CN207748994U (en) * | 2017-11-01 | 2018-08-21 | 杭州开源环保工程有限公司 | A kind of printing and dyeing sewage disposal system containing antimony |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109970278A (en) | 2019-07-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107555701B (en) | Low-cost coking wastewater treatment method | |
| CN105948336B (en) | A kind for the treatment of process of electroplating wastewater containing cyanogens and chrome | |
| CN103288309A (en) | Coal gasification wastewater zero-emission treatment method, treatment system and application thereof | |
| CN104310700A (en) | Treatment method for wastewater containing high-concentration organic phosphorus | |
| CN106554126B (en) | Deep standard-reaching treatment method and system for reverse osmosis concentrated water | |
| CN111573970A (en) | Method for treating coking wastewater by physicochemical and biochemical combination | |
| CN109970278B (en) | Method and equipment for efficiently and economically removing antimony in printing and dyeing wastewater | |
| CN104193123A (en) | Gold mine cyanide-containing wastewater system treating method | |
| CN107265777B (en) | Method for treating membrane filtration concentrated solution of landfill leachate | |
| CN104961272A (en) | Method for treating cyaniding tailing pulp in gold industry | |
| CN114180753A (en) | Method for treating wastewater containing cyanide and oxalate | |
| CN105712564A (en) | Equipment for processing waste water through glyphosate production | |
| CN103332827A (en) | Desalination and organic matter degradation recycling technology for RO (reverse osmosis) concentrated water | |
| CN111099784A (en) | Treatment method of desulfurization wastewater | |
| CN104230122A (en) | Gold mine cyaniding waste residue leaching solution treating method | |
| CN111995167A (en) | Treatment method of acidic heavy metal wastewater | |
| CN111138040A (en) | Landfill leachate treatment method | |
| CN104193122A (en) | Gold mine cyanided waste residue leaching solution treating method | |
| CN111196668A (en) | Emergency treatment method for benzene-containing strong-acid chemical wastewater | |
| CN112110601A (en) | Method and device for treating landfill leachate | |
| CN110963612A (en) | Method for co-processing lead and arsenic composite pollutants in underground water by adopting pre-oxidation | |
| CN115196828A (en) | Stainless steel pickling waste water denitrification processing system | |
| CN101723497B (en) | Method for processing oily waste water by utilizing ferric hydroxide waste residue | |
| CN113371934A (en) | Sewage treatment method | |
| CN106746065A (en) | A kind of method for the treatment of electroplating wastewater by microwave |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |