CN210505916U - Shunting electroplating sewage zero discharge treatment device - Google Patents
Shunting electroplating sewage zero discharge treatment device Download PDFInfo
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- CN210505916U CN210505916U CN201920840467.5U CN201920840467U CN210505916U CN 210505916 U CN210505916 U CN 210505916U CN 201920840467 U CN201920840467 U CN 201920840467U CN 210505916 U CN210505916 U CN 210505916U
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Abstract
The utility model relates to a shunting electroplating sewage zero discharge treatment device, which comprises a first treatment component for treating cleaning wastewater, a second treatment component for treating oil-removing and wax-removing wastewater and a third treatment component for treating high-concentration wastewater; the first treatment component comprises a first filtering mechanism, a first MCR system, a resin exchange system, a carbon filtration system, a UF membrane system and a three-stage reverse osmosis Ro membrane treatment system which are sequentially communicated; the second treatment component comprises an acid out oxidation treatment system; the third treatment component comprises a pretreatment mechanism, a second filtering mechanism, a second MCR system and an STUF membrane system which are sequentially communicated. The utility model provides a shunting is electroplated sewage zero release processing apparatus can reach industry reuse water standard after handling electroplating effluent, and the conductivity is low, is difficult for stifled membrane, and waste water rate of recovery is more than 99%, only produces about 1% waste liquid after handling, can realize the waste water zero release.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment plant, concretely relates to shunting is electroplated sewage zero release processing apparatus.
Background
The electroplating process waste water contains a large amount of pollutants such as chelating agent, heavy metal, high COD and the like. The wastewater contains a plurality of chelating types, has strong chelating capacity to heavy metals such as metallic nickel and the like, and does not precipitate heavy metals such as nickel and the like under alkaline conditions. The problems of difficult wastewater treatment, high cost and incapability of stably reaching the standard always trouble the development of the electroplating industry.
At present, electroplating wastewater is generally treated by adopting a pretreatment + UF + Ro membrane method and a corresponding device, but the method and the device have the defects of high water production conductivity and easy membrane blockage.
Therefore, the development of a treatment device for zero discharge of wastewater has important research significance and application value.
Disclosure of Invention
The utility model aims to overcome the defects that the electric conductivity of the electroplating wastewater is higher and the membrane is easily blocked in the prior art, and provide a shunting electroplating wastewater zero-discharge treatment device. The utility model provides a processing apparatus is categorised, the pertinence is handled the electroplating effluent of different classes, utilizes full physics piece-rate system, and waste water can reach industry reuse water standard after handling, and the conductivity is low, is difficult for stifled membrane, and waste water reuse rate more than 99%, only produces about 1% waste liquid after handling, can realize the waste water zero release.
In order to realize the novel purpose of the above use, the utility model adopts the following technical scheme:
a flow-dividing electroplating sewage zero-discharge treatment device comprises a first treatment component for treating cleaning wastewater, a second treatment component for treating oil-removing and wax-removing wastewater and a third treatment component for treating high-concentration wastewater; the first treatment component comprises a first filtering mechanism, a first MCR system, a resin exchange system, a carbon filtration system, a UF membrane system and a three-stage reverse osmosis Ro membrane treatment system which are sequentially communicated; the second treatment component comprises an acid out oxidation treatment system; the third treatment component comprises a pretreatment mechanism, a second filtering mechanism, a second MCR system and an STUF membrane system which are sequentially communicated; the water outlet of the acid precipitation oxidation treatment system and the water outlet of the STUF membrane system are both communicated with a first filtering mechanism; and the Ro concentrated water outlet of the three-stage reverse osmosis Ro membrane treatment system is communicated with the pretreatment mechanism.
The general electroplating process comprises the following steps: the method comprises the steps of pretreatment, preplating, cleaning, electroplating, cleaning, gold plating, palladium plating and cleaning, if the electroplating effect is not good, the method also comprises the steps of cleaning, deplating, cleaning, electroplating and the like after electroplating, the types and the contents of pollutants such as chelating agents, heavy metals, COD and the like in the wastewater obtained in each process step are greatly different, if the pollutants are mixed together for treatment, more high-concentration waste liquid is generated, the high-load operation of a special membrane and an evaporation system is caused, and the operation cost is greatly increased. The utility model discloses try to classify the waste water of each step, include washing waste water specifically, deoiling and dewaxing waste water and high concentration waste water, wherein wash waste water for each washing step produced waste water, pH is 5 ~ 6, COD is less than or equal to 50mg/L, the conductivity is less than or equal to 500 mus/cm; the oil and wax removal wastewater is wastewater in a pretreatment step, wherein a large amount of surfactant is added, the pH is generally 10-12, the COD is more than or equal to 5000mg/L, and the conductivity is less than or equal to 1000 mu s/cm; and treating the waste liquid with higher COD and conductivity serving as high-concentration waste water in other steps, wherein the pH is 5-6, the COD is more than or equal to 3000mg/L, the conductivity is more than or equal to 10000 mus/cm, and the conductivity is more than or equal to 10000 mus/cm.
In the processing of washing waste water, the utility model discloses at first utilize first filtering component to carry out the colating in order to get rid of big particulate matter in the waste water, behind the silt, utilize first MCR system to filter once more. The MCR system can intercept and remove small amounts of fine suspended and colloidal substances that may be present in the wastewater. And then, carrying out ion exchange by using a resin exchange system to remove heavy metals and COD (chemical oxygen demand) substances in the wastewater, carrying out carbon filtration, and then treating by using a UF (ultraviolet) membrane system and a three-stage reverse osmosis Ro (Ro) membrane system to obtain produced water, wherein the conductivity of the produced water is less than or equal to 6 mu s/cm, and the COD (carbon dioxide) is less than or equal to 5mg/L, and the produced water can be directly reused in an electroplating workshop for.
The oil and wax removing wastewater contains a large amount of wax, oily substances and jelly, the COD content is high, and the treatment difficulty is high. If the conventional coagulating sedimentation method is adopted for treatment, the use of a large amount of chemicals is increased and more solid wastes are generated. The utility model discloses utilize acid-out oxidation system in proper order to carry out acid-out oxidation treatment, reduction treatment and oxidation treatment, can fully get rid of the organic class material in the waste water. Then the condensate after evaporation treatment can enter cleaning wastewater, the COD content in the effluent is greatly reduced, then the effluent of the acidification oxidation treatment system is returned to the first treatment part for corresponding treatment, after particulate matter, silt, fine suspended matters, colloidal substances, heavy metals and a small amount of COD substances are removed, the conductivity of the obtained produced water is less than or equal to 6 mu s/cm, and the COD is less than or equal to 5mg/L, and the produced water can be directly reused in an electroplating workshop for normal production.
The treatment of high concentration waste water is the most difficult, mainly because the high concentration waste water is high in organic content and salt content and contains a small amount of fluoride and calcium carbonate. The utility model discloses tried multiple processing mode and device, for example UF + sea water membrane device, nevertheless the treatment effect is general. After a plurality of researches, a device with better treatment effect is found.
The utility model discloses at first adjust the pH of high enriched waste water through pretreatment mechanism to add the reductant and carry out the reduction with the oxidizing substance in the waste water, then carry out the colating through second filter mechanism, after getting rid of big particulate matter in the waste water, silt, utilize second MCR system to carry out secondary filter interception and get rid of a small amount of tiny suspended solid and colloidal substance that probably exist in the waste water. Then, filtering and separating pollutants such as SS, colloid, particulate matters and the like in the wastewater by using an STUF membrane system, and avoiding the problems of membrane blockage and poor treatment effect in the subsequent concentration treatment; then concentrating, separating and dissolving inorganic salt and heavy metal pollutants, greatly reducing organic matters and conductivity in the effluent after evaporation, and then treating according to the treatment process flow of cleaning wastewater to obtain produced water with the conductivity of less than or equal to 6 mu s/cm and the Cod of less than or equal to 5mg/L, which can be directly reused in an electroplating workshop for normal production.
Specifically, utilize the utility model provides a process that processing apparatus carries out processing to electroplating effluent is as follows:
s1: the electroplating wastewater is divided into cleaning wastewater, oil and wax removing wastewater and high-concentration wastewater.
S2: after rough filtration, the cleaning wastewater is filtered again by using MCR technology, then anion exchange is carried out by using anion resin and cation resin, and then the wastewater is treated by a UF membrane and a three-level reverse osmosis Ro membrane in sequence after carbon filtration, the Ro produced water is the recyclable water quality, and the Ro concentrated water is used as high-concentration wastewater for subsequent treatment.
S3: after the oil and wax removal wastewater is subjected to acidification and oxidation treatment, aerating, stirring, adjusting the pH to 3.5-4, then sequentially adding a reducing agent and an oxidizing agent for treatment, adjusting the pH to 9-10, standing to obtain a supernatant and sludge, and treating the supernatant as cleaning wastewater after evaporation and separation according to the step S2;
s4: adjusting the pH of the high-concentration wastewater to 3-4, adding a reducing agent, adjusting the pH back to 8-10, performing rough filtration, performing secondary filtration by using an MCR (modified cellulose reactor) technology, performing filtration and concentration treatment by using an STUF (super micro filter membrane) system technology, and performing evaporation and separation to obtain effluent serving as cleaning wastewater to be treated according to the step S2. After evaporation separation treatment, 99% of reclaimed water with the conductivity less than or equal to 6 mu s/cm and the COD less than or equal to 5mg/L can be obtained, in addition, evaporation waste liquid with the concentration not higher than 1% also exists, and the evaporation waste liquid can be treated by other methods after being concentrated.
The utility model provides a shunting is electroplated sewage zero release processing apparatus can reach industry reuse water standard after handling electroplating effluent, and the conductivity is low, is difficult for stifled membrane, and waste water rate of recovery is more than 99%, only produces about 1% waste liquid after handling, can realize the waste water zero release.
In the S3, the pH value can be adjusted by one or more of a sulfuric acid solution, a hydrochloric acid solution or a nitric acid solution.
Preferably, the pH is adjusted in S3 with a sulfuric acid solution.
Both reducing and oxidizing agents conventional in the art may be used in the present invention. In S3, the reducing agent is ferrous sulfate and sodium bisulfite; and in S3, the oxidant is hydrogen peroxide and bleaching water.
Preferably, the pH value of the cleaning wastewater is 5-6, the COD is less than or equal to 50mg/L, and the conductivity is less than or equal to 500 mu s/cm; the pH value of the oil and wax removing wastewater is 10-12, and the COD is more than or equal to 5000 mg/L; the pH value of the high-concentration wastewater is 5-6, the COD is more than or equal to 3000mg/L, and the conductivity is more than or equal to 10000 mus/cm.
Any filtering mechanism conventional in the art for coarse filtration may be used in the present invention.
Preferably, the first filtering mechanism is a coarse filtering mechanism.
More preferably, the coarse filtration mechanism is an activated carbon filter.
Preferably, the first treatment component further comprises a sump in communication with the first filter mechanism.
The cleaning wastewater can be collected through the water collecting tank and then processed subsequently.
More preferably, a water pump is communicated between the water collecting tank and the first filtering mechanism.
The water pump can realize that the washing waste water in the catch basin pumps to first filtering mechanism in.
MCR systems conventional in the art may be used in the present invention.
Preferably, the first MCR system includes a product water collection tank in communication with the first filtration mechanism and a bag filter in communication with the resin exchange system.
More preferably, the first MCR system is a vertical hanging MCR film (LGJ1E3-1500 × 14).
Preferably, the resin exchange system comprises a negative resin and a positive resin.
More preferably, the number of the female resins is plural groups, and the number of the male resins is plural groups.
Multiple groups of resins can realize multiple exchange of ions. The order of resin exchange of the cation resin and the anion resin can be selected according to the needs, the order of the cation resin and the anion resin has no requirement, and the cation resin and the anion resin can be firstly used for ion exchange and then used for ion exchange; or firstly, a plurality of groups of anion resins are used for ion exchange, and then a plurality of groups of cation resins are used for ion exchange; alternatively, the negative resin and the positive resin may be alternately used.
The utility model discloses carry out preferred discovery to the conventional positive resin in this area (such as domestic positive resin, TP-207) and negative resin (such as domestic negative resin, MP-68-P2), each resin is handled the initial stage and is had better ion exchange effect, but the domestic resin loss (the loss that the backwash brought) after handling for a long time, and the cost of regeneration (acid-base agent quantity), the cleaning cost of resin equipment all are greater than TP-207 and MP-68-P2.
Preferably, the positive resin is TP-207 and the negative resin is MP-68-P2.
In order to fully utilize the negative resin and the positive resin and save cost, the negative resin and the positive resin can be regenerated.
The regeneration treatment may be carried out in a manner conventional in the art.
The cation resin is regenerated by hydrochloric acid in general; and (3) regenerating the anion resin by using a sodium hydroxide solution.
Preferably, the carbon filtration system is a coconut shell activated carbon filtration system (1000X1850X4X 4).
Preferably, the UF membrane system is a vertical-liter ultrafiltration membrane module (LH 3-1060-V).
Preferably, the three-stage reverse osmosis Ro membrane treatment system comprises a three-stage Ro primary water production tank, an evaporation treatment pretreatment water tank, a triple-effect evaporator preheater and a triple-effect evaporator separator which are communicated with each other; the three-stage Ro primary water production tank is communicated with the UF membrane system, and the three-effect evaporator separator comprises a condensed water outlet and a Ro concentrated water outlet.
More preferably, the condensed water outlet is communicated with the cleaning water supply mechanism of the electroplating workshop through a condensed water pump.
The electroplating workshop cleaning water supply mechanism provides cleaning water for the cleaning process.
Preferably, the three-stage reverse osmosis Ro membrane treatment system is an american dow reverse osmosis membrane system.
Preferably, the acidification oxidation treatment system comprises an acidification tank, an aerator and an acidification filter press which are arranged in the acidification tank, and a three-effect evaporator.
The aerator can realize aeration and stir the solution in the acid precipitation tank.
More preferably, the triple effect evaporator comprises a pre-treatment water tank, a pre-heater and a separator.
Acid out oxidation treatment systems conventional in the art may be used in the present invention.
More preferably, the number of the acid separation oxidation treatment systems is multiple, and the multiple acid separation oxidation treatment systems can be efficiently used in batches by two or more rotation.
Preferably, the acid precipitation tank is communicated with an acid precipitation filter press.
The acidification filter press can pack and transport the sludge separated by the acidification oxidation treatment system.
Preferably, the acidification oxidation treatment system further comprises a diaphragm pump for pumping the waste liquid in the acidification tank into the acidification filter press.
Preferably, the pretreatment tank mechanism comprises a reduction tank, a pH adjusting tank and a sedimentation tank.
Preferably, the second filtering mechanism comprises a produced water collecting tank and a bag filter which are communicated; the produced water collecting water tank is communicated with the pretreatment tank mechanism; the bag filter is in communication with the second MCR system.
Preferably, the second MCR system comprises a produced water collection tank in communication with the second filtration mechanism and a bag filter in communication with the stun membrane system.
More preferably, the second MCR system is a concentrated water type MCR film (LGJ1E-1500 × 6).
Preferably, the STUF membrane system comprises a STRO pre-concentration mechanism and a DTRO secondary concentration mechanism.
The STRO preconcentration mechanism is mainly used for separating and dissolving inorganic salts and heavy metal pollutants.
The DTRO secondary concentration mechanism is mainly used for treating concentrated water generated by STRO to realize concentration and evaporation.
More preferably, the STRO pre-concentration mechanism comprises a STRO system buffer water tank, a buffer water tank high-pressure pump, a cartridge filter and a STRO concentrator which are sequentially communicated, the outlet water of the STRO concentrator is communicated with the secondary Ro primary production water tank, and the concentrate outlet of the STRO concentrator is communicated with the DTRO secondary concentration mechanism.
A surge tank high pressure pump is used to pump the STRO system surge tank into the cartridge filter.
More preferably, the DTRO secondary concentration mechanism comprises a DTRO concentrator and a triple-effect evaporator, the water outlet of the DTRO concentrator is communicated with the secondary Ro primary water production tank, and the concentrate outlet of the DTRO concentrator is communicated with the triple-effect evaporator.
More preferably, the triple effect evaporator comprises a pre-treatment water tank, a pre-heater and a separator.
More preferably, the STUF membrane system is a Zhejiang Meiyi membrane STUF 4040.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model provides a processing apparatus is categorised, the pertinence is handled the electroplating effluent of different classes, utilizes full physics piece-rate system, and waste water can reach industry reuse water standard after handling, and the conductivity is low, is difficult for stifled membrane, and waste water reuse rate more than 99%, only produces about 1% waste liquid after handling, can realize the waste water zero release.
Drawings
FIG. 1 is a schematic structural view provided in example 1;
wherein, 1 is a first filtering mechanism, 2 is a first MCR system, 3 is a resin exchange system, 4 is a carbon filtering system, 5 is a UF membrane system, 6 is a three-stage reverse osmosis Ro membrane treatment system, 7 is an acid precipitation oxidation treatment system, 8 is a pretreatment mechanism, 9 is a second filtering mechanism, 10 is a second MCR system, 11 is an STUF membrane system, and 12 is an acid precipitation filter press; a is cleaning wastewater, b is high-concentration wastewater, c is oil and wax removal wastewater, d is final produced water, and e is sludge.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention. Furthermore, the technical features mentioned in the embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.
It will be understood that when an element is referred to as being "disposed on" or "mounted on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present.
Classifying electroplating sewage, and collecting waste water generated in the cleaning step as cleaning waste water a; collecting the pretreatment wastewater as oil and wax removal wastewater c; and collecting the rest wastewater as high-concentration wastewater b. The results of the measurements on the three wastewaters are shown in Table 1.
TABLE 1 quality of wastewater in examples
Example 1
The embodiment provides a flow-dividing electroplating sewage zero-discharge treatment device, which comprises a first treatment component for treating cleaning wastewater, a second treatment component for treating oil and wax removal wastewater and a third treatment component for treating high-concentration wastewater, as shown in figure 1.
Specifically, the first treatment means includes a water collecting tank, a water pump, a first filtration mechanism 1, a first MCR system 2 (LGJ1E-1500 × 14 in the present embodiment), a resin exchange system (3), a carbon filtration system 4 (1000X 1850-4-4 in the present embodiment), a UF membrane system 5 (LH3-1060-V in the present embodiment), and a three-stage reverse osmosis Ro membrane treatment system 6 (riser CPA3-LD8040 in the present embodiment), which are connected in this order.
Wherein, the first filtering mechanism 1 is a rough filtering mechanism, in particular to an active carbon filter. The first MCR system 2 includes a produced water collection tank in communication with an activated carbon filter and a bag filter in communication with the resin exchange system 3. The resin exchange system 3 comprises a plurality of groups of negative resins MP-68-P2 and a plurality of groups of positive resins TP-207. The three-stage reverse osmosis Ro membrane treatment system 6 comprises a two-stage Ro primary water production tank, an evaporation treatment pretreatment water tank, a triple-effect evaporator preheater and a triple-effect evaporator separator which are communicated with each other; the secondary Ro primary water production tank is communicated with the UF membrane system, the triple-effect evaporator separator comprises a condensed water outlet and an Ro concentrated water outlet, and the condensed water outlet is communicated with a cleaning water supply mechanism of an electroplating workshop through a condensed water pump.
Specifically, the second processing component includes an acid out oxidation processing system 7. The acid separation oxidation treatment system 7 comprises an acid separation tank, an aerator arranged in the acid separation tank, a triple-effect evaporator and a diaphragm pump. The diaphragm pump is communicated with the acid separation filter press 12 and is used for pumping the sludge in the acid separation tank to the acid separation filter press so as to realize the packing and outward transportation of the sludge. The triple-effect evaporator is used for evaporating and separating the supernatant in the acid precipitation tank, and the water outlet of the triple-effect evaporator is communicated with the first filtering mechanism, so that the effluent is reprocessed according to the treatment process of the cleaning wastewater.
The effluent of the concentrated water port of the triple-effect evaporator can be transported outside by a special tank car.
Specifically, the third processing unit includes a pretreatment mechanism 9, a second filtration mechanism 10, a second MCR system 11 (LGJ1E-1500 × 6 in this embodiment), and an STUF membrane system 12 (STUF 4040 in this embodiment), which are sequentially connected. Wherein, pretreatment tank mechanism 8 is including the reduction pond, pH adjusting tank and the sedimentation tank that communicate in proper order, and second filter mechanism is activated carbon filter. The second MCR system 11 includes a produced water collection tank and a bag filter which are communicated with each other, the produced water collection tank is communicated with the second filtering mechanism 10, the stun membrane system 12 includes an STRO pre-concentration mechanism and a DTRO secondary concentration mechanism, and the bag filter is communicated with the STRO pre-concentration mechanism. The STRO pre-concentration mechanism comprises a STRO system buffer water tank, a buffer water tank high-pressure pump, a cartridge filter and a STRO concentrator which are sequentially communicated. The DTRO secondary concentration mechanism comprises a DTRO concentrator and a triple-effect evaporator, and the triple-effect evaporator comprises a pretreatment water tank, a preheater and a separator which are sequentially communicated. The water outlet of the STRO concentrator and the water outlet of the DTRO concentrator are both communicated with the secondary Ro primary water production tank, the concentrated water port of the STRO concentrator is communicated with the DTRO concentrator, and the concentrated water port of the DTRO concentrator is communicated with the pretreatment water tank of the triple-effect evaporator. The concentrated water of the triple-effect evaporator can be transported and treated.
The water outlets of the DTRO secondary concentration mechanisms are communicated with the first filtering mechanism 1, so that effluent is retreated according to the treatment process of cleaning wastewater.
The process of treating three types of wastewater by using the treatment device provided in this example is as follows.
(1) Treatment of cleaning wastewater
Cleaning wastewater is collected by a water collecting tank, and then is lifted to an activated carbon filter by a water pump, large particles, silt and the like in the wastewater are removed, and then the wastewater enters a water production collecting tank of a first MCR system; the pretreated cleaning wastewater enters a resin exchange system through a bag filter, and cation resin (TP-207) is used for carrying out resin exchange on heavy metal pollutants such as Cu, Ge and the like in the wastewater; then, carrying out resin exchange on heavy metal pollutants such as Ni and the like in the wastewater by using negative resin (MP-68-P2); after the resin is saturated, 35 wt% of hydrochloric acid and 25 wt% of NaOH are respectively used for resin regeneration so as to ensure the exchange efficiency. In order to strictly ensure good water quality of water used in a workshop, heavy metals and partial COD in wastewater are removed (the conductivity is less than or equal to 50 mu s/cm, and the COD is less than or equal to 30mg/L), then the wastewater enters a reuse water system, a produced water carbon filtering system and a UF membrane system enter a three-stage reverse osmosis Ro membrane, and finally produced water d is directly reused in an electroplating workshop for normal production; and the Ro concentrated water enters a third treatment part for subsequent treatment.
(2) Treatment of oil and wax removing waste water
After the oil-removing and wax-removing waste water is collected, it is lifted to an acid precipitation tank (tank volume is 2 m)3) The acidification oxidation treatment is carried out in batches, and the process is as follows: and (3) fully and uniformly stirring the waste liquid by using an aerator, adding sulfuric acid to adjust the pH to about 3.5-4, adding 12.5kg of ferrous sulfate, and adding 40kg of hydrogen peroxide after about 20 minutes. And (3) adjusting pH to 9-10 after oxidizing for 3 hours, closing the aerator, after precipitating for 30 minutes, pumping the waste liquid in the tank into an acidification filter press by using a diaphragm pump, performing sludge-water separation, packaging and transporting sludge e, and treating the filtrate in a triple-effect evaporator: the method comprises the steps of firstly entering an evaporation treatment pretreatment water tank, enabling concentrated solution to enter a triple-effect evaporator preheater through an evaporation system in a vacuum self-absorption mode, enabling the concentrated solution to enter a triple-effect evaporator separator after the concentrated solution is evaporated through the triple-effect evaporator, enabling condensed water to pass through the separator, pumping the condensed water to an electroplating general cleaning wastewater pool through a condensate pump, processing the electroplating general cleaning wastewater together with the electroplating cleaning wastewater, and then recycling the electroplating general cleaning wastewater to an electroplating workshop. A small amount of evaporation waste (about 5%) is discharged into a high concentration waste tank and entrusted to a qualified processing company for further processing.
(3) Treatment of high concentration wastewater
Pretreatment: after the pH value of high-concentration wastewater in a workshop is adjusted to 3-4, the high-concentration wastewater enters a reduction tank, a reducing agent (sodium bisulfite) is added to reduce oxidized substances in the wastewater, the wastewater automatically flows into a pH adjusting tank, the pH value is adjusted to 8-9, the wastewater automatically flows into a sedimentation tank, large particles, silt and the like in the wastewater are removed, then the wastewater automatically flows into an MCR system, and a small amount of fine suspended matters and colloidal substances possibly existing in the wastewater are intercepted and then enter a concentrated water collection tank; the pretreated wastewater enters an STUF membrane system to separate pollutants such as SS, colloid, particulate matters and the like in the wastewater; the water produced by the STUF membrane system enters a buffer water tank of the STRO system, the water enters the STRO system to pre-concentrate raw water after being pumped by the buffer water tank through a security filter at high pressure, inorganic salt and heavy metal pollutants are separated and dissolved, the produced water enters a secondary Ro primary water production tank, concentrated water enters a DTRO system buffer water tank, the concentrated water enters DTRO through the buffer water tank after being pumped by the security filter at high pressure, the water produced by the DTRO system enters the secondary Ro primary water production tank, the concentrated water enters an evaporation treatment pre-treatment water tank, concentrated liquid enters a triple-effect evaporator preheater through an evaporation system through vacuum self-suction, the concentrated liquid enters a triple-effect evaporator separator after being evaporated through the triple-effect evaporator, and condensed water is pumped to an electroplating general cleaning wastewater pool through a condensed water pump and is treated together with electroplating cleaning wastewater through the. A small amount of evaporation waste (about 1%) is discharged into a high concentration waste tank and entrusted to a qualified processing company for further processing.
The total water quality after the cleaning wastewater, the oil and wax removing wastewater and the high concentration wastewater (three treatment modes) are treated is detected, and the results are shown in table 2.
TABLE 2 Total Water quality after treatment
From the above, the utility model provides a processing apparatus classifies, the pertinence is handled electroplating effluent, selects for use the full physics separation technology system that only introduces a small amount of external medicaments, can reach industry reuse water standard after the waste water is handled, and the conductivity is low, and difficult stifled membrane, waste water reuse rate more than 99%, only produce about 1% waste liquid after handling, can realize the waste water zero release; the treated reuse water is directly returned to an electroplating workshop for normal production.
It will be appreciated by those of ordinary skill in the art that the examples provided herein are intended to assist the reader in understanding the principles of the invention and are to be construed as being without limitation to such specifically recited examples and embodiments. Those skilled in the art can make various other specific modifications and combinations based on the teachings of the present invention without departing from the spirit of the invention, and such modifications and combinations are still within the scope of the invention.
Claims (10)
1. The shunting electroplating sewage zero-discharge treatment device is characterized by comprising a first treatment component for treating cleaning wastewater, a second treatment component for treating oil-removing and wax-removing wastewater and a third treatment component for treating high-concentration wastewater; the first treatment component comprises a first filtering mechanism (1), a first MCR system (2), a resin exchange system (3), a carbon filtration system (4), a UF membrane system (5) and a three-stage reverse osmosis Ro membrane treatment system (6) which are sequentially communicated; the second treatment component comprises an acid out oxidation treatment system (7); the third treatment component comprises a pretreatment mechanism (8), a second filtering mechanism (9), a second MCR system (10) and an STUF membrane system (11) which are communicated in sequence; the water outlet of the acid precipitation oxidation treatment system (7) and the water outlet of the STUF membrane system (11) are both communicated with the first filtering mechanism (1); and an Ro concentrated water outlet of the three-stage reverse osmosis Ro membrane treatment system (6) is communicated with the pretreatment mechanism (8).
2. The split-flow electroplating wastewater zero-emission treatment device according to claim 1, wherein the first filtering mechanism (1) and the second filtering mechanism (9) are both coarse filtering mechanisms.
3. The split-flow electroplating wastewater zero-emission treatment device according to claim 1, wherein the first MCR system (2) comprises a produced water collection tank and a bag filter, the produced water collection tank is communicated with the first filtering mechanism (2), and the bag filter is communicated with the resin exchange system (3).
4. The split-flow electroplating wastewater zero-emission treatment device according to claim 1, wherein the resin exchange system (3) comprises a negative resin and a positive resin.
5. The split-flow type electroplating sewage zero-emission treatment device according to claim 1, wherein the carbon filtration system (4) is an activated carbon filter, and coconut shell activated carbon with the particle size of 6-10 meshes is adopted; the UF membrane system (5) is a vertical-liter ultrafiltration membrane group.
6. The split-flow electroplating wastewater zero-emission treatment device as claimed in claim 1, wherein the three-stage reverse osmosis Ro membrane treatment system (6) comprises a three-stage Ro primary water production tank, an evaporation treatment pretreatment water tank, a triple-effect evaporator preheater and a triple-effect evaporator separator which are communicated with each other; the three-stage Ro primary water production tank is communicated with a UF membrane system (5), and the three-effect evaporator separator comprises a condensed water outlet and an evaporation and concentration waste liquid outlet.
7. The split-flow electroplating wastewater zero-emission treatment device according to claim 1, wherein the acidification and oxidation treatment system (7) comprises an acidification tank, an aerator and a triple-effect evaporator, wherein the aerator is arranged in the acidification tank.
8. The split-flow electroplating wastewater zero-discharge treatment device according to claim 1, wherein the pretreatment tank mechanism (8) comprises a reduction tank, a pH adjusting tank and a sedimentation tank.
9. The split-flow electroplating wastewater zero-emission treatment device according to claim 1, wherein the second MCR system (11) comprises a produced water collection tank and a bag filter, the produced water collection tank is communicated with the second filtering mechanism (10), and the bag filter is communicated with the STUF membrane system (12).
10. The device for zero discharge of electroplating wastewater according to claim 1, wherein the STUF membrane system (12) comprises a STRO pre-concentration mechanism and a DTRO secondary concentration mechanism.
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| CN201920840467.5U CN210505916U (en) | 2019-06-03 | 2019-06-03 | Shunting electroplating sewage zero discharge treatment device |
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